Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
  • B01J39/26—Cation exchangers for chromatographic processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
  • B01D15/08—Selective adsorption, e.g. chromatography
  • B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
  • B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
  • B01D15/1864—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns using two or more columns
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
  • B01D15/08—Selective adsorption, e.g. chromatography
  • B01D15/26—Selective adsorption, e.g. chromatography characterised by the separation mechanism
  • B01D15/34—Size selective separation, e.g. size exclusion chromatography, gel filtration, permeation
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
  • B01D15/08—Selective adsorption, e.g. chromatography
  • B01D15/26—Selective adsorption, e.g. chromatography characterised by the separation mechanism
  • B01D15/36—Selective adsorption, e.g. chromatography characterised by the separation mechanism involving ionic interaction
  • B01D15/361—Ion-exchange
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
  • B01D15/08—Selective adsorption, e.g. chromatography
  • B01D15/26—Selective adsorption, e.g. chromatography characterised by the separation mechanism
  • B01D15/36—Selective adsorption, e.g. chromatography characterised by the separation mechanism involving ionic interaction
  • B01D15/361—Ion-exchange
  • B01D15/362—Cation-exchange
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
  • B01D15/08—Selective adsorption, e.g. chromatography
  • B01D15/26—Selective adsorption, e.g. chromatography characterised by the separation mechanism
  • B01D15/38—Selective adsorption, e.g. chromatography characterised by the separation mechanism involving specific interaction not covered by one or more of groups B01D15/265 - B01D15/36
  • B01D15/3804—Affinity chromatography
  • B01D15/3809—Affinity chromatography of the antigen-antibody type, e.g. protein A, G, L chromatography
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/22—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising organic material
  • B01J20/24—Naturally occurring macromolecular compounds, e.g. humic acids or their derivatives
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/22—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising organic material
  • B01J20/26—Synthetic macromolecular compounds
  • B01J20/261—Synthetic macromolecular compounds obtained by reactions only involving carbon to carbon unsaturated bonds
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/22—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising organic material
  • B01J20/26—Synthetic macromolecular compounds
  • B01J20/265—Synthetic macromolecular compounds modified or post-treated polymers
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/22—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising organic material
  • B01J20/26—Synthetic macromolecular compounds
  • B01J20/265—Synthetic macromolecular compounds modified or post-treated polymers
  • B01J20/267—Cross-linked polymers
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
  • B01J20/28014—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their form
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
  • B01J20/28014—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their form
  • B01J20/28033—Membrane, sheet, cloth, pad, lamellar or mat
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/281—Sorbents specially adapted for preparative, analytical or investigative chromatography
  • B01J20/286—Phases chemically bonded to a substrate, e.g. to silica or to polymers
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/281—Sorbents specially adapted for preparative, analytical or investigative chromatography
  • B01J20/286—Phases chemically bonded to a substrate, e.g. to silica or to polymers
  • B01J20/289—Phases chemically bonded to a substrate, e.g. to silica or to polymers bonded via a spacer
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/30—Processes for preparing, regenerating, or reactivating
  • B01J20/3085—Chemical treatments not covered by groups B01J20/3007 - B01J20/3078
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/30—Processes for preparing, regenerating, or reactivating
  • B01J20/32—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating
  • B01J20/3202—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating characterised by the carrier, support or substrate used for impregnation or coating
  • B01J20/3206—Organic carriers, supports or substrates
  • B01J20/3208—Polymeric carriers, supports or substrates
  • B01J20/3212—Polymeric carriers, supports or substrates consisting of a polymer obtained by reactions otherwise than involving only carbon to carbon unsaturated bonds
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/30—Processes for preparing, regenerating, or reactivating
  • B01J20/32—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating
  • B01J20/3231—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating characterised by the coating or impregnating layer
  • B01J20/3242—Layers with a functional group, e.g. an affinity material, a ligand, a reactant or a complexing group
  • B01J20/3268—Macromolecular compounds
  • B01J20/3278—Polymers being grafted on the carrier
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
  • B01J20/30—Processes for preparing, regenerating, or reactivating
  • B01J20/32—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating
  • B01J20/3231—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating characterised by the coating or impregnating layer
  • B01J20/3242—Layers with a functional group, e.g. an affinity material, a ligand, a reactant or a complexing group
  • B01J20/3268—Macromolecular compounds
  • B01J20/328—Polymers on the carrier being further modified
  • B01J20/3282—Crosslinked polymers
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
  • C07H1/00—Processes for the preparation of sugar derivatives
  • C07H1/06—Separation; Purification
  • C07H1/08—Separation; Purification from natural products
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07K—PEPTIDES
  • C07K1/00—General methods for the preparation of peptides, i.e. processes for the organic chemical preparation of peptides or proteins of any length
  • C07K1/14—Extraction; Separation; Purification
  • C07K1/16—Extraction; Separation; Purification by chromatography
  • C07K1/22—Affinity chromatography or related techniques based upon selective absorption processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2220/00—Aspects relating to sorbent materials
  • B01J2220/80—Aspects related to sorbents specially adapted for preparative, analytical or investigative chromatography
• • G—PHYSICS
  • G01—MEASURING; TESTING
  • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
  • G01N30/00—Investigating or analysing materials by separation into components using adsorption, absorption or similar phenomena or using ion-exchange, e.g. chromatography or field flow fractionation
  • G01N30/02—Column chromatography
  • G01N30/88—Integrated analysis systems specially adapted therefor, not covered by a single one of the groups G01N30/04 - G01N30/86
  • G01N2030/8809—Integrated analysis systems specially adapted therefor, not covered by a single one of the groups G01N30/04 - G01N30/86 analysis specially adapted for the sample
  • G01N2030/8813—Integrated analysis systems specially adapted therefor, not covered by a single one of the groups G01N30/04 - G01N30/86 analysis specially adapted for the sample biological materials
  • G01N2030/8827—Integrated analysis systems specially adapted therefor, not covered by a single one of the groups G01N30/04 - G01N30/86 analysis specially adapted for the sample biological materials involving nucleic acids
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/50—Improvements relating to the production of bulk chemicals
  • Y02P20/582—Recycling of unreacted starting or intermediate materials

Definitions

• the present invention relates to separation of biomolecules, and more particularly to ion exchange separation of proteins.
• the invention also relates to a separation matrix suitable for separation of biomolecules and to a method of manufacturing such a matrix.
• target compounds such as drug or drug candidates usually need to be separated from contaminating species originating from the process of manufacture.
• a protein drug or drug candidate produced by expression of recombinant host cells will need to be separated e.g. from the host cells and possibly cell debris, other host cell proteins, DNA, RNA, and any other compounds originating from the fermentation or cell culture broth.
• chromatography is involved as at least one step in many of the currently used biotech purification schemes.
• the term chromatography embraces a family of closely related separation methods, which are all based on the principle that two mutually immiscible phases are brought into contact.
• the target compound is introduced into a mobile phase, which is contacted with a stationary phase.
• the target compound will then undergo a series of interactions between the stationary and mobile phases as it is being carried through the system by the mobile phase.
• the interactions exploit differences in the physical or chemical properties of the components of the sample.
• the stationary phase in chromatography is comprised of a solid carrier to which ligands, which are functional groups capable of interaction with the target compound, have been coupled. Consequently, the ligands will impart to the carrier the ability to effect the separation, identification, and/or purification of molecules of interest.
• Liquid chromatography methods are commonly named after the interaction principle utilized to separate compounds. For example, ion exchange chromatography is based on charge-charge interactions; hydrophobic interaction chromatography (HIC) utilizes hydrophobic interactions; and affinity chromatography is based on specific biological affinities.
• ion exchange is based on the reversible interaction between a charged target compound and an oppositely charged chromatography matrix. The elution is most commonly performed by increasing the salt concentration, but changing the pH is equally possible. Ion- exchangers are divided into cation-exchangers, wherein a negatively charged chromatography matrix is used to adsorb a positively charged target compound; and anion-exchangers, wherein a positively charged chromatography matrix is used to adsorb a negatively charged target compound.
• strong ion exchanger is used for an ion-exchanger which is charged over broad pH intervals, while a "weak” ion-exchanger is chargeable at certain pH values.
• One commonly used strong cation-exchanger comprises sulphonate ligands, known as S groups.
• S groups sulphonate ligands
• SP cation exchangers wherein the S groups are linked by propyl to the carrier.
• the charged groups in ion exchangers can be attached to the carriers or support materials in different ways.
• One aspect of the invention is to provide a separation method with high throughput and high selectivity. This is achieved with a method as defined in claim 1.
• One advantage is that a high binding capacity for target proteins can be achieved, in combination with a high selectivity between e.g. monomeric and aggregated immunoglobulins. Further advantages are that high binding capacities at elevated ionic strengths, rapid mass transport/binding kinetics and high alkali stabilities - allowing a large number of cycles to be performed before the matrix has to be exchanged - can be achieved.
• Another aspect of the invention is to provide a separation matrix with high binding capacity and high selectivity for target proteins, as well as a high alkali stability. This is achieved with a matrix as defined in claim 16.
• a third aspect of the invention is to provide a method of manufacturing a separation matrix with high binding capacity and high selectivity for target proteins, as well as a high alkali stability. This is achieved with a method as described in claim 29.
• Figure 1 shows the reaction scheme for allylation of hydroxyl groups on a support with allyl glycidyl ether.
• Figure 2 shows mixtures of monomers used for grafting: a) vinyl sulfonic acid (VSA) and vinylpyrrolidone (VP), b) 3-allyloxy, 2-hydroxy-l-propanesulfonic acid (APS) and
• FIG. 3 shows an ideal (solid line) selectivity curve for removal of aggregated antibodies and a less than ideal (dotted line) curve.
• Figure 4 shows aggregate removal selectivity curves for VP-VSA prototypes S67-G1-A100 and S67-G1-A200 compared with a reference.
• Figure 5 shows aggregate removal selectivity curves for VP-VSA prototypes S50-G1-A25 and S50-G1-A50 compared with a reference.
• Figure 6 shows aggregate removal selectivity curves for VP-VSA prototypes S50-G2-A25 and S50-G3-A25 compared with a reference.
• Figure 7 shows aggregate removal selectivity curves for VP-VSA prototypes S50-G4-A200 and S67-G1-A200 compared with a reference. The initial aggregate concentration was 7%.
• Figure 8 shows aggregate removal selectivity curves for VP-VSA prototypes S67-G1-A200, S67-G1-A450 and S50-G4-A200 compared with a reference. The initial aggregate concentration was 7%.
• Figure 9 shows aggregate removal selectivity curves for VP-VSA prototypes S77-G1-A200 and S77-G1-A450 compared with a reference.
• Figure 10 shows an aggregate removal selectivity curve for VP-VSA prototype S80-G1-A200 compared with a reference.
• Figure 1 1 shows an aggregate removal selectivity curve for polydivinylbenzene-based VP-VSA prototype P63-G1-A200 at pH 5.0 compared with a reference.
• Figure 12 shows an aggregate removal selectivity curve for polydivinylbenzene-based VP-VSA prototype P63-G1-A200 at pH 5.25 compared with a reference.
• Figure 13 shows chromatograms for a protein mixture and a monoclonal antibody on a) the reference matrix SP Sepharose FIP and b) a VPA-grafted matrix of the invention.
• the present invention discloses a method of separating a biomolecule from at least one other component in a liquid.
• the biomolecule can be dissolved in the liquid and the other component(s) can also be dissolved in the liquid.
• the contacting step can e.g. take place by conveying the liquid through a column, a membrane adsorber or other device packed with the separation matrix, but it can also be carried out by e.g. batch adsorption where matrix and liquid are mixed in a container.
• the separation can occur through adsorption of the biomolecule or of the other component(s) to the matrix.
• the pH in the contacting step may e.g. be 4-7, such as 4.5-6 or 4.75-5.5 and the ionic strength may be e.g. 10-100 mM, such as 20-60 mM.
• the liquid may be an aqueous buffer and may comprise a buffering component such as acetate, phosphates, citrates, succinates etc and a salt such as an alkali chloride, an alkali sulfate, ammonium sulfate etc. It may also comprise additives such as detergents, amino acids, water-miscible solvents, water soluble polymers, chaotropes, cosmotropes etc.
• a buffering component such as acetate, phosphates, citrates, succinates etc and a salt such as an alkali chloride, an alkali sulfate, ammonium sulfate etc.
• a salt such as an alkali chloride, an alkali sulfate, ammonium sulfate etc. It may also comprise additives such as detergents, amino acids, water-miscible solvents, water soluble polymers, chaotropes, cosmotropes etc.
• the biomolecule is a biomacromolecule, such as protein, a peptide or a nucleic acid.
• suitable proteins include plasma proteins, immunoglobulins and recombinant proteins like e.g. erythropoietin, interferons, blood coagulation factors etc, while examples of peptides can be insulin etc.
• the biomolecule can also be a vaccine antigen, including virus particles, virus proteins, bacterial polysaccharides and bacterial proteins.
• the biomolecule is an immunoglobulin, immunoglobulin fragment or an immunoglobulin-containing protein, such as an antibody, an antibody fragment, an antibody conjugate or an antibody fusion protein.
• immunoglobulin fusion proteins is an important class of biopharmaceuticals and the method of the invention is particularly suitable for removal of contaminants from these substances.
• said at least other component is a protein, such as a host cell protein, Protein A or an aggregate of immunoglobulins, immunoglobulin fragments or immunoglobulin- containing proteins.
• aggregates can be e.g. dimers, trimers and/or higher multimers.
• the method of the invention is particularly suitable for protein-protein separations, such as removal of host cell proteins, Protein A, aggregates, charge variants, misfolded proteins etc from immunoglobulins and related substances. Efficient clearance of these contaminants is essential in the production of biopharmaceuticals, as they can cause immunogenicity and other undesirable side effects.
• the other component can also be e.g. antibiotics added during cell culture, endotoxins, viruses or solvents and detergents added for inactivation of viruses.
• the other component can further be a reactant used to form a conjugate, such as e.g. the drug component of an antibody-drug conjugate or PEG in the case of a PEG-ylated protein.
• a conjugate such as e.g. the drug component of an antibody-drug conjugate or PEG in the case of a PEG-ylated protein.
• the liquid is an eluate from a previous chromatography step, such as an affinity step, an ion exchange step, a multimodal step or a hydrophobic interaction step.
• the method of the invention is particularly suitable for removal of residual contaminants present in e.g. protein solutions eluted form a previous chromatography step.
• the previous step can be a capture step such as e.g. a protein A or a protein L chromatography step and the residual contaminants may be e.g. host cell proteins, aggregates, leached protein A or L or viruses.
• the liquid is the flow-through from a separation matrix, such as an ion exchange matrix, a multimodal matrix or a hydrophobic interaction matrix.
• a separation matrix such as an ion exchange matrix, a multimodal matrix or a hydrophobic interaction matrix.
• the method can e.g. be applied after a previous flow-through chromatography step, such as an anion exchange or multimodal anion exchange flow-through step applied after a protein A step in an antibody process.
• said biomolecule is an immunoglobulin, immunoglobulin fragment or an immunoglobulin-containing protein, such as an antibody, an antibody fragment, an antibody conjugate or an antibody fusion protein and wherein at least 1%, such as at least 5% or at least 10% of said biomolecule is in the form of aggregates, such as dimers, trimers and higher multimers.
• the method is particularly useful for removal of aggregates, which can be produced either during cell cultivation or during processing, e.g. when the immunoglobulins are exposed to low pH during elution of a protein A column or during virus inactivation.
• the method further comprises a step of eluting said biomolecule from said separation matrix with an elution buffer.
• the method of the invention may be carried out in bind-elute mode, in which case the biomolecule is adsorbed to the matrix and afterwards eluted with the elution buffer.
• the other component(s) may pass through the matrix in the flow-through or they may bind to some extent and be eluted separately from the biomolecule.
• the elution can be performed as a step change in buffer composition or pH, a series of step changes or by a gradient in buffer composition or pH.
• the method can also comprise a washing step with a washing buffer. This step serves the purpose of removing non-bound or loosely bound other components and can e.g.
• Elution and wash buffers may comprise buffering substances such as acetate, phosphates, citrates, succinates, Tris, glycine etc. They may also comprise neutral salts, lyotropic salts, detergents, amino acids, water-mi scible solvents, water soluble polymers, chaotropes, cosmotropes and other additives.
• the method may also be applied in flow-through mode, where the other component(s) adsorb to the matrix, while the biomolecule does not adsorb or adsorbs very weakly and can be recovered in purified form in the flow-through. The adsorbed other component(s) may then be removed by a strip buffer applied to the matrix.
• the method further comprises a step of cleaning said separation matrix with a cleaning liquid.
• the cleaning liquid can be an alkaline cleaning liquid comprising at least 0.1 mol/1 of an alkali hydroxide such as NaOH or KOH. It can e.g. be a 0.5-2 mol/1 NaOH or KOH solution, such as an aqueous solution of about 1 M NaOH.
• the solution may also comprise chaotropic agents, solvents, detergents, salts etc to improve the cleaning efficiency.
• alkaline cleaning can be used without causing degradation to the matrix.
• the method, including the cleaning step with an alkaline cleaning liquid can be repeated many times, such as at least 10, at least 50 , 10-100 or 50-100 times. This allows for repeated use of the matrix over a large number of cycles, which is important for a good process economy.
• the method may also comprise further subsequent separation steps. It may e.g. be followed by one or more chromatography steps, such as anion exchange, cation exchange, multimodal, hydroxyapatite, hydrophobic interaction or size exclusion chromatography. It can also be followed by membrane filtration, e.g. ultrafiltration.
• chromatography steps such as anion exchange, cation exchange, multimodal, hydroxyapatite, hydrophobic interaction or size exclusion chromatography.
• membrane filtration e.g. ultrafiltration.
• the polymer chains are copolymer chains and further comprise units derived from a second non-charged monomer.
• the copolymer chains can e.g. be random copolymer chains or they can have an alternating or segmented structure.
• An advantage of having the non-charged units in the chains is that the local charge density of the chains can be controlled, which enables improvements in binding capacity and selectivity.
• the second non-charged monomer is an N-vinylamide.
• the n-vinylamide can e.g.
• L is a covalent bond or -CH 2 -0-L'- , where L' is a C 2 -C 4 or C3-C 4 alkylene chain, optionally substituted with at least one hydroxyl group.
• the first monomer is selected from the group consisting of vinyl sulfonate, vinyl phosphonate and allyloxyhydroxypropyl sulfonate.
• the first monomer is selected from this group, or is vinyl sulfonate
• the second monomer is an N-vinyl amide, such as N-vinyl pyrrolidone.
• the molar ratio of the units derived from the first monomer to the units derived from the second monomer is 0.05 to 5, such as 0.10 to 2 or 0.5 to 2.
• the polymer or copolymer chains are bound to the support by linker units derived from allyl ethers, such as e.g. allyl hydroxypropyl ethers.
• the present invention discloses a separation matrix comprising a solid support and copolymer chains bound to the solid support, wherein the copolymer chains comprise units derived from
• a) a first monomer of structure CH 2 CH-L-X, where L is a covalent bond or an alkyl ether or hydroxysubstituted alkyl ether chain comprising 2-6 carbon atoms, and X is a sulfonate or phosphonate group and
• the copolymer chains may be grafted to the solid support, with one or more links to the support for each chain.
• the chains may e.g. consist essentially of the first and second monomer units but they can also comprise other monomer units.
• the copolymer chains can have a random structure but they can also be alternating or segmented.
• the embodiments of the matrix of the invention are suitable for use in the separation methods described above.
• L is a covalent bond or -CH 2 -0-L'- , where L' is a C2-C4 or C3-C4 alkylene chain, optionally substituted with at least one hydroxyl group. As described above these structures provide high alkali resistance and are beneficial for providing high capacities and selectivities.
• the charged monomer is selected from the group consisting of vinyl sulfonate, vinyl phosphonate and allyloxyhydroxypropyl sulfonate. These commercially available monomers are suitable for grafting and provide good capacities/selectivities as well as alkali stability.
• said second non-charged monomer is an N-vinyl amide.
• N-vinyl amides copolymerize well with the charged monomers and give remarkably alkali-resistant polymers. This applies in particular to cyclic N-vinyl amides (e.g. N-vinyl lactams).
• said second non-charged monomer is selected from the group consisting of N-vinyl pyrrolidone, N-vinyl caprolactam, N-vinyl formamide and N-vinyl acetamide.
• the first monomer is selected from this group, or is vinyl sulfonate
• the second monomer is an N-vinyl amide, such as N-vinyl pyrrolidone.
• the combinations of these monomers give particularly alkali stable polymers and the monomers show favourable copolymerization behavior, such that matrices with suitable amounts of grafted polymer, suitable compositions of the grafted polymer and suitable ionic capacities can be prepared.
• the alkali stability of these copolymers is higher than for acrylamide or (meth)acrylate polymers, as described e.g.
• the molar ratio of the units derived from the first monomer to the units derived from the second monomer is 0.05 to 5, such as 0.10 to 2 or 0.5 to 2.
• the molar ratio can be determined by spectroscopic methods and it can also be calculated from the ion capacity and the total content of copolymer chains (see below). If sulfur or phosphorus is only present in the first monomer and nitrogen is only present in the second monomer, the molar ration can also be determined from elemental analysis data.
• the (hydrogen) ion capacity of the matrix is 15-300 or 20-300
• micromol/ml such as 70 - 300, 20-200, 20-80 or 30-70 micromol/ml.
• the hydrogen ion capacity can be determined by well-known titration methods. If sulfur or phosphorus is only present in the acidic groups, the ion capacity can also be calculated from elemental analysis data. Ionic capacities around 30-70 micromol/ml can provide both high protein capacities and high monomer-aggregate selectivities, but it is also possible to use ion capacities up to at least 200 micromol/ml, particularly when high protein capacities are desired.
• the total content of (co)polymer chains in the matrix may be 2-80 or 2-60 mg/ml, such as 4-35, 4-20, 3-12, 12-20, 20-80 or 25-75 mg/ml. This can be determined by spectroscopic methods, by elementary analysis (depending on the monomers used) and as the weight add-on during preparation of the matrix.
• a relatively low content e.g. 2-20 mg/ml
• a higher content e.g. 20-80 mg/ml
• the polymer or copolymer chains are bound to the support by linker units derived from allyl ethers, such as e.g. allyl hydroxypropyl ethers.
• the chains may be bound by one or more such linker units per chain.
• the solid support comprises a polyhydroxy polymer, such as a polysaccharide.
• polysaccharides include agar, agarose, carrageenan, dextran, cellulose, pullulan etc.
• examples of other polyhydroxy polymers include polyvinyl alcohol, polyglycidol etc.
• Advantages of polyhydroxy polymer supports include their hydrophilicity (which can eliminate or reduce non-specific interactions), their alkali stability and their propensity to forming porous structures with large surface areas and rapid mass transport.
• the solid support comprises agar or agarose in native or derivatized form.
• agar or agarose in native or derivatized form.
• Agarose supports in bead form are commercially available e.g under the trade names of Sepharose and Capto (GE Healthcare Bio-Sciences AB) and they can be prepared e.g. as described in Hjerten et al (Biochim Biophys Acta 79, 393-398 (1964)).
• the pore size of the supports can be controlled by the concentration of the agarose solution used to manufacture them and to some extent by the crosslinking conditions.
• the particle size of the beads can be controlled by the input of mechanical energy during emulsion (or aerosol) formation and it is also possible to prepare fractions of polydisperse bead materials by sieving.
• the solid support is crosslinked, such as with hydroxyalkyl ether crosslinks.
• Crosslinking improves rigidity and chemical stability and an advantage of using hydroxyalkyl ether crosslinks is that they are alkali stable and do not cause non-specific interactions with proteins.
• Such crosslinks can be produced e.g. by the use of epihalohydrins, diepoxides and allyl halides/allyl glycidyl ethers as crosslinking reagents.
• Crosslinked agarose of high rigidity prepared e.g. by the methods described in US6602990 or US7396467, can advantageously be used as a solid support.
• the solid support is porous, such as in the form of porous beads or a porous membrane.
• the solid support has a pore size corresponding to a K d value of 0.5-0.9, such as 0.6-0.8, measured with dextran of Mw 110 kDa as the probe molecule.
• the pore size has importance for the capacity but also for the selectivity. In swelling materials like agarose and other polysaccharide gels, the pore size is best estimated by an inverse size exclusion
• volume fraction K d accessible for a probe molecule e.g. dextran of Mw 110 kDa
• This method is described in e.g. L Hagel et al: J
• the separation matrix has a pore size corresponding to a 3 ⁇ 4 value of 0.1- 0.8, such as 0.2-0.6 or 0.2-0.4, measured with dextran of Mw 110 kDa as the probe molecule.
• the Kd value is by definition a value between 0 and 1 and since material has been added to the solid support by the grafting, in most cases the Kd value of the matrix (with the grafted polymer) will be lower than the corresponding value for the solid support before grafting. Kd values between 0.2 and 0.6 or 0.2 and 0.4 provide god aggregate removal in combination with a high capacity.
• the present invention discloses a method of manufacturing a separation matrix according to any one of the embodiments described above, comprising the steps of:
• a) providing a solid support comprising moieties with copolymerizable C C double bonds or moieties susceptible to formation of free radicals; b) contacting the solid support with a mixture comprising the first and second monomer and; c) initiating radical polymerization.
• the support may inherently comprise double bonds (e.g. residual double bonds on methacrylate or styrene-divinylbenzene supports) or moieties susceptible to formation of free radicals (e.g. alpha-hydrogens to hydroxyl groups in polyhydroxy polymer supports) or either of these moieties may be introduced as described below.
• the initiation of radical polymerization may be accomplished by irradiation or by thermal/chemical initiation using one of many known initiation systems such as e.g. peroxide initiators, azo initiators, persulphate, hydrogen peroxide, cerium(IV) salts, photoinitiators, redox systems, ATRP etc.
• Moieties susceptible to formation of free radicals can be e.g. a) initiator species like
• hydroperoxides that can be formed by gamma or E-beam irradiation in the presence of oxygen or azo initiators formed by reaction with e.g. azobiscyanopentanoic acid or b) chain transfer groups like thiols that can be introduced e.g. by reacting an epoxy-activated support with a dithiol or sulfide ions.
• said moieties susceptible to formation of free radicals comprise i) chain transfer groups such as thiols or hydrogens in alpha position to hydroxyl groups or ii) initiating groups such as peroxides, hydroperoxides, persulfates or azo compounds.
• the amount of grafted polymer can be controlled by providing different concentrations of copolymerizable double bonds on the base matrix and by providing different monomer concentrations during grafting.
• the ionic capacity can be controlled by varying the monomer composition and by varying the amount of grafted polymer.
• a 50% (v/v) slurry of the prototype suspension was added to a glass filter with a 1.00 ml chamber above the filter.
• the gel was then drained by vacuum suction, and when a dry surface was spotted the gel was sucked dry for another 30 s.
• 1 ml of the drained gel was then added to a pre-weighed glass filter to be washed with 5*20 ml acetone.
• the glass filter was then put in an oven at 105°C for 24 h before measuring the dry weight (four digits). Duplicate samples were measured.
• Approximately 4ml drained gel was put on a small glass filter and was then washed several times with a total amount of 40ml 0,5M HCl and then several times with a total amount of 100ml ImM HCl. The particles were then brought to a 1ml cube whereupon the gel was drained by vacuum suction, and when a dry surface was spotted the gel was sucked dry for another 30 s. lml of the drained gel was then added to a 40ml beaker together with 20ml of distilled water. The hydrogen ion capacity of ml 1 gel was then determined by titration.
• AKTATMexplorer equipped with an A-900 autosampler.
• a Shimadzu Rl-detector (RID-bA) was connected to the AKTATM system for detection of the dextran samples. The following conditions were used: Flow: 0, 2rnl/rnin Mobile phase: 0,2M NaCl Sample volume: 100 microliters.
• the dextran peaks were evaluated according to well-known methods in this field.
• Ve retention volume eluted dextran (ml)
• V0 void volume (retention of raw dextran void marker) (ml)
• Vc calculated column volume (bed height (cm) x surface area column (cm2) ) (ml)
• Vt total liquid volume (retention volume NaCl) (ml).
• the a, a, Azodiisobutyramidine di hydrochloride (ADBA) initiator was added to a 40 ml glass vial whereupon 17g drained allylated beads added. Distilled water, VP and aqueous VSA solution were then added to the vial. The vial was closed with a plastic top and then put in a heated shaking equipment where the vial was shaken at r.t. for 5min before raising the temperature to 55C. The polymerisation reactions proceeded for 17h overnight and the particles was then washed on a glass filter with 8 gel volumes (GV) of distilled water, 8 GV of 99.5% ethanol and then 8 GV of water.
• GV gel volumes
• Prototype S67-G1-A200 had a Kd value of 0.295 for dextran 110 kD and the reference
• the prototype media were settled and compressed in Tricorn 5/50 columns. After packing, the columns were tested in 0.4 M NaCl at 0.065 ml/min by injecting 10 ⁇ of 2 M NaCl containing 3% (v/v) acetone. A 280 , A 26 o and conductivity peaks were registered and integrated.
• the acceptance criteria for a successful packing was an asymmetry value between 0.8 and 1.5.
• Protein A purified Mab was buffer-exchanged with a HiPrep Desalting 26/10 column to 50 mM Na-acetate + 10 mM NaCl pH 5.25. Protein concentration was then determined by
• the protein concentration was determined by spectrophotometry at 280 nm using Lambert- Beers law (Equation 1).
• AKTA explorer 100 system with Unicorn 5.11 as control software.
• the prototypes and reference media were tested with the same start and elution buffers to achieve the same gradient length and slope. Therefore, the start buffers (both acetate and phosphate) were supplied with 10 mM NaCl to diminish the possible non-traditional behavior.
• Monomer purity was assessed by size exclusion chromatography (SEC) using two SuperdexTM 200 5/150 GLcolumns connected in series.
• the mobile phase was phosphate buffered saline (PBS) and the flow rate was 0.35 ml/min for 15 min (8 minutes for prototypes). Ten microliters of each sample was applied to the columns.
• the analyses were performed on an AKTA explorer 10 system with Unicorn 5.11 as control software.
• SEC was also used for monomer concentration determination. Essentially, the monomer concentration was determined by correlating the monomer area of the sample to the monomer area of the start sample. First, the monomer start concentration was determined (Equation 2).
• HCP levels were measured using commercial anti-CHO HCP antibodies (Cygnus).
• the prototype media were settled and compressed in Tricorn 5/50 columns at 4 ml/min using 0.2 M NaCl + 20% ethanol as mobile phase.
• MAb eluate (-24 mg/mL) was buffer exchanged by using a HiPrep Desalting 26/10 column, giving a concentration of approximately 15 mg/ml with 50 mM acetate buffer pH 5.25.
• the sample was then diluted to a concentration of 3.7-3.8 mg/ml.
• the concentration for the sample solution was determined by measuring UV at 280nm and calculated using Lambert Beer law and the extinction coefficient 1.5 DBC method
• Equilibration of the gels filled in the plate was performed by addition of 200 microliters equilibration buffers from the plate prepared in the Tecan robot, followed by agitation at 1100 rpm for 1 minute, after which the buffer was removed by vacuum suction. The equilibration step was performed three times and after the last equilibration the buffer was removed with centrifugation.
• the ADBA initiator was added to a 30 ml glass vial whereupon 15g of dry sucked gel (pre- washed with 40% APS) was added. Distilled water, the neutral monomer and the ionic monomer solution were then added to the vial. The vial were closed with a plastic top and then put in a heat-shaking equipment where the vials were shaken in r.t. for 5min before raising the temperature to 55C. The polymerisation reactions proceeded for 17h over night and the particles was then put on a glass filter to be washed with 8 x gel volume of distilled water, 8 x gel volume of 99.5% ethanol and then 8 x gel volume of water. The synthesis conditions, the amount of grafted polymer and the ionic capacity are listed in Table 9 and the static binding capacity of polyclonal IgG on the prototypes is listed in Table 10. Table 9. VPA grafting conditions.
• VPA and VPA/HEMA grafted prototypes are remarkably insensitive to the salt
• VPA2 gave a selectivity very similar to VPA1.
• selectivity test a mixture of the test proteins lysozyme, cytochrome C and ribonuclease A was injected and eluted with a salt gradient.
• a monoclonal antibody was also injected separately and eluted under the same conditions.

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