Patent Application
20130079498
The present invention pertains to a process of purifying vitamin K dependent proteins such as coagulation factor IX (abbreviated as FIX) and a fraction containing a vitamin K dependent protein such as FIX obtainable by the process of the invention.
Hemophilia is a group of hereditary genetic disorders that impair the body's ability to control blood clotting or coagulation. In one of its forms, Hemophilia B, clotting factor IX (FIX) is deficient, Hemophilia B occurs in about 1 in 25,000 male births. Factor IX (or Christmas factor) is one of the serine proteases of the coagulation system. It is a vitamin K-dependent plasma protein that participates in the intrinsic pathway of blood coagulation by converting factor X to its active form in the presence of Ca2+ ions, phospholipids, and factor VIIIa. The FIX protein is an essential factor in blood coagulation with multifunctional properties.
Factor IX (FIX) is a single-chain glycoprotein containing 461 amino acids. It is synthesized primarily in the liver and secreted in plasma. The factor IX molecule consists of several discrete functional domains, including a signal peptide, propeptide, a Gla domain, two epidermal growth factor-like (EGF) domains, an activation peptide and a catalytic, trypsin-like domain (serine protease domain) (The propeptide is cleaved prior to secretion to generate the mature 415 aa FIX molecule. The protein is further processed into an active form, to a heterodimer consisting of a light chain and a heavy chain linked by a disulfide bond.
The deficiency of FIX can be treated with plasma-derived concentrates of FIX or with recombinantly produced FIX. The treatment with FIX concentrates has led to a normalized life of the hemophilia patients. Historically, Hemophilia B has been treated with FIX originating from human blood plasma. In blood plasma, under normal conditions, the FIX molecule is circulating in its native form, whereas it is activated through a complicated process initiated in the blood cascade of coagulation enzymes.
Plasma derived FIX products occur on the market with different purities depending on which purification method which is applied. The methods used to purify FIX were normally a combination of different chromatography steps (mainly ion exchange and affinity steps, for purifying and ultra filtration step (s) for concentration/desalting of the product.
Harrison et al. (S. Harrison et al. Sem Hematol 35 (Suppl 2): 4-10 (1998) describes the manufacturing process for a recombinant FIX (Benefix®) produced in CHO cells. The cells are harvested by microfiltration and subsequently concentrated in a ultrafiltration/diafiltration step were the buffer is exchanged to a Tris buffer to provide a consistent buffer for loading onto the first chromatography column. Four independent chromatography steps is used for the purification of rFIX, the first is an anion exchange step (Q Sepharose FF), which is performed in a pseudoaffinity mode. The column is eluted with 10 mM calcium chloride at pH 8.0. The calcium chloride induces a conformational change in the FIX molecule which causes it to detach from the column.
The Q Sepharose step is followed by purification on a Matrex cellufine sulfate column, which is a heparin analog used for affinity purification of proteins with heparin-binding domains. It also behaves as a cation exchange resin due to the negatively charged sulfate groups. The cellufine purification step removes low levels of HCPs.
The cellufine eluate is loaded onto a Ceramic-Hydroxyapatite column, which is a synthetic form of calcium phosphate. It is used to separate proteins of varying charges and it provides the possibility to remove lower specific activity forms of rFIX. This column is eluted with a stepwise elution by increasing the phosphate concentration to a final concentration of 0.5 M.
The final purification step in the manufacturing process of Benefix® is Chelate-EMD-Cu(II). Proteins interacts with the immobilized metals retained by the resin. Bound rFIX is eluted with imidazole as a displacer and trace contaminants is removed in this purification step, which is followed by a virus filtration step (Viresolve-70) and finally by a ultrafiltration/diafiltration step where rFIX is concentrated and the buffer is exchanged to the formulation buffer. The above described rFIX manufacturing process is consistent, 65 batches have been analysed and the specific activity was found to be 276±23 IU/mg. The Gla content was 11.4±0.1 mol Gla/mol rFIX and the total impurities were found to be 0.01±0.01% and 0.03±0.01% determined by RP-HPLC and HCP-ELISA, respectively.
Lindsay et al. (J Chrom A 1026: 149-157 (2004)) describes a method to purify rFIX from transgenic pig milk. Heparin Sepharose FF was used as the first step in the purification scheme, followed by an anion exchange step.
The heparin binding domain of factor IX is located in the C-terminal end of the molecule. This region lacks PTMs and thus the heparin chromatography step allows the entire population of rFIX to be isolated. The specific activity of the eluate was 30-35 IU/mg, which indicates that a large fraction is inactive. Active rFIX subpopulations were separated from inactive subpopulations during a gradient elution of the AIEX column.
Kaufman et al. (JBC 261:9622-9628 (1986)) describes expression of rFIX in CHO cells and purification of the protein. The rFIX containing cell culture medium was concentrated by ultrafiltration and dialyzed against a buffer containing 3 mM CaCl2, 0.05 M Tris-HCl and 0.5 M NaCl prior to application to an immunoaffinity column with conformation specific antibodies (anti-FIX:Ca(II) antibodies). The column was subsequently eluted with 10 mM EDTA, 0.05 M Tris-HCl and 0.15 M NaCl.
The presence of 3 mM CaCl2 in the starting material prior to application to the column resulted in a separation between active and inactive species of FIX. The inactive species failed to bind to the column and active FIX could be eluted from the column with EDTA.
WO-A-2009/007451 discloses a purification method of FVIII using a mixedmode or multimodal resin. The purification method is based on contacting FVIII protein with a multimodal or mixed-mode resin containing ligands which comprise a hydrophobic part and a negatively charged part and eluting said FVIII protein with an elution buffer containing at least 1.5 M salt and at least 40% (w/v) of ethylene glycol, propylene glycol or a mixture thereof, and calcium ions.
EP-A-1 707 634 discloses a method for isolation of recombinantly produced proterms i.a. by various methods such as immuno-affinity chromatography, affinity chromatography, protein precipitation, buffer exchanges, ionic exchange chromatography, hydrophobic interaction chromatography, mixed-mode hydrophobic/ion exchange chromatography media, chelating chromatography, carbohydrate affinity like lectin or heparin affinity chromatography, size-exclusion chromatography, electrophoresis, dialysis, different precipitation agents such as polyethylene glycol, ammonium sulphate, ethanol, hydroxy apatite adsorption, filter membrane adsorption, ligands coupled to magnetic particles etc. However, it is identifying no particular chromatographic purification steps.
WO-A-2005-082483 discloses a process for the purification of antibodies from one or more impurities in a liquid, which process comprises contacting said liquid with a first chromatography resin comprised of a support to which multi-modal ligands have been immobilised to adsorb the antibodies to the resin, wherein each multi-modal ligand comprises at least one cation-exchanging group and at least one aromatic or hetero aromatic ring system. An eluant is added to release the antibodies from the resin and the eluate is contacted with a second chromatography resin.
WO-A-2005/121163 discloses a process for the isolation of one or more proteins from a protein solution. The process comprises the steps of providing a protein solution comprising one or more specific proteins and having a preset pH and a preset ionic strength or conductivity, applying the protein solution to an adsorption column comprising a particle with at least on high density non-porous core surrounded by a porous material, the adsorbent comprises a particle density of at least 1.5 g/ml and a mean volume particle diameter of at most 150 um. The column is optionally washed before eluting the protein (s) from the adsorbent.
WO-A-2009/156430A1 discloses a purification method of FVIII using a mixed-mode or multimodal resin. The purification method is based on contacting FVIII protein in a solution having a high ionic strength with a multimodal or mixed-mode resin containing ligands which comprise a hydrophobic part and a negatively charged part and eluting said FVIII protein with an elution buffer comprising at least one amino acid which is positively charged at pH 6-8.
In order to improve FIX containing products, specific affinity chromatography directed against the FIX molecule was employed, which effectively removed contaminants to a high degree of FIX purity. The disadvantage with the often used immuno affinity chromatography was that it is relatively expensive and that the monoclonal antibodies used as affinity ligands, where of animal origin.
In the mid 80's there were some virus transmissions associated with plasma derived FIX products. Even if this problem was solved through implementation of specific virus reduction steps, this was the starting point of the development of recombinant FIX products (rFIX). In the 90's, the first rFIX product was marketed and up to date the only one.
One object of the invention was to provide a process by which the drawbacks of the purification processes of vitamin K dependent proteins, in particular FIX in prior art could be avoided. It is known from prior art that one disadvantage of traditional ion exchange chromatography resins (as for example SP-, CM-, Q- or DEAE Sepharose FF ion exchange chromatography resins) is that the binding of protein to the resin only can be performed within relatively low salt concentration (conductivity) and pH, typically in the range of 0.01-0.15M of salt (NaCl etc.) concentration. The optimal pH range is dependent if a cation exchanger or an anion exchanger is used and the iso-electric point of the target product to be bound on the resin. In general the pH range in which a target protein binds to an ion exchange resin is typically approximately one pH unit up or down from the iso-electrical point of the target product.
In certain applications there would be a demand to be able to use the relatively mild purification conditions an ion exchange chromatography step exerts towards the proteins, also directly (without further dilution) to a chromatography resin at somewhat increased ionic strength and at a pH out of the normal range which cannot be used for conventional ion exchange chromatography.
Multimodal (or mixed mode) chromatography is a tool for purifying proteins. Described in, for example, Manufacturer data sheet GE Healthcare (11-0035-45AA) Capto Adhere, Manufacturer data sheet GE Healthcare (28-9078-88AA) Capto MMC and WO-A-2009/024620 “A process for the isolation and purification of a target protein, free of prion proteins”. A disadvantage is that the elution often includes relatively harsh conditions like for example pH below or above neutral pH, alone or in combination with other elution parameters such as for example ethylene glycol, and as for example described in WO-A-2009/007451.
An increased ionic strength can be of significant advantage for the protein stability in a protein solution, especially in a crude protein preparation like in the harvest of recombinant proteins or in plasma derived products where potential proteases are present in the solution which can affect the target protein negatively.
As proteases often work best at physiological conditions (like is the case in most cell systems), i.e approximately pH 7 and a salt concentration of approximately 0.15M, it can be advantageous to change these conditions to minimize the effects of proteases. Such changes can typically be performed by addition of salt and/or change of the pH. Both of these parameters are critical for the performance of a conventional ion-exchange chromatography step and thus often impossible to achieve. Thus another object of the invention was to provide a process in which this problem has been solved and rendering possible to add salt and/or change the pH in crude protein samples comprising potentially proteolytic factors such as proteases which could degrade the target protein. The process should further be able to process the protein solution with as less as possible further measures and to bind the target protein to a chromatography resin. This would provide an optimized step of concentration and purification of the target protein from a crude sample or further purification downstream using e.g. other chromatography steps such as affinity chromatography.
This need is of specific importance, because degradation of the target protein during purification would be prevented or at least diminished.
This makes it possible to remove proteases and other contaminants, which might be present in a crude harvest, before elution of the target protein.
Another object of the invention was to provide a process of purifying a vitamin K dependent protein such as FIX, in particular starting from a cell culture harvest of recombinant FIX.
According to the invention the object is accomplished by a process of purifying a vitamin K dependent protein such as FIX in a purification sequence employing chromatography wherein
Seven plasma glycoproteins are known to be dependent on vitamin K for their biosynthesis. They are prothrombin (factor II), factor VII, factor IX, factor X, protein C, protein S and protein Z. The Gla domain is a common structural feature in all these vitamin K-dependent proteins and immediately after the Gla domain, each of the proteins (except prothrombin) has one or more EGF-like domains. The vitamin K-dependent proteins require Ca2+ ions to express their physiological function and the calcium binding sites involve at least the Gla domain and the EGF-like domains. Calcium binding enables these proteins to bind to phospholipids/cell membranes and thus express their full biological activities.
The present invention using a multimodal resin as a capture purification step provides the possibility to adjust the salt concentration and pH to values which minimize the risk of active proteases in the protein solution during binding of the target protein to the multimodal chromatography step.
An advantage of the process of the invention is the possibility to further apply a wash step before elution of the target protein after binding of the target protein to the multimodal resin for example used as a capture step in a recombinant process. is. This is achieved by using the multimodal resin was to wash the resin by selecting a suitable washing buffer to remove proteases and other contaminants which adheres to the multimodal resin, before eluting the target protein. The suitable wash buffer preferably is containing a salt or an amino acid or a buffer component, or mixtures thereof at a pH suitable to still inhibit protease activity during the wash removal step.
The process of the invention renders possible to elute the target protein, bound to the multimodal resin, in a mild elution environment with distinct elution properties (i.e in a volume as small as possible). This was achieved by using an increased pH or an increased salt concentration or addition of an amino acid or combination thereof. The process of the invention provides advantages such as inhibition of aggregates, preserving the native molecule structure and providing a low volume for the further down stream processing.
The present invention also facilitates a process of purification without addition of human or animal derived stabilizing additives and the use of a whole process which is absent thereof (monoclonal antibody based immuno affinity resins). The use of the multimodal resin, in particular as capture step, facilitates also a higher binding capacity in comparison with conventional ion exchangers, which results in a more concentrated product eluate from the column, which can be of advantage for the product stability.
According to one embodiment of the invention the multimodal chromatography may be performed in a chromatographic column. This may be regarded as a first capture step. The process of the invention can also be performed in a batch mode.
In one embodiment of the invention the chromatography on multimodal resins is combined with a chromatography on a resin having a yeast derived affinity ligand, employing a purity of >90% after elution of the vitamin K dependent protein such as FIX Protein.
In another further embodiment of the invention the multimodal resin step and the yeast derived affinity ligand chromatography step is combined with other chromatography purification step to exert a purity of more than 99% in the final vitamin K dependent product such as FIX Protein.
Therefore also a composition of matter is subject of the invention which composition of matter is comprising a purified vitamin K dependent protein such as FIX obtainable by the process according to the invention (without the addition or use of any human or animal additatives like albumin or monoclonal antibody based immunoaffinity ligands).
In another embodiment of the invention the multimodal resin comprises moieties bound to a matrix and the moieties are able to interact with vitamin K dependent protein such as FIX in a mixture by ionic interactions and other types of interactions such as hydrogen bonding, hydrophobic and thiophilic interactions.
In a further embodiment of the invention the affinity ligand is a yeast derived Fab fragment directed towards vitamin K dependent protein such as FIX.
In a further embodiment of the invention the multimodal resin step is performed to capture the vitamin K dependent protein such as FIX from a crude protein solution where after processing the resulting multimodal chromatography resin eluate on the yeast derived affinity ligand chromatography step and after elution of vitamin K dependent protein such as FIX from said affinity chromatography step, exerting a purity of more than 90% in relation to proteins and DNA.
In another further embodiment of the invention is characterised in that the purity of the final product is more than 99%, if the multimodal resin step performed to capture the vitamin K dependent protein such as FIX from a crude protein solution where after processing the resulting multimodal chromatography resin eluate is further processed on additional chromatography step (s) selected from size exclusion, anion exchange, cation exchange, hydrophobic interaction and immobilized metal affinity chromatography and a yeast derived affinity ligand.
In still another embodiment of the invention the mixture comprising vitamin K dependent protein such as FIX is present in a solution.
In yet another embodiment of the invention the vitamin K dependent protein such as FIX is in a crude protein solution including potentially proteases which can degrade the product.
It can be advantageous to apply the washing buffer to the multimodal resin, to wash away contaminants (proteases, DNA etc.) and retain the vitamin K dependent protein such as FIX, before it is released.
In an additional embodiment of the invention, the multimodal resin is washed with a wash buffer at a pH between 6-9, before eluting the vitamin K dependent protein such as FIX.
In a further embodiment of the invention the elution is performed with arginine as the elution agent. According to the invention, the elution agent can be combined with an increased salt concentration in which the salt is selected from the Hofmeister series. According to the invention the elution can take part either with arginine alone or in combination with increased salt concentration or only with increased salt concentration, all of this within the pH range between 6-9, preferably at pH 7.0.
According to the invention NaCl and KCl are preferred in regard of salt comprised in the Hofmeister series which for example are sodium, potassium, ammonium, magnesium, calcium, barium, acetate, phosphate and sulphate.
According to the invention the concentration of arginine is in particular in the range of from about 0.1M to about 2M and 0.1 M to 4M for the salt according to Hofmeister series; in particular in the range of from about 0.4M to about 1.5M for arginine and 0.6 M to 2M for the salt according to Hofmeister series or in the range of from about 0.3M to about 0.7M for arginine and 0.8 M to 1.2 M for the salt according to Hofmeister series
According to another embodiment of the invention the vitamin K dependent protein such as FIX binds to the multimodal resin at a pH between 6-9, preferably at pH 7.0.
In a further embodiment of the invention a buffering substance is used comprising preferably at least one of the substances selected from the group consisting of sodium citrate, histidine, 2-(4-(2-Hydroxyethyl)-1-piperazinyl)-ethane sulfonic acid (HEPES), 2-(N-Morpholino)ethane sulfonic acid (MES), Tris base and sodium acetate in particular in a range of about pH 6 to about pH 9.
In the process of the invention a non-ionic detergent can be present in any of the buffers used, which non-ionic detergent is in particular selected from the group consisting of Polysorbates (Polysorbate 20, 40, 60, 80) and Pluronic F68.
In the elution buffer with a pH 6-9, preferably at pH 7.0, the amount of arginine is typically in the range of 0.1 to 2M, in particular 0.5M.
In the elution buffer with a pH 6-9, preferably pH 7.0, sodium chloride is included in a range of 0.1-4M, in particular in a range from 0.05 to 0.3M.
In the elution buffer with a pH 6-9, preferably at pH 7.0, arginine and sodium chloride is included in a range of 0.1-0.5M, in particular in a range from 0.3 to 0.7M.
In the wash buffer with a pH 6-9, preferably pH 7.0, sodium chloride is included in a range of 0.01-0.3M, in particular in a range from 0.05 to 0.15M.
The amount of non-ionic detergent is typically in the range of 0.001 to 1%, in particular in the buffers for multimodal chromatography 0.02%.
The multimodal chromatography resin which can be employed according to the invention may contain at least one of the following moieties:
In particular, a multimodal chromatography resin for use according to the present invention is selected from the following commercially available resins HEP Hypercel™; PPA Hypercel™; Capto Adhere™; Capto MMC™; MEP Hypercel™.
In another embodiment the process of the invention, the multimodal chromatography step is combined with a vitamin K dependent protein such as FIX affinity chromatographic step wherein the affinity is provided by a protein ligand such as an antibody fragment which is expressed e.g. in yeast.
In another embodiment of the present invention the purification sequence may further comprise pathogen removal/inactivation steps comprising a chemically based inactivation step, a size based removal step, chromatography steps or combinations thereof which steps are based on different physiological properties directed to the pathogen to be removed. An example of a pathogen inactivation step well described in literature is the chemically based solvent detergent method, for example based on tri-n-butyl phosphate and Triton X-100, which disrupt all lipid enveloped viruses, disclosed in EP-A-131 740. An example of a pathogen removal step based on size, is for example a nanofilter with a mean poresize of app. 20 nm, such as a Planova 20 filter. Another example of pathogen removal is based on chromatography. For example affinity chromatography is known to exert pathogen removal properties in general, for example a yeast derived vitamin K dependent protein such as FIX affinity ligand chromatography resin.
In a particular embodiment of the process of the invention the purification sequence further comprises the following steps:
In a particular embodiment the process of the invention could comprise the following steps;
Multimodal (or mixed mode) chromatography is a tool for purifying proteins. Described in, for example, Manufacturer data sheet GE Health Care (11-0035-45AA) Capto Adhere, Manufacturer data sheet GE Health Care (28-9078-88AA) Capto MMC and patent application WO-A-2009/024620 “A process for the isolation and purification of a target protein, free of prion proteins”.
The aforementioned disadvantage of multimodal chromatography is avoided by mild elution conditions in a pH range about neutral which retains the activity of the vitamin K dependent protein such as FIX molecule and facilitates the use of multi modal chromatography in combination with the stabilisation effects of the increased salt concentration, described in for example in EP-A-1 707 634.
According to one embodiment of the invention the multi modal chromatography may be performed in a chromatographic column. This may be regarded as a first capture step. The process of the invention can also be performed in a batch mode. The present invention also facilitates a process of purification without addition of human or animal derived stabilizing additives and the use of a whole process which is absent thereof (monoclonal antibody based immuno affinity resins). The use of the multimodal resin, in particular as capture step, facilitates also a higher binding capacity in comparison with conventional ion exchangers, which results in a more concentrated product eluate from the step, which is of advantage for the product stability.
The process of the invention is typically related with the purification of recombinant vitamin K dependent protein such as FIX (rFIX).
In another embodiment the process of the invention, the multimodal chromatography step is combined with a vitamin K dependent protein such as FIX affinity chromatography step wherein the affinity is provided by a protein ligand such as an antibody fragment which is expressed in yeast.
Therefore also a composition of matter is subject of the invention which composition of matter is comprising a purified recombinant the vitamin K dependent protein such as FIX obtainable by the process according to the invention (with-out the addition or use of any human or animal additives like albumin or monoclonal antibody based immuno affinity ligands).
The invention is further described by the following non-limiting examples.
The biological activity of factor IX was measured with a one-stage clotting assay and the unit of factor IX was expressed in International Units (IU) as defined by the current WHO factor IX concentrate standard.
The one-stage clotting assay is the method prescribed in the European Pharmacopoeia. The principle of the assay is based on the ability of a factor IX containing sample to correct the coagulation time of a factor IX deficient plasma in the presence of phospholipids, contact activator and calcium ions. The time of appearance of a fibrin clot is measured in one step. The factor IX activity is inversely proportional to the coagulation time. The method was performed on Siemens BCS XP instrument.
SDS polyacrylamide gel electrophoresis (SDS-PAGE) involves the separation of proteins based on their size. This method describes the SDS-PAGE of proteins, which is run under reduced conditions. By heating the sample under denaturing and reducing conditions, proteins become unfolded and coated with anionic detergent sodium dodecyl sulphate (SDS), acquiring a high net negative charge that is proportional to the length of the polypeptide chain. When loaded onto a polyacrylamide gel matrix and placed in an electric field, the negatively charged protein molecules migrate towards the positively charged electrode and are separated by a molecular sieving effect, i.e. by their molecular weight. Poly-acrylamide gels restrain larger molecules from migrating as fast as smaller molecules. Because the charge-to-mass ratio is nearly the same among SDS-denatured polypeptides, the final separation of proteins is dependent almost entirely on the differences in relative molecular mass of polypeptides. In a gel of uniform density the relative migration distance of a protein (Rf) is negatively proportional to the log of its mass. If proteins of known mass are run simultaneously with the unknowns, the relationship between Rf and mass can be plotted, and the masses of unknown proteins estimated. The protein bands separated by electrophoresis are visualized by silver staining. Evaluation is done visually by judging the appearances of the standards, reference (control sample) and analysed samples.
The material used in these experiments origins from the commercially available product Nanotiv®, which is a high purity SD treated and nano-filtered Factor IX concentrate.
The cell line used is a derivative of human embryonic kidney cell 293 (HEK 293), which was adapted to serum-free growth. This host, HEK 293F, was stably transfected with an expression cassette carrying the cDNA coding sequence for human FIX and human furin (PACE). The same strong promoter was used for both cassettes. The general process is also described in EP-A-1 739 179 (Schrö-der et al).
The cells were cultivated in serum-free medium in general equipment and according to general methods well known in the art, for example shaken or stirred cultures in t-flasks, shaker flasks and bioreactors (disposable systems and conventional stirred tanks) run as batch, fed-batch, perfusion or continuous chemostat cultures (Freshney, R I (2000), Culture of animal cells: a manual of basic technique, 4th ed, Wiley-Liss; Spier, R E ed (2000), Encyclopedia of cell technology, Wiley, New York; Enfors, S-O and Häggström, L (2000), Bioprocess technology: fundamentals and applications, Högskoletryckeriet, Royal Institute of Technology, Stockholm; Vinci, V A and Parekh, S R (2003), Handbook of industrial cell culture: mammalian, microbial, and plant cells, Humana Press, USA). Typically, perfusion of medium was used to increase cell numbers and product titers beyond standard batch culture levels. The product yield and the amount of host cell proteins differ depending on the cultivation mode:
The recombinant product is released from the cells and the cell suspension or the cell suspension supernatant is the harvest. The properties of the harvest (product titres and impurities as mentioned above) differ depending on the cultivation mode used.
The cell suspension has been used in some of the below described FIX examples.
Plasma derived FIX (pdFIX, Nanotiv®) was used. Freeze dried Nanotiv was dissolved and diluted in an equilibration buffer prior to be loaded on a Capto MMC column.
Capto MMC, a mixed mode resin from GE Healthcare (cat no. 17-5317), was use as capture step for the FIX molecule. Capto MMC is a weak cationic resin with hydrophobic and thiophilic interactions and hydrogen bonding. A Tricorn 5/150 column was packed with Capto MMC resin to a bed height of 15.7 cm. The column volume (CV) was 3.1 ml.
Equilibration buffer: 20 mM sodium citrate, 0.1M NaCl, 0.02% Polysorbate 80, pH 7.0
Low salt wash buffer: 20 mM sodium citrate, 0.2M NaCl, 0.02% Polysorbate 80, pH 6.5
High salt wash buffer: 20 mM sodium sitrate, 0.7M NaCl, 0.02% Polysorbate 80, pH 6.5
Eluting buffer: 20 mM sodium citrate, 0.2M NaCl, 0.5M arginine mono hydrochloride, 0.02% Polysorbate 80, pH 6.5
The column was equilibrated with equilibration buffer followed by loading the start material at a flow rate of 1 ml/min. pdFIX bound to the Capto MMC resin during theses buffer conditions. As seen in Table 1 no pdFIX was found in the flow through. The resin was thereafter subjected to different washing conditions as described in Table 1 and no pdFIX was detected in any of the tested wash buffers. By adding 0.5M arginin to the buffer FIX was eluted from the resin and a yield of 85% was obtained.
Plasma derived FIX (pdFIX, Nanotiv) binds to Capto MMC at pH 7 and can be washed with at least 0.7M NaCl buffer without being eluted from the resin. By addition of 0.5M arginine mono hydrochloride to the buffer, pdFIX is eluted from the column.
Recombinant human FIX (rhFIX) produced in HEK 293 cells. The cells were removed and the cell free supernatant was the start material loaded onto the Capto MMC column.
Capto MMC, a mixed mode resin from GE Healthcare (cat no. 17-5317), was used as capture step for the FIX molecule. Capto MMC is a weak cationic resin with hydrophobic and thiophilic interactions and hydrogen bonding. A XK 26 column was packed with Capto MMC resin to a bed height of 15 cm. The column volume (CV) was 80 ml.
Equilibration buffer: 20 mM sodium citrate, 0.1M NaCl, 0.02% Polysorbate 80, pH 7.0
High salt wash buffer: 20 mM sodium citrate, 0.7M NaCl, 0.02% Polysorbate 80, pH 6.5
Eluting buffer: 20 mM sodium citrate, 0.2M NaCl, 0.5M arginine mono hydrochloride, 0.02% Polysorbate 80, pH 6.5
The column was equilibrated with equilibration buffer followed by loading the start material at a flow rate of 26 ml/min. rhFIX bound to the Capto MMC resin during theses buffer conditions. As seen in Table 2 no rhFIX was found in the flow through. The high salt wash did not elute any rhFIX from the column. By adding 0.5M arginine to the buffer rhFIX was eluted from the resin and a yield of 92% was obtained.
Recombinant FIX (rhFIX) binds to Capto MMC at pH 7 and can be washed with at least 0.7M NaCl buffer without being eluted from the resin. By addition of 0.5M arginine mono hydrochloride to the buffer, rhFIX is eluted from the column.
The buffers used contained 0.02% Polysorbate 80 (a non ionic detergent) which did not result in any negative effects. Possibly it was of an advantage to use Polysorbate 80 in the buffers; compare with the results obtained in the experiment below (Example 3) where no Polysorbate 80 was added to the buffers used.
Recombinant human FIX (rhFIX) was produced in HEK 293 cells. The cells were removed and the cell free supernatant was the start material loaded onto the Capto MMC column.
Capto MMC, a mixed mode resin from GE Healthcare (cat no. 17-5317), was used as capture step for the FIX molecule. Capto MMC is a weak cationic resin with hydrophobic and thiophilic interactions and hydrogen bonding. A XK 26 column was packed with Capto MMC resin to a bed height of 15 cm. The column volume (CV) was 80 ml.
Equilibration buffer: 20 mM sodium citrate, 0.1M NaCl, pH 7.0
High salt wash buffer: 20 mM sodium citrate, 0.7M NaCl, pH 6.5
Eluting buffer: 20 mM sodium citrate, 0.2M NaCl, 0.8M arginine mono hydrochloride, pH 6.5
The column was equilibrated with equilibration buffer followed by loading the start material at a flow rate of 26 ml/min. rhFIX bound to the Capto MMC resin during theses buffer conditions. As seen in Table 3 a low amount of the rhFIX loaded onto the column was found in the flow through. The resin was thereafter washed with a buffer with a fairly high NaCl concentration, 0.7M. As described in Table 3 less than 1% rhFIX was detected in this wash. By adding 0.8M arginine to the buffer rhFIX was eluted from the resin and a yield of 84% was obtained. The buffer used in this experiment did not contain any Polysorbate 80 compared to Experiment 2 and Experiment 5.
Recombinant human FIX (rhFIX) binds to Capto MMC at pH 7 and can be washed with at least 0.7M NaCl buffer without being eluted from the resin. By addition of 0.8M arginine mono hydrochloride to the buffer, rhFIX is eluted from the column.
No detergent was added to the buffers, which can indicate of a somewhat lower recovery of rhFIX in the elution fraction.
Plasma derived FIX (pdFIX, Nanotiv®) was used. Freeze dried Nanotiv was dissolved and diluted in an equilibration buffer prior to be loaded on a Capto MMC column.
Capto MMC, a mixed mode resin from GE Healthcare (cat no. 17-5317), was used as capture step for the FIX molecule. Capto MMC is a weak cationic resin with hydrophobic and thiophilic interactions and hydrogen bonding. A Tricorn 5/150 column was packed with Capto MMC resin to a bed height of 15 cm. The column volume (CV) was 3 ml.
Equilibration buffer: 20 mM sodium citrate, 0.1M NaCl, pH 7.0
Eluting buffer: 20 mM sodium citrate, 0.1M NaCl, 0.5M arginine mono hydrochloride, pH 7.0
Equilibration buffer: 20 mM sodium citrate, 0.1M NaCl, 0.02% Polysorbate 80, pH 7.0
Eluting buffer: 20 mM sodium citrate, 0.1M NaCl, 0.5M arginine mono hydrochloride, 0.02% Polysorbate 80, pH 7.0
A comparison of purifying pdFIX on a Capto MMC column with buffers with or without Polysorbate 80 and a pH set at 7.0. The column was equilibrated with equilibration buffer followed by loading the start material at a flow rate of 1 ml/min. pdFIX bound to the Capto MMC resin during theses buffer conditions. As seen in Table 4 no pdFIX was found in the flow through and equilibration wash fraction.
A 5% increase of plasma derived FIX was eluted when Polysorbate 80 was included in the buffers compared to when no Polysorbate 80 was in the buffers. The difference was low, but the results point towards a benefit of using Polysorbate 80 in the buffers. The yield of pdFIX was high in both experiments. This also shows that pH 7.0 in the buffers used resulted in good data regarding both binding and in the eluting pdFIX from the Capto MMC resin.
Plasma derived FIX (Nanotiv) was used. Freeze dried Nanotiv was dissolved and diluted in an equilibration buffer prior to be loaded on a Capto MMC column.
Chromatographic Resin and Column
Capto MMC, a mixed mode resin from GE Healthcare (cat no. 17-5317), was use as capture step for the FIX molecule. Capto MMC is a weak cationic resin with hydrophobic and thiophilic interactions and hydrogen bonding. A Tricorn 5/150 column was packed with Capto MMC resin to a bed height of 15 cm. The column volume (CV) was 3 ml.
Equilibration buffer: 20 mM HEPES, 0.1M NaCl, pH 8.0
Eluting buffer: 20 mM HEPES, 0.1M NaCl, 0.5M arginine mono hydrochloride, pH 8.0
Equilibration buffer: 20 mM sodium citrate, 0.1M NaCl, pH 6.0
Eluting buffer: 20 mM sodium citrate, 0.1M NaCl, 0.5M arginine mono hydrochloride, pH 6.0
A comparison of purifying pdFIX on a Capto MMC column with buffers with two different pH, 8.0 and 6.0, used both in the binding and eluting buffers. The column was equilibrated with equilibration buffer followed by loading the start material at a flow rate of 1 ml/min. pdFIX bound to the Capto MMC resin during theses buffer conditions. As seen in Table 5 no pdFIX was found in the flow through. The pdFIX yield was equally high in the eluting fraction for both pH tested.
These experiments show that plasma derived FIX can bind to the Capto MMC resin in buffers with pH of 8.0 and 6.0 and that both these pH also can be used in the eluting buffer.
The aim of these experiments was to study the capture and elution of recombinant human FIX (rhFIX) on a Capto MMC resin at three different pH; 6.0, 7.0 and 8.0. The benefit of 0.02% Polysorbate 80 in these buffers used regarding binding and elution of rhFIX was also investigated.
Recombinant human FIX produced in HEK 293 cells. The cells were removed and the cell free supernatant was the start material loaded onto the Capto MMC column.
Capto MMC, a mixed mode resin from GE Healthcare (cat no. 17-5317), was used as capture step for the FIX molecule. Capto MMC is a weak cationic resin with hydrophobic and thiophilic interactions and hydrogen bonding. A XK 16 column was packed with Capto MMC resin to a bed height of 13.5 cm. The column volume (CV) was 27 ml.
The column was equilibrated with equilibration buffer followed by loading the start material at a flow rate of 9 ml/min. The column was then washed with equilibration buffer followed by eluting the bound rhFIX from the Capto MMC column. The results are presented in Table 6.
The data presented in table 6 shows that rhFIX binds to Capto MMC at pH 6, pH 7 and pH 8. No rhFIX was found in the flow though. The bound rhFIX can also be eluted from the Capto MMC resin at these pH with a recovery of >75%. The best recovery was obtained with a eluting buffer with pH 7. The addition of Polysorbate 80 in the equilibration and eluting buffer resulted in an increase of at least 5% when pH 7 or 6 was used. No benefit was obtained for Polysorbate 80 when buffers with pH 8 was used.
These data and the data obtained in experiment 5 indicate for a positive effect of Polysorbate 80 for the recovery of rhFIX and pdFIX on a Capto MMC resin.
Recombinant human FIX can bind to Capto MMC at a pH range of at least 6-8. The rhFIX molecules are eluted from the Capto MMC resin by addition of 0.5M arginine mono hydrochloride to the buffers independent of which of the three tested pH that was used.
But the results obtained shows that pH 7 results in a larger rhFIX yield. The addition of the detergent Polysorbate 80 indicates for an increase of the rhFIX recovery when pH 7 or 6 was used.
The aim of this work was to purify recombinant human FIX from cultivation media to a pure product. This included three steps; a capture step, an affinity step and a concentrating and buffer exchanging step. A Capto MMC resin was used as a capture step and a non animal derived FIX affinity ligand step was used as the major purification step. As the final step an ultra filtration system with a 10 kDa cut off was used, first to concentrate the molecule and then to exchange the buffer to a physiological buffer environment.
Recombinant human FIX produced in HEK 293 cells. The cells were removed and the cell free supernatant was the start material loaded onto the Capto MMC column.
Capto MMC, a mixed mode resin from GE Healthcare (cat no. 17-5317), was used as capture step for the FIX molecule. Capto MMC is a weak cationic resin with hydrophobic and thiophilic interactions and hydrogen bonding. A XK 50 column was packed with Capto MMC resin to a bed height of 16.5 cm. The column volume (CV) was 324 ml.
The column was equilibrated with equilibration buffer followed by loading the start material at a flow rate of 75 ml/min. The column was then washed with equilibration buffer followed by eluting the bound rhFIX from the Capto MMC column. The results are presented in Table 7. The purification of rhFIX was performed in three separate runs, using the same experimental set up and the same type of buffers. These capture purifications were performed at pH 7.0.
The data presented in table 7 shows that rhFIX binds to Capto MMC at pH 7. No or very little rhFIX was found in the flow though. The bound rhFIX could also be eluted from the Capto MMC resin at pH 7.0 by adding arginine-HCl to a final concentration of 0.5M. The average recovery of these three captures of rhFIX was 92%.
As an affinity step a non animal derived FIX affinity ligand (Fab fragment) produced in yeast was used (developed in co-operation with BAC BV, the Bio Affinity Company). This ligand was coupled to a Capto MP resin (GE Healthcare) according to standard coupling techniques and is referred to as “the FIX affinity resin”.
A XK 26 column was packed with the FIX affinity resin to a bed height of 7.5 cm. The column volume (CV) was 40 ml.
The eluates from the three capture steps were pooled and used as start material on the affinity column. The column was equilibrated with equilibration buffer followed by loading the start material at a flow rate of 10 ml/min. The column was then washed with equilibration buffer followed by eluting the bound rhFIX from the affinity column. The results are presented in Table 8. The purification of rhFIX was performed in two separate runs, using the same experimental set up and the same type of buffers.
The data presented in table 8 shows that rhFIX binds to FIX affinity resin at pH 7. The flow through obtained was an effect of the binding capacity of the amount of resin used. Approximately 100% of the rhFIX used in both experiments are detectable. The bound rhFIX could be eluted from FIX affinity resin by using a buffer containing 2M MgCl2.
By using a UF system the rhFIX in the eluate from the affinity column was concentrated and then the buffer was exchanged by a dia-filtration using the same UF filter.
A Pellicon 3 filter with a 10 kDa cut off mounted in a Pellicon 2 system was used.
By pumping the sample in a tangential flow and allowing a small part of the volume continuously passing through the Pellicon 3 filter, the volume was decreased. Because of the pore size used in the filter, the rhFIX molecule was contained in the re-circulating fraction. The Molecular weight of rhFIX is approximately 55 kDa and is retained when a filter with a pore size of 10 kDa is used.
A volume of 310 ml affinity eluate was concentrated to approximately 60 ml. This volume was the dia-filtrated by continuously adding dia-filtration buffer at the same speed as is filtered through the Pellicon 3 filter. The buffer in this 60 ml concentrate was exchanged approximately 18 times. The conductivity of this concentrate was changed from 123 mS/cm to 18.6 mS/cm at 25° C.
The rhFIX recovery over this concentration and buffer exchange step was 86%. A wash step of the UF filter with the dialysis buffer was performed to recover as much rhFIX as possible.
| Number | Date | Country | Kind |
|---|---|---|---|
| 10158511.5 | Mar 2010 | EP | regional |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP11/54906 | 3/30/2011 | WO | 00 | 12/12/2012 |
| Number | Date | Country | |
|---|---|---|---|
| 61282895 | Apr 2010 | US |
