Patent Application
20220395800
The present invention generally relates to automated synthesis technology, and more particularly, to a device and method for automated synthesis of oligo- and polysaccharides on a solid support. In particular the present invention relates to a device for automated synthesis of oligo- and polysaccharides on a solid support comprising a reaction vessel, a reagent storing component, a reagent delivery system, a cooling device for cooling the reaction vessel, and a pre-cooling device for pre-cooling the reagents to be supplied.
Certain biopolymers, including polypeptides and polynucleotides are routinely synthesized by solid-phase methods in which individual subunits are added stepwise to a growing chain tethered to a solid support. Those approaches can be carried out using commercially available synthesizers in an automated or semi-automated manner. However, those general synthesizers do not allow the efficient synthesis of oligosaccharides on a solid support and typically result in poor yields and selectivity, due to the lack of control of reaction temperature.
Polysaccharides are the most abundant biomolecules on Earth and are essential for many vital biological functions. Energy, structural support, cell proliferation and differentiation, host-pathogen recognition and cancer invasion are among the numerous areas that oligosaccharides and glycoconjugates participate and regulate. Because biochemical techniques to purify pure oligosaccharides from natural sources are difficult and inefficient, chemical and enzymatic approaches, or combinations thereof, are often the only reliable methods to access pure oligosaccharides. Efforts to reduce the time and resources spent on traditional chemical syntheses have focused mainly on automated glycan assembly (AGA) on solid supports.
The advantages of solid-support synthesis have been appreciated since the development of peptide synthesis by Merrifield and oligonucleotide synthesis on polymer supports developed by Caruthers. Automated synthesis machines carry out the reaction sequences and the reactions are carried out in high yields by using excess reagents, which are simply removed by washing steps. Separation from the solid carrier and purification as post-automation steps are typically standardized. The keys to successful automated synthesis are reliable building blocks and resins, high-yield couplings and reliable instrumentation.
Since the introduction of AGA by Seeberger in 2001, many aspects of the synthesis process have been systematically improved. Synthetic glycans of increasing length and complexity up to a chain length of 50 units were assembled with the help of AGA. The quality control of the stereo- and regiochemical composition of synthetic products was greatly accelerated by the use of ion mobility mass spectrometry (IM-MS). The overall AGA process was greatly improved and led to the development of the first commercial Glyconeer 2.1© automated oligosaccharide synthesizer.
Depending on the molecular weight of the sugar, 10-50 mg of completely protected oligosaccharide is obtained from the resin in this batch size. After deprotection and purification of the final product, usually only 2-15 mg of the desired oligosaccharide product remain. These amounts are often sufficient for biochemical investigations and have been successfully used to produce glycan arrays. However, significantly more material is required for studies in other scientific areas. Carbohydrates in the form of cellulose and chitin are the two dominant biopolymers that require 100 mg or more of synthetic compounds to investigate their material properties.
EP 1 315 559 A2 discloses a device comprising a reaction vessel, at least one donor vessel, at least one activator vessel, at least one deblocking vessel, at least one solvent vessel, a solution transfer system capable of transferring the donor solution, activating reagent solution, deblocking solution and solvent, and a computer for controlling the solution transfer system. The device further comprises a temperature control unit for regulating the temperature of the reaction vessel.
US 2011/313148 A1 and US 2010/159604 A1 disclose devices comprising a reaction vessel equipped with a temperature control system, reagent bottles, a solution transfer system, a computer and a pump operably connected to a first fluidic valve and a second fluidic valve connected to the reaction vessel. The second fluidic valve is connected to the first fluidic valve via a first fluid line and to the reaction vessel via a second fluid line. The reagents can be delivered via the second fluidic valve into the first fluid line and then through the second fluidic line into the reaction vessel.
US 2007/189934A1 discloses an apparatus comprising a reaction vessel, a structural unit chemical dispensing unit fluidly coupled to the reaction vessel via a first fluid line, a synthesis chemical dispensing unit fluidly coupled to the reaction vessel via a second fluid line and a controller. The first and second fluid lines are fluidly isolated from each other so that the structural unit chemicals and the synthesis chemicals are fluidly isolated from each other prior to entering the reaction vessel to avoid cross-contamination.
US 2005/042768 A1 discloses a device for reactions on a solid substrate. A device is disclosed comprising one or more flow devices, multiple reagent reservoirs with pre-heating and pre-cooling capability and associated fluid routing valves, a liquid waste collection reservoir, solvent vapor generator to assist drying a hydrophilic-surfaced substrate, and a computer. The flow device comprises a housing comprising a housing chamber. The housing comprises an opening through which a substrate may be inserted into the housing chamber. At least one inlet is in fluid communication with the housing chamber, at least one outlet is in fluid communication with the housing chamber and at least one inlet is in gaseous communication with the housing chamber. The housing may be surrounded with a thermally insulating jacket to maintain it and its fluid contents at a stable temperature. The device may further comprise a heat exchanger where fluid reagent is either heated by means of a heater unit or cooled by means of a cooling unit, wherein the fluid of reagents exiting the flow cell may be passed through the heat exchanger and resupplied to the flow cell. The heat exchanger is part of a recirculation cycle of reagents.
The devices known in the art have shown several disadvantages in performing coupling reactions in connection with the use of common reagents especially during scale-up of the synthesis of oligo- and polysaccharides on the solid support. Even if the devices known in the art allow for active cooling of the reaction vessel during the coupling reactions, not sufficiently high yields were obtained, decomposition of reagents and formation of side and decomposition products were detected.
Thus, there is a need in the art for improved devices for automated synthesis of oligo- and polysaccharides on a solid support that allow efficient up-scaling and larger batch sizes, wherein the formation of side and decomposition products and decomposition of intermediates are effectively prevented.
It is therefore the objective of the present invention to provide an improved device and method for automated synthesis of oligo- and polysaccharides on a solid support. Especially desired is a device for easily scaling up the synthesis of oligo- and polysaccharides on a solid support, shortening the reaction time, increasing yield and decreasing side and decomposition products.
The objective of the present invention is solved by the teachings of the independent claims. Further advantageous features, aspects and details of the invention are evident from the dependent claims, the description, the figures, and the examples of the present application.
The present invention relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
According to an aspect of the invention the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400); wherein the pre-cooling device (300) is interposed between the reaction vessel (400) and the reagent delivery system (600); and wherein the pre-cooling device (300) is in thermal communication with the reagent delivery system (600).
According to an aspect of the present invention the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600) so that the reagents along their way from the pre-cooling device (300) to the reaction vessel (400) do not increase their temperature for more than 0.5° C. According to an aspect of the present invention the pre-cooling device (300) may be positioned downstream to the reagent delivery system (600) and upstream to reaction vessel (400).
According to an aspect of the present invention the reagent delivery system (600) being in fluid communication with the reaction vessel (400) through one or more reagent delivery lines (601, 602); and the pre-cooling device (300) being in thermal communication with the one or more reagent delivery lines (601, 602). Thus, it is preferred that at least one liquid line between the reagent delivery system (600) and the reaction vessel (400) is pre-cooled by the pre-cooling device (300) located between the reagent delivery system (600) and the reaction vessel (400).
According to an aspect of the present invention the reaction vessel (400), the pre-cooling device (300), the reagent delivery system (600) and the reagent storing component (660) are successively connected in the following sequence: reagent storing component—reagent delivery system—pre-cooling device—reaction vessel.
According to an aspect of the present invention the reagent delivery system (600) being in fluid communication with the reagent storing component (660) and further being in fluid communication with the reaction vessel (400).
According to an aspect of the present invention the reagent storing component (660) and the pre-cooling device (330) are connected through the reagent delivery system (600).
According to an aspect of the present invention the pre-cooling device (300) may be a thermoelectric cooler.
According to an aspect of the present invention the device may comprise a computing device (200) comprising at least one processor configured to control one or more components of the device for automated synthesis of oligo- and polysaccharides on a solid support.
According to an aspect of the present invention the reaction vessel (400) may be adapted for receiving the solid support.
According to an aspect of the present invention the device may be adapted for reactions under anhydrous and inert atmosphere.
According to an aspect of the present invention the device may further comprise an inert gas delivery system (800).
According to an aspect of the present invention the cooling device (350) may comprise a cooling jacket (307) or a cooling coil.
According to an aspect of the present invention the pre-cooling device (300) may be adapted to cool the reagents to be supplied to a temperature not higher than +3° C. of the temperature in the reaction vessel.
According to an aspect of the present invention the pre-cooling device (300) may be adapted to cool the reagents to be supplied in a temperature range of +3° C. to −3° C. of the temperature in the reaction vessel or more precisely of the temperature of the content in the reaction vessel.
According to an aspect of the present invention the pre-cooling device (300) may be a part or component of the cooling device (350) using the same cooling circuit together. Reworded, the pre-cooling device (300) and the cooling device (350) may form a single component.
According to an aspect of the present invention the reaction vessel (400) may be provided as an interchangeable reaction vessel.
According to an aspect of the present invention the reaction vessel (400) may be made of fluoropolymers such as perfluoroalkoxy alkanes (PFA).
According to an aspect of the present invention the device may comprise a reagent storing component (660) suitable for storing at least building blocks and/or building block solution, activators and/or activator solutions, washing solutions and deprotection solutions.
According to an aspect of the present invention the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400).
According to an aspect of the present invention the device may further comprise a microwave generator component (500). According to an aspect of the present invention the reaction vessel may be a microwave transparent reaction vessel. According to an aspect of the present invention the cooling jacket or the cooling coil may be a microwave transparent cooling jacket or cooling coil.
In one embodiment of the present invention, the device comprises a first reagent delivery system (600) or top delivery system comprising a distribution component (651, 652, 653) or top distribution component for delivery of building blocks and/or building block solutions, activators and/or activator solutions and washing solution; and a second reagent delivery system (700) or bottom delivery system comprising a distribution component (719, 720) or bottom distribution component for delivery of deprotection solutions and optionally capping solutions. Preferably the device further comprises an exhaust gas exit (655).
According to an aspect of the present invention the device may further comprise a light source for cleaving photo-cleavable linkers.
The present invention further relates to a method for synthesizing oligo- and polysaccharides with a device according the present invention, the method comprising the following steps:
wherein in step b) at least the glycosylation reagent is pre-cooled to a temperature of at least −40° C. to −9° C. by a pre-cooling device (300) during delivery to and before addition to the reaction vessel (400).
Solid phase synthesis of oligo- or polysaccharides has been proven as suitable synthesis strategy for automation of the synthesis process. For solid phase synthesis of oligo- or polysaccharides the repetitive nature of glycosylation and deprotection can easily be framed into a coupling cycle. Excess reagents may be used to drive reactions to completion, while resin washes, for example through use of solvents, remove any soluble impurities. Only a single purification step is necessary after the oligo- or polysaccharide is liberated from the solid support.
The term “glycosylation reaction” or “coupling reaction” as used herein relates in the most general sense to a formation of an acetal connecting two sugar units. The anomeric substituent of a glycosyl donor acts as a leaving group thereby generating an electrophilic intermediate. Reaction of this species with a nucleophile, typically a hydroxyl group of a glycosyl acceptor, leads to the formation of a glycosidic linkage. Thus, the term “glycosylation reaction” or “coupling reaction” refers to reactions between a glycosyl donor and a glycosyl acceptor, wherein the reducing end of the donor reacts with a free hydroxy or amine group of the acceptor. Thus, O-glycosylation or N-glycosylation methods are preferably employed in the coupling reaction of the method according to the invention. More preferably, O-glycosylation methods are employed in the coupling reaction of the method according to the invention. These glycosylation methods are known from the state of the art. Generally, they require a leaving group at the reducing end of the donor, which is activated in the presence of a catalyst.
The glycosylation reactions take place upon treatment of a donor and an acceptor with a “glycosylation reagent” or “activator” which acts as an activator or an activating agent. Glycosylation reagents known to the skilled person include, but are not restricted to: AgOTf, BF3.OEt2, trimethylsilyl trifluoromethanesulfonate (TMSOTf), trifluoromethanesulfonic acid (TfOH), trifluoromethanesulfonic anhydride (Tf2O, triflic anhydride), lanthanoid(III) triflates, NIS/AgOTf, NIS/TfOH or dimethyl(methylthio)sulfonium trifluoromethanesulfonate (DMTST).
The term “coupling cycle” or “synthesis cycle” or “glycosylation cycle” as used herein relates to an iterative or repetitive sequence of coupling reactions and deprotection steps in the synthesis of oligo- or polysaccharides on a solid support. In this synthesis strategy, the carbohydrate chain is elongated in a stepwise manner and thus gradually extended through each synthesis cycle until the desired oligo- or polysaccharide is obtained.
As used herein, the term “saccharide” refers to but is not restricted to monosaccharide, disaccharide, trisaccharide, tetrasaccharide, pentasaccharide, hexasaccharide, heptasaccharide, octasaccharide . . . , oligosaccharide, polysaccharide and glycan. The saccharide comprises preferably monosaccharide units selected from:
The saccharides are further optionally modified to carry amide, carbonate, carbamate, carbonyl, thiocarbonyl, carboxy, thiocarboxy, ester, thioester, ether, epoxy, hydroxyalkyl, alkylenyl, phenylene, alkenyl, imino, imide, isourea, thiocarbamate, thiourea and/or urea moieties.
The term “saccharide building block” or “building block” as used herein refers to a saccharide acceptor or saccharide donor, i.e. to a saccharide that is capable of forming a glycosidic bond when being exposed to a glycosylating agent. The saccharide building block can be fully protected (i.e. each hydroxy or amino group is blocked by a protecting group), partially protected (i.e. at least one hydroxy or amino groups is blocked by a protecting group) or unprotected (i.e. none of hydroxy or amino groups is blocked by a protecting group). For forming an amide bond with an anchoring group present on the solid support the saccharide building block may also be modified at the reducing end with a suitable functional group such as a carboxylic acid (e.g. hydroxyacetate), azide, alkyne, thiol or an amine (e.g. aminopropyl or aminopentyl). Any known saccharide building block can be employed in the inventive methods described herein, including saccharides, glycopeptides or glycopeptoids as described in Beilstein J. Org. Chem. 2014, 10, 2453-2460. The building blocks for the glycosylation reaction may be provided as glycosyl donor or glycosyl acceptor molecules. Glycosyl donor building blocks relate preferably to carbohydrate molecules with a suitable leaving group at the anomeric position, which may be used as glycosyl donors for the glycosylation reaction. Glycosyl acceptor building blocks relate preferably to carbohydrate molecules with an unprotected nucleophilic hydroxyl group or a protected carbohydrate molecule which allows orthogonal deprotection of one protecting group, which may be used as glycosyl acceptors for the glycosylation reaction.
“Alkyl” refers to saturated hydrocarbon groups of from 1 to 18 carbon atoms, either straight chained or branched, more preferably from 1 to 8 carbon atoms, and most preferably 1 to 6 carbon atoms. An alkyl with a specified number of carbon atoms is denoted as C1-C8 alkyl and refers to a linear C1-C8 alkyl of —CH3, —C2H5, —C3H7, —C4H9, —C5H11, —C6H13, —C7H15, —C8H17, —CH2-Ph, —CH2—CH2-Ph or a branched C1-C8 alkyl or preferably branched C3-C8 alkyl of —CH(CH3)2, —CH2—CH(CH3)2, —CH(CH3)—C2H5, —C(CH3)3, —CH(CH3)—C3H7, —CH2—CH(CH3)—C2H5, —CH(CH3)—CH(CH3)2, —C(CH3)2—C2H5, —CH2—C(CH3)3, —CH(C2H5)2, —C2H4—CH(CH3)2, —C3H6—CH(CH3)2, —C2H4—CH(CH3)—C2H5, —CH(CH3)—C4H9, —CH2—CH(CH3)—C3H7, —CH(CH3)—CH2—CH(CH3)2, —CH(CH3)—CH(CH3)—C2H5, —CH2—CH(CH3)—CH(CH3)2, —CH2—C(CH3)2—C2H5, —C(CH3)2—C3H7, —C(CH3)2—CH(CH3)2, —C2H4—C(CH3)3, —CH(CH3)—C(CH3)3, —C4H8—CH(CH3)2, —C3H6—CH(CH3)—C2H5, —C3H6—CH(CH3)—C2H5, —C2H4—CH(CH3)—C3H7, —CH2—CH(CH3)—C4H9, —CH(CH3)—C5H11, —CH(C2H5)—C4H9, —C2H4—CH(CH3)—C3H7, —CH2—CH(C2H5)—C3H7, —CH2—CH(CH3)—C4H9, —CH2—CH(CH3)—CH2—CH(CH3)2, —CH(C2H5)—CH2—CH(CH3)2, —CH(CH3)—C2H4—CH(CH3)2, —CH(CH3)—CH2—CH(CH3)—C2H5, —CH2—CH(CH3)—CH(CH3)—C2H5, —CH(CH3)—CH2—CH(CH3)—C2H5, —CH(CH3)—CH(C2H5)—C2H5, —CH(C2H5)—CH(CH3)—C2H5, —CH(CH3)—CH(CH3)—C3H7, —C2H4—CH(CH3)—CH(CH3)2, —CH2—CH(C2H5)—CH(CH3)2, —CH2—CH(CH3)—CH2—CH(CH3)2, —CH2—CH(CH3)—CH(CH3)—C2H5, —C2H4—C(CH3)2—C2H5, —CH2—C(CH3)(C2H5)2, —CH2—C(CH3)2—C3H7, —CH2—C(CH3)2—C3H7, —C(CH3)(C2H5)—C3H7, —C(CH3)2—C4H9, —CH2—C(CH3)2—CH(CH3)2, —C(CH3)(C2H5)—CH(CH3)2, —C(CH3)2—CH2—CH(CH3)2, —C(CH3)2—C(CH3)3, —C(CH3)2—CH(CH3)—C2H5, —C3H6—C(CH3)3, —C2H4—C(CH3)2—C2H5, —CH2—CH(CH3)—C(CH3)3, —CH(C2H5)—C(CH3)3, —CH(CH3)—CH2—C(CH3)3, —CH(CH3)—C(CH3)2—C2H5, —C5H10—CH(CH3)2, —C4H8—C(CH3)3, —C4H8—CH(CH3)—C2H5, —C4H8—CH(CH3)—C2H5, —C3H6—C(CH3)2—C2H5, —C3H6—CH(C2H5)—C2H5, —C3H6—CH(CH3)—C3H7, —C2H4—C(CH3)2—C3H7, —C2H4—CH(C2H5)—C3H7, —C2H4—CH(CH3)—C4H9, —CH2—C(CH3)2—C4H9, —CH2—CH(C2H5)—C4H9, —CH2—CH(CH3)—C5H11, —C(CH3)2—C5H11, —CH(CH3)—C6H13, —CH(C3H7)—C4H9, —CH(C2H5)—C5H11, —CH2—C(CH3)(C2H5)—C3H7, —C2H4—CH(CH3)—CH2—CH(CH3)2, —CH2—C(CH3)2—CH2—CH(CH3)2, —CH2—CH(C2H5)—CH2—CH(CH3)2, —CH2—CH(CH3)—C2H4—CH(CH3)2, —CH2—CH(CH3)—CH2—C(CH3)3, —CH2—CH(CH3)—CH2—CH(CH3)—C2H5, —C(CH3)(C2H5)—CH2—CH(CH3)2, —CH(C3H7)—CH2—CH(CH3)2, —CH(C2H5)—C2H4—CH(CH3)2, —CH(C2H5)—CH2—C(CH3)3, —CH(C2H5)—CH2—CH(CH3)—C2H5, —CH2—CH(CH3)—C2H4—CH(CH3)2, —C(CH3)2—C2H4—CH(CH3)2, —CH(C2H5)—C2H4—CH(CH3)2, —CH(CH3)—C3H6—CH(CH3)2, —CH(CH3)—C2H4—C(CH3)3, —CH(CH3)—C2H4—CH(CH3)—C2H5, —CH2—CH(CH3)—CH2—CH(CH3)—C2H5, —C(CH3)2—CH2—CH(CH3)—C2H5, —CH(CH3)—C2H4—CH(CH3)—C2H5, —CH(CH3)—CH2—C(CH3)2—C2H5, —CH(CH3)—CH2—CH(CH3)—C3H7, —C2H4—CH(CH3)—CH(CH3)—C2H5, —CH2—C(CH3)2—CH(CH3)—C2H5, —CH2—CH(C2H5)—CH(CH3)—C2H5, —CH2—CH(CH3)—CH2—CH(CH3)—C2H5, —CH2—CH(CH3)—C(CH3)2—C2H5, —CH2—CH(CH3)—CH(C2H5)2, —C3H6—CH(CH3)—CH(CH3)2, —C2H4—C(CH3)2—CH(CH3)2, —C2H4—CH(C2H5)—CH(CH3)2, —C2H4—CH(CH3)—C(CH3)3, —C2H4 CH(CH3)—CH(CH3)—C2H5, —C3H6—C(CH3)2—C2H5, —C2H4—C(CH3)2—C3H7, —CH2—C(CH3)(C2H5)2, —C2H4—C(C2H5)3, —C2H4—C(CH3)2—C3H7, —CH2—C(CH3)2—C4H9, —C(C2H5)2—C3H7, —C(CH3)(C3H7)—C3H7, —C(CH3)(C2H5)—C4H9, —C(CH3)(—C2H5)—C4H9, —C(CH3)2—C5H11, —C2H4—C(CH3)2—CH(CH3)2, —CH2—C(CH3)2—C(CH3)3, —C(C2H5)2—CH(CH3)2, —C(CH3)(C3H7)—CH(CH3)2, —C(CH3)(C2H5)—C(CH3)3, —CH2—C(CH3)2—CH2—CH(CH3)2, —C(CH3)2—C2H4—CH(CH3)2, —C(CH3)2—CH2—C(CH3)3, —CH2—C(CH3)2—C(CH3)3, —C4H8—C(CH3)3, —C3H6—C(CH3)2—C2H5, —C2H4—C(CH3)2—C3H7, —C2H4—CH(CH3)—C(CH3)3, —CH2—C(CH3)2—C(CH3)3.
“Aryl” refers to an unsaturated aromatic carbocyclic group of from 6 to 12 carbon atoms inclusively having a single ring (e.g., phenyl) or multiple condensed rings (e.g., naphthyl or anthryl). Exemplary aryls include phenyl, pyridyl, naphthyl and the like.
The term “glycosyl donor” as used herein relates to a saccharide having a suitable leaving group at the anomeric position, which may be used as reactant for the coupling reaction. A donor or glycosyl donor refers to a saccharide that forms a glycal, or a saccharide comprising an epoxide or orthoester group or a saccharide that contains a leaving group at the reducing end. Suitable leaving groups include halogen, —O—C(═NH)—CCl3, —O—C(═NPh)-CF3, —OAc, —SR5, —SO-Ph, —SO2-Ph, —O—(CH2)3—CH═CH2, —O—P(OR5)2, —O—PO(OR5)2, —O—CO—OR5,
wherein R5 represents an alkyl or aryl group.
The term “glycosyl acceptor” as used herein relates to a carbohydrate molecule or a saccharide that contains at least one free hydroxy or amine function and is capable of forming a glycosidic bond with a glycosyl donor under suitable reaction conditions.
The term “protecting group” or “protective group” as used herein refers to commonly used groups in organic synthesis, preferably used for protection of amines, hydroxyl groups, thiols, imines, carbonyls, carboxyls or other common functional groups, and particularly preferred for amines and hydroxyl groups. The protecting groups are characterized in that they are stable under reaction conditions applied during the synthesis, i.e. they are not cleaved off or undergo undesired side reactions and prevent any reaction of the protected functional group they are bonded to. Additionally, the protecting groups are selected to not hinder or to not affect the performed reaction steps in terms of yield or stereoselectivity.
Preferred protecting groups for hydroxyl groups are acetyl, phenyl, benzyl, isopropylidene, benzylidene, benzoyl, p-methoxybenzyl, p-methoxybenzylidene, p-methoxyphenyl, p-bromobenzylidene, p-nitrophenyl, allyl, allyloxycarbonyl, monochloroacetyl, isopropyl, p-bromobenzyl, dimethoxytrityl, trityl, 2-naphthylmethyl, pivaloyl, triisopropylsilyl, tert-butyldimethylsilyl, tert-butyldiphenylsilyl, tert-butylmethoxyphenylsilyl, triethylsilyl, trimethylsilyl, 2-trimethylsilylethoxymethyl, 9-fluorenylmethoxycarbonyl, tert-butyloxycarbonyl, benzyloxymethyl, methyloxymethyl, tert-butyloxymethyl, methoxyethyloxymethyl, and levulinoyl.
The protecting groups can be differentiated in “permanent protecting groups” and “temporary protecting groups”. Permanent protecting groups are protecting groups that are stable during the entire synthesis and that can be efficiently removed at the late stage of the synthesis. In this case, permanent protecting groups are masking the hydroxyl groups and amino groups, if present, during the entire synthesis. Preferably permanent protecting groups are benzyl, benzoyl, acetyl, allyloxycarbonyl (alloc) and benzyloxycarbonyl group (Cbz).
The term “temporary protecting group” as used herein relates to a protecting group of a protected saccharide which may be selectively removed from the protected saccharide, wherein the remaining further protecting groups or the “permanent protecting groups” are not removed under the same conditions. Preferably, removal of a temporary protecting group allows conversion of the protected saccharide to a saccharide having at least one unprotected hydroxyl group or amine function. Thus, a glycosyl acceptor for use in a subsequent coupling reaction may be provided by removing a temporary protecting group of the protected saccharide.
The temporary protecting groups are generally orthogonal protecting groups that can be selectively removed at different levels of the synthesis to free hydroxyl groups for subsequent introduction of different substituents, including monosaccharides, other protecting groups or other residues present on the molecule. Temporary protecting groups are preferably selected from, but are not restricted to: allyl, p-methoxybenzyl, 2-naphthylmethyl, tri-isopropylsilyl, tert-butyldimethylsilyl, tert-butylmethoxyphenylsilyl, triethylsilyl, trimethylsilyl, 2-trimethylsilylethoxymethyl, 9-fluorenylmethoxycarbonyl and levulinoyl.
The ingenious choice of protecting groups allows expedient access to a library of saccharides. It is apparent for a skilled person to choose the protecting groups in such a manner that they can be removed from the saccharide without cleaving the saccharide from the solid support.
The term “deprotection” as used herein relates to the removal of one or more protecting groups of a molecule functionalized with one or more protecting groups. The deprotection step of a coupling cycle as described herein preferably relates to the removal of a specific protecting group of a protected carbohydrate molecule. As a carbohydrate molecule typically exhibits several hydroxyl groups it is preferred that only one of said hydroxyl groups participates as nucleophile in the glycosylation reaction. Therefore, orthogonal protecting group strategy is typically applied to provide carbohydrate molecules with only one free hydroxyl group, wherein the protecting groups of the remaining hydroxyl groups are not removed. Orthogonal protecting group strategies are often the key step of a successful regioselective functionalization of a carbohydrate molecule. Suitable protecting groups and orthogonal protecting group strategies are therefore well known to the skilled person.
The term “capping” as used herein relates to blocking or capping of free hydroxyl groups by a highly reactive blocking group to avoid elongation of failure sequences of the oligo- or polysaccharide during the synthesis cycles. Deletion sequences missing just one sugar unit (n−1) are the most difficult to separate from the desired product and arise from incomplete coupling steps during any coupling cycle of the sequence. The oligosaccharide chains that fail to couple during one cycle may be successfully glycosylated during the following elongation steps. Therefore, a severe purification problem may exist at the end of the synthesis. To avoid the elongation of failure sequences, a capping step (i.e., a blocking step) may be included into the coupling cycle. After each completed coupling, a highly reactive blocking group can be used to cap any free hydroxyl group. For example, benzyl trichloroacetimidate can be employed as a capping reagent (activated with TMSOTf) to yield benzyl ethers in positions that were not glycosylated and render them unreactive throughout the synthesis. Using this straightforward capping step, the purification of the finished oligosaccharide products may be greatly simplified, since the presence of (n−1)-deletion sequences will be minimized.
The term “solid support” as used herein refers to an insoluble, functionalized, polymeric material to which saccharides or other reagents may be attached or immobilized, directly or via a linker bearing an anchoring group, allowing saccharides to be readily separated (by washing, filtration, centrifugation, etc.) from excess reagents, soluble reaction by-products, or solvents. The solid support has preferably the form of a resin bead or CPG (Controlled Pore Glass) bead.
The inventors of the present invention considered the following key issues for the development and improvement of an automated oligo- and polysaccharide synthesizer: design of an overall synthesis strategy with either the reducing or the non-reducing end of the growing carbohydrate chain attached to the support, selection of a polymer and linker that are inert to all reaction conditions during the synthesis but cleaved efficiently when desired, a protecting group strategy consistent with the complexity of the target oligo- or polysaccharide, stereospecific and high yielding glycosylation reactions, and a device capable of performing repetitive chemical manipulations at variable temperatures.
Surprisingly, it has been found that a device for automated synthesis of oligo- and polysaccharides on a solid support comprising a reaction vessel, a reagent storing component, a reagent delivery system, a cooling device for cooling the reaction vessel, and a pre-cooling device for pre-cooling the reagents to be supplied, resolves the above objective.
Thus, the present invention relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
According to the present invention, the device for automated synthesis of oligo- or polysaccharides on a solid support comprises an improved cooling system to prevent fluctuations in temperature of a reaction mixture which may otherwise result in loss of sensitive intermediates and reagents, in particular in the coupling steps of the synthesis cycles. Thus, with the cooling system of the device of the present invention unfavorable temperature spikes may be effectively prevented during the transfer of building blocks and activators to the reaction vessel. Furthermore, the cooling system of the present invention allows for advantageous temperature adjustment of the reaction vessel and further of the reaction mixture to prevent decomposition of the reactants, sensitive intermediates and desired products at different thermal stages of the synthesis cycles. According to the present invention the improved cooling system consists of a cooling device and a pre-cooling device. The device of the present invention for automated synthesis of oligo- or polysaccharides on a solid support therefore comprises a cooling device for cooling the reaction vessel and a pre-cooling device for pre-cooling the reagents to be supplied for control of the temperature of one or more reagents and/or the reaction mixture during one or more synthesis steps of the synthesis cycles to prevent decomposition of the sensitive intermediates and reagents. Of course, the cooling device for cooling the reaction vessel and the pre-cooling device for pre-cooling the reagents can be combined to a single cooling device for cooling both, the reaction vessel and the reagents to be supplied. Most preferably the one cooling device for both is a Peltier cooling element. Most preferably the one cooling device for both is a thermoelectric cooling element.
As used herein, the term >>pre-cooling the reagents <<refers to the cooling of the reagent storing component and/or the cooling of the reagent delivery system to the reaction vessel and preferably to the cooling of the reagent delivery system and more preferably to the cooling of the reagent storing component and the cooling of the reagent delivery system.
As used herein, the term >>pre-cooling device <<refers to a cooling device adapted for cooling of reagents during delivery of reagents from a reagent storing component to a reaction vessel and further adapted for cooling of reagents just before the addition of said reagents to the reaction vessel. Thus, as used herein, the pre-cooling device is configured for pre-cooling reagents directly before addition to the reaction mixture. Thus, the term pre-cooling device herein does not relate to a cooling means for cooling the reagent storing component or one or more reagent containers. However, the device according to the present invention may comprise additional cooling means, for example, for cooling of the reagent storing component or one or more reagent or solvent vessels. However, such cooling means are not a pre-cooling device in accordance with the present invention. Herein, the pre-cooling device is defined as a cooling device that is installed between a reagent delivery system and a reaction vessel, preferably at a minimum distance to the reaction vessel in order to allow cooling of reagents during the delivery to the reaction vessel.
According to a preferred embodiment of the present invention, the device for automated synthesis of oligo- and polysaccharides on a solid support may further comprise a microwave generator component to enable rapid microwave-assisted blocking/deblocking synthesis steps, such as deprotection or capping steps that allow for efficient and rapid syntheses in different batch sizes. Use of microwave radiation during part of the synthesis cycles may significantly shorten the time to achieve complete conversion, which is important for scale-up.
According to the present invention the device for automated synthesis of oligo- and polysaccharides on a solid support comprises a reaction vessel. The reaction vessel may be made of any material known in the art which is chemically and physically compatible with the reagents used and reaction conditions applied in the automated synthesis of oligo- and polysaccharides on a solid support. Examples of reaction vessel materials include, but are not limited to, glass, quartz, PTFE (Teflon), polypropylene. In preferred embodiments the reaction vessel is inter-changeable. In preferred embodiments the reaction vessel is made of fluoropolymers such as PFA for improved chemical resistance and ease of swapping reactions vessels of different sizes.
The reaction vessel of the present invention is adapted for holding a reaction mixture. The reaction vessel therefore comprises an inner cavity or effective loading space for performing one or more synthesis steps of the synthesis cycles to obtain the desired oligo- or polysaccharide. The reaction vessel is adapted to enable performance of one or more synthesis steps or even all of the synthesis steps of the synthesis cycles in an isolated, anhydrous and inert atmosphere. These steps may include, but are not limited to, coupling steps, washing steps, deprotection steps, capping steps and decoupling from the solid phase resin. The solid support or solid phase resin may be initially loaded into the reaction vessel. With other words the solid support or solid phase resin may be loaded into the inner cavity or effective loading space of the reaction vessel. The loading of the reaction vessel with the solid phase resin may be performed as part of a pre-automation process but may also be part of the automation process. Thus, the loading with the solid support may be also performed in an automated manner. The solid support may be provided in form of insoluble resin bead(s) and is preferably a functionalized resin suitable for oligo- and polysaccharide synthesis on a solid support, such as a resin equipped with an appropriate linker or in particular a polystyrene-based resin functionalized with an appropriate linker. Several suitable functionalized solid phase resins for oligo- or polysaccharide synthesis on a solid support have been described in the prior art. Examples of functionalized solid phase resins suitable for use with the device of the present invention are described further below.
Thus, it is preferred that the reaction vessel is adapted for receiving a solid support. Therefore, the reaction vessel preferably comprises an inner chamber or effective loading space for performing one or more synthesis steps of the synthesis of oligo- and polysaccharides on a solid support, preferably in an isolated, anhydrous and inert atmosphere. It is preferred that the inner cavity or effective loading space holds between 1 mL and 100 mL solvent, more preferably 5-20 mL solvent. It is preferred that the inner cavity or the effective loading space is sized to accommodate the solid support, reagents and solvent.
Therefore the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
For performing the coupling reactions appropriate building blocks and activators are supplied or added to the reaction vessel. Preferably, the building blocks and activators are supplied or added to the reaction vessel already containing the solid support or solid phase resin. The coupling reactions preferably take place inside the reaction vessel followed by appropriate deprotection, capping and/or washing steps. All of these synthesis steps and treatments in the synthesis cycles are preferably performed inside of the reaction vessel of the device of the present invention. The synthesis cycles are repeated as often as necessary to achieve the desired length of the desired oligo- or polysaccharide. The synthesis cycle is preferably repeated at least three times, more preferably at least four times or more preferably more than four times for obtaining an oligo- or polysaccharide.
For supplying liquids, solutions and/or gases the reaction vessel of the device of the present invention may further comprise one or more inlets, for example, for supplying washing solvents or washing solutions, building blocks or building block solutions, activators or activator solutions, capping solutions, deprotection solutions and inert gas, and may further comprise one or more outlets, for example, for discharging the liquids or solutions after each chemical reaction and/or also ventilation exits for inert gas or other gases from the reaction mixture.
In preferred embodiments of the present invention the one or more inlets may also function as one or more outlets, that means one or more inlets for supplying reagents, solvents, reaction mixtures, inert gas and the like can also be used to remove a solution, inert gas, reaction components and the like from the device for automated synthesis. In such embodiments one or more technical means such as one or more valves, valve assemblies, one or more vents, one or more manifolds and/or similar technical means may be located and mounted upstream to the one or more inlets of the reaction vessel. For example, by implementing a valve assembly or one or more valves in the device of the present invention the delivery of liquids, solutions and/or gases and also the discharging of liquids, solutions and/or gases after or during each chemical reaction or treatment may be realized through one inlet of the reaction vessel only or through two, three or more inlets of the reaction vessel. By implementation of technical means such as valves, valve assemblies, vents, manifolds or similar technical means, the total number of in- and outlets of the reaction vessel may be reduced.
Furthermore, technical means such as valves, valve assemblies, vents and manifolds and similar technical means may be electronically coupled to a computing device comprising at least one processor and therefore may be under control of a computing device comprising at least one processor. Thus, the delivery of the liquids, solutions and/or gases and also the discharging of liquids and solutions may be under control of the computing device comprising the at least one processor. The computing device comprising the at least one processor may be configured to control said technical means in order to deliver liquids, solutions and/or gases to the reaction vessel and further to discharge liquids and solutions from the reaction vessel in a controlled and automated manner to allow automation of the synthesis of oligo- or polysaccharide on a solid support with the device of the present invention.
The reaction vessel may further comprise one or more openings or apertures for insertion of various other components or technical means. For example, the reaction vessel may further comprise an opening or aperture for insertion of a temperature probe or a temperature sensor for monitoring and measuring the temperature inside of the reaction vessel. Monitoring and measuring the temperature inside of the reaction vessel thereby also means monitoring and measuring the temperature of the reaction mixture during one or more or even all synthesis steps of the synthesis cycles. Thus, it is preferred that the reaction vessel further comprises at least one opening or aperture for insertion of a temperature sensor for monitoring and measuring the temperature inside of the reaction vessel.
The one or more inlets of the reaction vessel may be located at various positions of the reaction vessel body. In preferred embodiments of the present invention the reaction vessel may comprise one or more inlets at the top of the reaction vessel, for example, for delivery of washing solvents or washing solutions, building blocks or building block solutions, and activators or activator solutions and may further comprise one or more outlets at the top of the reaction vessel, for example, for exits for inert gas or other gases and may further comprise one or more inlets at the bottom of the reaction vessel, for example, for delivery of capping solutions, deprotection solutions and inert gas and may further comprise one or more outlets for discharging the liquids or solutions after each chemical reaction or after each washing step. As mentioned above, by implementing further technical means such as one or more valves, valve assemblies or similar technical means, these one or more inlets may also function as outlets for the liquids, solution and/or gases.
Thus, in preferred embodiments of the present invention the reaction vessel comprises one or more inlets at the top of the reaction vessel and one or more inlets at the bottom of the reaction vessel to enable two delivery methods for solvents and reagents, one from the top and another from the bottom of the reaction vessel. The usage of two different ports allows for the separation of incompatible reagents such as acids and bases, which may produce salts when combined. Over time these salts may build up and block tubing that may corrode components of the device of the present invention, which may lead to costly repairs. It is therefore preferred that the solutions to remove the temporary protecting groups (for example protecting groups such as Fmoc, Lev, CIAc, and NAP) and acetyl capping solutions are delivered via the one or more bottom inlets or bottom port of the reaction vessel. These reactions are desired to be performed rapidly and solutions are provided in excess, so these solutions will be pushed into the reaction vessel for example by pressurized inert gas such as argon. The inert gas inlet may serve for a dual purpose to not only deliver the reagents, but to efficiently mix the reaction. In addition, the one or more bottom inlets may serve to remove all the reagents and solutions from the reaction vessel. Oppositely, the activators or activator solutions and the building blocks or building block solutions are preferably delivered through the one or more top inlets or top port of the reaction vessel. These reagents are more valuable and are required to be delivered in a controlled stoichiometry, so these are delivered preferably dropwise, for example, via a syringe pump system.
In preferred embodiments of the present invention the reaction vessel may comprise only one inlet at the bottom of the reaction vessel, for example, for delivery of capping solutions, deprotection solutions and inert gas and for discharging the liquids or solutions after each chemical reaction or after each washing step and one or more inlets at the top of the reaction vessel, for example, for delivery of washing solvents or washing solutions, building blocks or building block solutions, and activators or activator solutions. The reaction vessel may further comprise openings or apertures at the top of the reaction vessel for insertion of, for example, a temperature probe or a temperature sensor. The reaction may further comprise an exhaust gases exit at the top of the reaction vessel.
In preferred embodiments of the present invention the reaction vessel may comprise at least three inlets/outlets, preferably four inlets/outlets (601, 602, 645, 655) at the top of the reaction vessel, for example, one inlet for delivery of washing solvents or washing solutions, one inlet for delivery of building blocks or building block solutions and one inlet for delivery of activators or activator solutions and preferably a further outlet for the exhaust of gases and/or mixing gas (655). The separate and distinct delivery of the building blocks and activators to the microwave transparent reaction vessel is advantageous for preventing a contacting of the building blocks and activators before supplying the building blocks and activators to the reaction mixture inside of the reaction vessel. It is particular preferred that the building blocks or building block solutions and the activators or activator solutions are not mixed or merged with each other before delivery to the reaction vessel. It is further advantageous that the washing solvents or washing solutions are separately supplied to the reaction vessel to allow rapid delivery of washing solvents or washing solution in a larger amount and to ensure well distribution of the washing solvents or washing solutions inside of the reaction vessel. For example, a channel for supplying the washing solvents or washing solution may be used to supply the washing solvents or washing solution to the reaction vessel. Such a channel may be adapted for spraying the washing solvents or washing solutions by splitting the liquid among a series of holes at the tip of the channel. The channel may also comprise a conical end to assure complete dropping of the washing solvents or washing solutions. Such a channel for delivery of washing solvents or washing solution allows to effectively wash-off other reagent solutions, reagents or adhered solid support from the inner walls of the reaction vessel. In contrary, the building blocks and activators are preferably supplied directly into the reaction mixture in a dropwise manner.
In embodiments of the present invention wherein the reaction vessel comprises one or more inlets at the bottom of the reaction vessel or only one inlet at the bottom of the reaction vessel it is preferred that the effective loading space or inner chamber of the reaction vessel is fenced by the bottom inlet. The bottom compartment may prevent canalization of fluid through a frit. A frit allows for dispersion of inert gas bubbling for mixing purposes. The frit may also ensure that the solid support remains inside of the reaction vessel. Thus, in preferred embodiments of the present invention the reaction vessel may further comprise a frit. It is preferred that the frit is located in the bottom compartment of the reaction vessel. Thus, to prevent solid support from being drawn from the bottom inlet, the end in the reaction vessel may be fitted with a frit or a filter.
Preferably the reaction vessel is made of a material such as glass, quartz, PTFE (Teflon), polypropylene or fluoropolymers. A reaction vessel made of glass may be provided in form of a triple-jacketed glass reaction vessel. The reaction vessel may be provided as a glass reaction vessel surrounded by a second cavity that allows for circulation of coolant fluid to control the temperature of the reaction mixture. Thus, the reaction vessel may be provided with a cooling jacket for cooling the reaction vessel.
In preferred embodiments of the present invention the reaction vessel may be provided as interchangeable reaction vessel. In such embodiments it is preferred that the reaction vessel may be removed from a cooling means such as a cooling jacket without interrupting the flow of a circulating coolant fluid.
In such embodiments the reaction vessel may be removed for example for loading with solid support or for discharging the solid support. Furthermore such an interchangeable reaction vessel allows use of various reaction vessels of different sizes for different batch sizes.
Therefore the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The inventors have surprisingly found that a reaction vessel made of fluoropolymers such as polytetrafluoroethylene (PTFE), perfluoroalkoxy alkanes (PFA), fluorinated ethylene propylene (FEP), ethylene tetrafluoroethylene (ETFE) or a reaction vessel comprising a coating of polytetrafluoroethylene (PTFE), perfluoroalkoxy alkanes (PFA), fluorinated ethylene propylene (FEP), ethylene tetrafluoroethylene (ETFE) is particularly suitable for the device of the present invention for the synthesis of oligo- and polysaccharides on a solid support.
The inventors of the present invention have found that the change in the manufacturing of the reaction vessels from silicate glass to fluoropolymer allows on the one hand integration of a microwave device into the synthesis cycle, and on the other hand improves chemical resistance, as well as eases of swapping reaction vessels of different sizes. Thus, it is advantageous to switch from a glass reaction vessel to one made of fluoropolymers such as perfluoroalkoxy alkanes (PFA). Microwave transparency, improved flow, minimal resin adherence, thermal resistance, and chemical resistance are among the many properties that PFA excels over glass. Typical silicate glass contains hydroxyl groups, which creates a hydrophilic surface. During the synthesis cycles, the resin often adheres to glass walls above the reaction solution causing deletion sequences and mixtures in the final product. To prevent adhesion problems, regular silanization of the glass reactor is necessary. On the other hand, PFA reactors have better hydrophobic properties and are non-adherent to the resin. This allows for reaction vessels made from PFA materials to tolerate a wider range of chemical reactions that are incompatible with silane coating on glass. An additional advantage is the physical durability of the PFA reactor compared to glass. Typically, AGA synthesizers are utilized for high throughput synthesis and are in constant use, so durable components are preferred.
In preferred embodiments of the present invention the reaction vessel is made of perfluoroalkoxy alkanes (PFA). In further preferred embodiments of the present invention the reaction vessel comprises a coating of perfluoroalkoxy alkanes (PFA). Perfluoroalkoxy alkanes are copolymers of tetrafluoroethylene (C2F4) and perfluoroethers (C2F3ORf, where Rf is a perfluorinated group such as trifluoromethyl (CF3).
Therefore the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
In preferred embodiments of the present invention the reaction vessel may further comprise a cap adapted for closing the reaction vessel for protecting the inner chamber or effective loading space from the external atmosphere. Thus, a cap may be provided for closing the reaction vessel in order to provide an isolated, anhydrous and inert atmosphere inside of the reaction vessel.
According to the present invention the device for automated synthesis of oligo- or polysaccharides on a solid support comprises a reagent storing component. The device for automated synthesis of oligo- or polysaccharides on a solid support of the present invention may comprise one or more reagent storing components. The device for automated synthesis of oligo- or polysaccharides on a solid support of the present invention may comprise at least one reagent storing component. The reagent storing component or the one or more reagent storing components are preferably adapted for storing the building blocks and/or building block solutions, activators and/or activator solutions, washing solvents and/or washing solutions, deprotection solutions and/or capping solutions. The reagent storing component or the one or more reagent storing components may comprise one or more reagent containers or may comprise a plurality of reagent containers. The reagent storing component or the one or more reagent storing components may comprise one or more reagent containers for storing building blocks, one or more reagent containers for storing building block solutions, one or more reagent containers for storing activators, one or more reagent containers for storing activator solutions, one or more reagent containers for storing washing solvents and/or washing solutions, one or more reagent containers for storing deprotection solutions and one or more reagent containers for storing capping solutions. The reagent storing component or the one or more reagent storing components are preferably adapted for storing reagents and solvents in an anhydrous and inert atmosphere. In preferred embodiments of the present invention the reagents and solvents are stored under argon pressure. In preferred embodiments the reagent storing component or the one or more reagent storing components are connected to an inert gas delivery system or gas distribution system. The gas delivery system or gas distribution system may provide inert gas, such as argon, to the reagent storing component or the one or more reagent storing components. The inert gas delivery system or gas distribution system may provide inert gas, such as argon, to each of the containers of the reagent storing component or the one or more reagent storing components. Thus, in preferred embodiments of the present invention each of the containers of the reagent storing component or the one or more reagent storing components may be connected to an inert gas delivery system or gas distribution system.
The containers may be made of any suitable chemical resistant material known in the art which is suitable for storing chemical reagents and/or solutions and furthermore suitable for storing the building blocks and/or building block solutions, activators and/or activator solutions, washing solvents or washing solutions, deprotection solutions and also capping solutions. The containers may preferably be adapted for storing the reagents in an anhydrous and inert atmosphere, for example, under argon pressure. For example, synthesis-ready building blocks may be pre-weighed and either dissolved in the appropriate anhydrous solvent or kept as solids and placed in sealed vials, for example, on a 64-position carousel or a 4-position means (e.g. test tube type containers) were a solution of building block (e.g. up to 8 mL of the appropriate concentration) is coupled to the system by a multiport valves or similar technical means. Preferably a cap seals the reaction vessel which has an inlet for inert gas, such as argon, providing an anhydrous atmosphere and an outlet for the building block solution extraction. The extraction tube may reach the bottom container and may be allowed to take out the required volume of building block solutions. The building blocks are preferably those that can be synthesized in large quantities, are stable upon storage for extended periods of time, and upon activation result in very high coupling yields with excellent stereo-control. Solvents and reagents may for example be placed in various sizes of glass bottles and kept under inert gas, for example, under argon pressure.
Preferably the device for automated synthesis of oligo- and polysaccharides on a solid support comprises a reagent storing component for storing building blocks and/or building block solutions, activators and/or activator solutions, washing solutions and/or washing solvents and/or deprotection solutions. Preferably the device for automated synthesis of oligo- and polysaccharides on a solid support comprises a reagent storing component for storing one or more reagents and/or reagent solution and/or solvents. The reagents and/or reagent solutions preferably comprise building blocks, building block solutions, activator, activators solutions, washing solutions, washing solvents and deprotection solutions. Preferably the device for automated synthesis of oligo- and polysaccharides on a solid support comprises a reagent storing component for storing building blocks or building block solutions, activators or activator solutions, washing solutions or washing solvents, deprotection solutions and capping solutions.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising: (a) a reaction vessel,
The device of the present invention may comprise one or more liquid, solution or inert gas delivery systems for driving the flow of liquids or gases to the reaction vessel.
According to the present invention the device for automated synthesis of oligo- or polysaccharides on a solid support comprises a reagent delivery system. The device of the present invention may comprise at least one reagent delivery system. Preferably the device of the present invention comprise a reagent delivery system adapted for delivery of building blocks or building block solutions, activators or activator solutions, washing solvents or washing solutions, deprotection solutions, capping solutions and inert gas to the reaction vessel.
Preferably the device of the present invention comprises a reagent delivery system adapted for receiving building blocks or building block solutions, activators or activator solutions, washing solvents or washing solutions, deprotection solutions and capping solutions from the reagent storing component. The device of the present invention may also comprise one or more reagent delivery systems. The reagent delivery system may comprise one or more reagent delivery sub-systems or reagent delivery sub-components for delivery of one or more of the one or more reagents, solutions and/or reagent solution to the reaction vessel.
Therefore, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Preferably, the present invention relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Preferably the reagent delivery system connects the reagent storing component with the reaction vessel. Preferably the reagent delivery system is connected to the reagent storing component and is further connected to the reaction vessel. It is preferred that the reagent storing component and the reaction vessel are not directly connected to each other, in other words it is preferred that the reagent storing component and the reaction vessel are not in direct fluid communication with each other. Preferably the reagent delivery system is interposed between the reaction vessel and the reagent storing component. Preferably the reagent delivery system is in fluid communication with the reagent storing component and is further in fluid communication with the reaction vessel. It is preferred that the reagent delivery system receives the reagents from the reagent storing component and after receiving the reagents from the reagent storing component the reagents delivery system may deliver the reagents to the reaction vessel in order supply the reagents to the reaction mixture inside the reaction vessel.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reagent delivery system connects the reagent storing component with the reaction vessel via the pre-cooling device.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reagent delivery system connects the reagent storing component with the reaction vessel; wherein the pre-cooling device is interposed between the reaction vessel and the reagent delivery system; and wherein the pre-cooling device is in thermal communication with the reagent delivery system.
Preferably, the reagent storing component and the pre-cooling device are connected through the reagent delivery system. Preferably, at least one liquid line between the reagent delivery system and the reaction vessel is pre-cooled by the pre-cooling device located between the reagent delivery system and the reaction vessel.
The reagent delivery system may be connected to the reaction vessel through one or more inlets of the reaction vessel for delivery of the reagents and/or reagents solution and/or solvents to the reaction vessel through the one or more inlets of the reaction vessel. The reagent delivery system may be connected to the reaction vessel through one or more reagent delivery lines. Thus, the reagent delivery system may be adapted to deliver reagents and/or reagent solutions and/or solutions and/or solvents to the reaction vessel and may be further adapted to supply the reagents and/or reagent solution and/or solutions or solvents through the one or more inlets of the reaction vessel. Preferably the reagent delivery system may be adapted to deliver one or more reagents and/or one or more reagent solutions and/or one or more solutions in different amounts, at different points in time and in a specific sequence or specific order, and further through specific inlets of the one or more inlets of the reaction vessel during the synthesis cycles of the automated synthesis of oligo- and polysaccharides on a solid support. It is therefore preferred that the reagent delivery system comprises suitable technical means, preferably suitable technical means electronically coupled to a computing device comprising at least one processor, for delivery of one or more reagents and/or one or more reagent solutions and/or one or more solutions in different amounts, at different points in time and in a specific sequence or specific order during the synthesis cycles of the automated synthesis of oligo- and polysaccharides on solid support. The reagent delivery system may comprise a pump system or one or more pumps such as syringe pumps, peristaltic pumps or other suitable pumps and may further comprise one or more valves or one or more valve assemblies, one or more manifolds, one or more distributing components and similar suitable technical means. It is preferred that the pump system or the one or more pumps, the one or more valves or the one or more valve assemblies, the one or more manifolds and/or the one or more distributing components and similar technical means are under control of a computing device comprising at least one processor.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reagent delivery system connects the reagent storing component with the reaction vessel; wherein the reagent delivery system comprises a pump system, wherein the pre-cooling device is interposed between the pump system and the reaction vessel. Preferably, the pre-cooling device is located downstream to the pump system and upstream to the reaction vessel.
The device of the present invention may therefore comprise one or more valves or valve assemblies for regulating, directing or controlling the flow of fluids like gases or liquids. Valves or valve assemblies may be adapted for opening, closing or partially obstructing various passageways. Valves may be operated in gradual change between two or more positions, such as in two-port, three-port, four-port or in multiport valves. The device of the present invention may comprise one or more fluidic valves operably connected to one or more components of the device for automated synthesis of oligo- and polysaccharides on a solid support. Each fluidic valve of the device of the present invention may be a rotary valve, solenoid valve block or other multi-port valve or valve system or other suitable valves known to those skilled in the art. The device of the present invention may further comprise one or more pumps such as syringe pumps, peristaltic pumps or other pumps known to those skilled in the art which may be operably connected to one or more fluidic valves or valve assemblies of the device of the present invention.
In preferred embodiments of the device of the present invention the reagent delivery system may comprise one or more valves, preferably one or more fluidic valves, more preferably one or more rotary valves, and even more preferably one or more rotary valves with 3, 4, 5, 6, 7, 8, 9 or 10 ports. Preferably the reagent delivery system may comprise one or more valves such as one or more rotary valves, one or more solenoid valve blocks or other multiport valves. The reagent delivery system may further comprise one or more pumps or a pump system.
Preferably, the reagent delivery system comprises at least one syringe pump.
Preferably, the reagents may be delivered via a syringe pump system. Preferably the reagents may be delivered via a syringe pump system as a component of the reagent delivery system. Preferably, the syringe pump system may be a component of the reagent delivery system.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reagent delivery system connects the reagent storing component with the reaction vessel; wherein the reagent delivery system comprises at least one syringe pump system for delivery of reagents, wherein the pre-cooling device is interposed between the at least one syringe pump system and the reaction vessel.
Preferably, the pre-cooling device is located downstream to the syringe pump system and upstream to the reaction vessel.
In preferred embodiments of the present invention a syringe pump may drive the fluids within the reagent delivery system. The syringe pump and the reagent delivery system may be connected through one or more loop lines. Loop lines allow for careful delivery of sensitive and/or corrosive chemical solutions. The resting volume of the loops is defined as a function of the tubing length. A driving solvent may be taken to fill up the loops ahead the withdrawing of chemical solution from the reagent delivery system. This avoids the direct contact of the reagents with the syringe pump, which prevents pump deterioration and cross-contamination. The loops may be made from an inert material such as, for example, Teflon, poly-(tetrafluoroethylene) (PTFE), polypropylene and the like. The size of the loops may be varied. The exact size will depend on the capacity of the syringe pump and the amount of reagent to be delivered to the reaction vessel. The size of each loop will also depend on the nature of the reagent to which it is associated. For example, if the reaction vessel is 20 mL, then a loop sized from about 1 to 5 mL may be used, preferably from about 2 to 4 mL. Each loop may be sized the same or different. For example, loops attached to building blocks may be smaller than those attached to basic reagents such as the deprotection or capping reagents as the quantity of the former used during any synthesis step is relatively small compared to the amount of such basic reagents.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reagent delivery system connects the reagent storing component with the reaction vessel; wherein the reagent delivery system comprises at least one syringe pump system for delivery of reagents, wherein the syringe pump system is connected to one or more loop lines having a resting volume which is defined as a function of the tubing length, wherein the pre-cooling device is interposed between the reagent delivery system and the reaction vessel, wherein the pre-cooling device is located downstream to the one or more loop lines and upstream to the reaction vessel.
In preferred embodiments of the present invention the reagent delivery system may be connected to a pre-cooling device. With other words, in preferred embodiments of the present invention the reagent delivery system may be connected to a pre-cooling device for pre-cooling the reagents to be supplied. The reagent delivery system device may be adapted for receiving reagents from the reagent storing device and may be further adapted for delivery of the received reagents to a pre-cooling device for pre-cooling the reagents to be supplied and may be further adapted for delivery of the pre-cooled reagents to the reaction vessel. Thus, in preferred embodiments of the present invention the reagent delivery system may be adapted for receiving one or more reagents such as building blocks and activators and/or one or more reagent solutions such as building block solutions and activator solutions and/or one or more washing solutions and/or one or more deprotection solutions from a reagent storing component or one or more reagent storing components and may be further adapted for delivery of the received one or more reagents and/or one or more reagent solutions and/or one or more washing solution and/or one or more deprotection solutions to a pre-cooling device for pre-cooling the reagents to be supplied and may be further adapted to deliver the pre-cooled one or more reagents and/or one or more reagent solutions and/or one or more washing solutions and/or one or more deprotection solutions to the reaction vessel.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
the reagent delivery system being connected to the pre-cooling device, the reagent delivery system being adapted for receiving reagents from the reagent storing component and being adapted for delivery of the received reagents to the pre-cooling device and being adapted for delivery of the pre-cooled reagents to the reaction vessel.
Thus, the reagent delivery system preferably connects the reagent storing component with the reaction vessel; wherein the pre-cooling device is interposed between the reaction vessel and the reagent delivery system; and wherein the pre-cooling device is in thermal communication with the reagent delivery system.
In preferred embodiment of the present invention the reagent delivery system may be adapted for delivery of one or more of the reagents and/or reagents solutions and/or washing solutions and/or deprotection solution to the pre-cooling device for pre-cooling the reagents to be supplied. In such embodiments it is particularly preferred that at least the building blocks and the activators are delivered to the pre-cooling device for pre-cooling the reagents to be supplied. In further preferred embodiments the reagent delivery system may also be adapted for delivery of the washing solutions or washing solvents to the pre-cooling device for pre-cooling the reagents to be supplied.
In preferred embodiments of the present invention the reagent delivery system may be in thermal communication with a pre-cooling device for pre-cooling the reagents to be supplied. In further preferred embodiments of the present invention one or more delivery lines connecting the reagent delivery system and the reaction vessel may be in thermal communication with a pre-cooling device for pre-cooling the reagents to be supplied. With other words, it is preferred that the reagent delivery system and the reaction vessel are connected by tubing which is in thermal communication with a pre-cooling device for pre-cooling the reagents to be supplied. Thus, in preferred embodiments of the present invention the reagent delivery system may be adapted for delivery of one or more reagents to the reaction vessel, the reagent delivery system in thermal communication with a pre-cooling device for pre-cooling the reagents to be supplied, wherein the one or more reagents are pre-cooled by the pre-cooling device before entering the reaction vessel, and preferably wherein the one or more reagents are pre-cooled through contact cooling by the pre-cooling device for pre-cooling the reagents to be supplied.
In preferred embodiments of the present invention the reagent delivery system may be interposed between a pre-cooling device and the reagent storing component. In preferred embodiments of the present invention the reagent delivery system is connected to the reagent storing component and is further connected to a pre-cooling device. It is particularly preferred that the reagent storing component and the pre-cooling device are not directly connected to each other. In other words it is preferred that the reagent storing component and the pre-cooling device are connected through the reagent delivery system. It is further preferred that the pre-cooling device for pre-cooling the reagents to be supplied connects the reagent delivery system with the reaction vessel. Thus, in particularly preferred embodiments of the present invention the reaction vessel, the pre-cooling device, the reagent delivery system and the reagent storing device are successively connected in the following sequence: reaction vessel—pre-cooling device—reagent delivery system—reagent storing device. With other words it is preferred that the reaction vessel, the pre-cooling device, the reagent delivery system and the reagent storing device are successively connected in the following sequence: reagent storing device—reagent delivery system—pre-cooling device—reaction vessel.
As already described above in preferred embodiments of the present invention the reaction vessel may comprise one or more inlets at the top of the reaction vessel and may comprise one or more inlets at the bottom of the reaction vessel. In further preferred embodiments the reaction vessel may comprise one or more inlets at the top of the reaction vessel and may comprise only one inlet at the bottom of the reaction vessel. The reagent delivery system may be connected to the reaction vessel through the one or more inlets at the top of the reaction vessel and/or through the one or more inlets at the bottom of the reaction vessel. In preferred embodiments of the present invention the reagent delivery system may be adapted to deliver building blocks or building block solutions, activators or activator solutions, and washing solvents or washing solutions through the one or more inlets at the top of the reaction vessel. The reagent delivery system may be further adapted to deliver deprotection solutions and capping solutions through the one or more inlets at the bottom of the reaction vessel. The reagent delivery system may be further adapted to deliver inert gas, such as argon, to the reaction vessel.
The reagent delivery system may comprise one or more reagent distribution components. The reagent delivery system may comprise one or more reagent distribution components for delivery of reagents and/or solutions and/or reagent solution to the reaction vessel. Each of the reagent distribution components may be connected to the reagent storing component or one or more reagent storing components. In preferred embodiments of the present invention the reagent delivery system comprises a first and a second reagent distribution component for driving the flow of fluids or gases to the reaction vessel. In preferred embodiments of the present invention the device comprises a first reagent distribution component and a second reagent distribution component.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The first reagent distribution component may be connected to the reaction vessel through the one or more inlets on the top of the reaction vessel. Thus, the first distribution component or the top distribution component may be in fluid communication with the reaction vessel through the one or more inlets at the top of the reaction vessel. The second distribution component may be connected to the one or more inlets at the bottom of the reaction vessel. Thus, the second distribution component or bottom distribution component may be in fluid communication with the reaction vessel through the one or more inlets at the bottom of the reaction vessel.
Preferably the first distribution component or the top distribution component supplies the washing solvents, building blocks or building block solutions and activators or activator solutions to the reaction vessel. It is particularly preferred that the first distribution component or the top distribution component is connected to a pre-cooling device for pre-cooling the reagents to be supplied for delivery of pre-cooled building blocks or building block solutions and activators or activator solutions to the reaction vessel. In preferred embodiments of the present invention the first distribution component or the top distribution component may also deliver the washing solvents or washing solution to the pre-cooling device and thereafter may supply pre-cooled washing solvents or washing solution to the reaction vessel. The top distribution component may be also adapted to provide a ventilation exit for gases.
Preferably the second distribution component or the bottom distribution component supplies the deprotection solutions, capping solutions and supplies inert gas (bubbling gas) to the reaction vessel. The inert gas may be provided as bubbling gas which may be used for mixing and creating an inert and anhydrous atmosphere inside the reaction vessel. In preferred embodiments the bottom distribution component is also adapted for discharging the liquids or solution after one or more synthesis or washing steps.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
In preferred embodiments of the present invention the reagent delivery system or the one or more reagent distribution components may further comprise one or more reagent distribution sub-components. In preferred embodiments of the present invention the reagent delivery system may comprise a building block distribution component for delivery of the building blocks and/or building block solutions, an activator distribution component for delivery of the activators and/or the activator solutions and/or a washing solvent distribution component for delivery of washing solvents or washing solution, a deprotection distribution component for delivery of deprotection solution and may further comprise a capping distribution component for delivery of capping solutions to the reaction vessel.
In preferred embodiments of the present invention the top distribution component may comprise a building block distribution component, an activator distribution component and a washing solvents or washing solutions distribution component. The top distribution component may further comprise a syringe pump for driving the fluids within the top distribution component. The lines between the syringe pump and the top distribution component may be provided in form of loop lines to allow for careful delivery of sensitive and/or corrosive chemical solutions.
The resting volume of the loops is defined as a function of the tubing length. The top distribution component may further comprise a washing solvents component, wherein a driving solvent may be taken to fill up the loops ahead the withdrawing of chemical solutions from the building blocks distribution component and the activator distribution component. This avoids the direct contact of the reagents with the syringe pump, which prevents the pump deterioration and cross-contamination.
The building block distribution component may comprise one or more valves or a valve assembly or similar technical means, for example, a rotary valve that distributes the fluids within the building block distribution component. The building block distribution component is connected to the reagent storing component, preferably to a building blocks storing component which may comprise one or more building block containers or building block solution containers. Each of the building block containers or building block solution containers may be connected to the one or more valves or valve assembly or similar technical means. The building block containers of the building block storing component may be connected to a gas distribution system to provide inert gas to each of the building block containers. Thus, each of the building block containers may be stored under anhydrous and inert atmosphere. Each of the building block containers or building block solutions containers may be in fluid communication with the building block distribution component through the one or more valves or valve assembly or similar technical means. The one or more valves or the valve assembly may be further connected to the reaction vessel. Thus, the reaction vessel may be in fluid communication with the building block distribution component through the one or more valves or valve assembly or similar technical means. The reaction vessel may be in fluid communication with the building block distribution component through, for example, one or more valves or valve assembly and may be further connected through a building blocks delivery line. The building block distribution component may be adapted to deliver the building blocks to a pre-cooling device for pre-cooling the reagents to be supplied and may be further adapted to deliver pre-cooled building blocks to the reaction vessel. The building block distribution component may be also connected to a waste container and/or gas distribution system for receiving inert gas through one or more further delivery lines. The one or more valves or valve assembly or other suitable technical means for distribution of the building blocks within the building block distribution component may be under control of a processor of a computing device configured to control the distribution of the building blocks and preferably configured to control the one or more valves or valve assembly such as a rotary valve distributor. The building block distribution component may be connected to a syringe pump system, for example, through one or more valves or valve assembly and may be further connected to the syringe pump via a loop line.
The activator distribution component may comprise one or more valves or a valve assembly or similar technical means for example a rotary valve that distributes the fluids within the activator distribution component. The activator distribution component is connected to a reagent storing component, preferably an activator or activator solution storing component which may comprise one or more activator containers or activator solution containers. The activator containers of the activator storing component may be connected to a gas distribution system to provide inert gas to each of the activator containers. Thus, each of the activator containers may be stored under anhydrous and inert atmosphere. Each of the activator containers or activator solution containers may be connected to the one or more valves or valve assembly or similar technical means of the activator distribution component. Thus, each of the activator containers or activator solutions container may be in fluid communication with the one or more valves or valve assembly of the activator distribution component. The activator distribution component may be connected to the reaction vessel through the one or more valves or valve assembly or similar technical means. Thus, the reaction vessel may be in fluid communication with the activator distribution component through the one or more valves or valve assembly or similar technical means. The reaction vessel may be in fluid communication with the activator distribution component through one or more valves or valve assembly or similar technical means and may be further connected through an activator delivery line. The activator distribution component may be adapted to deliver the activators to a pre-cooling device for pre-cooling the reagents to be supplied and may be further adapted to deliver pre-cooled activators to the reaction vessel. The activator distribution component may be also connected to a waste container and/or to a gas distribution system for receiving inert gas through one or more delivery lines. The one or more valves or valve assembly or similar technical means may be under control of a processor of a computing device configured to control the distribution of the activators within the activator distribution component and preferably configured to control the one or more valves or valve assembly and similar technical means such as a rotary valve distributor. The activator distribution component may be connected to a syringe pump system, for example, through one or more valves or valve assembly and may be further connected to the syringe pump via a loop line.
The washing solvent distribution component may provide the reaction vessel with one or more washing solvents or washing solutions. Exemplary washing solvents suitable for automated synthesis of oligo- and polysaccharides on a solid support include, but are not limited to dichloromethane (DCM), tetrahydrofuran (THF) and dimethylformamide (DMF). The washing solvent distribution component is connected to a reagent storing component, preferably a washing solvent storing component. Each of the washing solvents may be stored in a respective solvent container of the washing solvent storing component. Thus, the washing solvent distribution component may be connected to a washing solvent storing component comprising one or more solvent containers. The washing solvent distribution component may be further connected to a syringe pump. One or more of the solvent containers may be connected to the syringe pump through the washing solvent distribution component. The washing solvent distribution component may comprise one or more valves or valve assembly or similar technical means which may be connected to each of the solvent containers of the washing solvents storing component. As an example, the washing solvent distribution component may comprise a multi-port valve, such as a four way magnetic valve. The washing solvents may be delivered to the reaction vessel by the washing solvent distribution component. The washing solvents may be delivered to the reaction vessel through a washing solvent delivery line. The washing solvent distribution component may be adapted to deliver the washing solvents to a pre-cooling device and may be further adapted to deliver pre-cooled washing solvents to the reaction vessel. The washing solvent containers of the washing solvent storing component may be connected to a gas distribution system to provide inert gas to the each washing solvent container. Thus, each of the washing solvent containers may be stored under anhydrous and inert atmosphere, such as under argon atmosphere. The magnetic valve may be further connected to the gas distribution system to receive inert gas and to provide and deliver inert gas to the microwave transparent reaction vessel. The one or more valves or valve assembly or similar technical means suitable for distribution of the washing solvents within the washing solvent distribution component may be under control of a processor of a computing device configured to control the distribution of the washing solvents and washing solution and preferably configured to control the one or more valves or valve assembly and similar technical means such as a magnetic valve distributor.
The bottom distribution component may comprise one or more valves such as one or more multi-port valves, or valve assemblies, or similar technical means. The bottom distribution component may comprise a deprotection distribution component for delivery of deprotection solutions to the reaction vessel and may further comprise a capping distribution component for delivery of capping solution to the reaction vessel. The bottom distribution component may be further connected to a waste container. The bottom distribution component may be further connected with a gas distribution component for delivery of inert gas, such as argon, to the reaction vessel. One or more of the components of the bottom distribution component may be connected to the reaction vessel through a loop line which allows for delivery of chemical solutions from the deprotection distribution component, the capping distribution component and delivery of inert gas from the gas distribution component. The loop lines may be also adapted for discharge of waste liquids from the reaction vessel. The bottom distribution component may comprise for example a multiple ways magnetic valve which may be electronically coupled to a computing device comprising at least one processor configured to control the delivery of deprotection solutions, capping solutions and inert gas to the reaction vessel and further configured to control the discharging of liquids and solutions of the reaction vessel after each reaction or washing step. The deprotection distribution component is connected to a reagent storing component, preferably a deprotection solution storing component. The deprotection storing component may comprise one or more containers for storing deprotection reagents. The deprotection storing component may be connected to a gas distribution system to provide inert gas to the each deprotection reagent container. Thus, each of the deprotection reagent containers may be stored under anhydrous and inert atmosphere, such as under argon atmosphere. The capping distribution component is connected to a reagent storing component, preferably a capping solution storing component. The capping storing component may comprise one or more containers for storing capping reagents. The capping storing component may be connected to a gas distribution system to provide inert gas to the each capping reagent container. Thus, each of the capping reagent containers may be stored under anhydrous and inert atmosphere, such as under argon pressure.
The device of the present invention may further comprise a gas distribution system to provide anhydrous and inert gas to one or more components of the device of the present invention for mixing, atmosphere conditioning and driving fluid purposes. Preferably the device for automated synthesis of oligo- and polysaccharides on a solid support is adapted for performing reactions under anhydrous and inert atmosphere. The gas distribution system comprises at least one gas container, such as an argon container, to provide inert gas to the one or more components of the device of the present invention. The gas distribution system may comprise one or more valves, valve assemblies, one or more vents and/or one or more manifolds or similar technical means to allow the distribution and delivery of inert gas to the one or more components of the device of the present invention. The one or more valves, valve assemblies, one or more vents and/or one or more manifolds or similar technical means allow control of the pressure within the one or more lines which connect the one or more components of the device of the present invention. The one or more valves, valve assemblies, one or more vents and/or one or more manifolds or similar technical means may be under control of a computing device comprising at least one processor. The processor may be configured to control the delivery and distribution of the inert gas within the device of the present invention and is configured to control gas pressure within the one or more lines and one or more components of the device of the present invention.
According to the present invention the device for automated synthesis of oligo- and polysaccharides on a solid support comprises a cooling system. According to the present invention the device for automated synthesis of oligo- and polysaccharides on a solid support comprises at least one cooling device for cooling the reaction vessel or more precisely for cooling the content of the reaction vessel and at least one pre-cooling device for pre-cooling the reagents to be supplied to the reaction vessel. The cooling device provides at least active cooling of the reaction vessel. The pre-cooling device provides at least active cooling of one or more of the reagents to be supplied to the reaction vessel.
Currently, the automated glycosylation process requires expensive and large cooling systems. Thus, the devices for automated synthesis of oligo- and polysaccharides on a solid support known in the art require expensive and large cooling systems. However, the devices known in the art have shown several disadvantages in performing coupling reactions in connection with the use of common reagents especially during scale-up of the synthesis of oligo- and polysaccharides on the solid support. Even if the devices known in the art allow for active cooling of the reaction vessel during the coupling reactions, not sufficiently high yields were obtained, decomposition of reagents and formation of side and decomposition products were detected.
Even when the cooling of the reaction vessel was adjusted to even lower temperatures did actually not result in the desired improvement of yield and reduction of decomposition and decrease of formation of side and decomposition products.
Also a very slow addition and careful delivery of the reagents to the reaction mixture under simultaneous monitoring of the temperature of the reaction mixture in the reaction vessel did also not bring the expected improvement in yield and reduction of side and decomposition products. Moreover, due to the very slow addition and careful delivery of the reagents, the total reaction time increased to an inacceptable degree while simultaneously also the side and decomposition products increased without the desired enhancement of the yield. In addition, up-scaling of this way running the reaction was almost impossible.
Thus, also with the devices known in the art allowing slow and careful delivery of the reagents to the reaction mixture under simultaneous monitoring of the temperature of the reaction mixture have shown a disadvantageous impact on the resulting yield of the desired products, in particular with regard to larger batch sizes. The delayed addition of the reagents, particularly in larger batch sizes, resulted in still unsatisfying overall yields of the desired oligo- and poly-saccharides.
However, after several attempts failed to increase yield and reduce side and decomposition products especially by up-scaled reactions, the objective could be solved by the pre-cooling device and by pre-cooling the reagents to be supplied to a temperature close to the temperature of the reaction mixture in the reaction vessel. Thus, the device of the present invention comprises an improved cooling system, in particular comprises a cooling device for cooling the reaction vessel and a pre-cooling device for pre-cooling the reagents to be supplied and has been shown to be particularly advantageous for automated synthesis of oligo- and poly-saccharides on a solid support especially in connection with larger batch sizes and therefore overcomes the disadvantages of the devices known in the art.
Thus, the inventors of the present patent application have surprisingly found that a device for automated synthesis of oligo- and polysaccharides on a solid support comprising a reaction vessel, a reagent storing component, a reagent delivery system, a cooling device for cooling the reaction vessel, and a pre-cooling device for pre-cooling the reagents to be supplied to a temperature close to the temperature of the reaction mixture in the reaction vessel, overcomes the disadvantages of the devices known in the art for automated synthesis of oligo- and polysaccharides on a solid support.
The inventors have found that pre-cooling of the reagents prevents and avoids decomposition of the reagents during the synthesis cycles which otherwise could result in undesired side-products and decomposition products. The inventors have found that with a device for automated synthesis of oligo- and polysaccharides on a solid support comprising at least a cooling device for cooling the reaction vessel and a pre-cooling device for pre-cooling the reagents to be supplied, conversion and yield could be increased, decomposition of reagents could be decreased and formation of side and decomposition products could effectively be prevented as the device allows for active cooling of the reaction vessel and additionally allows for active cooling of the reagents to be supplied to the reaction vessel.
For example,
As a further example,
As a further example,
As a further example,
As a further example,
The advantages and improvement of the automated glycosylation via pre-cooling of the reagents are most apparent on
The inventors of the present invention have further investigated the effect of pre-cooling reagents or reagent solutions in the reagent storing component, i.e. pre-cooling reagents or reagent solutions in one or more of the reagent containers. Thereby, it has been found that additional pre-cooling of reagents by the pre-cooling device according to the invention is also particularly advantageous when the reagent storing component or one or more reagent containers are already pre-cooled.
In accordance with the examples shown in
In a further example, the inventors have further investigated the effect of pre-cooling reagents or reagent solutions in the reagent storing component, i.e. pre-cooling reagents or reagent solutions in one or more of the reagent containers to a temperature at or below −10° C. At first, the reagent container containing the dichloromethane was pre-cooled to a temperature of −10° C. and the pre-cooled dichloromethane was delivered to the reaction vessel in the presence or absence of further pre-cooling by the pre-cooling device according to the invention. Also in this example, thermal perturbations could still be observed although the dichloromethane has been pre-cooled to −10° C. in the respective reagent container. Thus, in conclusion an unfavorable increase in temperature of the pre-cooled dichloromethane occurred during the delivery from the pre-cooled reagent container to the reaction vessel. Such an increase in temperature leading to the observed thermal perturbations could be effectively avoided and prevented by additional pre-cooling via the pre-cooling device of the present invention. Second, the reagent container containing the dichloromethane was pre-cooled to −15° C. and the pre-cooled dichloromethane was delivered to the reaction vessel in the presence or absence of further pre-cooling by the pre-cooling device according to the invention. Also in this example, thermal perturbations could still be observed although the dichloromethane has been pre-cooled to −15° C. in the respective reagent container. Although the thermal perturbations could be reduced since the initial temperature of the dichloromethane solution at begin of the delivery starting from the reagent container was at −15° C., thermal perturbations leading to formation of side and decomposition products still were measurable and were detectable. Furthermore, the observed thermal perturbations have shown to be dependent of the flow rate and the overall volume of the dichloromethane supplied to the reaction vessel. In conclusion, thermal perturbations could be prevented the most by advantageous additional pre-cooling via the pre-cooling device of the present invention.
It should be noted that, as it is preferred in some embodiments of the present invention, the reagent delivery system may comprise a syringe pump for driving the fluids within the reagent delivery system which may connected through one or more loop lines. The resting volume of the loops is defined as a function of the tubing length. Thus, prior to the delivery of the reagents from the reagent delivery system to the reaction vessel, the loop lines may be filled-up with the required amount of reagent to be delivered to the reaction vessel. Each loop may be sized the same or different. Thus, prior to the delivery of the reagents to be supplied to the reaction vessel the loop lines may be filled with the required amount of reagents, wherein the time period for filling-up the loop lines differs if the required volume of a reagent solution varies. Thus, in case of larger batch sizes a greater volume of reagents to be supplied to the reaction vessel may be required so that the respective solutions may disadvantageously warm-up during preparation of the required amount of reagents before delivery to the reaction-vessel.
It should be further noted that as the surroundings or the environmental conditions, i.e. of the reagent delivery system or the one or more delivery lines are at a different temperature, such as room temperature, compared to the pre-cooled dichloromethane solution, spontaneous heat transfer occurs during delivery to the reaction vessel which leads to an increase of the temperature of the pre-cooled reagent solution. This is especially true the higher the initial temperature difference ΔT between the surroundings and the preset pre-cooling temperature is. Thus, the pre-cooling device has been proven to be particularly advantageous for the automated synthesis of oligo- and polysaccharides on a solid support, as the reagents to be supplied to the reaction vessel are actively pre-cooled directly before entering the reaction vessel. Thus, the pre-cooling device is preferably located in close proximity to the reaction vessel or one or more of the inlets of the reaction vessel. Thus, the pre-cooling device is preferably positioned close by the reaction vessel or by one or more of the inlets of the reaction vessel. In other words, the pre-cooling device is preferably located adjacent to the reaction vessel or adjacent to one or more of the inlets of the reaction vessel. Preferably, the pre-cooling device is located downstream to the reagent delivery system and upstream to the reaction vessel.
Furthermore, for the synthesis of biological relevant structures (such as the Lewis antigens); it is necessary to alternate poorly reactive building block/donors (such as glucosamine), with highly reactive and temperature sensitive ones (such as fucose). As described in Example 13 the inventors have shown that without a pre-cooling device to adjust the temperature of donor and activator (see
In
Thus, as a result
A technical advantage of a pre-cooling device located between the reagent storing component and the reaction vessel is the control of the temperature of the added reagents regardless the length of the tubing or pathway through the delivery system connecting the reagent storing component and the reaction vessel. This means that the construction and final design of the synthesizer is flexible in terms of configuration of the reagent storage component, reagent delivery system and reaction vessel (such as the location, distancing, and part arrangement).
This results in a robust design in terms of the final environmental conditions (ventilations, temperature, light intensity) where the synthesizer is operating. Thus, the pre-cooling device improves the reproducibility and stability of the system.
Although the reagent storing component (660) might also be cooled by a cooling device or a further cooling means, it is economically not reasonable to cool the normally large reagent storing component (660) to a temperature much below the reaction temperature in the reaction vessel (400) and to assume a certain warm up of the reagents and reagent solutions when processing through the a reagent delivery system (600) on the way to the reaction vessel (400). Moreover, the inventors could show that when adding reagents and reagent solutions to the reaction vessel (400) which do not have the appropriate temperature, i.e. which have too high temperature, local heat spots occur in the reaction solution causing side and degradation products during the solid phase synthesis of oligo- and polysaccharides. According to the invention, the yield and the purity of the synthesized oligo- and polysaccharides is increased by adjusting the temperature of the reagents and reagent solutions to be added to the reaction vessel (400) immediately before that addition.
The pre-cooling device (300) is positioned within the a reagent delivery system (600) and between the reagent storing component (660) or more precisely the outlet of the reagent storing component (660) and the reaction vessel (400) or more precisely the inlet of the reaction vessel (400). Moreover, the pre-cooling device (300) is positioned in close proximity to the reaction vessel (400). The term “close proximity” refers to a length of the tubing (e.g. reagent delivery lines) between the pre-cooling device (300) or more precisely between the outlet of the pre-cooling device (300) and the reaction vessel (400) or more precisely the inlet of the reaction vessel (400) of less than 40 cm, preferably of less than 30 cm, more preferably of less than 25 cm, more preferably of less than 20 cm, more preferably of less than 15 cm, and most preferably of less than 10 cm or less than 5 cm.
Alternatively, the pre-cooling device (300) is positioned between the reagent storing component (660) or more precisely the outlet of the reagent storing component (660) and the reaction vessel (400) or more precisely the inlet of the reaction vessel (400) in a way that the length of the tubing from the outlet of the pre-cooling device (300) to the inlet of the reaction vessel (400) is less than one fifth (i.e. ⅕) of the length of the tubing from the outlet of the reagent storing component (660) to the inlet of the pre-cooling device (300), more preferably less than one eighth (i.e. ⅛), more preferably less than one tenth (i.e. 1/10), more preferably less than one twelfth (i.e. 1/12), more preferably less than one fourteenth (i.e. 1/14), more preferably less than one sixteenth (i.e. 1/16), more preferably less than one eighteenth (i.e. 1/18), more preferably less than one twentieth (i.e. 1/20). The term tubing herein also refers to the one or more reagent delivery lines.
Consequently, the present application is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprises:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) through tubings;
wherein the pre-cooling device (300) is interposed between the reaction vessel (400) and the reagent delivery system (600) so that the length of the tubing from the pre-cooling device (300) or more precisely from the outlet of the pre-cooling device (300) to the reaction vessel (400) or more precisely to the inlet of the reaction vessel (400) is less than one fifth (i.e. ⅕) of the length of the tubing from the reagent storing component (660) or more precisely from the outlet of the reagent storing component (660) to the pre-cooling device (300) or more precisely to the inlet of the pre-cooling device (300), more preferably less than one eighth (i.e. ⅛), more preferably less than one tenth (i.e. 1/10), more preferably less than one twelfth (i.e. 1/12), more preferably less than one fourteenth (i.e. 1/14), more preferably less than one sixteenth (i.e. 1/16), more preferably less than one eighteenth (i.e. 1/18), more preferably less than one twentieth (i.e. 1/20); and wherein the pre-cooling device (300) is in thermal communication with the reagent delivery system (600).
Consequently, the present application is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprises:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) through one or more reagent delivery lines;
wherein the pre-cooling device (300) is interposed between the reaction vessel (400) and the reagent delivery system (600) so that the length of the one or more reagent delivery lines from the pre-cooling device (300) or more precisely from the outlet of the pre-cooling device (300) to the reaction vessel (400) or more precisely to the inlet of the reaction vessel (400) is less than one fifth (i.e. ⅕) of the length of the one or more reagent delivery lines from the reagent storing component (660) or more precisely from the outlet of the reagent storing component (660) to the pre-cooling device (300) or more precisely to the inlet of the pre-cooling device (300), more preferably less than one eighth (i.e. ⅛), more preferably less than one tenth (i.e. 1/10), more preferably less than one twelfth (i.e. 1/12), more preferably less than one fourteenth (i.e. 1/14), more preferably less than one sixteenth (i.e. 1/16), more preferably less than one eighteenth (i.e. 1/18), more preferably less than one twentieth (i.e. 1/20); and
wherein the pre-cooling device (300) is in thermal communication with the reagent delivery system (600).
The reagents to be supplied to the reaction vessel are preferably pre-cooled to a temperature Tpre-reagent by the pre-cooling device according to the invention. The pre-cooling device is preferably in thermal communication with the reagent delivery system and is configured to pre-cool the reagents to be supplied to a temperature Tpre-reagent. In order to pre-cool the reagent to be supplied to the reaction vessel, the pre-cooling device may be adjusted to a temperature Tpre-device. The temperature Tpre-device may be adjusted to the temperature Tpre-reagent or may be set to a temperature below the temperature Tpre-reagent. Thus, preferably the preset temperature of the pre-cooling device Tpre-device is less or equal to the pre-cooling temperature Tpre-reagent, and thus it is preferred that Tpre-device≤Tpre-reagent.
Preferably Tpre-device is selected from a temperature range of −40° C. to −10° C., preferably −30° C. to −11° C., preferably −25° C. to −13° C., preferably −20° C. to −15° C. Preferably Tpre-reagent is selected from a temperature range of −40° C. to −9° C., preferably −30° C. to −11° C., preferably −25° C. to −13° C., and most preferably −20° C. to −15° C. The incoming solutions from the reagent delivery system are therefore preferably pre-cooled to the pre-cooling temperature Tpre-reagent preferably selected from a temperature range of −40° C. to −9° C., preferably −30° C. to −11° C., preferably −25° C. to −13° C., and preferably −20° C. to −15° C.
The temperature difference between the adjusted temperature of the pre-cooling device Tpre-device and the pre-cooling temperature Tpre-reagent of the reagents at the time of leaving the pre-cooling device may be 0° C.-15° C., 0° C.-10° C., preferably 0° C.-9° C., preferably 0° C.-8° C., preferably 0° C.-7° C., particularly preferably 0° C.-6° C., preferably 0° C.-5° C., preferably 0° C.-4° C., preferably 0° C.-3° C., preferably 0° C.-2° C., preferably 0° C.-1° C., preferably 0° C.-0.1° C., preferably 0° C.-0.05° C.
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the temperature difference between the temperature of the pre-cooling device Tpre-device and the temperature Tpre-reagent of the pre-cooled reagents at the time of leaving the pre-cooling device is 0° C.-15° C., 0° C.-10° C., preferably 0° C.-9° C., preferably 0° C.-8° C., preferably 0° C.-7° C., particularly preferably 0° C.-6° C., preferably 0° C.-5° C., preferably 0° C.-4° C., preferably 0° C.-3° C., preferably 0° C.-2° C., preferably 0° C.-1° C., preferably 0° C.-0.1° C., preferably 0° C.-0.05° C., wherein Tpre-device≤Tpre-reagent.
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the temperature of the pre-cooling device Tpre-device is less or equal to the temperature Tpre-reagent of the pre-cooled reagents at the time of leaving the pre-cooling device, wherein Tpre-reagent is selected from a temperature range of −40° C. to −9° C., preferably −30° C. to −11° C., preferably −25° C. to −13° C., and most preferably −20° C. to −15° C.
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the pre-cooling device is set to a temperature Tpre-device less or equal to the temperature Tpre-reagent of the pre-cooled reagents at the time of leaving the pre-cooling device, wherein Tpre-reagent is selected from a temperature range of −40° C. to −9° C., preferably −30° C. to −11° C., preferably −25° C. to −13° C., and most preferably −20° C. to −15° C.
The pre-cooling device may be adjusted to a pre-cooling temperature Tpre-device and is preferably in thermal communication with the reagent delivery system so that the reagents to be supplied are pre-cooled preferably through heat transfer between the pre-cooling device and the reagent delivery system. In preferred embodiments, the reagent delivery system may have one or more reagent delivery lines or tubing and it is then preferred that the pre-cooling device being in thermal communication with the one or more reagent delivery lines or tubing. During the delivery of the reagents to be supplied to the reaction vessel, the reagents pass or traverse the pre-cooling device and the reagents are thereby pre-cooled to the pre-cooling temperature Tpre-reagent via heat transfer.
In general, heat flow or heat transfer is proportional to the temperature difference ΔT or the temperature difference T1-T2 of the media involved. The rate of heat loss or the rate of heat absorption of the reagents or the reagent solutions is proportional to the temperature difference between the reagents or reagent solutions and the surroundings. The rate of heat loss or the rate of heat absorption also depends on the period of time Δt or t1-t2 within which the media involved are in thermal communication with each other. Thus, the rate of heat loss depends on the time interval Δt within which the reagents pass or traverse the pre-cooling device or within which the reagents are in thermal communication with the pre-cooling device. Furthermore, the rate of heat absorption also depends on the time interval Δt within which the reagents are delivered from the reagent storing component to the reaction vessel, for instance, without pre-cooling by the pre-cooling device. Furthermore, the contact surface, the heat transfer coefficients, the thermal conductivities of the materials involved, such as the material of the reagent delivery lines or the tubing, the flow rate of the reagents through the delivery lines, the length of the reagent delivery lines and the like also affect the rate of heat loss or the rate of heat absorption. In general, a heat transfer takes place in the direction of the medium with the lower temperature. The heat transfer may be described by the heat transfer coefficient.
The reagent to be supplied to the reaction vessel may be delivered at different flow rates from the reagent storing component to the reaction vessel. The flow rate therefore affects the time interval Δt within which the reagents to be supplied to the reaction vessel are in thermal communication with the pre-cooling device. Thus, the higher the flow rates the smaller the time interval Δt within which the reagents to be supplied to the reaction vessel are in thermal communication with the pre-cooling device. A shorter time interval Δt may result in a lower heat loss of the reagents to be supplied. This means that different reagents having the temperature T1 entering the pre-cooling device may exit the pre-cooling device with different temperatures Tpre-reagent when the reagents pass or traverse the pre-cooling device at different flow rates. Also when the reagents entering the pre-cooling device are retained in the pre-cooling device within a time interval Δt the reagents may have different temperatures Tpre-reagent when leaving the pre-cooling device depending on the overall volume of reagent solutions retained in the pre-cooling device. In order to provide reagents to be supplied to the reaction vessel having equal and desired pre-cooling temperatures Tpre-reagent, the pre-cooling device may be easily adjusted to a lower temperature than the desired pre-cooling temperature Tpre-reagent, so that the reagents that pass or traverse the pre-cooling device or greater volumes of reagent solutions that is retained in the pre-cooling device are more effectively cooled due to the greater temperature difference ΔT between the reagents or reagent solutions and the pre-cooling device. As mentioned above the temperature difference between the adjusted temperature of the pre-cooling device Tpre-device and the desired pre-cooling temperature Tpre-reagent of the reagents may be 0° C.-15° C., 0° C.-10° C., preferably 0° C.-9° C., preferably 0° C.-8° C., preferably 0° C.-7° C., particularly preferably 0° C.-6° C., preferably 0° C.-5° C., preferably 0° C.-4° C., preferably 0° C.-3° C., preferably 0° C.-2° C., preferably 0° C.-1° C., preferably 0° C.-0.1° C., preferably 0° C.-0.05° C. Thus, the pre-cooling device is advantageous in that different volumes of reagent solutions may be supplied to the reaction vessel having the desired pre-cooling temperatures Tpre-reagent by convenient adjustment of the preset temperature of the pre-cooling device. For example, in one embodiment the difference of temperature between the pre-cooling device (300) to the reaction vessel (400) may be 10° C. The pre-cooling device (300) may be adjusted to a temperature range between −25° C. to −20° C. so that the addition temperature of the reagents to be supplied to the reaction vessel will be −15° C.
For preventing a rewarming and thermal absorption of pre-cooled reagents during the delivery to the reaction vessel it would be necessary to provide, for example, reagent delivery lines made from chemically resistant and thermal resistant materials or to provide a suitable insulation for the reagent delivery lines. Furthermore, also the reagent delivery system as a whole need to be designed in such a way that rewarming will be prevented. It should be noted that, the greater the temperature difference ΔT the greater the heat flow or heat transfer. Furthermore, the greater the time period Δt the greater the heat flow or heat transfer. Thus, the lower the desired target pre-cooling temperature Tpre-reagent the higher are the demands to be fulfilled by the device for prevention of heat absorption of the pre-cooled reagents or reagent solutions in order to ensure that the temperature of the pre-cooled reagents or reagent solution is maintained throughout the delivery from the reagent containers to the reaction vessel. This is particularly important, as the pre-cooling temperature Tpre-reagent is preferably selected from a temperature range of −40° C. to −9° C. Furthermore, as the pre-cooling temperature Tpre-reagent is selected from a temperature range of −40° C. to −9° C., preferably −30° C. to −11° C., preferably −25° C. to −13° C., and most preferably −20° C. to −15° C., the pre-cooling temperature Tpre-reagent is thus particularly preferably below 0° C. Thus, the pre-cooling temperature is preferably below the freezing point of water and thus condensation of water and ice crystal formation from air humidity must be observed to ensure that the components of the reagent delivery system, i.e. the pump system or the one or more pumps such as syringe pumps, peristaltic pumps or other pumps and the one or more valves or one or more valve assemblies, one or more manifolds, one or more distributing components and similar suitable technical means are not damaged. Thus, in some embodiments, it is preferred that the reagents to be supplied have a temperature of above 0° C. during delivery from the reagent storing component to the pre-cooling device and are then pre-cooled to a desired pre-cooling temperature Tpre-reagent in a range of −40° C. to −9° C. by passing or traversing the pre-cooling device and are supplied or added to the reaction vessel when having a temperature in a range of −40° C. to −9° C.
The device for automated synthesis of oligo- and polysaccharides on a solid support of the present invention is suitable for the automated synthesis of complex or branched saccharides such as synthetic glycans of increasing length and complexity up to a chain length of 50 units. Thus, different building blocks and/or different glycosylation reagents are often required for the synthesis of such oligo- and/or polysaccharides. Thereby, each synthesis cycle includes different thermal stages and the device of the present invention allows advantageous rapid and dynamic temperature adjustment for the different thermal stages of the synthesis cycles. The pre-cooling device of the present invention thereby allows rapid and dynamic cooling of the reagents to be supplied during the delivery to the reaction vessel in a simple and convenient way. Thus, with the pre-cooling device according to the invention it is not necessary that all of the different reagent containers containing the different building blocks and/or different glycosylation reagents are pre-cooled to the preferred range of the pre-cooling temperature Tpre-reagent selected from a temperature range of −40° C. to −9° C., preferably −30° C. to −11° C., preferably −25° to −13° C., and most preferably −20° C. to −15° C. With the pre-cooling device according to the invention it is possible to pre-cool only the building block and/or glycosylation reagent really required for performing the current synthesis cycle.
The pre-cooling device is preferably interposed between the reaction vessel and the reagent delivery system, wherein the pre-cooling device is in thermal communication with the reagent delivery system. Thereby, interposed means that the pre-cooling device is positioned between the reagent delivery system and the reaction vessel in such a way that at least one of the reagents to be supplied to the reaction vessel is delivered from the reagent storing component to the pre-cooling device and then the reagents pass or traverse the pre-cooling device so that said reagent is pre-cooled to a desired pre-cooling temperature Tpre-reagent. Thus, preferably the pre-cooling device is upstream to one or more inlets of the reaction vessel and is not positioned downstream to the reaction vessel. As used herein interposed preferably does not mean that reagents that exit the reaction vessel through one or more outlets are passed through the pre-cooling device in order to maintain the reagent temperature for resupplying the reagents to the reaction vessel. Thus, the pre-cooling device may preferably not be connected to the outlets of the reaction vessel. Furthermore interposed as used herein means further that the pre-cooling device is preferably in thermal communication with direct connections between the reagent delivery system and the reaction vessel, such as one or more direct reagent delivery lines connecting the reagent delivery system and the reaction vessel. The pre-cooling device according to the present invention is positioned such that at least the reagents and solvents supplied in the pre-coupling stage of a respective glycosylation cycle are pre-cooled during delivery and before addition to the reaction vessel. Thus, it is particularly preferred that the reagent delivery lines or the tubing connecting the outlet of the pre-cooling device and one or more inlets of the reaction vessel are continuous reagent delivery lines or continuous tubing. A continuous reagent delivery line or continuous tubing means e.g. that no valve or vent or similar technical means is interposed or interconnected in the reagent delivery line or tubing.
The reagents to be supplied to the reaction vessel therefore pass or traverse the pre-cooling device during delivery and before addition to the reaction vessel and are preferably pre-cooled to a temperature Tpre-reagent when passing or traversing the pre-cooling device according to the invention. Thereby, the reagents to be supplied pass or traverse the pre-cooling device within a time interval Δt. The time interval Δt may also include a resting time of the reagents within the pre-cooling device. For example, the reagents to be supplied may be delivered to the pre-cooling device and then the reagents may be retained in the pre-cooling device for a time interval Δt to allow further pre-cooling of the reagents. The reagents to be supplied may be also delivered to the pre-cooling device and then the reagents pass or traverse the pre-cooling device with a specific flow rate within a time interval Δt to allow pre-cooling of the reagents while the reagents flow through the pre-cooling device. In preferred embodiments, the reagent delivery system may have one or more reagent delivery lines. Thus, the reagents to be supplied to the reaction vessel are preferably delivered by the reagent delivery system to the reaction vessel through one or more reagent delivery lines and thus it is preferred that the reagents pass or traverse the pre-cooling device with a specific flow rate within a time interval Δt, wherein the reagents are pre-cooled preferably via heat transfer to a temperature Tpre-reagent. Thus, during the delivery of the reagents to be supplied to the reaction vessel, the reagents pass or traverse the pre-cooling device and the reagents are thereby preferably pre-cooled to the pre-cooling temperature Tpre-reagent via heat transfer.
Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400);
wherein the pre-cooling device (300) is interposed between the reaction vessel (400) and the reagent delivery system (600); and wherein the pre-cooling device (300) is in thermal communication with the reagent delivery system (600),
wherein the pre-cooling device (300) and the reaction vessel (400) are connected via continuous reagent delivery lines.
Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400);
wherein the pre-cooling device (300) is interposed between the reaction vessel (400) and the reagent delivery system (600); and
wherein the pre-cooling device (300) is in thermal communication with the reagent delivery system (600),
wherein the pre-cooling device (300) and the reaction vessel (400) are connected via continuous tubing.
The reagents or reagents solutions in the reagent storing component i.e. the one or more reagent containers may have a temperature T1 and at the time of entering the reaction vessel the reagents or reagents solutions may have a temperature T2, wherein T2 preferably corresponds to the temperature Tves in the reaction vessel. Preferably, the temperature T2 also corresponds to the pre-cooling temperature Tpre-reagent. Thus, the pre-cooling device is preferably located adjacent to the reaction vessel or adjacent to one or more of the inlets of the reaction vessel so that the reagents or reagents solutions added to the reaction vessel have a temperature T2, wherein the temperature T2 corresponds to the pre-cooling temperature Tpre-reagent. Therefore, it is preferred that the reagents or reagents solutions having a temperature T1 are pre-cooled by the pre-cooling device according to the invention to a pre-cooling temperature Tpre-reagent, wherein Tpre-reagent is selected from a temperature range of −40° C. to −9° C., preferably −30° C. to −11° C., preferably −25° C. to −13° C., and most preferably −20° C. to −15° C. After the pre-cooling of the reagents to be supplied by the pre-cooling device, the reagents or reagent solutions having the pre-cooling temperature Tpre-reagent are finally delivered to the reaction vessel or to one or more of the inlets of the reaction vessel and are supplied to the reaction mixture inside the reaction vessel. Preferably, the reagents or reagents solutions thereby have the pre-cooling temperature Tpre-reagent. However, if e.g. thermal absorption occurs during the period of time of the delivery from the pre-cooling device to the reaction vessel and the reagents or reagents solutions have the temperature T2>Tpre-reagent at the time of addition to the reaction vessel, it is particularly preferred that the temperature difference ΔT=T2−Tpre-reagent is between 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C., particularly preferably 0° C.-0.1° C., preferably 0° C.-0.09° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C.
Furthermore, it is preferred that the distance between the pre-cooling device and the reaction vessel is such that the incoming solutions from the reagent delivery system are pre-cooled by the pre-cooling device to a pre-cooling temperature Tpre-reagent preferably in the range of −40° C. to −9° C., preferably −30° C. to −11° C., preferably −25° C. to −13° C., and most preferably −20° C. to −1500 and such that the temperature difference ΔT of the reagents or reagent solutions pre-cooled to the temperature Tpre-reagent and temperature of the reagents or reagent solutions at the time of addition to the reaction vessel is between 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C., particularly preferably 0° C.-0.1° C., preferably 0° C.-0.09° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C. Thus, the temperature difference ΔT of the pre-cooled reagents before addition and at the time of addition to the reaction vessel is between 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C. particularly preferably 0° C.-0.1° C. preferably 0° C.-0.09° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C.
The inventors have further investigated the effect of rewarming and heat absorption of the reagents to be supplied after the reagents leave the pre-cooling device and before addition to the reaction vessel. For this experiment a temperature probe has been installed at the outlet or output of the pre-cooling device in order to examine temperature changes of the pre-cooled reagents during the delivery to the reaction vessel. Furthermore, the distance between the reaction vessel and the pre-cooling device has been varied in order to examine temperature changes in dependence of the distance between the pre-cooling device and the reaction vessel. In this experiment the temperature of the surroundings was at room temperature, and the delivery lines were made of PTFE. The pre-cooling device was set to temperature Tpre-device such that the reagents leaving the pre-cooling device have a temperature of Tpre-reagent in the range between −40° C. to −9° C. At first the pre-cooling device was set to temperature Tpre-device such that the reagents leaving the pre-cooling device were at −15° C. The temperature of the reagents was confirmed by temperature measurement through the temperature probe. The temperature of the reagents at the time of addition was measured by temperature measurement of the reaction mixture inside the reaction vessel. A slight temperature increase was observed at higher distances between the pre-cooling device and the reaction vessel. When the pre-cooling device is positioned directly before the reaction vessel, thus at minimum distance to the reaction vessel no temperature changes have been observed. Second the pre-cooling device was set to temperature Tpre-device such that the reagents leaving the pre-cooling device were at −20° C. or −25° C. Slightly greater temperature changes of the pre-cooled reagents occurred during delivery to the reaction vessel. The temperature changes of the pre-cooled reagents were at higher magnitude for the pre-cooling temperatures of −20° C. or −25° C., as in the case of −15° C. However, positioning of the pre-cooling device at the minimum possible distance to the reaction vessel has been shown to prevent temperature changes the most effective. However, in embodiments wherein the device of the present invention, for example, further comprises a microwave generator component, the reaction vessel may be positioned in a chamber to provide microwave radiation to the reaction vessel. In such embodiment, it may be preferred that the pre-cooling device is not positioned directly by the one or more inlets of the reaction vessel, for example in case the pre-cooling device comprises a thermoelectric cooling device and a metal plate as heat exchanging material. It is apparent that the positioning of such a metal plate is not desired inside the microwave chamber. However, it has been found that positioning of the pre-cooling device in close proximity to the reaction vessel, such as at distances of 1 cm-30 cm, preferably, 1 cm-25 cm, preferably 1 cm-20 cm, preferably 3 cm-10 cm, preferably 1-10 cm, results in insignificant temperature changes. As used herein positioning of the pre-cooling device in close proximity to the reaction vessel also includes the lengths of the delivery lines or the tubing between the pre-cooling device and the reaction vessel. Thus, it is not preferred that the pre-cooling device is positioned at a distance of e.g. 20 cm to the reaction vessel, wherein the delivery lines (tubing) have a length of e.g. 30 cm or even 50 cm. Thus, it is preferred that the pre-cooling device is located in close proximity to the reaction vessel or in close proximity to one or more of the inlets of the reaction vessel. Thus, the pre-cooling device is preferably positioned close by the reaction vessel or by one or more of the inlets of the reaction vessel. With other word the pre-cooling device is preferably located adjacent to the reaction vessel or adjacent to one or more of the inlets of the reaction vessel. Preferably, the pre-cooling device is located downstream to the reagent delivery system and upstream to the reaction vessel.
Thus, it is preferred that the pre-cooling device is interposed between the reaction vessel and the reagent delivery system, wherein the pre-cooling device is in thermal communication with the reagent delivery system, wherein the distance between the pre-cooling device and the reaction vessel is such that the incoming solutions from the reagent delivery system are pre-cooled by the pre-cooling device to a pre-cooling temperature Tpre-reagent preferably in the range of −40° C. to −9° C., preferably −30° C. to −11° C., preferably −25° C. to −13° C., and most preferably −20° C. to −15° C. and such that the temperature difference ΔT of the reagents or reagent solutions pre-cooled to the temperature Tpre-reagent and temperature of the reagents or reagent solutions at the time of addition to the reaction vessel is between 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C., particularly preferably 0° C.-0.1° C., preferably 0° C.-0.09° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C. Thus, the temperature difference ΔT of the pre-cooled reagents before addition and at the time of addition to the reaction vessel is between 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C., particularly preferably 0° C.-0.1° C., preferably 0° C.-0.09° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C.
Consequently, the pre-cooled reagents or the pre-cooled reagent solutions have the temperature Tpre-reagent when leaving the pre-cooling device. Along the way between leaving the pre-cooling device and entering the reaction vessel the pre-cooled reagent or the pre-cooled reagent solution does not warm up more than maximal 0.5° C., preferably 0.4° C., more preferably 0.3° C., more preferably 0.2° C., more preferably 0.1° C., more preferably 0.09° C., more preferably 0.08° C., more preferably 0.07° C., more preferably 0.08° C., more preferably 0.07° C., more preferably 0.06° C., and most preferably not more than maximal 0.05° C.
It should be noted that distances between the pre-cooling device and the reaction vessel of 1 cm-60 cm, preferably, 1 cm-50 cm, preferably 1 cm-40 cm, preferably 1 cm-30 cm are also possible, e.g. in case heat absorption can be prevented and the pre-cooled reagent solution does not warm up more than maximal 0.5° C., preferably 0.4° C., more preferably 0.3° C., more preferably 0.2° C., more preferably 0.1° C., more preferably 0.09° C., more preferably 0.08° C., more preferably 0.07° C., more preferably 0.08° C., more preferably 0.07° C., more preferably 0.06° C., and most preferably not more than maximal 0.05° C. In some embodiments the delivery lines between the pre-cooling device and the reaction vessel may further comprise an insulation to prevent heat absorption and a temperature increase of the pre-cooled reagents.
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600) so that the reagents along their way from the pre-cooling device (300) to the reaction vessel (400) do not increase their temperature for more than 0.5° C., preferably 0.4° C., more preferably 0.3° C., more preferably 0.2° C., more preferably 0.1° C., more preferably 0.09° C., more preferably 0.08° C., more preferably 0.07° C., more preferably 0.08° C., more preferably 0.07° C., more preferably 0.06° C., and most preferably do not increase their temperature for more than 0.05° C.
Or in other words, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600) so that temperature difference ΔT=T2−Tpre-reagent is between 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C., particularly preferably 0° C.-0.1° C., preferably 0° C.-0.09° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C., wherein Tpre-reagent is the temperature of the reagents when leaving the pre-cooling device (300) and T2 is the temperature of the reagents when entering the reaction vessel (400).
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the reagents to be supplied have a temperature T1 when entering the pre-cooling device and have a temperature Tpre-reagent when leaving the pre-cooling device, wherein T1>Tpre-reagent; and wherein the reagents to be supplied have a temperature T2 when entering the reaction vessel (400); and wherein the temperature difference ΔT=T2−Tpre-reagent is between 0° C.-0.5° C.; wherein the pre-cooling device is set to a temperature Tpre-device less or equal to the temperature Tpre-reagent; wherein Tpre-device≤Tpre-reagent; and wherein the temperature Tpre-reagent of the pre-cooled reagents at the time of leaving ΔT=Tpre-device−Tpre-reagent is 0° C.-10° C., preferably 0° C.-9° C., preferably 0° C.-8° C., preferably 0° C.-7° C., particularly preferably 0° C.-6° C., preferably 0° C.-5° C., preferably 0° C.-4° C., preferably 0° C.-3° C., preferably 0° C.-2° C., preferably 0° C.-1° C., preferably 0° C.-0.1° C., preferably 0° C.-0.05° C.
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the reagents have a temperature T1 when entering the pre-cooling device and have a temperature Tpre-reagent when leaving the pre-cooling device, wherein T1>Tpre-reagent; and wherein the reagents have a temperature T2 when entering the reaction vessel (400); wherein the temperature of the pre-cooling device Tpre-device is less or equal to the temperature Tpre-reagent; and wherein the temperature difference ΔT=T2−Tpre-reagent is between 0° C.-0.5° C.
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the reagents have a temperature T1 when entering the pre-cooling device and have a temperature Tpre-reagent when leaving the pre-cooling device, wherein T1>Tpre-reagent; and wherein the reagents have a temperature T2 when entering the reaction vessel (400); wherein the temperature of the pre-cooling device Tpre-device is less or equal to the temperature Tpre-reagent; and wherein the temperature difference ΔT=T2−Tpre-reagent is between 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C., particularly preferably 0° C.-0.1° C., preferably 0° C.-0.09° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C.
Moreover, it is preferred that the temperature difference ΔT=T2−Tves of the temperature T2 of the reagents when entering the reaction vessel (400) and the temperature Tves of the solution in the reaction vessel (400) or the absolute value of that temperature difference |ΔT1=|T2−Tves| is within the range of 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C., particularly preferably 0° C.-0.1° C., preferably 0° C.-0.09° C., preferably 0° C.-0.08° C. preferably 0° C.-0.07° C. preferably 0° C.-0.08° C. preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C. Thus, the temperature difference ΔT or the absolute value of the temperature difference |ΔT| of the pre-cooled reagents before addition and at the time of addition to the reaction vessel is between 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C., particularly preferably 0° C.-0.1° C., preferably 0° C.-0.09° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C.
Since many glycosylation reactions require low temperatures and the formation of the intermediate reactive species could take place rather fast, the pre-cooling device according to the invention can assure a minimum temperature difference between the inside of the reaction vessel and the incoming reagents, in particular the building blocks and the activators. A cooling device provides a better control of the temperature at which the solid phase support and reagents (such as the building block and activators) get mixed. At the same time a pre-cooling device provides active cooling that allows reaching temperatures until e.g. −30° C.
Thus, in some preferred embodiments the pre-cooling device is positioned in a distance of 1 cm-20 cm, preferably 3 cm-10 cm, preferably 1-10 cm, preferably 1 cm-5 cm, and further preferably 0-1 cm to the reaction vessel to assure a minimum temperature difference between the inside of the reaction vessel and the incoming reagents. In embodiments, wherein the pre-cooling device is preferably positioned in close proximity to the one or more inlets of the reaction vessel e.g. at a distance of 0 cm-1 cm or 0 cm-2 cm, the pre-cooling device functions as a pre-cooling inlet for pre-cooling the reagents to be supplied. Thus, in several embodiments, the pre-cooling device is preferably a pre-cooling inlet for pre-cooling the reagents to be supplied.
Thus, it is preferred that the distance between the pre-cooling device and the reaction vessel is shorter than the distance between the pre-cooling device and the reagent delivery system. The reagent delivery system and the reaction vessel have a distance to each other. Furthermore, the reagent delivery lines between the reagent delivery system and the reaction vessel have a length, for instance, a length corresponding to the distance between the reaction vessel and the reagent delivery system. It is preferred that the pre-cooling device is positioned at the half of the distance adjacent to the reaction vessel, preferably in the third which is adjacent to the reaction vessel, more preferably at the quarter which is adjacent to the reaction vessel.
Thus, in preferred embodiments the distance between the pre-cooling device and the reaction vessel is 50%, preferably 40%, more preferably 30%, more preferably 25%, more preferably 20%, more preferably 15%, more preferably 10% and even more preferably 5% of the distance between the reagent delivery system and the reaction vessel.
Thus, in preferred embodiments the length of the reagent delivery lines between the pre-cooling device and the reaction vessel is 50%, preferably 40%, more preferably 30%, more preferably 25%, more preferably 20%, more preferably 15%, more preferably 10% and even more preferably 5% of the length of the reagent delivery lines between the reagent delivery system and the pre-cooling device.
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the distance between the pre-cooling device and the reaction vessel is 50%, preferably 40%, more preferably 30%, more preferably 25%, more preferably 20%, more preferably 15%, more preferably 10% and even more preferably 5% of the distance between the reagent delivery system and the reaction vessel.
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the distance between the pre-cooling device and the reaction vessel is 50%, preferably 40%, more preferably 30%, more preferably 25%, more preferably 20%, more preferably 15%, more preferably 10% and even more preferably 5% of the distance between the reagent delivery system and the reaction vessel, wherein the reagents have a temperature T1 when entering the pre-cooling device and have a temperature Tpre-reagent when leaving the pre-cooling device, wherein T1>Tpre-reagent; and wherein the reagents have a temperature T2 when entering the reaction vessel (400); wherein the temperature of the pre-cooling device Tpre-device is less or equal to the temperature Tpre-reagent; and wherein the temperature difference ΔT=T2−Tpre-reagent is between 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C., particularly preferably 0° C.-0.1° C., preferably 0° C.-0.09° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C., Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the distance between the pre-cooling device and the reaction vessel is 50%, preferably 40%, more preferably 30%, more preferably 25%, more preferably 20%, more preferably 15%, more preferably 10% and even more preferably 5% of the distance between the reagent delivery system and the reaction vessel, wherein the pre-cooled reagent solution does not warm up more than maximal 0.5° C., preferably 0.4° C., more preferably 0.3° C., more preferably 0.2° C., more preferably 0.1° C., more preferably 0.09° C., more preferably 0.08° C., more preferably 0.07° C., more preferably 0.08° C., more preferably 0.07° C., more preferably 0.06° C., and most preferably not more than maximal 0.05° C.
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the length of the reagent delivery lines between the pre-cooling device and the reaction vessel is 50%, preferably 40%, more preferably 30%, more preferably 25%, more preferably 20%, more preferably 15%, more preferably 10% and even more preferably 5% of the length of the reagent delivery lines between the reagent delivery system and the pre-cooling device.
Thus, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400) and the pre-cooling device (300) is positioned between the reaction vessel (400) and the reagent delivery system (600), wherein the length of the reagent delivery lines between the pre-cooling device and the reaction vessel is 50%, preferably 40%, more preferably 30%, more preferably 25%, more preferably 20%, more preferably 15%, more preferably 10% and even more preferably 5% of the length of the reagent delivery lines between the reagent delivery system and the pre-cooling device, wherein the reagents have a temperature T1 when entering the pre-cooling device and have a temperature Tpre-reagent when leaving the pre-cooling device, wherein T1>Tpre-reagent; and wherein the reagents have a temperature T2 when entering the reaction vessel (400); wherein the temperature of the pre-cooling device Tpre-device is less or equal to the temperature Tpre-reagent; and wherein the temperature difference ΔT=T2−Tpre-reagent is between 0° C.-0.5° C., preferably 0° C.-0.4° C., preferably 0° C.-0.3° C., preferably 0° C.-0.2° C., particularly preferably 0° C.-0.1° C., preferably 0° C.-0.09° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.08° C., preferably 0° C.-0.07° C., preferably 0° C.-0.06° C., preferably 0° C.-0.05° C.
In some embodiments it may be preferred that the pre-cooling device is adjusted to a temperature so that the reagents to be supplied are pre-cooled to a temperature of 0.0500-0.5° C. below the desired pre-cooling temperature Tpre-reagent. This is particularly preferred in case the pre-cooled reagent solution warms up by 0.05° C.-0.5° C. during delivery from the pre-cooling device to the reaction vessel, so that the temperature of the pre-cooled reagent solution is at the desired temperature Tpre-reagent=T2 at the time of addition to the reaction vessel.
As one synthesis cycle includes different thermal stages the device of the present invention additionally allows advantageous rapid and dynamic temperature adjustment for the different thermal stages of the synthesis cycles. Therefore, the device of the present invention allows dynamic cooling of the reaction mixture and simple and convenient adjustment of the temperature of the reaction vessel during the synthesis cycles of the synthesis of oligo- and polysaccharides on a solid support.
The synthesis cycle or glycosylation cycle or coupling cycle includes three stages. The first stage relates to providing and supplying of the reagents to the reaction vessel, the second stage relates to the coupling reaction which takes place inside of the reaction vessel followed by capping, deprotection and/or washing steps as third stage. Following the deprotection steps and optional capping steps the next synthesis cycle or glycosylation cycle may follow for introducing the next building block for building up the desired oligo- or polysaccharide in a step-by-step procedure. Therefore, three thermal stages are present in a synthesis cycle or glycosylation cycle. Thus, a synthesis cycle or glycosylation cycle may be classified into three temperature regimes or stages as shown in
The first stage relates to the pre-coupling regime in the range of −40° C. to room temperature, in other words in the range of −40° C. to 25° C. and preferably in the range of −40° C. to −10° C. In this pre-coupling regime the building block and activator are supplied or added and are allowed to impregnate the resin and to diffuse through the porous solid. The low temperature in the range of preferably −40° C. to −10° C. prevents the early decomposition of the intermediates before the actual coupling reaction.
The second stage relates to the coupling regime at a temperature around 0° C. or in the range of −10° C. to room temperature, in other words in the range of −10° to 25° C., preferably −10° C. to 5° C., more preferably −10° C.±3° C. to 0° C.±3° C. The increase in the temperature to preferably around 0° C. allows the initiation of the coupling reaction by promoting the formation of the intermediates.
The third stage relates to the post-coupling regime at a temperature around 25° C. (room temperature or standard temperature) or above. The capping and deprotection reactions take place at higher temperatures than the coupling reaction. These reactions complete the glycosylation cycle. Then, the next coupling cycle or termination of the process may take place.
According to the present invention the device for automated synthesis for oligo- and polysaccharides on a solid support comprises a cooling device for cooling the reaction vessel. The cooling device therefore provides active cooling to the reaction vessel and thus provides active cooling of the reaction mixture inside of the reaction vessel. The cooling device is therefore preferably in thermal communication with the reaction vessel. The cooling device is preferably adapted for cooling the reaction vessel to temperatures of −80° C. to +60° C., preferably −40° C. to 40° C. Thus, the device of the present invention may comprise a cooling device for regulating the temperature of the reaction vessel. The cooling device may be under control of a computing device comprising at least one processor. The cooling device may be further adapted to maintain the temperature within the reaction vessel. The cooling device may be adapted to adjust the temperature within +1° C. and −1° C. of the reaction temperature. The cooling device may be a heating and/or cooling device equipped with a temperature sensor or thermo-meter, wherein the cooling device temperature may be adjusted either manually or preferably by a computing device. For example, the cooling device could be a heating bath, an external refrigerated circulator or a heating/cooling block. The heating/cooling block may be made of any heat transfer material. The block may have channels running through to pass coolant fluid through. The reaction vessel may be placed in a cavity of the heating/cooling block. In a preferred embodiment of the present invention the coolant fluid may be circulated around the reaction vessel via a sleeve surrounding the reaction vessel. In preferred embodiments of the present invention the cooling device may comprise a cooling jacket. The cooling jacket may be in form of a cooling coil surrounding the reaction vessel. Preferably, the cooling jacket is in thermal communication with the reaction vessel. The cooling coil or cooling jacket may be further provided with a thermal isolation/insulation cover to increase the heat exchange efficiency of the cooling jacket or cooling coil.
The reaction vessel may be constructed as a double-wall structure which forms two cavities, wherein the first cavity accommodates the synthesis of oligo- and polysaccharides and wherein the second cavity accommodates a coolant fluid.
The double-wall structure of the reaction vessel may be made of glass. Thus, the reaction vessel may be provided with a cooling jacket for cooling the reaction vessel. Preferably, the cooling jacket may be made of a material such as glass, quartz, PTFE (Teflon), polypropylene or fluoropolymers. In preferred embodiments of the present invention the reaction vessel may be provided as an interchangeable reaction vessel. In such embodiments it is preferred that the reaction vessel may be removed from a cooling means such as a cooling jacket without interrupting the flow of a circulating coolant fluid. In such embodiments the reaction vessel may be removed for example for loading with solid support or for discharging the solid support. Furthermore such an interchangeable reaction vessel allows use of various reaction vessels with different sizes for different batch sizes.
The cooling device may be connected to a coolant fluid reservoir. The cooling device may be connected to a cooling circuit pump. In preferred embodiments of the invention the cooling jacket surrounding the reaction vessel may be connected to a coolant fluid reservoir and a coolant circuit pump. The coolant fluid reservoir, the coolant circuit pump and the cooling jacket surrounding the reaction vessel may form a closed cooling circuit. The cooling jacket may be provided in form of a cooling coil surrounding the reaction vessel. The coolant circuit pump may be under control of a computer comprising at least one processor. The cooling device may comprise a cooling unit configured to control the temperature of the cooling device. The cooling unit may be electronically coupled to a computing device comprising at least one processor. The cooling circuit pump may be electronically coupled to a computing device comprising at least one processor to control the flow of the coolant fluid through the cooling circuit.
In general, the incoming solutions are delivered at room temperature from the reagent delivery system to the reaction vessel. This supposes an increase of the temperature within the reactor vessel. Such a temperature increase is proportional to the incoming mass. This results in a detriment for the reagents and sensitive intermediates before the coupling. A pre-cooling component is introduced as a solution to this issue. Furthermore, the inventors have found that delivery of the incoming solutions at lower temperatures such as below 0° C. from the reagent containers to the reaction vessel still supposes an increase of the temperature and a thermal absorption without pre-cooling by the pre-cooling device according to the present invention.
Since many glycosylation reactions require low temperatures and the formation of the intermediate reactive species could take place rather fast, the device of the present invention comprises a pre-cooling device to assure a minimum temperature difference between the inside of the reaction vessel and the incoming reagents, in particular the building blocks and the activators. A cooling device provides a better control of the temperature at which the solid phase support and reagents (such as the building block and activators) get mixed. At the same time a pre-cooling device provides active cooling that allows reaching temperatures until −30° C.
Thus, according to the present invention the device for automated synthesis of oligo- and polysaccharides comprises a pre-cooling device for pre-cooling the reagents to be supplied.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device (100) comprising:
wherein the reagent delivery system (600) connects the reagent storing component (660) with the reaction vessel (400); wherein the pre-cooling device (300) is interposed between the reaction vessel (400) and the reagent delivery system (600); and wherein the pre-cooling device (300) is in thermal communication with the reagent delivery system (600).
Preferably the pre-cooling device is in thermal communication with the reagent delivery system. The pre-cooling device is preferably interposed between the reaction vessel and the reagent delivery device. The pre-cooling device is preferable positioned in close proximity to the one or more inlets of the reaction vessel. Thus, the pre-cooling device may be adapted to function as a pre-cooling inlet for pre-cooling the reagents to be supplied. The pre-cooling component may be adapted for active cooling of the reagents to be supplied. In other words the incoming solutions at room temperature from the reagent delivery system are actively cooled by the pre-cooling device to a temperature around the preset temperature of the reaction mixture in the reaction vessel. By pre-cooling the at room temperature incoming solutions to around the temperature of the reaction vessel the reagents to be supplied are added to the reaction mixture at a temperature that preferably corresponds to the temperature of the reaction mixture in the reaction vessel. Furthermore, the incoming solutions from the reagent delivery system at a temperature below 0° C. are actively cooled by the pre-cooling device to a reproducible and stable temperature around the preset temperature of the reaction mixture in the reaction vessel. Thus, temperature fluctuations and a rewarming of cooled incoming solutions can be avoided and prevented by the pre-cooling device as the incoming solutions are pre-cooled to a preset temperature, the pre-cooling temperature, independent of the temperature before passing or traversing the pre-cooling device. The pre-cooling device therefore guarantees that the incoming solutions and the reagents to be supplied to the reaction vessel have the desired temperature at the time of addition in the reaction vessel.
Preferably, the reagent delivery system (600) being in fluid communication with the reaction vessel (400) through one or more reagent delivery lines (601, 602); and the pre-cooling device (300) being in thermal communication with the one or more reagent delivery lines (601, 602). Preferably, the reaction vessel (400), the pre-cooling device (300), the reagent delivery system (600) and the reagent storing component (660) are successively connected in the following sequence: reaction vessel—pre-cooling device—reagent delivery system—reagent storing component. The reagent delivery system (600) being preferably in fluid communication with the reagent storing component (660) and being further in fluid communication with the reaction vessel (400). Preferably, the reagent storing component (660) and the pre-cooling device (330) are connected through the reagent delivery system (600). Preferably, at least one liquid line between the reagent delivery system (600) and the reaction vessel (400) is pre-cooled by the pre-cooling device (300) located between the reagent delivery system (600) and the reaction vessel (400).
In one embodiment, all reagents and solvents, including, building blocks, activators and washing solvents, are pre-cooled before addition to the reaction mixture in the reaction vessel. In one embodiment, only the activators or activator solutions are pre-cooled before addition to the reaction mixture in the reaction vessel. Preferably at least the building blocks and activators (or a solution thereof) are pre-cooled before addition to the reaction mixture in the reaction vessel and preferably all reagents and solutions added to perform the coupling reaction are pre-cooled close to the temperature of the reaction mixture in the reaction vessel. Furthermore, the resulting intermediates are often temperature sensitive and may decompose at higher temperatures then the desired temperature of the reaction mixture. It should be clear that already formed temperature sensitive intermediates in the reaction mixture may decompose in case further warmer reagents or solvents are added to the reaction mixture, such as reagents or solvents at room temperature. In such a case it may be suitable to supply these reagents or solvents in a slow and careful manner, for example dropwise manner, by monitoring the temperature of the reaction mixture at the same time. However, in larger batch sizes a larger amount of the reagents to be supplied are added to the reaction mixture. The delayed addition, for example dropwise addition, and the period of time until the reaction mixture is adjusted to the desired and preset temperature may also result in decomposition of the reagents and in particular the sensitive intermediates. The inventors of the present invention have found that on the one hand the rapid addition of the reagents to the reaction mixture in the pre-coupling stage and impregnating of the resin to allow these reagents to diffuse through the porous solid for a period of time of 1 minute to 20 minutes, preferably 5 minutes has an advantageous effect on the overall yield of the desired oligo- and polysaccharide. On the other hand the inventors have found that the monitoring of the reaction mixture temperature during the addition of reagents and solvents and the careful and slow addition of these reagents such that the reaction mixtures maintains the desired reaction mixture has also an advantageous effect on the overall yield of the desired oligo- and polysaccharide. The device of the present invention comprising a reaction vessel, a reagent storing component, a reagent delivery system, a cooling device for cooling the reaction vessel, and a pre-cooling device for pre-cooling the reagents to be supplied has the advantage that the pre-cooled reagents to be supplied may be added in a faster and rapid manner to the reaction mixture without unfavorable temperature fluctuations in the reaction mixture in the pre-coupling stage at preferably −40° C. to −10° C. and has the advantages that the added pre-cooled reagents may be allowed to impregnate the resin to diffuse through the porous solid for a period of time of 1 minute to 20 minutes, preferably 5 minutes such that the overall time of the pre-coupling stage including the adding and impregnating of the reagents may be reduced such that decompositions of the reagents and the resulting intermediates may be effectively prevented in comparison to a slow and careful addition of the reagents to be supplied which may result in an overall time of the pre-coupling stage of over 25 minutes or 30 minutes or more.
The rapid addition of the pre-cooled reagents in the pre-coupling stage to allow effective impregnation of the resin and the prevention of the temperature fluctuation during the addition of the pre-cooled reagents has been shown to be particularly advantageous with regard to the glycosylation reactions in the synthesis of oligo- and polysaccharides.
The pre-cooling device is preferably adapted for pre-cooling of the reagents to be supplied to the corresponding temperature of the reaction mixture in the reaction vessel. For example, if the reaction vessel is actively cooled to a temperature of −30° in the pre-coupling stage of a synthesis cycle the reagents to be supplied may preferably be pre-cooled also to a temperature of −30° C. by the pre-cooling device or preferably to −31° C. or −32° C. or −33° C. or to a lower temperature. In such a case the pre-cooled reagents at a temperature of −30° C. are added to the reaction mixture having a temperature of −30° C., wherein temperature fluctuations in the reaction mixture are prevented during addition of the reagents. However, the reagents to be supplied to the reaction vessel may be also added at a slightly higher temperature then the temperature of the reaction mixture in the reaction vessel.
Preferably the reagents are pre-cooled by the pre-cooling device to a temperature in the temperature range corresponding to the temperature range of −40° C. to −8° C., preferably of −30° C. to −9° C., and more preferably to the temperature range of −20° C. to −10° C. of the pre-coupling stage. In preferred embodiments of the present invention the pre-cooling device may be adapted for pre-cooling the reagents to be supplied at least to a temperature which is not higher than −3° C., preferably −6° C., more preferably −8° C. or −10° C. of the temperature of the reaction mixture in the reaction vessel so that the temperature of the supplied reagents is not higher than 3° C., preferably 600, more preferably 8° C. or 10° C. below the temperature of the reaction mixture in the reaction vessel. Preferably the pre-cooling device may be adapted to cool the reagents to be supplied to a temperature in the range of 3° C. to 6° C. below the temperature of the reaction mixture in the reaction vessel. Thus, it is preferred that the reagents to be supplied are pre-cooled to the corresponding temperature of the reaction vessel with a maximum variance of 0° C. to 10° C. below the temperature of the reaction mixture in the reaction vessel. Most preferably the temperature of the reaction mixture in the reaction vessel does not exceed a temperature of −10° C. in the pre-coupling stage of the synthesis cycle.
Thus, it is preferred that the reagents to be supplied are pre-cooled to the corresponding temperature of the reaction vessel with a maximum variance of 10° C. or maximum deviation of 10° C., preferably with a maximum variance of 5° C. or maximum deviation of 5° C., more preferably with a maximum variance of 3° C. or maximum deviation of 3° C. In preferred embodiments it is preferred that the temperature of the reaction mixture in the reaction vessel does not exceed a temperature of −10° C. in the pre-coupling stage of the synthesis cycle.
Most preferably, the temperature of the reagents to be supplied to the reaction vessel is in the range of −18° C. to −8° C., preferably in the range of −1600 to −9° C., more preferably in the range of −1400 to −10° C. and still more preferably in the range of −12° C. to −10° C.
In preferred embodiments of the present invention various liquid lines such as washing solvents lines, building block lines, and activator solution lines may be pre-cooled before feeding the reaction vessel. In other words the pre-cooling device may be located upstream to the reaction vessel. The pre-cooling device may be interposed between the reaction vessel and the reagent delivery system.
Thus, the reaction vessel may be connected to a pre-cooling device which allows active pre-cooling of various liquid lines such as washing solvents, building blocks, activator solution before said washing solvents, building blocks, activator solution are delivered and supplied to the reaction vessel. In such embodiments the flow of liquid to the reaction vessel from the reagent delivery system is not interrupted as the reagents to be supplied to the reaction vessel are pre-cooled during the delivery to the reaction vessel. Preferably the flow speed of the liquids through the various liquid lines are taken into account as by lower flow speeds the reagents may be pre-cooled for a longer period of time to enable effective cooling to the desired temperatures. In one embodiment, all liquid lines between the reagent delivery system and the reaction vessel are pre-cooled by the pre-cooling device located between the reagent delivery system and the reaction vessel. In one embodiment, only one liquid line between the reagent delivery system and the reaction vessel is pre-cooled by the pre-cooling device located between the reagent delivery system and the reaction vessel. In a further embodiment, at least one liquid line between the reagent delivery system and the reaction vessel is pre-cooled by the pre-cooling device located between the reagent delivery system and the reaction vessel.
In preferred embodiments of the present invention the pre-cooling device may comprise a metal cooling surface made of a metal heat exchange material. In such embodiment the building block delivery line and activator line may contact the metal cooling surface at a preset temperature. Thus, the metal cooling surface may be cooled to a predefined temperature. Preferably the predefined temperature corresponds to the temperature of the reaction mixture in the reaction vessel, thus preferably corresponds to the desired reaction temperature. The metal cooling surface may be made of any known metal heat exchange material. In further preferred embodiments the washing solvent delivery line may also contact the metal cooling surface at a preset temperature.
In preferred embodiments of the present invention the pre-cooling device may comprise a thermoelectric contact-cooling device such as a Peltier cooler. The cooling effect provided by a Peltier cooler is based on the well-known Peltier effect. The Peltier cooler is adapted to provide the means to reach the preset temperature. Thus, the Peltier cooler may be in thermal communication with the metal cooling surface.
In preferred embodiments the thermoelectric contact-cooling device is assisted by a line of coolant fluid, such as for example cooling water, preferably at a temperature of 15° C. to cool down the warm side of the thermoelectric contact-cooling device. The cooling water line could be provided by a central cooling system or a compact commercial cooling unit.
In preferred embodiments of the present invention the pre-cooling device may also provide active cooling to the reaction vessel. In other words the pre-cooling device may be a part or component of the cooling device. In such embodiments the pre-cooling device may provide active cooling to the cooling jacket surrounding the reaction vessel. Thus, the pre-cooling device may be adapted to provide active cooling to the cooling circuit comprising the cooling jacket, cooling circuit pump and the coolant fluid reservoir. In such embodiments the cooling device for cooling the reaction vessel and the pre-cooling device for pre-cooling the reagents to be supplied are adjusted simultaneously to the same preset temperature. Thus, based on the preset temperature for cooling of the reaction vessel the reagents to be supplied will be pre-cooled to the temperature of the reaction vessel.
The cooling device serves as temperature control unit and should be capable of regulating and maintain the temperature of the inside of the reaction vessel at a desired temperature(s). To accomplish the automated solid-phase synthesis of many different types of oligosaccharides, the temperature control unit in form of the cooling device may be capable of maintaining the temperate inside of the reaction vessel at a set temperature of between room temperature and −30° C. To achieve this the Peltier cooler (thermoelectric) contact-cooling device may provide the means to cool down a metal surface of the pre-cooling device reaching temperature equal or lower to the set reaction temperature to compensate later temperature increases downstream. Channels or grooves on the cooling surface may enhance the contact with the reagent delivery lines improving the heat transfer. The pre-cooling device is placed external to a reaction chamber and before the inlets to the reaction vessel. Pre-cooling action may be provided by contacting the surface with lines for delivering the building blocks and activator solution. The washing solvents delivered by the solvent delivery line could be pre-cooled as well by the action of the Peltier cooler by contacting the cooling surface. An active cooling action may be given by a coolant liquid served from a coolant reservoir that is immediately adjacent to the cooling surface, which provides the heat-exchange surface. The coolant reservoir may also contain a microwave transparent coolant that is driven by a cooling circuit pump and may be circulated through a cooling coil around the reactor vessel, in another embodiment the coil could be substituted by a cooling jacket surrounding the reaction vessel walls. The cooling coil or jacket may provide active cooling to the reaction vessel.
As an example,
Thus, the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support comprising a reaction vessel, a cooling jacket in thermal communication with the reaction vessel, a reagent storing component, a reagent delivery system in fluid communication with the reaction vessel, a pre-cooling device interposed between the reaction vessel and the reagent delivery system.
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support comprising a reaction vessel, a cooling jacket in thermal communication with the reaction vessel and surrounding the reaction vessel, a reagent storing component, a reagent delivery system in fluid communication with the reaction vessel, a pre-cooling device interposed between the reaction vessel and the reagent delivery system.
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support comprising a reaction vessel, a cooling jacket in thermal communication with the reaction vessel and surrounding the reaction vessel, a reagent storing component, a reagent delivery system in fluid communication with the reaction vessel through one or more reagents delivery lines, a pre-cooling device interposed between the reaction vessel and the reagent delivery system, the pre-cooling device in thermal communication with the one or more reagents delivery lines.
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support comprising a reaction vessel, a cooling jacket in thermal communication with the reaction vessel and surrounding the reaction vessel, the cooling jacket arranged and/or integrated in a cooling circuit, a reagent storing component, a reagent delivery system in fluid communication with the reaction vessel through one or more reagent delivery lines, a pre-cooling device interposed between the reaction vessel and the reagent delivery system, the pre-cooling device in thermal communication with the one or more reagents delivery lines and in thermal communication with the cooling circuit and a computing device comprising at least one processor configured to control one or more components of the device.
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the pre-cooling device is interposed between the reaction vessel and the reagent delivery device.
Therefore, the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the pre-cooling device is upstream to the cooling device.
Therefore, the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the pre-cooling device is located downstream to the reagent delivery system and upstream to the reaction vessel.
Therefore, the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising: the device (100) comprising:
The device for automated synthesis of oligo- or polysaccharide may further comprise a microwave generator component. Microwave-assisted organic chemical synthesis refers to the use of electromagnetic radiation within the microwave frequencies to provide the energy required to initiate, drive or accelerate certain chemical reactions. Several multimode or mono-mode/single-mode microwave generator components for microwave-assisted organic synthesis are known in the art, for example, in multimode instruments microwaves are reflected by the walls of a relatively large cavity, which may generate pockets of high and low energy as the moving waves either reinforce (hot spots) or cancel out each other (cold spots) leading to a non-homogeneous microwave field in the cavity. In order to provide a homogeneous field, multimode instruments may be equipped with a mechanical mode stirrer inside the cavity. In mono-mode cavities a standing wave may be created when the electromagnetic irradiation is passed by a waveguide that directs the microwaves directly through a reaction vessel that is positioned in a fixed distance from the radiation source or by generating travelling waves where the microwaves make a single pass through the reaction vessel, are reflected off the cavity wall and pass through the reaction vessel a second time. Multimode microwave components enable performance of parallel synthesis, whereas mono-mode microwave components provide a high degree of reproducibility due to a very precise heating. The microwave generator component may be one of a magnetron, klystron and solid state devices. A solid-state microwave generator component uses a semiconductor transistor which generates single, defined microwave frequencies in a controlled manner.
Thus, in preferred embodiments of the present invention the device may further comprise a microwave generator component, preferably a mono-mode/single-mode microwave generator component. The microwave generator component may further comprise a waveguide. The microwave generator component preferably comprises a chamber for insertion and fixing of the reaction vessel to provide microwave radiation to the reaction vessel.
In comparison to conductive heating microwave heating (dielectric heating at 2.45 GHz) occurs by disposing the energy directly to the solvent and some reagents, due to interactions of the solvents and reagents with the alternating electric field. Material interacts with the electromagnetic field differently, i.e. materials store and convert the energy to heat to different extents, which have huge impact on their ability to be heated by microwaves. Besides the solvent, several other factors influence the dielectric properties, such as sample volume, vessel material, and the mode of stirring. The application of heat energy (thermal transfer) is one of the most significant factors in increasing the rate of a wide variety of chemical reactions. Microwave-assisted reactions, however, transfer energy to chemical reactions in a different, much faster manner than the conductive devices. Microwave energy directly interacts with polar or ionic molecules. This, effect, known as dipole rotation, is a result of the polar or ionic molecules trying to align themselves with the rapidly changing electric field of the microwaves. The rotational movement of molecules as they try to orient themselves with the electric field creates localized superheating and generates thermal energy as a by-product.
Thermal energy may be raised beyond a critical point for a given reaction, resulting in excess thermal energy. Excess thermal energy increases the temperature of a reaction mixture. This excess thermal energy may have detrimental effects on heat-sensitive reactions or compositions. Excess thermal energy can drive side reactions that degrade the reactants, catalysts and desired product of the desired reaction. Furthermore, some products may be unstable at room temperature. Therefore it is advantageous to maintain a low bulk reaction mixture temperature. The beneficial effects of simultaneous cooling during microwave irradiation have been described in the art to be useful for chemical synthesis with solid phase supports.
The inventors of the present invention have found that the utilization of a microwave generator component is not only instrumental for hastening the cooling to heating process, microwave-assisted synthesis has also been shown to drastically reduce chemical reaction time. During a typical AGA cycle there is the glycosylation coupling step as well as several auxiliary steps (acetyl capping and temporary group deprotection). These auxiliary steps increase the overall yield of the final glycan by terminating unglycosylated nucleophiles as well as they remove temporary protecting groups that allows the next coupling to occur. These auxiliary steps have been a bottleneck in the overall time required for one AGA cycle and the use of microwave radiation drastically reduces the reaction time. Under these rapid microwave-assisted conditions, the steps remained orthogonal and few side reactions were observed. With shortened reaction times for these auxiliary steps, the overall duration of a standard AGA cycle could be successfully reduced from 100 minutes to below 60 minutes and even to 45 minutes. Thus, the auxiliary steps carried out in the automated saccharide synthesis benefit from the use of microwave radiation.
The inventors were able to selectively manipulate protecting groups at oligosaccharides under microwave irradiation, which allows the production of complex saccharide structures. Overall, the inventors were able to achieve the synthesis of a Lewis antigen tetrasaccharide in 6.6 hours (see Example 12). The inventive device therefore enables the efficient synthesis of complex oligosaccharides and polysaccharides by selective protecting group manipulations under microwave irradiation (see Examples 7 to 10).
A solid support or solid phase resin which is stable under microwave conditions or microwave irradiation is particularly preferred with regard to embodiments of the device of the present invention further comprising a microwave generator component. Such a microwave-stable solid support or solid phase resin is particularly suitable for performing microwave-assisted synthesis of oligo- and polysaccharides on a solid support. Therefore, it is particularly preferred that no decomposition of the solid phase resin occurs during the microwave-assisted synthesis steps of the synthesis cycles. In other words a solid support material is preferred which is stable under microwave conditions and also a linker is preferred which is stable under microwave conditions. Thus, a solid phase resin functionalized with an appropriate linker which is stable under microwave conditions is particularly preferred, which also means that no decoupling from the solid phase resin occurs during the microwave-assisted synthesis steps of the synthesis cycles.
In embodiments of the device of the present invention further comprising a microwave generator component it is particularly preferred that the reaction vessel is made of a microwave transparent material. Examples of microwave transparent materials include, but are not limited to, glass, quartz, PTFE (Teflon), perfluoroalkoxy alkane (PFA), polypropylene. A microwave transparent reaction vessel is particularly preferred in embodiments, wherein the device of the present invention further comprises a microwave generator component and the synthesis cycles comprise one or more microwave-assisted synthesis steps performed inside of the reaction vessel.
It is preferred that the microwave transparent reaction vessel further comprises at least one opening or aperture for insertion of a microwave compatible temperature sensor for monitoring and measuring the temperature inside of the reaction vessel. Thus, it is preferred that the temperature sensor is a microwave-compatible temperature sensor and suitable for monitoring and measuring the temperature inside of the reaction vessel during microwave-assisted synthesis steps.
The inventors have found that microwave-assisted synthesis steps advantageously reduce the overall period of time of the overall synthesis of the desired oligo- or polysaccharides, which was also shown to increase the yield of the desired oligo- or polysaccharide.
The cooling device may be a microwave transparent heating and/or cooling device equipped with a microwave transparent temperature sensor or thermometer, wherein the cooling device temperature may be adjusted either manually or preferably by a computing device. For example, the cooling device could be a heating bath, an external refrigerated circulator or a heating/cooling block. The heating/cooling block may be made of any microwave transparent heat transfer material known in the art. The block may have channels running through to pass microwave transparent coolant fluid through. The microwave transparent reaction vessel may be placed in a cavity of the microwave transparent heating/cooling block. In a preferred embodiment of the present invention a microwave transparent coolant fluid may be circulated around the microwave transparent reaction vessel via a microwave transparent sleeve surrounding the microwave transparent reaction vessel. In preferred embodiments the cooling device may comprise a microwave transparent cooling jacket. In preferred embodiments the microwave transparent cooling jacket may be in form of a microwave transparent cooling coil surrounding the microwave transparent reaction vessel. The microwave transparent cooling jacket is preferably in thermal communication with the microwave transparent reaction vessel. The cooling coil or cooling jacket may be further provided with a microwave transparent thermal isolation/insulation cover to cover the cooling jacket or cooling coil from exposure to the chamber to increase the heat exchange efficiency of the cooling jacket or cooling coil.
The cooling device may be connected to a coolant fluid reservoir. The cooling device may be connected to a cooling circuit pump. In preferred embodiments of the present invention the microwave transparent cooling jacket surrounding the microwave transparent reaction vessel may be connected to a coolant fluid reservoir and a coolant circuit pump. The coolant fluid reservoir, the coolant circuit pump and the microwave transparent cooling jacket surrounding the microwave transparent reaction vessel may form a closed cooling circuit. The microwave transparent cooling jacket may be provided in form of a cooling coil surrounding the microwave transparent reaction vessel. The coolant circuit pump may be under control of a computer comprising at least one processor. The cooling device may comprise a cooling unit configured to control the temperature of the cooling device. The cooling unit may be electronically coupled to a computing device comprising at least one processor. The cooling circuit pump may be electronically coupled to a computing device comprising at least one processor to control the flow of the coolant fluid through the cooling circuit.
The present invention relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reagent delivery system connects the reagent storing component with the reaction vessel.
The present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the cooling device is upstream to the pre-cooling device.
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
Therefore, the present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably relates to a device for automated synthesis of oligo- and polysaccharides on a solid support in the range of 12.5-200 μmol per synthesis.
The present invention preferably ably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reagent delivery system connects the reagent storing component with the reaction vessel;
wherein the pre-cooling device is interposed between the reaction vessel and the reagent delivery system; and
wherein the pre-cooling device is in thermal communication with the reagent delivery system (600).
A further aspect of the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reagent delivery system connects the reagent storing component with the reaction vessel;
wherein the pre-cooling device is interposed between the reaction vessel and the reagent delivery system; and
wherein the pre-cooling device is in thermal communication with the reagent delivery system (600).
The device according to the present invention is particularly suitable for automated multi-step synthesis on solid support, wherein each step requires a different temperature regime. The device may comprise a cooling device and a microwave generator component which are regulated or controlled by a thermal controller, thereby allowing rapid adjustment of the reaction temperature and therefore shorter reaction times.
A typical coupling cycle in a glycan synthesis comprises a glycosylation step and several protecting group manipulations (“auxiliary steps”) including a capping reaction in order to terminate unreacted saccharides, deprotection of a temporary protecting group and washing of the solid support. These steps of each coupling cycle are conducted in three different three temperature regimes or stages (as described above).
The first stage relates to the pre-coupling regime in the temperature range TA of preferably −40° C. to −10° C. The low temperature in the range of preferably −40° C. to −10° C. prevents the early decomposition of the intermediate before the actual coupling reaction. The second stage relates to the coupling regime at a temperature TB around 0° C., i.e. −10° C. and +5° C. The increase in the temperature to preferably around 0° C. allows the initiation of the coupling reaction by promoting the formation of the intermediates. Thus, during the coupling regime, the glycosylation reaction takes place. The third stage relates to the post-coupling regime at a temperature Tc around 25° C. (room temperature or standard temperature) or above, up to 70° C. The high reaction temperature Tc can be achieved by microwave irradiation. Thus, the capping and deprotection reactions can take place under microwave irradiation and at higher temperatures than the coupling reaction. These reactions complete the coupling cycle. Then, the next coupling cycle or termination of the process may take place.
As can be seen in
Particularly, the thermal controller can be connected to the temperature sensor in the microwave transparent reaction vessel and the microwave generator component, thereby allowing the reaction mixture to reach the reaction temperature of Tc in the post-coupling regime. The thermal controller may adjust the power output of the microwave generator component based on the measured temperature inside the reaction vessel in order to maintain the temperature Tc. Also, the thermal controller may connected to the temperature sensor in the microwave transparent reaction vessel and the microwave generator component thereby allowing the reaction mixture to warm up more rapidly from a reaction temperature of TA to TB during the coupling regime.
The thermal controller may be also connected to the cooling device thereby allowing setting a fixed cooling temperature TA during pre-coupling regime and/or TB during the coupling and post-coupling regime. The microwave generator component is usually turned off by the thermal controller during pre-coupling and coupling regime and only turned on during the post-coupling regime. However, in one embodiment the microwave generator component is already turned on by the thermal controller during coupling regime in order to speed up the warming from TB to Tc.
Thus, the thermal controller connected to a cooling device and a microwave generator component allows the use of the microwave generator component as a heater, so that no additional heater is required for performing the auxiliary steps at elevated temperatures. Therefore, due to the thermal controller a simpler and more compact setup of the synthesizer is achieved as no additional cooler or heater are necessary for performing the multi-step reactions at different temperature regimes as set forth above.
A further aspect of the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the gas container (801) is in fluid communication with the manifold line (840), the one or more reagent containers (630, 631, 632 . . . ) and the reaction vessel (400) are in separate fluid communications with the output lines (852) of the gas valve manifold (802), and wherein the at least three output lines (852) are equipped with a means for preventing flow of reagents into the manifold line, wherein the means for preventing flow of reagents into the manifold line is check valve (833-839).
The present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the gas container (801) is in fluid communication with the manifold line (840), the one or more reagent containers (630, 631, 632 . . . ) and the reaction vessel (400) are in separate fluid communications with the output lines (852) of the gas valve manifold (802), and wherein the at least three output lines (852) are equipped with a means for preventing flow of reagents into the manifold line,
wherein the means for preventing flow of reagents into the manifold line is check valve (833-839),
wherein the reagent delivery system connects the reagent storing component with the reaction vessel;
wherein the pre-cooling device is interposed between the reaction vessel and the reagent delivery system; and
wherein the pre-cooling device is in thermal communication with the reagent delivery system (600).
Therefore, the present invention is directed to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the gas container (801) is in fluid communication with the manifold line (840), the one or more reagent containers (630, 631, 632 . . . ) and the reaction vessel (400) are in separate fluid communications with the output lines (852) of the gas valve manifold (802), wherein the means for preventing flow of reagents into the manifold line is check valve (833-839).
Therefore, the present invention is also related to a synthesizer (100) for automated multistep synthesis on a solid support comprising:
wherein the gas container (801) is in fluid communication with the manifold line (840), the one or more reagent containers (630, 631, 632 . . . ) and the reaction vessel (400) are in separate fluid communications with the output lines (852) of the gas valve manifold (802), wherein the means for preventing flow of reagents into the manifold line is check valve (833-839).
In another embodiment of the present invention the reaction vessel may be provided as a flow reaction vessel to allow automated synthesis of oligo- and polysaccharides on a solid support in a continuous flow process. The reaction vessel may be provided in form of a tube reaction vessel or preferably may be provided as a packed-bed reaction vessel or column reaction vessel which allows heterogeneous transformations where reagents are on solid support.
Thus, in one embodiment the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reaction vessel is a flow reaction vessel.
The device may also comprise a microwave generator component. The flow reaction vessel may be made for example of glass, borosilicate, Teflon, fluoropolymer or SiC. Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the microwave transparent reaction vessel is a microwave transparent flow reaction vessel.
Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reaction vessel is a packed-bed reaction vessel.
The device may also comprise a microwave generator component. Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the microwave transparent reaction vessel is a microwave transparent packed-bed reaction vessel.
For performing the coupling reactions appropriate building blocks and activators may be provided in a continuous flow through the flow reaction vessel. Preferably, the building blocks and activators may be provided in a continuous flow through the flow reaction vessel already containing the solid support or solid phase resin. In such a case the flow reaction vessel is preferably a packed-bed reaction vessel. The coupling reactions preferably take place inside the flow reaction vessel followed by appropriate deprotection, capping and/or washing steps. All of these synthesis steps and treatments in the synthesis cycles are preferably performed inside of the flow reaction vessel of the device of the present invention and the reagents and/or solution and/or solvents are provided in a continuous flow through the flow reaction vessel. The synthesis cycles are repeated as often as necessary to achieve the desired length of the desired oligo- or polysaccharide. The synthesis cycle is preferably repeated at least three times, more preferably at least four times or more preferably more than four times for obtaining an oligo- or polysaccharide.
The reagent delivery system may be connected to the flow reaction vessel through one or more inlets of the flow reaction vessel for delivery of the reagents and/or reagents solution and/or solvents in a continuous flow through the continuous flow reaction vessel. The reagent delivery system may be connected to the flow reaction vessel through one or more reagent delivery lines. Thus, the reagent delivery system may be adapted to deliver reagents and/or reagent solutions and/or solutions and/or solvents in a continuous flow through the flow reaction vessel and may be further adapted to supply the reagents and/or reagent solution and/or solutions or solvents through the one or more inlets of the flow reaction vessel. Preferably the reagent delivery system may be adapted to deliver one or more reagents and/or one or more reagent solutions and/or one or more solutions in different amounts, at different points in time and in a specific sequence or specific order, and at a specific flow rate or different flow rates and further through specific inlets of the one or more inlets of the flow reaction vessel during the synthesis cycles of the automated synthesis of oligo- and polysaccharides on a solid support. It is therefore preferred that the reagent delivery system comprises suitable technical means, preferably suitable technical means electronically coupled to a computing device comprising at least one processor, for delivery of one or more reagents and/or one or more reagent solutions and/or one or more solutions in different amounts, at different points in time and in a specific sequence or specific order and at a specific flow rate or at different flow rates during the synthesis cycles of the automated synthesis of oligo- and polysaccharides on solid support. The reagent delivery system may comprise a pump system or one or more pumps such as syringe pumps, peristaltic pumps or other suitable pumps and may further comprise one or more valves or one or more valve assemblies, one or more manifolds, one or more distributing components and similar suitable technical means. It is preferred that the pump system or the one or more pumps, the one or more valves or the one or more valve assemblies, the one or more manifolds and/or the one or more distributing components and similar technical means are under control of a computing device comprising at least one processor.
In a further embodiment only specific reaction steps of the synthesis cycle may be performed in a continuous flow process. Thus, the automated synthesis of oligo- and polysaccharides on a solid support may be performed in a semi-continuous flow process. For example, the glycosylation reaction or coupling reaction may be performed without continuous flow of the reagents through the reactor, whereas the deprotection steps and/or capping steps may be performed in a continuous flow process. In such embodiments the building blocks and activators may be provided to the flow reaction vessel without simultaneous discharging the reagents to be supplied or without recirculating the reagents to be supplied. Thus, in the pre-coupling regime the building blocks and activators are allowed to impregnate the resin and to diffuse through the porous solid. As mentioned above the flow reaction vessel may be connected to one or more valves or one or more valve assemblies, one or more manifolds, one or more distributing components and similar suitable technical means. The one or more valves or one or more valve assemblies, one or more manifolds, one or more distributing components and similar suitable technical means may be adapted to hold the reagents, solvents or solutions inside the flow reaction vessel and may be further adapted to discharge the reagents, solvents or solutions from the flow reaction vessel and may even be adapted to allow recirculation of the reagents, solvents or solutions through the flow reaction vessel. Therefore, the flow reaction vessel may be operated in a continuous flow mode or may be operated in a non-continuous flow mode. Thus, the flow reactor may be switchable between a continuous flow mode and a non-continuous flow mode. Thus, the flow reactor may be switchable between a continuous flow mode and a semi-batch or batch mode. The modes may be switched via one or more valves or one or more valve assemblies or one or more manifolds and/or one or more distributing components or similar technical means.
In a further embodiment the flow reactor may comprise a frit or a filter to prevent canalization of fluid through. As already described above a frit allows for dispersion of inert gas bubbling for mixing purposes and the frit may also ensure that the solid support remains inside of the reaction vessel. Thus, in preferred embodiments of the present invention the flow reaction vessel may further comprise a frit or a filter. It is preferred that the frit is located in the bottom compartment of the flow reaction vessel. Thus, it is preferred that the frit is located close to the outlet where the flow of solvents and solutions leave the flow reaction vessel. Thus, to prevent solid support from being drawn from the bottom inlet, the end-part in the flow reaction vessel may be fitted with a frit or a filter. In a further embodiment a frit or filter may be used which only allows passage or through-flow of solvents and solutions through the frit or filter by applying an elevated pressure from the top or reduced pressure at the bottom of the frit or filter. For example the continuous flow of a solvent or solution may be achieved in that the solvent or solution is supplied under elevated pressure to the flow reaction vessel. In such embodiments the solvent or solution may pass the frit or filter to allow continuous flow of the solvent or solution through the flow reaction vessel. In another example the solvent or solution may be applied without elevated pressure or only at slightly elevated pressure such that the solvent or solution may not pass the frit or filter. In such a case the flow reaction vessel may be filled with the solvent and solution, for example, building blocks or activators, and in this example the building blocks and/or activators may impregnate the solid phase resin as it is beneficial in the pre-coupling stage as already described above. In such embodiment it is further preferred that bubbling gas for agitating the reaction mixture, such as inert gas is provided to the flow reaction vessel.
Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reaction vessel is a flow reaction vessel, wherein the flow reaction vessel is switchable between a continuous flow mode and a semi-batch mode.
The device may also comprise a microwave generator component. Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the microwave transparent reaction vessel is a microwave transparent flow reaction vessel, wherein the microwave transparent flow reaction vessel is switchable between a continuous flow mode and a semi-batch mode.
Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reaction vessel is flow reaction vessel, wherein the flow reaction vessel is switchable between a continuous flow mode and a semi-batch or batch mode via one or more valves or one or more valve assemblies or one or more manifolds and/or one or more distributing components or similar technical means.
The device may also comprise a microwave generator component. Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the microwave transparent reaction vessel is a flow reaction vessel,
wherein the microwave transparent flow reaction vessel is switchable between a continuous flow mode and a semi-batch mode via one or more valves or one or more valve assemblies or one or more manifolds and/or one or more distributing components or similar technical means.
Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reaction vessel is a flow reaction vessel, wherein the flow reaction vessel comprises a frit, wherein the flow of solvent and/or solution through the frit is pressure-dependent.
The device may also comprise a microwave generator component. Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the microwave transparent reaction vessel is a flow reaction vessel,
wherein the microwave transparent flow reactor comprises a frit, wherein the flow of solvent and/or solution through the frit is pressure-dependent.
In a further embodiment the continuous flow process may be performed by recirculating the reagents, solvents and/or solutions through the flow reaction vessel. The flow reaction vessel may connected to itself via one or more valves, one or more valve assemblies, one or more manifolds and/or the one, one or more distributing components and similar technical means so that a flow can pass the flow reaction vessel repeated times. Thus, one or more outlets (or bottom inlets) of the flow reaction vessel may be connected through one or more valves, one or more valve assemblies, one or more manifolds, one or more distributing components and/or similar suitable technical means with one or more inlets of the flow reaction vessel. Preferably one or more inlets at the bottom of the flow reaction vessel are connected with one or more inlets at the top of the flow reaction vessel via one or more valves, one or more valve assemblies, one or more manifolds and/or the one, one or more distributing components and similar technical means so that a flow can pass the flow reaction vessel repeated times. For example the deprotection reagents and/or capping reagents may recirculate through the flow reaction vessel. In a further example all reagents, solvents and solutions may recirculate through the flow reaction vessel. In case of building blocks and activators it is preferred that the building blocks or building block solution and the activators or activator solution are mixed or merged before passing through the flow reaction vessel. The building blocks or building block solution and the activators or activator solutions may be mixed or merged directly at the time of supplying the building blocks or building block solution and the activators or activator solution to the flow reaction vessel.
Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the reaction vessel is a flow reaction vessel and wherein the flow reaction vessel is connected to itself via one or more valves or one or more valve assemblies or one or more manifolds and/or one or more distributing components or similar technical means so that a flow can pass the flow reaction vessel repeated times.
The device may also comprise a microwave generator component. Thus, the present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
wherein the microwave transparent reaction vessel is a microwave transparent flow reaction vessel and wherein the microwave transparent flow reaction vessel is connected to itself via one or more valves or one or more valve assemblies or one or more manifolds and/or one or more distributing components or similar technical means so that a flow can pass the microwave transparent flow reaction vessel repeated times.
The device of the present invention may further comprise a computing device comprising at least one processor and a computer-readable storage medium comprising computer readable instructions that may be executed by the processor. The processor may be configured to control the temperature setting of the pre-cooling device, may be configured to control the temperature setting of the cooling device, and may be configured to set the time, temperature and power of the microwave generator component, may be configured to control the amount and speed of delivering fluid from the reagent delivery system. The device of the present invention preferably comprises one or more or a plurality of technical means electronically coupled to the computing device comprising at least one processor to allow the processor to control the one or more or plurality of technical means based on computer readable instructions stored on a computer readable medium which may be executed by the processor to enable the automation of the synthesis of oligo- and polysaccharides on a solid support with the device of the present invention. The one or more technical means or plurality of technical means may be wired or wirelessly connected to the computing device. The one or more technical means or plurality of technical means may comprise one or more valves, valve assemblies, one or more vents and similar technical means of the one or more components and systems of the device of the present invention. The device of the present invention may further comprise one or more temperature monitoring means to allow temperature control of the cooling device and/or pre-cooling device and to allow temperature control of the reaction mixture inside of the reaction vessel. The computing device comprising the at least one processor may be configured to receive the temperature monitoring data from the cooling device, pre-cooling device and from one or more temperature monitoring means such as a temperature sensor or temperature probe. Based on the received temperature monitoring data the processor may be configured to adjust the cooling device and/or pre-cooling device to maintain a temperature inside of the reaction vessel.
Thus, the present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
The present invention preferably further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
In
The bottom delivery system 700 receives the deprotection reagent solutions and capping reagent solution from a reagent storing component 760.
By splitting the reagent delivery system in a top and a bottom delivery system optimizes the number and the use of driving fluid components. The top delivery system feeds precisely the coupling reagents for instance by using syringe pump, while washing solvents and evacuating anhydrous gas are driven from the top for instance by gas differential pressure. The bottom delivery system is driven by gas differential pressure and directs the different deprotection and capping reagents into the reaction vessel 400. This prevents potential mixing of incompatible chemicals (e.g. acids and bases) used at different steps of the synthesis program, and economizes the number of mechanical fluid driving devices.
An inert gas delivery system 800 provides anhydrous and inert gas to the device for mixing, atmosphere conditioning and driving fluids purposes.
In the embodiment shown in
The process is automated and controlled by a computing device comprising at least one processor 200. The processor controls the execution of commands, which adjusts the temperature of pre-cooling component 300; sets the time, temperature and power of the microwave generator component 500; controls the amount and speed of delivering fluid from the top delivery system 600 and bottom delivery system 700.
The rotary valve 607 distributes the fluids within the activator distribution component 652. The lines 627-629 allows for withdrawal of activator solutions from an activator storing component 662 comprising the containers 630-632. The line 602 delivers activator solution to the reaction vessel by passing through the pre-cooling component 300. The line 623 delivers excess activator solution to the waste container 704. The line 624 supplies inert gas to the rotary valve distributor 607 from the splitter 618. By the lines 634-636 the splitter 633 provides an anhydrous and inert gas atmosphere to the containers 630-632. The signal line 208 delivers the command from the computing device 200 to the rotary valve distributor 607. The loop line 626 communicates the rotary valve 607 with the syringe pump 603. The signal line 209 delivers the commands to the syringe pump 603. One or more of the containers may be cooled for example by a cooling bath 654, which provides the mean to adjust the temperature of an activator reagent below the room temperature. For example, a Dewar filled with ice or a contact cooling device, such a Peltier cooling element may be used to provide cooling of the one or more containers.
The washing solvent distribution component 651 provides the reactor vessel 400 with the following exemplary washing solvents of a washing solvent storing component 661: Dichloromethane line 643 from solvent container 639, tetrahydrofuran line 644 from the solvent container 640, dimethylformamide line 645 from solvent container 641. The solvent container 638 provides 1,2-dichloroethane line to the syringe pump 603 as driving fluid by the line 642. The order of delivery is controlled by the four way magnetic valve 637. The washing line 645 delivers washing solvents to the top of the reaction vessel 400 by passing through the pre-cooling component 300, which was regulated by the valve 605. The magnetic valve 637 also serves to deliver inert gas to the top of the reactor vessel via the line 645. The washing solvent containers 638-641 are pressurized with gas from the lines 646-649, which is provided by the splitter 650. The signal line 210 delivers the command from the computing device to the multiple ways valve 637 while the line 211 communicates to the valve 605. The line 818 serves with gas the syringe pump 603.
In preferred embodiments of the present invention the device may further comprise a light source for cleaving photo-cleavable linkers.
The present invention further relates to a device for automated synthesis of oligo- and polysaccharides on a solid support, the device comprising:
In one embodiment the device may further comprise a microwave generator component and the reaction vessel may be microwave transparent.
The present invention further relates to a method for automated synthesis of oligo- and polysaccharides on a solid support with a device comprising:
The present invention preferably relates to a method for automated synthesis of oligo- and polysaccharides on a solid support with a device comprising:
wherein the reagent delivery system connects the reagent storing component with the reaction vessel;
wherein the pre-cooling device is interposed between the reaction vessel and the reagent delivery system; and
wherein the pre-cooling device is in thermal communication with the reagent delivery system.
The device may further comprise a microwave generator component and the reaction vessel may be microwave transparent.
The present invention further relates to a method for automated synthesis of oligo- and polysaccharides on a solid support with a device comprising:
The device may further comprise a microwave generator component and the reaction vessel may be microwave transparent.
The present invention further relates to a method for automated synthesis of oligo- and polysaccharides on a solid support with a device comprising:
wherein the reagent delivery system connects the reagent storing component with the reaction vessel;
wherein the pre-cooling device is interposed between the reaction vessel (400) and the reagent delivery system; and
wherein the pre-cooling device is in thermal communication with the reagent delivery system.
The present invention further relates to a method for automated synthesis of oligo- and polysaccharides on a solid support with a device comprising:
the method comprising at least the following steps:
The present invention further relates to a method for automated synthesis of oligo- and polysaccharides on a solid support with a device comprising:
The present invention further relates to a method for synthesizing oligo- and polysaccharides with a device (100) comprising:
the method comprising the following steps:
The present invention further relates to a method for synthesizing oligo- and polysaccharides with a device (100) comprising:
the method comprising the following steps:
The present invention further relates to a method for automated synthesis of oligo- and polysaccharides on a solid support with a device comprising:
The present invention further relates to a method for synthesizing oligo- and polysaccharides, comprising the following steps:
wherein the further saccharide and/or the glycosylation reagent are added to the solid support at a temperature in the range of −40° C. to −9° C., the temperature of the further saccharide and/or the glycosylation reagent being ±1° C. of the temperature of the reaction mixture.
The present invention further relates to a method for synthesizing oligo- and polysaccharides, comprising the following steps:
wherein the further saccharide and the glycosylation reagent are added to the solid support at a temperature in the range of −20° C. to −10° C., the temperature of the further saccharide and the glycosylation reagent being ±3° C., preferably ±1° C. of the temperature of the reaction mixture.
The present invention further relates to a method for synthesizing oligo- and polysaccharides with a device (100) comprising:
the method comprising the following steps:
wherein the further saccharide and the glycosylation reagent are added to the solid support at a temperature in the range of −40° C. to −9° C., the temperature of the further saccharide and the glycosylation reagent being maximum ±3° C., preferably ±1° C. of the temperature of the reaction mixture.
The present invention further relates to a method for synthesizing oligo- and polysaccharides with a device (100) comprising:
the method comprising the following steps:
The present invention preferably relates to a method for synthesizing oligo- and polysaccharides, comprising the following steps:
Preferably, in step b) the glycosylation reagent and the further saccharide are pre-cooled to a temperature of at least −40° C. to −9° C. during delivery to and before addition to the solid support. Preferably, in step a) the solid support is cooled to a temperature of at least −40° C. to −9° C. Preferably, in step a) the solid support is cooled to a temperature of at least −40° C. to −9° C. before addition of the glycosylation reagent. Preferably, in step b) the glycosylation reagent having a temperature of ±3° C., preferably ±1° C., of the temperature of the further saccharide and the solid support. Preferably, in step b) the glycosylation reagent having a temperature of ±1° C. of the temperature of the further saccharide and the solid support. Preferably, in step b) the glycosylation reagent has a temperature difference of ±3° C. to the temperature of the further saccharide and the solid support. Preferably, in step b) the glycosylation reagent has a temperature difference of ±1° C. to the temperature of the further saccharide and the solid support.
The present invention preferably relates to a method for synthesizing oligo- and polysaccharides, comprising the following steps:
The present invention preferably relates to a method for synthesizing oligo- and polysaccharides, comprising the following steps:
Preferably, in step a) the reaction vessel (400) containing the solid support is cooled to a temperature of at least −40° C. to −9° C. by a cooling device (350).
The present invention preferably relates to a method for synthesizing oligo- and polysaccharides, comprising the following steps:
Preferably, in step b) the glycosylation reagent has a temperature of ±3° C. of the temperature of the further saccharide and the solid support in the reaction vessel (400). Preferably, in step b) the glycosylation reagent has a temperature of ±1° C. of the temperature of the further saccharide and the solid support in the reaction vessel (400).
Preferably the saccharide immobilized on the solid support is a glycosyl acceptor comprising 1 to 20 monosaccharide units.
Preferably, the further saccharide is a glycosyl donor comprising a glycal, epoxide or orthoester group or having a leaving group at the reducing end selected from halogen, —O—C(═NH)—CCl3, —O—C(═NPh)-CF3, —OAc, —SR5, —SO-Ph, —SO2-Ph, —O—(CH2)3—CH═CH2, —O—P(OR5)2, —O—PO(OR5)2, —O—CO—OR5, —O—CO—SR5, —O—CS—SR5, —O—CS—OR5,
Preferably, the at least one protecting group of the further saccharide is a temporary protecting group selected from allyl, p-methoxybenzyl, 2-naphthylmethyl, tri-isopropylsilyl, tert-butyldimethylsilyl, tert-butylmethoxyphenylsilyl, triethylsilyl, trimethylsilyl, 2-trimethylsilylethoxymethyl, 9-fluorenylmethoxycarbonyl and levulinoyl.
Preferably, the immobilized saccharide comprises at least one permanent protecting group and/or the further saccharide comprises at least one permanent protecting group, in addition to the at least one protecting group, selected from acetyl, phenyl, benzyl, isopropylidene, benzylidene, benzoyl, p-methoxybenzyl, p-methoxy-benzylidene, p-methoxyphenyl, p-bromobenzylidene, p-nitrophenyl, allyl, allyloxycarbonyl, monochloroacetyl, isopropyl, p-bromobenzyl, dimethoxytrityl, trityl, 2-naphthylmethyl, pivaloyl, triisopropylsilyl, tert-butyldimethylsilyl, tert-butyldiphenylsilyl, tert-butylmethoxyphenylsilyl, triethylsilyl, trimethylsilyl, 2-trimethylsilylethoxymethyl, 9-fluorenylmethoxycarbonyl, tert-butyloxycarbonyl, benzyloxymethyl, methyloxymethyl, tert-butyloxymethyl, methoxyethyloxymethyl, and levulinoyl.
Preferably, the solid support obtained in step b) is treated with a capping reagent, optionally under microwave irradiation.
Preferably, the glycosylation reagent is a Lewis acid selected from: AgOTf, BF3.OEt2, trimethylsilyl trifluoromethanesulfonate, trifluoromethanesulfonic acid, trifluoromethanesulfonic anhydride, lanthanoid(III) triflates, NIS/AgOTf, NIS/TfOH or dimethyl(methylthio)sulfonium trifluoromethanesulfonate.
Preferably, the removal of the at least one protecting group is performed at a reaction temperature of at least 40° C.
Preferably, step b) is performed at a reaction temperature below 000 and optionally under microwave irradiation. Preferably, step b) is performed without microwave irradiation. Preferably, in step b) the glycosylation reagent is cooled to a temperature of at least −40° C. to −9° C., before addition to the further saccharide and the solid support.
Preferably, the method further comprises the steps:
d) cleaving the saccharide obtained in step c) from the solid support;
e) purifying the saccharide obtained in step d).
Preferably, the method further comprises a step a′) between step a) and step b):
a′) washing the solid support of step a) with an acidic solution.
The following examples are included to demonstrate preferred embodiments of the invention. It should be appreciated by those of skill in the art that the techniques disclosed in the examples which follow represent techniques discovered by the inventor to function well in the practice of the invention, and thus can be considered to constitute preferred modes for its practice. However, those of skill in the art should, in light of the present disclosure, appreciate that many changes can be made in the specific embodiments which are disclosed and still obtain a like or similar result without departing from the spirit and scope of the invention.
Further modifications and alternative embodiments of various aspects of the invention will be apparent to those skilled in the art in view of this description. Accordingly, this description is to be construed as illustrative only and is for the purpose of teaching those skilled in the art the general manner of carrying out the invention. It is to be understood that the forms of the invention shown and described herein are to be taken as examples of embodiments. Elements and materials may be substituted for those illustrated and described herein, parts and processes may be reversed, and certain features of the invention may be utilized independently, all as would be apparent to one skilled in the art after having the benefit of this description of the invention. Changes may be made in the elements described herein without departing from the spirit and scope of the invention as described in the following claims.
The improvement in conditions and reaction time for the capping and deprotection steps with microwave radiation was investigated. During a typical AGA cycle there is the glycosylation coupling step as well as several auxiliary steps (acetyl capping and temporary group deprotection). These auxiliary steps increase the overall yield of the final oligo- or polysaccharide (glycan) by terminating unglycosylated nucleophiles as well as they remove temporary protecting groups that allows the next coupling to occur. These auxiliary steps have been a bottleneck in the overall time required for one AGA cycle. The investigation of the overall time required for one AGA cycle by using microwave radiation during these auxiliary steps has shown that microwave assisted deprotection and capping steps drastically reduce the reaction time. The results shown in Table 1 demonstrate that the utilization of a microwave generator component is not only instrumental for hastening the cooling to heating process, microwave-assisted synthesis also drastically reduces chemical reaction time. Under these rapid microwave-assisted conditions, the steps remained orthogonal and few side reactions were observed. With shortened reaction times for these auxiliary steps the overall duration of a standard AGA cycle was successfully reduced from 100 minutes to below 60 minutes and even to 45 minutes. First results have also shown that the glycosylation reaction benefits from the use of microwave radiation.
The temperature development inside of the reaction vessel during a synthesis cycle in the presence and absence of pre-cooling device was investigated.
The three thermal stages are shown. Temperature spikes appear when a liquid is dispensed in the reaction vessel. The dashed curve shows the temperature profile for the device without pre-cooling of the reagents. The thermal spikes are remarkable at the pre-coupling regime (subzero temperatures). The solid line depicts the temperature profile with active pre-cooling. The incoming solution of reagents is pre-cooled and this suppresses the temperature spikes. Since there are three thermal stages during a glycosylation cycle: (1) The pre-coupling regime (−40° C. to −10° C.). The building block and activator are allowed to impregnate the resin and for diffusion through the porous solid. The low temperature prevents the early decomposition of the intermediate before the actual coupling; (2) the coupling regime (around 0° C.). The increase in the temperature allows for initiating the coupling reaction by promoting the formation of the intermediates; and (3) the post-coupling regime (room temperate or above). The capping and deprotection reactions take place at higher temperature. These reactions close out the glycosylation cycle. Then, the next coupling or process termination takes place.
In
In
In
In
In
In
In
The advantages and improvement of the automated glycosylation via pre-cooling of the reagents are most apparent in
The current example was performed with and without pre-cooling of the activators solution and building block/donor solution; within a glass reaction vessel.
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by the software. The reagent delivery system is based on valve-pressured control in which the entire platform is constantly pressurized so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves. Some of the reagents are delivered by the withdrawing and/or dispensing action of a syringe pump. Before start the modules, the program initializes all the components (valves, active cooling, pre-cooling, pump, sensors and actuators); renews the driving solvent in the loops 625 and 626; the program empties and flushes the reagents delivery lines.
The resin loaded into the reaction vessel is washed with DMF, THF, DCM (six times each with 3 mL for 15 s). The resin is swollen in 2 mL DCM, and the temperature of the reaction vessel was adjusted in the range of −18° C. to −17° C. For acidic washing, 1 mL of the solution of TMSOTf is delivered to the reaction vessel via the pre-cooling device which reaches a temperature of −15° C. After three minutes, the solution is drained. Finally, 3 mL DCM is added to the reaction vessel, incubated for 15 s, and drained out.
Thioglycoside building block is dissolved in the proper solvent mixture (4 mL for four glycosylation cycles) in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. During the adjustment of the temperature, the DCM in the reaction vessel is drained and 1 mL of thioglycoside building block (6.5 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device which cools the solution of thioglycoside building block to a temperature of −15° C. After the temperature reached the range of −18° C. to −17° C. ° C., 1.0 mL NIS and TfOH solution in DCM and dioxane (v/v, 2:1) is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device which cools the activator solution down to a temperature of −15° C. The glycosylation mixture is incubated for 5 min at the temperature range of −18° C. to −17° C., linearly ramped to 0° C., and after reaching 0° C. the reaction mixture is incubated for an additional 20 min. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCM (once, 2 mL for 15 s). Then the resin is washed with 2 mL of Dioxane. Finally, the resin is washed twice with DCM (2 mL for 15 s).
The temperature of the reaction vessel is adjusted to 25° C. The resin is washed twice with DMF (3 mL for 15 s). 2 mL of Pyridine solution (10% in volume in DMF) was delivered and the resin is incubated for one minute. The resin is washed three times with DCM (2 mL for 15 s). The capping of the unreacted acceptor groups is done by delivering 4 mL of methanesulfonic acid (2% in volume) and acetic anhydride (10% in volume) in DCM. The resin and the reagents are incubated for 10 min; then 1 mL of DCM in added to dilute the solution and the incubation continues for another 10 min. The solution is drained from the reaction vessel and the resin is washed 3 times with DCM (2 mL for 15 s).
The resin is washed with DMF (three times with 3 mL for 15 s), swollen in 2 mL DMF and the temperature of the reaction vessel is adjusted to 25° C. For Fmoc-deprotection the DMF is drained and 2 mL of a solution of 20% Piperidine in DMF was delivered to the reaction vessel. After 5 min the reaction solution is drained from the reactor vessel. Then, the resin is washed with DMF (three times with 3 mL for 15 s) and DCM (five times with 3 mL). After this module the resin is ready for the next glycosylation cycle.
Resin 1103 (see
After buildup of the tetramer on the resin the oligosaccharide was cleaved from solid support in a photo-reactor: A mercury lamp is turned on 30 min prior to the first cleavage event. The fluorinated-ethylene-propylene (FEP) tubing was washed with 20 mL DCM at a flow rate of 5 mL/min before cleavage. The solid support was pre-swelled in the dark in DCM for 30 min at least before being taken up with a 20 mL disposable syringe. The suspension of solid support in DCM was slowly injected from the disposable syringe (20 mL) into the FEP tubing using a syringe pump. The suspension was pushed through the FEP tubing into the photo-reactor with additional 18 mL DCM (flow rate: 700 μL/min). The photo-cleavage took place inside the reactor while solid support travelled toward the exit point of the reactor. The suspension leaving the reactor was directed into a syringe equipped with polyethylene filter frit where the resin was filtered off and the solution containing the cleaved oligosaccharide is collected in a separate glass vial. The tubing as washed with 20 mL DCM (flow rate: 2 mL/min) until any remaining resin exited the reactor and the remaining oligosaccharide solution is collected. The tubing was re-equilibrated with 20 mL DCM using a flow rate of 5 mL/min and the entire cleavage procedure was repeated. The combined solution that was collected in the photo-cleavage process was evaporated in vacuo and the crude material was analyzed by MALDI-TOF, and HPLC.
The current example was performed within a PFA/glass reactor, in a factorial experimental design with two factors: active cooling of the reaction vessel and pre-cooling action of the activators solution and building block/donor solution, each factor had two levels with and without active temperature control (on and off stage of the corresponding device).
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by the software. The reagent delivery system is based on valve-pressured control in which the entire platform is constantly pressurized so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves. Some of the reagents are delivered by the withdrawing and/or dispensing action of a syringe pump. Before start the modules, the program initializes all the components (valves, active cooling, precooling, pump, sensors and actuators); renews the driving solvent in the loops 625 and 626; the program empties and flushes the reagents delivery lines.
The resin loaded into the reaction vessel is washed with DMF, THF, DCM (six times each with 3 mL for 15 s). The resin is swollen in 2 mL DCM, and the temperature of the reaction vessel was adjusted in the range of −18° C. to −17° C. by cooling device (when it is programed to do so). For acidic washing 1 mL of the solution of 2% TMSOTf in DCM is delivered to the reaction vessel via the pre-cooling device which cools the solution to a temperature of −15° C. (when it is programed to do so). After three minutes, the solution is drained. Finally, 3 mL DCM is added to the reaction vessel.
Phosphate building block is dissolved in the proper solvent mixture e.g. DCM (5 mL for one initial double cycle for the first coupling and three more single glycosylation cycles to build up the tetramer) in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. During the adjustment of the temperature in the reactor vessel (when it is programed to do so), the DCM in the reaction vessel is drained and 1 mL of phosphate building block 2 (5.0 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device which cools the solution of phosphate building block (when it is programed to do so) to a temperature of −15° C. After the set temperature in the range of −18° C. to −17° C. is reached the resin is incubated in the solution of phosphate building block for 10 min. Then 1.0 mL of the solution of 2% TMSOTf in DCM is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device which cools the activator solution down to a temperature of −15° C. (when it is programed to do so). The glycosylation mixture is incubated for 30 min in the temperature range of −18° C. to −17° C., linearly ramped to 0° C. (when it is programed to do so), and after reaching 0° C. the reaction mixture is incubated for an additional 10 min. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCE (once, 2 mL for 5 s).
The temperature of the reactor vessel is adjusted to 25° C. The resin is washed twice with DMF (3 mL for 15 s). 2 mL of Pyridine solution (10% in volume in DMF) was delivered and the resin is incubated for one minute. The resin is washed three times with DCM (2 mL for 15). The capping of the unreacted acceptor groups is done by delivering 4 mL of Methanesulfonic acid (2% in volume) and Acetic anhydride (10% in volume) in DCM. The resin and the reagents are incubated for 10 min; then 1 mL of DCM in added to dilute the solution and the incubation continues for another 10 min. The solution is drained from the reactor vessel and the resin is washed 3 time with DCM (2 mL for 15 s).
The resin is washed with DMF (three times with 3 mL for 15 s), swollen in 2 mL DMF and the temperature of the reaction vessel is adjusted to 25° C. For Fmoc deprotection the DMF is drained and 2 mL of a solution of 20% Piperidine in DMF was delivered to the reaction vessel. After 5 min the reaction solution is drained from the reactor vessel. Then, the resin is washed with DMF (three times with 3 mL for 15 s) and DCM (five times with 3 mL). After this module the resin is ready for the next glycosylation cycle.
Resin 1103 (see
After buildup of the tetramer on the resin the oligosaccharide was cleaved from solid support in a photoreactor: A mercury lamp is turned on 30 min prior to the first cleavage event. The fluorinated-ethylene-propylene (FEP) tubing was washed with 20 mL DCM at a flow rate of 5 mL/min before cleavage. The solid support was pre-swelled in the dark in DCM for 30 min at least before being taken up with a 20 mL disposable syringe. The suspension of solid support in DCM was slowly injected from the disposable syringe (20 mL) into the FEP tubing using a syringe pump. The suspension was pushed through the FEP tubing into the photoreactor with additional 18 mL DCM (flow rate: 700 μL/min). The photo-cleavage took place inside the reactor while solid support travelled toward the exit point of the reactor. The suspension leaving the reactor was directed into a syringe equipped with polyethylene filter frit where the resin was filtered off and the solution containing the cleaved oligosaccharide is collected in a separate glass vial. The tubing as washed with 20 mL DCM (flow rate: 2 mL/min) until any remaining resin exited the reactor and the remaining oligosaccharide solution is collected. The tubing was re-equilibrated with 20 mL DCM using a flow rate of 5 mL/min and the entire cleavage procedure was repeated. The combined solution that was collected in the photo-cleavage process was evaporated in vacuo and the crude material was analyzed by MALDI-TOF, and HPLC.
The automated synthesis of tetramannose as shown in Scheme 1 was conducted by combining constant cooling with microwave radiation to adjust and control the temperature of the reagents during the glycosylation cycle.
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by software. The reagent delivery system utilizes pressure control valves, which constantly pressurize the entire platform, so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves. All the solvents are pre-cooled before they are delivered inside the reaction vessel.
The resin loaded into the reaction vessel is washed with DMF, THF, DCM (six times each with 3 mL for 15 s). The resin is swollen in 2 mL DCM, and the temperature of the reaction vessel was adjusted in the range of −22° C. to −20° C. by cooling device (when it is programmed to do so). For acidic washing, 1 mL of the solution of 2% TMSOTf in DCM is delivered to the reaction vessel via the pre-cooling device which cools the solution to a temperature of −20° C. (when it is programmed to do so). After three minutes, the solution is drained. Finally, 3 mL DCM is added to the reaction vessel.
Phosphate building block is dissolved in the proper solvent (6.5 eq. in 1.0 mL DCM) and loaded in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. During the adjustment of the temperature, the DCM in the reaction vessel is drained and 1 mL of phosphate building block (6.5 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device, which cools the solution of phosphate building block to a temperature of −15° C. After the temperature reached the range of −18° C. to −17° C., 1.0 mL NIS and TfOH solution in DCM and dioxane (v/v, 2:1) is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device, which cools the activator solution down to a temperature of −15° C. The glycosylation mixture is incubated for 5 min at the temperature range of −18° C. to −17° C., linearly ramped to 0° C., and after reaching 0° C. the reaction mixture is incubated for an additional 30 minutes. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCM (once, 2 mL for 15 s). Then the resin is washed with 2 mL of Dioxane. Finally the resin is washed twice with DCM (2 mL for 15 s).
While the temperature of the active cooling element is kept in the range of −22° C. to −20° C. preparing for the next coupling cycle. The temperature of the reactor vessel is kept between 70° C. and 20° C. by microwave irradiation of the washing solution and reagents, adjusting the irradiation power. The resin is washed twice with DMF (3 mL for 15 s). 2 mL of pyridine solution (10% in volume in DMF) were delivered and the microwave irradiation power is then adjusted to 40-50 W. The resin is incubated for one minute between 70° C. and 20° C. The resin is washed three times with DCM (2 mL for 15). The microwave irradiation power is then set to 150-180 W to proceed the capping of the unreacted acceptor groups. The capping is done by delivering 4 mL of methanesulfonic acid (2% in volume) and acetic anhydride (10% in volume) in DCM. The resin and the reagents are incubated for 1 min. The temperature of the reactor vessel is adjusted between 70° C. and 20° C. by microwave irradiation; then 1 mL of DCM in added to dilute the solution and the incubation continues for another 1 min. The solution is drained from the reactor vessel and the resin is washed 3 times with DCM (2 mL for 15 s).
The resin is washed with DMF (three times with 3 mL for 15 s), swollen in 2 mL DMF. For Fmoc deprotection, 2 mL of a solution of 20% piperidine in DMF were delivered to the reaction vessel. The temperature of the reagents inside the reactor vessel is adjusted between 70° C. and 20° C. by microwave irradiation (40 W). After 1 min, the reaction solution is drained from the reactor vessel. Then, the resin is washed with DMF (three times with 3 mL for 15 s) and DCM (five times with 3 mL). After this module, the resin is ready for the next glycosylation cycle.
The resin functionalized with a photo-cleavable linker (45 mg; loading 0.30 mmol/g) (see Scheme 1) was loaded into the reaction vessel of the synthesizer and swollen in 2 mL DCM.
The reaction sequence for the formation of tetramannose 9 was as follows:
1. Module 1 was performed with 1 mL TMSOTf solution at the temperature range of −22° C. to −20° C. (when it is programmed to do so) for 3 min.
2. Module 2 was performed with 5 equiv Building Block and 2% TMSOTf in DCM solution.
3. Module 3 was carried out in two steps; first 2 mL of pyridine solution (10% in volume in DMF); then in a second step with 4 mL of methanesulfonic acid (2% in volume) and acetic anhydride (10% in volume) in DCM.
4. Module 4 was carried out with 20% piperidine in DMF.
6. Subsequently, modules 1-4 were repeated four times in order to obtain a tetramer.
After build-up of the tetramer on the resin, the oligosaccharide was cleaved from solid support in a photoreactor: A mercury lamp is turned on 30 min prior to the first cleavage event. The fluorinated-ethylene-propylene (FEP) tubing was washed with 20 mL DCM at a flow rate of 5 mL/min before cleavage. The solid support was pre-swollen in the dark in DCM for 30 min at least before being taken up with a 20 mL disposable syringe. The suspension of solid support in DCM was slowly injected from the disposable syringe (20 mL) into the FEP tubing using a syringe pump. The suspension was pushed through the FEP tubing into the photo-reactor with additional 18 mL DCM (flow rate: 700 μL/min). The photo-cleavage took place inside the reactor while solid support travelled toward the exit point of the reactor. The suspension leaving the reactor was directed into a syringe equipped with polyethylene filter frit where the resin was filtered off and the solution containing the cleaved oligosaccharide is collected in a separate glass vial. The tubing was washed with 20 mL DCM (flow rate: 2 mL/min) until any remaining resin exited the reactor and the remaining oligosaccharide solution is collected. The tubing was re-equilibrated with 20 mL DCM using a flow rate of 5 mL/min and the entire cleavage procedure was repeated. The combined solution that was collected in the photo-cleavage process was evaporated in vacuo and the crude material was analyzed by MALDI-TOF, and HPLC.
After weighing, the recovered crude was 27 mg, which correspond to a 65% yield. This experiment demonstrates that high yields were obtained by combining pre-cooling of the reagents and constant cooling with microwave radiation even with short coupling times of 30 minutes.
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by software. The reagent delivery system is utilizes a pressure control syringe pump system, which constantly pressurize the entire platform, so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves, or withdrawing and dispensing with the motorized syringe in connection with a rotary valve.
Module 1: Acidic Washing: The same acidic washing module was applied as in Example 5.
Phosphate building block is dissolved in the proper solvent mixture, e.g. DCM (5 mL for one initial double cycle for the first coupling and three more single glycosylation cycles to build up the tetramer) in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. During the adjustment of the temperature in the reactor vessel (when it is programmed to do so), DCM is drained in the reaction vessel and 1 mL of phosphate building block (5.0 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device, which cools the solution of phosphate building block (when it is programmed to do so) to a temperature of −18° C. Then 1.0 mL of a solution of 2% TMSOTf in DCM is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device, which cools the activator solution down to a temperature of −18° C. (when it is programmed to do so). The glycosylation mixture is incubated for 20 min in the temperature range of −22° C. to −20° C. Keeping constant the active cooling action by microwave transparent coolant flowing in the jacket, the linearly ramped to 0° C. in 5 min (when it is programmed to do so) by the microwave radiation, adjusting the maximum radiation power to 180 W, and after reaching 0° C. the reaction mixture is incubated for additional 10 minutes. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCE (once, 2 mL for 5 s).
Module 3: NAP Deprotection (ca. 60 min):
The resin is washed with DCM (three times with 2 mL for 15 s). For NAP deprotection, 2 mL of a solution of 2% DDQ and 13% methanol in DCE was delivered to the reaction vessel. The temperature of the reagents inside the reactor vessel is adjusted between 60° C. and 20° C. by microwave irradiation (180 W). After 30 min, the reaction solution is drained from the reactor vessel. The resin is washed with DCM (three times with 2 mL for 15 s); the incubation in NAP deprotection solution between 60° C. and 20° C. by microwave irradiation (180 W) and the DCM washes were repeated twice more. Then, the resin is washed (3 times) with the following solvent sequence DMF, THE and DCM (3 mL for 120 s each). After this module, the resin is ready for the next glycosylation cycle.
The resin functionalized with a photo-cleavable linker (45 mg; loading 0.30 mmol/g) (see Scheme 2) was loaded into the reaction vessel of the synthesizer and swollen in 2 mL DCM.
The sequence of reaction steps for the formation of tetramannose was as follows:
1. Module 1 was performed with 1 mL TMSOTf solution at the temperature range of −22° C. to −20° C. (when it is programmed to do so) for 3 min.
2. Module 2 was performed twice with 5 equiv Building Block and 2% TMSOTf in DCM solution.
3. Module 3 was carried out with 2% DDQ and 13% methanol in DCE.
4. After Module 1 took place, the Module 2 repeated twice (for the first and last coupling). Then Module 3 was performed.
5. Subsequently, modules 1-3 were repeated three times in the same manner as described in steps 1-3 in order to obtain a tetramer 11.
After buildup of the tetramer on the resin, the oligosaccharide was cleaved from solid support in a photoreactor as described in Example 5.
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by software. The reagent delivery system is utilizes a pressure control syringe pump system, which constantly pressurize the entire platform, so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves, or withdrawing and dispensing with the motorized syringe in connection with a rotary valve.
The same acidic washing module was applied as in Example 5.
Phosphate building block is dissolved in the proper solvent mixture e.g. DCM (5 mL for one initial double cycle for the first coupling and three more single glycosylation cycles to build up the tetramer) in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. During the adjustment of the temperature in the reactor vessel (when it is programmed to do so), the DCM in the reaction vessel is drained and 1 mL of phosphate building block (5.0 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device which cools the solution of phosphate building block (when it is programmed to do so) to a temperature of −18° C. Then 1.0 mL of the solution of 2% TMSOTf in DCM is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device which cools the activator solution down to a temperature of −18° C. (when it is programmed to do so). The glycosylation mixture is incubated for 30 min in the temperature range of −22° C. to −20° C. Keeping constant the active cooling action by microwave transparent coolant flowing in the jacket, the linearly ramped to 0° C. in 5 min (when it is programmed to do so) by the microwave radiation, adjusting the maximum radiation power to 180 W, and after reaching 0° C. the reaction mixture is incubated for additional 10 min. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCE (once, 2 mL for 5 s).
Module 3: Lev Deprotection (ca. 5 min):
The resin is washed with DCM (three times with 2 mL for 15 s). For Lev deprotection, 2 mL of a solution of 1% hydrazine acetate and 21% acetic acid in pyridine was delivered to the reaction vessel. The temperature of the reagents inside the reactor vessel is adjusted between 40° C. and 20° C. by microwave irradiation (180 W). After 1 min, the reaction solution is drained from the reactor vessel. The resin is washed with DCM (three times with 2 mL for 15 s); the incubation in Lev deprotection solution between 40° C. and 20° C. by microwave irradiation (180 W) and the DCM washes were repeated twice more. Then, the resin is washed (3 times) with the following solvent sequence DMF, THE and DCM (3 mL for 15 s each). After this module the resin is ready for the next glycosylation cycle.
The resin functionalized with a photo-cleavable linker (45 mg; loading 0.30 mmol/g) (see Scheme 3) was loaded into the reaction vessel of the synthesizer and swollen in 2 mL DCM.
The sequence of reaction steps for the formation of 5-Amino-pentyl α-(1→3)-
1. Module 1 was performed with 1 mL TMSOTf solution at the temperature range of −22° C. to −20° C. (when it is programed to do so) for 3 min.
2. Module 2 was performed twice with 5 equiv Building Block and 2% TMSOTf in DCM solution.
3. Module 3 was carried out with 1% hydrazine acetate and 21% acetic acid in pyridine.
4. After Module 1 took place the Module 2 repeated twice (for the first coupling). Then Module 3 was performed.
5. Subsequently, modules 1-3 were repeated three times in the same manner as described in steps 1-3 in order to obtain a tetramer 12.
After buildup of the tetramer on the resin the oligosaccharide was cleaved from solid support in a photoreactor as described in Example 5. 13 mg of the crude product were obtained, which correspond to a yield of 36%.
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by software. The reagent delivery system is utilizes a pressure control syringe pump system, which constantly pressurize the entire platform, so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves, or withdrawing and dispensing with the motorized syringe in connection with a rotary valve.
The same acidic washing module was applied as in Example 5.
The same glycosylation module was used as in Example 6.
Module 3: Fmoc Deprotection (ca. 5 min):
The resin is washed with DMF (three times with 2 mL for 15 s). For Fmoc deprotection 2 mL of a solution of 20% triethylamine in DMF was delivered to the reaction vessel. The temperature of the reagents inside the reactor vessel is adjusted between 70 and 20° C. by microwave irradiation (50 W). After 1 min the reaction solution is drained from the reactor vessel. The resin is washed with DMF (three times with 2 mL for 15 s); the incubation in Fmoc deprotection solution between 70 and 20° C. by microwave irradiation (40 W) and the DMF washes were repeated twice more. Then, the resin is washed with the following solvent sequence DMF (3 times) and DCM (3 times) 3 mL for 15 s each time. After this module the resin is ready for the next glycosylation cycle.
The resin functionalized with a photo-cleavable linker (45 mg; loading 0.30 mmol/g) (see Scheme 4) was loaded into the reaction vessel of the synthesizer and swollen in 2 mL DCM. The sequence of reaction steps for the formation 5-Amino-pentyl α-(1→4)-
1. Module 1 was performed with 1 mL TMSOTf solution at the temperature range of −22° C. to −20° C. (when it is programmed to do so) for 3 min.
2. Module 2 was performed twice with 5 equiv Building Block and 2% TMSOTf in DCM solution.
3. Module 3 was carried out with 20% triethylamine in DMF.
4. After Module 1 took place the Module 2 repeated twice (for the first coupling). Then Module 3 was performed.
5. Subsequently, modules 1-3 were repeated three times in the same manner as described in steps 1-4 in order to obtain a tetramer 13.
After buildup of the tetramer on the resin, the oligosaccharide was cleaved from solid support in a photoreactor: A mercury lamp is turned on 30 min prior to the first cleavage event. The fluorinated-ethylene-propylene (FEP) tubing was washed with 20 mL DCM at a flow rate of 5 mL/min before cleavage. The solid support was pre-swelled in the dark in DCM for 30 min at least before being taken up with a 20 mL disposable syringe. The suspension of solid support in DCM was slowly injected from the disposable syringe (20 mL) into the FEP tubing using a syringe pump. The suspension was pushed through the FEP tubing into the photoreactor with additional 18 mL DCM (flow rate: 800 μL/min). The photocleavage took place inside the reactor while solid support travelled toward the exit point of the reactor. The suspension leaving the reactor was directed into a syringe equipped with polyethylene filter frit where the resin was filtered off and the solution containing the cleaved oligosaccharide is collected in a separate glass vial. The tubing as washed with 20 mL DCM (flow rate: 2 mL/min) until any remaining resin exited the reactor and the remaining oligosaccharide solution is collected. The tubing was re-equilibrated with 20 mL DCM using a flow rate of 5 mL/min and the entire cleavage procedure was repeated. The combined solution that was collected in the photocleavage process was evaporated in vacuo and the crude material was analyzed by MALDI-TOF, and HPLC.
15 mg of the crude product were recovered, which correspond to a yield of 51%.
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by software. The reagent delivery system is utilizes a pressure control syringe pump system, which constantly pressurize the entire platform, so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves, or withdrawing and dispensing with the motorized syringe in connection with a rotary valve.
The resin loaded into the reaction vessel is washed with DMF, THF, DCM (six times each with 3 mL for 15 s). The resin is swollen in 2 mL DCM, and the temperature of the reaction vessel was adjusted in the range of −22° C. to −20° C. by cooling device (when it is programmed to do so). For acidic washing, 1 mL of the solution of 1% TMSOTf in DCM is delivered to the reaction vessel via the pre-cooling device which, cools the solution to a temperature of −20° C. (when it is programmed to do so). After three minutes, the solution is drained. Finally, 3 mL DCM is added to the reaction vessel.
Thioglycoside building block is dissolved in the proper solvent mixture e.g. DCM (6 mL for two double cycles for the first and last coupling and two more single glycosylation cycles couplings between to build up the tetramer) in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. During the adjustment of the temperature in the reactor vessel (when it is programmed to do so), the DCM in the reaction vessel is drained and 1 mL of thioglycoside building block (6.5 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device which cools the solution of phosphate building block (when it is programmed to do so) to a temperature of −15° C. to −18° C. Then 1.0 mL NIS and TfOH solution in DCM and dioxane (v/v, 2:1) are delivered to the reaction vessel from the respective activator storing component via the pre-cooling device, which cools the activator solution down to a temperature of −15° C. to −18° C. (when it is programmed to do so). The glycosylation mixture is incubated for 5 min in the temperature range of −15° C. to −22° C. Keeping constant the active cooling action by microwave transparent coolant flowing in the jacket, the temperature linearly ramped to 0° C. in 5 min (when it is programmed to do so) by the microwave radiation, adjusting the maximum radiation power to 180 W, and after reaching 0° C. the reaction mixture is incubated for additional 20 min. Once incubation time is finished, the reaction mixture is drained and the resin is washed with mixture of DCM and dioxane (v/v, 2:1) (once, 2 mL for 5 s).
Module 3: CIAc (ca. 5 min):
The resin is washed with DMF (three times with 2 mL for 15 s). For CIAc deprotection 2 mL of a solution of 4% thiourea and 9% of pyridine in 2-methoxyethanol was delivered to the reaction vessel. The temperature of the reagents inside the reactor vessel is adjusted between 90° C. and 20° C. by microwave irradiation (180 W). After 22 min the reaction solution is drained from the reactor vessel. The resin is washed with DMF (three times with 2 mL for 15 s); the incubation in CIAc deprotection solution between 90 and 20° C. by microwave irradiation (180 W) and the DMF washes were repeated once more. Then, the resin is washed with the following solvent sequence DMF (3 times) and DCM (5 times) 3 mL for 15 s each time. After this module the resin is ready for the next glycosylation cycle.
The resin functionalized with a photo-cleavable linker (45 mg; loading 0.30 mmol/g) (see Scheme 5) was loaded into the reaction vessel of the synthesizer and swollen in 2 mL DCM.
The sequence of reaction steps for the formation of 5-Amino-pentyl α-(1→6)-
1. Module 1 was performed with 1 mL TMSOTf solution at the temperature range of −22° C. to −20° C. (when it is programmed to do so) for 3 min.
2. Module 2 was performed twice with 6.5 equiv Building Block and NIS and TfOH solution in DCM and dioxane (v/v, 2:1) solution.
3. Module 3 was carried out with 4% thiourea and 9% of pyridine in 2-methoxyethanol.
4. After Module 1 took place the Module 2 repeated twice (for the first coupling). Then Module 3 was performed.
5. Subsequently, modules 1-3 were repeated three times in the same manner as described in steps 1-4 in order to obtain a tetramer 13.
After buildup of the tetramer on the resin, the oligosaccharide was cleaved from solid support in a photo-reactor as described in Example 8. 22 mg of crude product were obtained, which correspond to a yield of 58%.
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by software. The reagent delivery system is utilizes a pressure control syringe pump system, which constantly pressurize the entire platform, so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves, or withdrawing and dispensing with the motorized syringe in connection with a rotary valve.
The same acidic washing module was applied as in Example 5.
The same glycosylation module was used as in Example 7.
Module 3: CIAc (ca. 5 min):
The same chloroacetyl deprotection module was used as in Example 9.
Module 4: Fmoc Deprotection (ca. 5 min):
The same Fmoc deprotection module was used as in Example 8.
Module 5: Lev Deprotection (ca. 5 min):
The same Lev deprotection modules was used as in Example 7.
The resin functionalized with a photo-cleavable linker (45 mg; loading 0.30 mmol/g) (see Scheme 6) was loaded into the reaction vessel of the synthesizer and swollen in 2 mL DCM.
The sequence of reaction steps for the formation α-(1→3)-α-(1→4)-α-(1→6)-
2. Module 2 was performed twice with 5 equiv Building Block and 2% TMSOTf in DCM solution.
3. Module 3 was carried out with 4% thiourea and 9% of pyridine in 2-methoxyethanol.
4. Module 4 was carried out with 20% triethylamine in DMF.
5. Module 5 was carried out with 1% hydrazine acetate and 21% acetic acid in pyridine.
4. After Module 1 took place, Module 2 was repeated twice (for the first coupling). Then Modules 3-5 were performed. Then Module 1 was performed.
5. Subsequently, Module 2 repeated three times in order to obtain a tetramer 17.
After buildup of the tetramer on the resin the oligosaccharide was cleaved from solid support in a photoreactor as described in the previous Example: 15 mg of the crude product were obtained, which correspond to yield of 51%.
The synthesis referred on the scheme 1 was attempted without the acidic was step between the deprotection and the following glycosylation. In the preceding examples, at least the eleven washing steps with solvent were performed between the deprotection and glycosylation module.
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by software. The reagent delivery system utilizes pressure control valves, which constantly pressurize the entire platform, so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves. All the solvents are pre-cooled before they are delivered inside the reaction vessel.
All solvents were pre-cooled before they are delivered inside the reaction vessel.
The same glycosylation module was used as in Example 5.
The same Fmoc deprotection module was used as in Example 5.
The resin functionalized with a photo-cleavable linker (45 mg; loading 0.30 mmol/g) (see Scheme 1) was loaded into the reaction vessel of the synthesizer and swollen in 2 mL DCM.
The sequence of reaction steps for the formation of tetramannose 9 was as follows:
1. Module 1 was performed with 5 equivalent Building Block and 2% TMSOTf in DCM solution.
2. Module 2 was carried out with 20% piperidine in DMF.
3. Subsequently, Modules 1 and 2 were repeated four times in order to obtain a tetramer.
After buildup of the tetramer on the resin, the oligosaccharide was cleaved from solid support in a photoreactor as described in Example 5. MALDI analysis revealed that no title compound was formed (see
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by software. The reagent delivery system utilizes pressure control valves, which constantly pressurize the entire platform, so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves. All the solvents are pre-cooled before they are delivered inside the reaction vessel.
The resin loaded into the reaction vessel is washed with DMF, THF, DCM (six times each with 3 mL for 15 s). The resin is swollen in 2 mL DCM, and the temperature of the reaction vessel was adjusted in the range of −20° C. to −16° C. by cooling device (when it is programmed to do so). For acidic washing, 1 mL of the solution of 2% TMSOTf in DCM is delivered to the reaction vessel via the pre-cooling device, which cools the solution to a temperature of −15° C. (when it is programmed to do so). After three minutes, the solution is drained. Finally, 3 mL DCM is added to the reaction vessel.
Thioglycoside building block (18) is dissolved in the proper solvent (6.5 eq. in 1.0 mL DCM) and loaded in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. After the temperature reached the range of −18° C. to −15° C. the DCM in the reaction vessel is drained and 1 mL of thioglycoside building block (6.5 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device, which cools the solution of thioglycoside building block to a temperature of −15° C. Then, 1.0 mL NIS and TfOH solution in DCM and dioxane (v/v, 2:1) is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device, which cools the activator solution down to a temperature of −15° C. The glycosylation mixture is incubated for 5 min at the temperature range of −18° C. to −17° C., the temperature linearly ramped during 5 min to 0° C. by microwave radiation, and after reaching 0° C., the reaction mixture is incubated for additional 20 min. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCM (once, 2 mL for 15 s). Then the resin is washed with 2 mL of DCM:dioxane 2:1 volume ratio. Finally, the resin is washed twice with DCM (2 mL for 15 s).
The resin is washed with DMF (three times with 3 mL for 15 s), swollen in 2 mL DMF. For Fmoc deprotection 2 mL of a solution of 20% piperidine in DMF was delivered to the reaction vessel. The temperature of the reagents inside the reactor vessel is adjusted between 70° C. and 20° C. by microwave irradiation (50 W). After 1 min the reaction solution is drained from the reactor vessel. Then, the resin is washed with DMF (three times with 3 mL for 15 s) and DCM (five times with 3 mL). After this module the resin is ready for the next glycosylation cycle.
The resin loaded into the reaction vessel is washed with DMF, THF, DCM (six times each with 3 mL for 15 s). The resin is swollen in 2 mL DCM, and the temperature of the reaction vessel was adjusted in the range of −30° C. to −26° C. by cooling device (when it is programmed to do so). For acidic washing, 1 mL of the solution of 2% TMSOTf in DCM is delivered to the reaction vessel via the pre-cooling device, which cools the solution to a temperature of −15° C. (when it is programmed to do so). After three minutes, the solution is drained. Finally, 3 mL DCM is added to the reaction vessel.
Thioglycoside building block (19) is dissolved in the proper solvent (6.5 eq. in 1.0 mL DCM) and loaded in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. After the temperature reached the range of −30° C. to −26° C., the DCM in the reaction vessel is drained and 1 mL of thioglycoside building block 19 (6.5 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device, which cools the solution of thioglycoside building block to a temperature of −15° C. Then, 1.0 mL NIS and TfOH solution in DCM and dioxane (v/v, 2:1) is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device, which cools the activator solution down to a temperature of −15° C. The glycosylation mixture is incubated for 10 min at the temperature range of −30° C. to −26° C., the temperature linearly ramped during 5 min to 0° C. by microwave radiation, and after reaching 0° C. the reaction mixture is incubated for additional 30 min. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCM (once, 2 mL for 15 s). Then the resin is washed with 2 mL of DCM:dioxane 2:1 volume ratio. Finally, the resin is washed twice with DCM (2 mL for 15 s).
The resin is washed with DCM (three times with 2 mL for 15 s). For Lev deprotection 2 mL of a solution of 1% hydrazine acetate and 21% acetic acid in pyridine was delivered to the reaction vessel. The temperature of the reagents inside the reactor vessel is adjusted between 40° C. and 20° C. by microwave irradiation (180 W). After 3 min, the reaction solution is drained from the reactor vessel. The resin is washed with DCM (three times with 2 mL for 15 s); the incubation in Lev deprotection solution between 40° C. and 20° C. by microwave irradiation (180 W) and the DCM washes were repeated twice more. Then, the resin is washed (3 times) with the following solvent sequence DMF, THE and DCM (3 mL for 15 s each). After this module the resin is ready for the next glycosylation cycle.
Thioglycoside building block (20) is dissolved in the proper solvent (6.5 eq. in 1.0 mL DCM) and loaded in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. After the temperature reached the range of −35° C. to −26° C., the DCM in the reaction vessel is drained and 1 mL of thioglycoside building block 20 (6.5 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device, which cools the solution of thioglycoside building block to a temperature of −15° C. Then, 1.0 mL NIS and TfOH solution in DCM and dioxane (v/v, 2:1) is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device, which cools the activator solution down to a temperature of −15° C. The glycosylation mixture is incubated for 10 min at the temperature range of −35° C. to −26° C., the temperature linearly ramped during 5 min to 0° C. by microwave radiation, and after reaching 0° C. the reaction mixture is incubated for additional 30 min. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCM (once, 2 mL for 15 s). Then the resin is washed with 2 mL of DCM:dioxane 2:1 volume ratio. Finally, the resin is washed twice with DCM (2 mL for 15 s).
Thioglycoside building block (18) is dissolved in the proper solvent (6.5 eq. in 1.0 mL DCM) and loaded in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. After the temperature reached the range of −30° C. to −26° C., the DCM in the reaction vessel is drained and 1 mL of thioglycoside building block 18 (6.5 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device which cools the solution of thioglycoside building block to a temperature of −15° C. Then, 1.0 mL NIS and TfOH solution in DCM and dioxane (v/v, 2:1) is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device, which cools the activator solution down to a temperature of −15° C. The glycosylation mixture is incubated for 5 min at the temperature range of −30° C. to −26° C., the temperature linearly ramped during 5 min to 0° C. by microwave radiation, and after reaching 0° C. the reaction mixture is incubated for additional 20 min. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCM (once, 2 mL for 15 s). Then the resin is washed with 2 mL of DCM:dioxane 2:1 volume ratio. Finally, the resin is washed twice with DCM (2 mL for 15 s).
The resin functionalized with a photo-cleavable linker (45 mg; loading 0.30 mmol/g) (see Scheme 7) was loaded into the reaction vessel of the synthesizer and swollen in 2 mL DCM. The sequence of reaction steps for the formation of protected Lewis antigen 21 was as follows:
1. Module 1 was performed with 1 mL TMSOTf solution at the temperature range of −22° C. to −16° C. (when it is programmed to do so) for 3 min.
2. Module 2 was performed with 6.5 equiv Building Block 18 and 2% TMSOTf in DCM solution. In the temperature range of −22° C. to 0° C.
3. Module 3 was carried out with 20% piperidine in DMF at the temperature range of 25° C. to 60° C. (when it is programmed to do so).
4. Module 4 was performed with 1 mL TMSOTf solution at the temperature range of −30° C. to −26° C. (when it is programmed to do so) for 3 min.
5. Module 5 was performed with 6.5 equiv Building Block 19 and 2% TMSOTf in DCM solution. In the temperature range of −35° C. to −10° C.
6. Module 6 was carried out with 1% hydrazine acetate and 21% acetic acid in pyridine at the temperature range of 25° C. to 60° C. (when it is programmed to do so).
7. Module 7 was performed with 6.5 equiv Building Block 20 and 2% TMSOTf in DCM solution in the temperature range of −35° C. to −10° C.
8. Module 3 was carried out with 20% Piperidine in DMF at the temperature range of 25° C. to 60° C. (when it is programmed to do so).
9. Module 4 was performed with 1 mL TMSOTf solution at the temperature range of −30° C. to −26° C. (when it is programmed to do so) for 3 min.
10. Module 8 was performed with 6.5 equiv Building Block 18 and 2% TMSOTf in DCM solution in the temperature range of −35° C. to −10° C.
11. Module 3 was carried out with 20% piperidine in DMF at the temperature range of 25° C. to 60° C. (when it is programmed to do so).
After build-up of the tetramer on the resin, the oligosaccharide was cleaved from solid support in a photoreactor as described in Example 5. The combined solution that was collected in the photocleavage process was evaporated in vacuo and the crude material was analyzed by MALDI-TOF, and HPLC. 14 mg of crude product were obtained, which correspond to a yield of 47%.
In
In
The timing and quantity of solvents/reagents transferred to the reaction vessel in each step is controlled by software. The reagent delivery system utilizes pressure control valves, which constantly pressurize the entire platform, so that the specific solvent/reagent is transferred from the respective storage components by timing the opening and closing of the appropriate valves. All the solvents are pre-cooled before they are delivered inside the reaction vessel.
The resin loaded into the reaction vessel is washed with DMF, THF, DCM (six times each with 3 mL for 15 s). The resin is swollen in 2 mL DCM, and the temperature of the reaction vessel was adjusted in the range of −30° C. to −26° C. by cooling device (when it is programmed to do so). For acidic washing, 1 mL of the solution of 2% TMSOTf in DCM is delivered to the reaction vessel via the pre-cooling device, which cools the solution to a temperature of −15° C. (when it is programmed to do so). After three minutes, the solution is drained. Finally, 3 mL DCM is added to the reaction vessel.
Thioglycoside building block (20) is dissolved in the proper solvent (6.5 eq. in 1.0 mL DCM) and loaded in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. After the temperature reached the range of −30° C. to −26° C., the DCM in the reaction vessel is drained and 1 mL of thioglycoside building block 20 (6.5 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device, which cools the solution of thioglycoside building block to a temperature of −15° C. Then, 1.0 mL NIS and TfOH solution in DCM and dioxane (v/v, 2:1) is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device, which cools the activator solution down to a temperature of −15° C. The glycosylation mixture is incubated for 10 min at the temperature range of −30° C. to −26° C., the temperature linearly ramped during 5 min to 0° C. by microwave radiation, and after reaching 0° C. the reaction mixture is incubated for additional 30 min. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCM (once, 2 mL for 15 s). Then the resin is washed with 2 mL of DCM:dioxane 2:1 volume ratio. Finally, the resin is washed twice with DCM (2 mL for 15 s).
The resin is washed with DCM (three times with 2 mL for 15 s). For Lev deprotection 2 mL of a solution of 1% hydrazine acetate and 21% acetic acid in pyridine was delivered to the reaction vessel. The temperature of the reagents inside the reactor vessel is adjusted between 40° C. and 20° C. by microwave irradiation (180 W). After 3 min, the reaction solution is drained from the reactor vessel. The resin is washed with DCM (three times with 2 mL for 15 s); the incubation in Lev deprotection solution between 40° C. and 20° C. by microwave irradiation (180 W) and the DCM washes were repeated twice more. Then, the resin is washed (3 times) with the following solvent sequence DMF, THF and DCM (3 mL for 15 s each). After this module the resin is ready for the next glycosylation cycle.
Thioglycoside building block (21) is dissolved in the proper solvent (6.5 eq. in 1.0 mL DCM) and loaded in the designated building block storing component. The reaction vessel is set to reach the initial glycosylation temperature. After the temperature reached the range of −35° C. to −26° C., the DCM in the reaction vessel is drained and 1 mL of thioglycoside building block 21 (6.5 eq. in 1.0 mL DCM) is delivered from the building block storing component to the reaction vessel via the pre-cooling device, which cools the solution of thioglycoside building block to a temperature of −15° C. Then, 1.0 mL NIS and TfOH solution in DCM and dioxane (v/v, 2:1) is delivered to the reaction vessel from the respective activator storing component via the pre-cooling device, which cools the activator solution down to a temperature of −15° C. The glycosylation mixture is incubated for 10 min at the temperature range of −35° C. to −26° C., the temperature linearly ramped during 5 min to 0° C. by microwave radiation, and after reaching 0° C. the reaction mixture is incubated for additional 30 min. Once incubation time is finished, the reaction mixture is drained and the resin is washed with DCM (once, 2 mL for 15 s). Then the resin is washed with 2 mL of DCM:dioxane 2:1 volume ratio. Finally, the resin is washed twice with DCM (2 mL for 15 s).
The resin is washed with DMF (three times with 3 mL for 15 s), swollen in 2 mL DMF. For Fmoc deprotection 2 mL of a solution of 20% piperidine in DMF was delivered to the reaction vessel. The temperature of the reagents inside the reactor vessel is adjusted between 70° C. and 20° C. by microwave irradiation (50 W). After 1 min the reaction solution is drained from the reactor vessel. Then, the resin is washed with DMF (three times with 3 mL for 15 s) and DCM (five times with 3 mL). After this module the resin is ready for the next glycosylation cycle.
The resin functionalized with a photo-cleavable linker (45 mg; loading 0.30 mmol/g) (see Scheme 9) was loaded into the reaction vessel of the synthesizer and swollen in 2 mL DCM. The sequence of reaction steps for the formation of protected Lewis antigen 23 was as follows:
1. Module 1 was performed with 1 mL TMSOTf solution at the temperature range of −30° C. to −26° C. (when it is programmed to do so) for 3 min.
2. Module 2 was performed with 6.5 equiv Building Block 20 and 2% TMSOTf in DCM solution in the temperature range of −35° C. to −10° C.
3. Module 3 was carried out with 1% hydrazine acetate and 21% acetic acid in pyridine at the temperature range of 25° C. to 60° C. (when it is programmed to do so).
4. Module 4 was performed with 6.5 equiv Building Block 21 and 2% TMSOTf in DCM solution in the temperature range of −35° C. to −10° C.
5. Module 5 was carried out with 20% piperidine in DMF at the temperature range of 25° C. to 60° C. (when it is programmed to do so).
After build-up of the tetramer on the resin, the oligosaccharide was cleaved from solid support in a photoreactor as described in previous examples. The combined solution that was collected in the photo-cleavage process was evaporated in vacuo and the crude material was analyzed by MALDI-TOF, and HPLC. By peak integration of the chromatograph a 90% yield is observed from the reaction with pre-cooling 14 mg of crude product were obtained, which correspond to a yield of 47% respect to the resin loading. By peak integration of the chromatograph 50% yield is observed from the reaction without pre-cooling.
| Number | Date | Country | Kind |
|---|---|---|---|
| EP 19 207 015.9 | Nov 2019 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2020/080922 | 11/4/2020 | WO |
