Patent Application
20190315916
The present invention generally relates to the polymerization of alkylene oxides, such as ethylene oxide, propylene oxide, or butylene oxide. In particular, it concerns a particularly efficient continuous flow process for the polymerization of alkylene oxide carried out at low temperatures, such as room temperature, and moderate pressure, such as 1 to 20 bar. The continuous flow process of the present invention is more efficiently carried out in a micro-polymerization line, wherein mixing and temperature of the components is rapid and easy to control.
Aliphatic polyethers are an important class of polymers used in many applications, ranging from pharmaceutical formulations to material technology. Among these polyethers, macromolecules synthesized from ethylene oxide, propylene oxide, and butylene oxide are the most common alkene oxides. Polyether-based polymers have unique properties arising from their hydrophilic backbone. Aliphatic polyethers can be prepared as homo- or heterobifunctional polymers with various end-chain functions, or can be incorporated in other macromolecular structures.
Several techniques for the polymerization of alkene oxides have been reported in the literature. Anionic polymerization has been used extensively. The anionic polymerization of alkene oxides uses nucleophiles as initiators. For example, low-molecular weight poly(ethylene oxide) (4 kDa) is commonly obtained by reacting ethylene oxide with water or alkali hydroxides as initiators. High-molecular weight poly(ethylene oxide) (50 kDa) architectures usually require alkali alkoxides (mostly sodium or potassium) or other nucleophiles such as hydrides or amines as initiators. Alkali alkoxides in polar solvents such as tetrahydrofuran (THF) constitute a well-known and efficient type of initiators for alkene oxide polymerization. Polymerization in bulk has also been reported, although it comes with a higher polydispersity. Fast kinetics are reported with primary alkoxides, while bulkier initiators tend to lower the reaction speed. Other additives such as crown ethers may be added to enhance the polymerization kinetics. High temperatures of up to 250° C. and high pressures of up to 150 bar, however, are generally required to yield industrially acceptable polymerization kinetics.
As an example, tetrahydropyranyl monoprotected ethylene glycol was reported by Hiki and Kataoka (in Bioconjugate Chem. 2010, 21, 248-254) as an efficient pre-initiator. In situ deprotonation of this pre-initiator, followed by addition of ethylene oxide yields α-(tetrahydropyranyl-O),ω(OH)-heterobifunctional poly(ethylene glycol) with yields of up to 97%, polydispersity of 1.03 to 1.04, and concordance of theoretical and experimental molar mass. Heterobifunctional polyethers with different chain-ends were prepared with this pre-initiator, which allowed independent functionalization or transformation of both chain-ends.
Most of the processes reported in the art for the polymerization of alkene oxides rely on macroscopic batch reactors (internal dimensions typically greater than 104 μm, and internal volumes ranging from 10−3 I to 103 I, as described in, for example, CN102453253, CN102391494, CN103554472, CN103709391, CN103709393, CN103709389. Since alkene oxides and, in particular, ethylene oxide are extremely reactive, highly explosive and toxic molecules, their handling in macroscopic batch reactors raises significant safety issues, especially when high temperature and pressure conditions are required. Besides safety issues, conventional macroscopic batch reactors also come with inherent limitations for heat exchange and mixing efficiency, which can account for poor reaction control, decrease in molecular weight and larger molecular weight distribution.
To overcome such limitations, continuous-flow methods were developed, as described in DE2900167, DD142809, CN102099396, CN1390240, CN104829824, CN101367925. Continuous-flow methods have the advantages over batch methods of more efficient heat exchanges and higher mixing efficiency. They also ensure a safer process with an enhanced control over the reaction conditions and homogeneity of the polymer thus produced. Continuous-flow reactors are composed of channels for the circulation of chemicals. The internal diameter of such channels is typically of the order of 250-800 μm in continuous-flow microreactors and is >1 mm in continuous-flow mesoreactors. The polymerization conditions in the continuous-flow processes reported in the foregoing documents for the production of alkene oxides comprise temperatures ranging from 100 to 250° C., pressures ranging from 0.2 to 15 MPa (=2 to 150 bar), and reaction times ranging from 0.5 to 3 h.
In particular, CN101367925, describes feeding into a continuous flow mesoreactor of internal diameter of 50-100 mm, three streams of materials including a regulator, oxirane monomer, and an ammonia-calcium catalyst, each in a solvent selected from n-hexane or n-heptane. The three materials are first blended at low temperature of −50 to −20° C., and then reacted at a temperature of 20 to 40° C. for 20 to 40 min.
CN104829824 describes a continuous flow polymerization process comprising (a) preparing a liquid catalyst by reacting an alkali base (KOH, NaOH or NaOR and KOR) and a pre-initiator (polyol or polyamine), and (b) reacting the thus prepared liquid catalyst with an alkene oxide in a continuous-flow microreactor equipped with a micro-mixer and a residence time unit. Reaction temperatures ranging from 150 to 250° C. and pressures ranging from 20 to 150 bar were required to polymerize ethylene oxide within reaction times comprised between 20 and 1000 s (=0.3 to 17 min).
The present invention proposes a polymerization process of alkylene oxides which is safe, has high yield, and can be carried out at moderate to low temperatures, pressures, and reaction times. These and other advantages of the present invention are described in continuation.
The present invention is defined by the attached independent claims. The dependent claims define preferred embodiments. In particular, the present invention concerns a continuous-flow process for the polymerization of an alkylene oxide comprising the following steps:
In a preferred embodiment, the monomer solvent can have:
For example, the monomer solvent can be one of dimethyl sulfoxide (DMSO), hexamethylphosphoramide (HMPA), tetraalkylureas, or cyclic alkylureas, preferably 1,3-Dimethyl-3,4,5,6-tetrahydro-2-pyrimidinone (DMPU) and pyridine.
The continuous-flow process of the present invention is preferably carried out in a polymerization line, wherein step (a) is carried out in a solution reactor module), step (b) is carried out in a mixing reactor module (103) in fluid communication with the first reactor module by means of a connecting tube, and wherein step (c) is carried out in a polymerization reactor module, preferably a tubular reactor forming a serpentine. For a more efficient control of the reaction, the continuous-flow process is preferably carried out in a micro-polymerization line, wherein the internal diameters of the solution and mixing reactor modules are comprised between 100 μm and 1000 μm, preferably between 200 and 800 μm and wherein the connecting tube and polymerization reactor module are capillary tubes of inner diameter comprised between 50 and 700 μm, preferably between 100 and 500 μm. For example, the total inner volume of the solution, mixing, and polymerization reactor modules and connecting tubes can be comprised between 1 and 10 ml, preferably between 2 and 6 ml
The molar ratio of monomer to initiator must be carefully controlled. It is preferred that the monomer to initiator molar ratio be comprised between 2000 and 20, preferably between 100 and 30, and more preferably between 50 and 40. The molar ratio is controlled, on the one hand, by the flowrates of the monomer solution and initiator (solution) and, on the other hand, on the monomer and initiator concentrations in their respective solutions.
For example, the following flowrates of the various components can be achieved with a micro-polymerization line:
The alkylene oxide and initiator can be present in their respective solutions at the following concentrations:
For optimizing the mixing efficacy of the components, the polymerization line preferably comprises mixing devices. For example, the solution and mixing reactor modules can be equipped with a mixing device comprising one or more of an arrow-head mixer, T-mixer, Y-mixer, cross-junction micromixer, or static micromixer, made of glass, stainless steel, polymeric material, or ceramics, or a combination of two or more of the foregoing materials.
The continuous-flow process of the present invention can comprise additional steps between steps (c) and (d) including,
After or within the separation unit, an extraction step can be used to recover and recycle the solvent.
Various embodiments of the present invention are illustrated in the attached Figures.
As can be seen in
In a second step (b), an anionic initiator (2) is mixed with the monomer solution to form a reaction mixture (3). The anionic initiator is an alkali or alkaline-earth alkoxide of general formula R-O-M, wherein,
The anionic initiator is preferably added to the monomer solution in a liquid form. The anionic initiator can either be liquid at the pressure and temperature of the system (cf.
The mixing reactor module (103) is also preferably provided with a mixing device (9). The mixing device can be selected among one or more of an arrow-head mixer, T-mixer, Y-mixer, cross-junction micromixer, or static micromixer. The mixer devices can be made of glass, stainless steel, polymeric material, or ceramics, or a combination of two or more of the foregoing materials. The quality of mixing of the various components is very important in the continuous process of the present invention, as it influences the polymerization kinetics, yield, and homogeneity (e.g., narrower molecular weight distribution).
The reaction mixture is allowed in a third step (c) to react for a polymerization time, t, at a polymerization temperature, T, and at a polymerization pressure, P, to form a polymerized solution (5): The polymerization solution is not necessarily a true solution and can be a suspension or simply a mixture of solvent and polymerized alkylene oxide instead. The polymerization reaction can be carried out in a polymerization reactor module (104), which is preferably a tubular reactor forming a serpentine in fluid communication with the mixing reactor module (103). The flow rate of the reaction mixture (3) from the mixing reactor module to the polymerization reactor module can be controlled by a valve or a pump. The polymerization time, temperature, and pressure required for completing polymerization strongly depend on the monomer solvent used, as can be seen in
By selecting an appropriate monomer solvent (21), polymerization times comprised between 1 s and 60 min can be reached, at a temperature comprised between 0 and 100° C., and at a pressure comprised between 1 and 20 bar above atmospheric pressure. Preferably, the polymerization time is comprised between 20 s and 50 min, more preferably between 30 s and 20 min. The temperature may be comprised between 20 and 50° C., preferably between 25 and 35° C. The polymerization pressure, P, may be comprised between 1.5 and 10 bar, preferably between 2 and 5 bar above atmospheric pressure.
After the polymerization reaction is completed, a polymerized solution (5) is collected at a step (e) in a polymer vessel (105). The polymerized alkylene oxide (5p) is then separated from the solvent (5s) in a separation unit (105p). The polymerized alkylene oxide (5p) is generally a solid in suspension in a solvent. The separation unit can then be simply a decantation vessel. The separation unit preferably comprises separation means, such as a filter. In order to accelerate the separation step, filtration can be carried out under pressure or centrifugal forces. If the polymerized alkylene oxide (5p) is dissolved in the solvent (5s), the polymerized alkylene oxide (5p) can be made to precipitate before reaching the separation unit. If the same solvent as the monomer solvent has been used throughout the process, the solvent (5s) of the polymerized solution is monomer solvent (21). This embodiment is preferred, because the monomer solvent can be recycled after separation to form new solutions. If different solvents are used to form the initiator solution, or a functionalization or termination solution, then the solvent (5s) is a mixture of solvents, which needs be separated again prior to re-use.
The various reactor modules (101-104), vessel (105) and separation unit (105p) are in fluid communication with one another has illustrated in
The continuous flow process of the present invention allows the functionalization of one or more of the two ends of the poly(alkylene oxide) chains formed in the polymerization reactor module (104). As illustrated in
As shown in
The polymerization line may be equipped with one or more in line analysis units for monitoring the polymerization of the reaction mixture. Spectroscopic analysis units are preferred such as an infrared spectroscopy unit (e.g., FTIR). Similarly, the polymerization line may be equipped with additional operations units such as,
The alkylene oxide monomer used in the process of the present invention is preferably selected among ethylene oxide, propylene oxide or butylene oxide. The alkylene oxide monomer may in some embodiments be admixed with a comonomer such as a lactide, caprolactone or a different alkene oxide. The alkylene oxide monomer is present in the monomer solution at a concentration preferably comprised between 0.1 and 10 M, more preferably between 1 and 5 M.
As explained supra, the anionic initiator suitable for the present invention is selected among the alkali or alkaline-earth alkoxides of general formula R-O-M, wherein,
M is preferably selected among lithium, sodium or potassium. In some embodiments, the anionic initiator may include an alkali tert-butoxide or a monotetrahydropyranylated ethylene glycol potassium salt. For example, the anionic initiator can be potassium 2-(tetrahydro-2H-pyran-2-yloxy)ethoxide (=THPOCH2CH2OK) or potassium tert-butoxide.
The alkylene oxide may be present in the monomer solution at a concentration comprised between 0.1 and 10 M, preferably between 1 and 5 M. If, as illustrated in
As shown in
It can be seen in
Without wishing to be bound by any theory, the surprising results obtained with DMSO compared with other, traditionally used solvents, can be explained as follows. DMSO is a polar aprotic solvent having a rather high donor number (DN) of 125 kJ/mol (=29.9 kcal/mol) according to Gutmann's scale. Polar aprotic solvents having a high donor number (DN) according to Gutmann's thermodynamic scale, and having a low acceptor number (AN) according to Gutmann-Beckett's 31P NMR scale are of particular interest for controlling the reactivity of alkoxide species used as anionic initiator in the continuous flow polymerization process according to the present invention.
Alkoxide species are responsible for the propagation of the anionic polymerization of ethylene oxide. As illustrated in
As illustrated in
As illustrated in
The Gutmann-Beckett Acceptor (AN) and Donor number (DN) are measures of the strength of solvents as Lewis acids or bases. The Acceptor Number is based on the 31P-NMR chemical shift of triethyiphosphine oxide in the solvent. The Donor Number is based on the heat of reaction between the ‘solvent’ and SbCl5 in CH2ClCH2Cl.
Some polar aprotic solvents, such as DMSO which yielded such superior polymerization kinetics in
Based on the above observation, a polar aprotic solvent suitable for use as monomer solvent in the present invention preferably has a donor number (DN) of at least 120 kJ/mol according to Gutmann's thermodynamic scale. The donor number, DN, preferably does not exceed 250 kJ/mol, preferably does not exceed 200 kJ/mol. The acceptor number (AN) should be low and is preferably not more than 20 according to Gutmann-Beckett's scale. For example, ethanol has a high value of DN=132 kJ/mol (=31.5 kcal/mol) but also a high value of AN=37.9 which makes it less suitable as a monomer solvent (21) than DMSO.
The dielectric constant (E) of a solvent also has an effect on solubility of anionic components. In a preferred embodiment, the monomer solvent is a polar aprotic solvent having a dielectric constant (E) greater than 30. If an initiator solvent (22) is used for forming an initiator solution (222) (cf.
Examples of monomer solvents suitable for the present invention include, dimethyl sulfoxide (DMSO), hexamethylphosphoramide (HMPA), tetraalkylureas, or cyclic alkylureas, such as 1,3-Dimethyl-3,4,5,6-tetrahydro-2-pyrimidinone (DMPU), or pyridine. Other solvents with DN- and AN-values comprised within the preferred ranges exist, but care must be taken with respect to the toxicity of the selected monomer solvent.
The gist of the present invention is to combine, on the one hand,
The combination of these two elements allows rapid polymerization times, below 60 min, at low temperature (including room temperature) and low to moderate pressures. This has the further benefit of reducing the thermal and mechanical resistance requirements of the polymerization set-up, and thus reducing its cost.
The choice of (a) an appropriate monomer solvent (and monomer and initiator) has been discussed in detail in the previous sections. According to the present invention, only a continuous flow polymerization line can reach the requirements defined in point (b) supra. Beside the poorer heat exchanges and mixing efficacy in batch processes, because of the high reactivity of the components, such as ethylene oxides, the risk of explosions is higher in a batch process than in a continuous flow process, wherein addition of monomer is spread over a longer period of time. The polymerization set-up according to the present invention must therefore include a continuous flow polymerization line.
High control of the temperature and high mixing speeds can be better achieved if the continuous flow polymerization line has reactor modules and connecting tubes of small dimensions. In particular, a meso-polymerization line can be used, with internal diameters of the reactor modules and connecting tubes of the order of 1 to 20 mm. Higher mixing rates and enhanced temperature control were achieved, however, with micro-polymerization lines defined by internal diameters of the solution and mixing reactor modules comprised between 100 μm and 1000 μm, preferably between 200 and 800 μm. The connecting tubes and polymerization reactor module are preferably composed of capillary tubes of inner diameter comprised between 50 and 700 μm, more preferably between 100 and 500 μm. The total inner volume of the solution, mixing, and polymerization reactor modules and connecting tubes can for example be comprised between 1 and 10 ml, preferably between 2 and 6 ml.
In a micro-polymerization line, the flow rate of monomer solution (121) into the mixing reactor module (103) can be comprised between 0.1 and 9 ml/min, preferably between 0.2 and 1 ml/min. Similarly, the flow rate of initiator (2) or initiator solution (222) into the mixing reactor module may be comprised between 0.1 and 1 ml/min, preferably between 0.2 and 0.5 ml/min. The monomer to initiator molar ratio is preferably controlled between 2000 and 20, preferably between 100 and 30, and more preferably between 50 and 40. The reaction mixture (3) is preferably fed from the mixing reactor module (103) through the polymerization reactor module (104) at a flow rate comprised between 0.1 and 10 ml/min, preferably between 0.3 and 1 ml/min.
The. microstructured polymerization line can be constructed from microfluidic modules made of glass, stainless steel, polymeric materials, ceramics, silicon carbide or a combination of two or several of the aforementioned materials. The microfluidic modules may include mixers, in-line check valves, pressure regulators, three-way valves, connectors, ferrules, and microreactors connected in series or in parallel through capillaries. The capillaries may be made of stainless steel or polymeric materials, such as PEEK, PFA, ETFE or PTFE. The general design of the micro-polymerization line may include microfluidic chips, coils or tubular fluidic reactors having an internal diameter comprised between 100 and 1000 μm, preferably between 200 and 800 μm. Mixers may be embedded in the microreactor or inserted as independent fluidic elements, such as arrow-head mixers, T-mixers, Y-mixers, cross-junctions or static micromixers, made either of glass, stainless steel, polymeric materials and ceramics, or a combination of two or several of the aforementioned materials.
In some embodiments, several micro-polymerization lines may be fluidically coupled in parallel to the sources of monomer solution (121) and anionic initiator (2) or initiator solution (222) to increase productivity. One micro-polymerization line unit is very cheap to produce and a large array of a number of such units can easily be thus arranged in parallel to reach high production rates.
A continuous-flow polymerization line was produced for the polymerization of ethylene oxide (1) in the presence of potassium tert-butoxide (2) in dimethylsulfoxide (21). The setup comprised two feed solutions for a monomer solution (121) and an initiator solution (222) to a perfluoroalkoxy alcane polymer (PFA) coil reactor (104) through a polyether ether ketone (PEEK) T-mixer (103, 9). High pressure Chemyx 6000 pumps (8) were used to deliver the reagents and a 3-way valve was inserted before the T-mixer to avoid back flush upon reactor operation.
A 0.2 M initiator solution (222) of potassium tert-butoxide in dry and degassed dimethylsulfoxide and a 4 M monomer solution (121) of ethylene oxide in dry and degassed dimethylsulfoxide were loaded in two 20 ml HP SS syringes, and then installed on HP syringe-pumps, and connected to the coil reactor via the PEEK T-mixer of internal diameter of 500 μm. The initiator solution was delivered at a flow rate of 0.48 ml/min, and mixed through the PEEK T-mixer with a stream of monomer solution flowing at 0.1 ml/min. The monomer solution was obtained by mixing ethylene oxide and dimethylsulfoxide in a mixing reactor module (101) fluidically connected upstream of the injection of the initiator solution. The flow rates were set to ensure a monomer to initiator molar ratio of 44.
The homogeneous stream of potassium tert-butoxide and ethylene oxide in dimethylsulfoxide was then reacted at 25° C. under 2 bar of pressure in a thermostatized microfluidic polymerization reactor module (104) constructed from 4 m of PFA capillary tubing with a 2 ml internal volume. The total flow rate through the polymerization reactor module was equal to 0.148 ml/min and the residence time was 15 min. The outlet of the PFA loop was fluidically connected to a PEEK T-mixer of internal diameter of 500 μm for downstream processing by quenching with aqueous acetic acid to terminate polymerization. The entire micro-polymerization line was operated during over 5 h at steady state. The polymerized ethylene oxide thus produced had the following properties: a theoretical molecular weight of Mn(Th)=1000 g/mol, assuming 100% polymerization, a measured molecular weight of Mn(Exp)=900, and a polydispersity of PDI=1.10. The structural characterization of the polymer by proton nuclear magnetic resonance in deuterated chloroform (=1H NMR (CDCl3)) yielded the following chemical shift results, δ, for CH2-PEG and CH3 moieties, respectively: δ=3.65 (s, 110H, CH2-PEG) and 1.20 (s, 9H, CH3) ppm.
The continuous-flow process for polymerization of an alkylene oxide of the present invention is highly advantageous. By a proper selection of the monomer solvent (21), the process may be carried out at low temperature, such as at room temperature and at low to moderate pressure, with short reaction times, typically shorter than one hour, and even shorter than 15 minutes. By carrying out the continuous-flow process of the present invention in a micro-polymerization line, the process can run optimally by an enhanced control on the reaction conditions, such as temperature, pressure, flow rate and local stoichiometry. The process also permits to obtain a product with well-defined molecular parameters such as molar mass and polydispersity. The continuous flow process of the present invention provides a substantially safer handling of alkylene oxides such as ethylene oxide. The process further enables the preparation of homo- or heterobifunctional polyalkylene oxides, such as homo- or heterobifunctional polyethylene oxide. Another advantage is the flexibility to produce polyalkylene oxide on-demand, for specific molecular parameters and even for small production volumes. The micro-polymerization line is compact and may be used as a mobile and/or a versatile reactor. This microfluidic process is straightforward, versatile, economic, safe, uses low process temperatures and pressures, and provides high yields and excellent molecular control for the production of polymeric architectures from alkylene oxides.
This method overcomes the drawbacks of the prior art including,
| Number | Date | Country | Kind |
|---|---|---|---|
| 16206775.5 | Dec 2016 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2017/082162 | 12/11/2017 | WO | 00 |
