EP1830947A1 - Purification d'immunoglobulines - Google Patents

Purification d'immunoglobulines

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Publication number
EP1830947A1
EP1830947A1 EP05815565A EP05815565A EP1830947A1 EP 1830947 A1 EP1830947 A1 EP 1830947A1 EP 05815565 A EP05815565 A EP 05815565A EP 05815565 A EP05815565 A EP 05815565A EP 1830947 A1 EP1830947 A1 EP 1830947A1
Authority
EP
European Patent Office
Prior art keywords
separation matrix
antibodies
protein
matrix according
chromatography
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP05815565A
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German (de)
English (en)
Other versions
EP1830947A4 (fr
Inventor
Hans Amersham Biosciences BERG
Hans J. Amersham Biosciences AB JOHANSSON
Gunnar Amersham Biosciences MALMQUIST
Per-Mikael Amersham Biosciences AB ÅBERG
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Cytiva Sweden AB
Original Assignee
GE Healthcare Bio Sciences AB
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Publication date
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Priority claimed from SE0403057A external-priority patent/SE0403057D0/sv
Application filed by GE Healthcare Bio Sciences AB filed Critical GE Healthcare Bio Sciences AB
Publication of EP1830947A1 publication Critical patent/EP1830947A1/fr
Publication of EP1830947A4 publication Critical patent/EP1830947A4/fr
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Classifications

    • 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
    • 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
    • B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
    • B01J20/28002—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 physical properties
    • B01J20/28004—Sorbent size or size distribution, e.g. particle size
    • 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
    • B01J20/30—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
    • B01J20/3244—Non-macromolecular compounds
    • 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
    • B01D15/1871—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns using two or more columns placed in series
    • 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
    • B01D15/32—Bonded phase chromatography
    • B01D15/325—Reversed phase
    • B01D15/327—Reversed phase with hydrophobic interaction
    • 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
    • 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
    • G01N30/26—Conditioning of the fluid carrier; Flow patterns
    • G01N30/38—Flow patterns
    • G01N30/46—Flow patterns using more than one column
    • G01N30/461—Flow patterns using more than one column with serial coupling of separation columns

Definitions

  • the present invention relates to the field of antibody preparation, and more specifically to a separation matrix for isolation and/or separation of antibodies.
  • the invention also encompasses a chromatography column that comprises the separation matrix of the invention, a method of isolating antibodies using said separation matrix and a multistep process for large-scale purification of antibodies from a crude feed.
  • the immune system is composed of many interdependent cell types that collectively protect the body from bacterial, parasitic, fungal, viral infections and from the growth of tumour cells.
  • the guards of the immune system are macrophages that continually roam the bloodstream of their host.
  • macro- phages respond by engulfing invaders marked with foreign molecules known as antigens. This event, mediated by helper T cells, sets forth a complicated chain of responses that result in the stimulation of B-cells.
  • B-cells in turn, produce proteins called antibodies, which bind to the foreign invader.
  • the binding event between antibody and antigen marks the foreign invader for destruction via phagocytosis or activation of the complement system.
  • IgA, IgD, IgE, IgG, and IgM differ not only in their physiological roles but also in their structures. From a structural point of view, IgG antibodies are a particular class of immunoglobulins that have been extensively studied, perhaps because of the dominant role they play in a mature immune response.
  • Ion exchange chromatography is a well-known method of protein fractionation fre- quently used for isolation of immunoglobulins. However, since the charged ion exchange ligands will react with all oppositely charged compounds, the selectivity of ion exchange chromatography may be somewhat lower than other chromatographic separations.
  • Hydrophobic interaction chromatography is another method described for isola- tion of immunoglobulins.
  • hydrophobic matrices require an addition of lyotropic salts to the raw material to make the immunoglobulin bind efficiently.
  • the bound antibody is released from the matrix by lowering the concentration of lyotropic salt in a continuous or stepwise gradient. If a highly pure product is the object, it is recommended to combine the hydrophobic chromatography with a further step.
  • a disadvantage of this procedure is the necessity to add lyotropic salt to the raw material as this gives and problem and thereby increased cost to the large-scale user.
  • Affinity chromatography occupies a unique and powerful role in separation technology as the only technique that enables purification of a biomolecule on the basis of biological function or individual chemical structure. High selectivity and high capacity make this technique ideally suited for the isolation of a specific substance from complex biological mixtures.
  • affinity chromatography the molecule to be purified is specifically and re- versibly adsorbed by a ligand comprising a complementary binding substance covalently attached to an insoluble support. The sample is applied under conditions which favour its specific binding to the immobilized ligand. Unbound substances are washed away and the substance of interest can be recovered by changing the experimental conditions to those which favour its desorption.
  • Affinity chromatography has a concentrating effect, which enables convenient processing of large sample volumes. Protein A and Protein G affinity chromatography are popular and widespread methods for isolation and purification of immunoglobulins, particularly for isolation of monoclonal antibodies, mainly due to the ease of use and the high purity obtained.
  • US 6,399,750 discloses an IgG-binding medium, and more specifically a separation medium having a base matrix and matrix-bound groups which exhibit recombinant Protein A (rProtein A) containing a cysteine.
  • the groups are of formula: ⁇ B ⁇ X ⁇ rProtein A, wherein B is a bridge which binds to the base matrix and X includes a heteroatom N or S from rProtein.
  • X is a thioether sulphur originating which also constitutes the C-terminal residue is the cysteine of rProtein A.
  • Millipore Billerca, Mass., USA
  • Prosep-A High Capacity made with natural protein A derived from Staphylococcus aureus
  • PROSEP-rPA High Capacity manufactured using recombinant protein A expressed in Escherichia coli.
  • the PROSEP matrix consists of glass particles permeated by interconnecting pores.
  • McCue et al (Journal of Chromatography A, 989 (2003) 139-153: "Evaluation of protein A chromatography media") studied two protein A media of different pore sizes, both having porous glass backbones. A larger static capacity was found for the smaller pore size material, which is suggested to result from the larger specific surface area and asso- ciated higher ligand concentration. A larger dynamic binding capacity was also found for the smaller pore size material.
  • MabSelectTM is a Protein A chromatography product available from Amersham Biosci- ences (Uppsala, Sweden) especially suitable for capture of monoclonal antibodies from large volumes of feed.
  • the ligands comprise recombinant Protein A coupled to a cross- linked agarose support via a C-terminal cysteine.
  • the median particle diameter of Mab- SelectTM is 85 ⁇ m.
  • WO 2004/074211 (Amersham Biosciences AB) relates to a method for the production of inorganic particles having a hierarchical pore structure. Thus, this method does not produce organic particles, such as carbohydrate particles.
  • US 5,672,276 (BioSepra Inc) relates to modified porous solid supports and processes for the preparation and use of same.
  • passivated porous polymeric supports are disclosed which are characterized by a reversible high sorptive capacity substantially unaccompanied by non-specific adsorption of or interaction with biomolecules.
  • a wide variety of non-passivated porous solid matrices are amenable to passivation as described in US 5,672,276.
  • porous matrices include (i) mineral oxide supports, (ii) "stabilized” mineral oxide supports rendered chemically resistant to leaching by the applica- tion of thin protective coatings of hydrophobic polymers to their surfaces, and (iii) porous matrices comprised solely of organic/polymeric materials, in particular hydrophobic polymers.
  • organic ionic-exchangers which are made from polysaccharide derivatives, e.g., derivatives of agarose, dextran and cellulose, etc., have many disadvantages.
  • polysaccharide-derived ion- exchangers are not very mechanically stable and are not resistant to strong acids.
  • the porous matrices which are passivated according to this reference are stated to be different from polysaccharides, such as carbohydrate materials.
  • FIG. 1 is a diagram wherein the dynamic binding capacity (DBC) is shown as a func- > tion of residence time for a separation matrix according to the invention. For comparison, the dynamic binding capacity of a prior art product is shown as well.
  • DBC dynamic binding capacity
  • One aspect of the present invention is a novel separation matrix suitable for purification of polyclonal or monoclonal antibodies. This can be achieved as defined in the claims.
  • Another aspect of the invention is a separation matrix which allows faster and more eco- nomic purification of antibodies than the prior art. This can be achieved by a novel separation matrix as defined in the appended claims, which enables a substantially increased binding capacity when used in chromatography.
  • a further aspect of the invention is a separation matrix as described above, which is suit- able for large scale operation.
  • a more specific aspect is such a separation matrix, which enables substantially increased binding capacity from a crude feed.
  • An additional aspect of the invention is a chromatography column packed or filled with a separation matrix according to the invention.
  • kits which comprises a chromatography column according to the invention, buffer suitable for antibody purification and written instructions.
  • One more aspect is a method of isolating antibodies from a liquid using a separation matrix according to the invention.
  • the separation matrix may be provided in a separation column according to the invention.
  • the method according to the invention is useful either to obtain a specific antibody species in substantially pure form, or to obtain a liquid from which one or more undesired antibodies have been removed.
  • antibody and “immunoglobulin” are used herein interchangeably.
  • ligand means herein molecules or compounds capable of interaction with target compounds, such as antibodies.
  • spacer arm or “bridge” means herein an element that distances a ligand from the support of a separation matrix.
  • the support of the separation matrix is also known as the "base matrix”, while the term “separation matrix” as used herein is also known as a separation media.
  • antibody-binding protein means herein a protein capable of binding antibodies, regardless of binding mechanism.
  • an "Fc-binding protein” means a protein capable of binding to the crystallisable part (Fc) of an antibody and includes e.g. Protein A and Protein G, or any fragment or genetic derivative or fusion protein thereof that has maintained said binding property.
  • eluent is used in its conventional meaning in this field, i.e. a buffer of suitable pH and/or ionic strength to release one or more compounds from a separation matrix.
  • K av refers to the gel phase distribution coefficient, which is a column independent variable calculated from the elution, or retention volume, V R (also denoted V e ) for a molecule of a given size, the interstitial void volume, V 0 , and the geometric volume of the column (V c ) according to
  • the present invention relates to a separation matrix comprised of porous particles to which antibody-binding protein ligands have been immobilised, wherein the gel phase distribution coefficient of the base matrix expressed as K av for a dextran of size 110 kDa is above 0.65 and the median particle diameter is between 65 and 84 ⁇ m.
  • the present invention relates to a separation matrix comprised of porous particles to which antibody-binding protein ligands have been immobilised, wherein the ligand density is in the range of 5.0-10 and the median particle diameter is between 65 and 84 ⁇ m.
  • the present invention relates to a separation matrix comprised of porous particles to which antibody-binding protein ligands have been immobilised, wherein the ligand density is in the range of 5.0-10 mg/ml; the gel phase distribution coefficient of the base matrix expressed as K av for a dextran of size 110 kDa is above 0.65 and the median particle diameter is between 65 and 84 ⁇ m.
  • the ligands of the present separation matrix comprise antibody- binding protein, such as Protein A, G and/or L.
  • the ligands comprise Fc-binding protein.
  • the Fc-binding protein is Protein A.
  • the ligands comprise recombinant Protein A produced in a non-mammalian source.
  • the phrase "com- prising" Protein A should be interpreted as comprising Protein A or a functional equivalent thereof, which has retained the Protein A IgG-binding properties.
  • the recombinant Protein A ligands may be coupled to the particles via single or multiple attachments, preferably via cysteine.
  • the ligands comprise ⁇ -binding protein, such as Protein L.
  • the ligands of the present separation matrix comprise a monomer, dimer or multimer of Protein A domains.
  • the ligands may comprise one or more of Domain A, B, C, D and E, preferably Domain B and/or Domain C.
  • such a dimer or multimer comprises Protein Z, which is a mutated form of Domain B, see e.g. US 5,143,844 (Abrahamsen et al).
  • the ligands comprises one or more alkali-stable Protein A domains.
  • the ligands comprise mutated protein, wherein one or more of said Protein A domains have been mutated, see e.g. WO 03/080655 (Amersham Biosciences), which is hereby incorporated herein via reference.
  • the ligands comprise one or more of Domain C from Protein A.
  • the separation matrix comprising alkali-stable monomelic or multimeric ligands are easily prepared by the skilled person in this field e.g. as described in WO 03/080655 (Amersham Biosciences).
  • the present ligands are antibody-binding peptides.
  • the separation matrix according to this embodiment is comprised of porous particles to which antibody-binding protein ligands have been immobilised, wherein the gel phase distribution coefficient of the base matrix expressed as K av for a dextran of size 110 kDa is above 0.65 and the median particle diameter is between 65 and 84 ⁇ m.
  • the present base matrix may comprise porous particles made from any material within the specified values of the gel phase distribution coefficient, which provides the substantial improvement of dynamic binding capacity (DBC) described herein.
  • the particles i.e. the support of the separa- tion matrix
  • the particles are made from a cross-linked carbohydrate material, such as agarose, agar, cellulose, dextran, chitosan, konjac, carrageenan, gellan, alginate etc, which are easily prepared according to standard methods, such as inverse suspension gelation (S Hjerten: Biochim Biophys Acta 79(2), 393-398 (1964).
  • the carbohydrate material is highly cross-linked agarose, such as SepharoseTM (Amersham Biosciences, Upp- sala, Sweden).
  • the support is a porous cross-linked agarose material that exhibits advantageous mechanical properties and consequently allows high flows without developing too high a pressure.
  • the agarose polymers have been allylated before gelation.
  • Such agarose particles may be prepared according to US 6,602,990 (Amersham Biosciences, Uppsala, Sweden); according to SE 0402322 (PCS/SE2005/001408) (Amersham Biosciences, Uppsala, Sweden); or SE 0501610 (Amersham Biosciences AB, Uppsala, Sweden).
  • the particles are prepared as described in US 6,602,990, which is hereby incorporated herein via reference.
  • a bifunctional cross-linking agent having one active site and one inactive site, is introduced into the agarose solution before gel formation, and allowed to react with the hydroxyl groups of the agarose whereby it is chemically bound to the agarose.
  • a solution or dispersion of the polysaccharide is formed.
  • a gel is then formed of the polysaccharide by emulsifying the water solution in an organic solvent, after which the inactive site of the cross-linking agent is activated and reacted with hydroxyl groups of the polysaccharide.
  • further cross-linking can be carried out by conventional methods.
  • the particles of the present separation matrix are polydisperse, and may be defined by a particle diameter within a range of 30-140 ⁇ m, preferably 43-128 ⁇ m and more prefera- bly 70-84 ⁇ m.
  • Another commonly used way of defining particle size within this field is the median particle diameter of the cumulative volume distribution (dso v ), which for the present separation matrix is in the range of 65-84 ⁇ m, such as about 75 ⁇ m.
  • the present particles are monodisperse and defined by a particle diameter of 74-76 ⁇ m, such as 75 ⁇ m.
  • the particle size is easily controlled during the process by withdrawing a sample of the emulsion, estimating the particle diameter under microscope and subsequently adjusting the stirring to decrease the particle size.
  • the ligands may be immobilised to the particles according to the invention using any well known method, such as epoxi coupling.
  • the ligand density is in the range of 5-10 mg/ml.
  • the density i.e. concentration of immobilised ligands is easily controlled by the skilled person in this field, see e.g. Hermanson, Greg T., MaI- Ha, A. Krishna, Smith, Paul K. Immobilized Affinity Ligand Techniques, p. 118. Academic Press. ISBN 0-12-342330-9. Specific methods of immobilisation of Protein A, such as recombinant Protein A, are also described in the literature.
  • the gel phase distribution coefficient of the particles expressed as K av for a dextran of size 110 kDa is above 0.60, and preferably above 0.65.
  • the gel phase distribution coefficient of the particles expressed as K av for a dextran of size 110 kDa is in the range of 0.60-0.90, preferably 0.65-0.85 and more preferably in the range of 0.65-0.75.
  • the gel phase distribution coefficient of such a support is easily controlled by the skilled person in this field by adjustment of the solids content.
  • the dynamic binding capacity of a separation matrix is a good indication of the suitability of a separation matrix for large scale operation, where process economy is greatly improved by such an increase.
  • the present invention is a separation matrix that provides a dynamic binding capacity above 40 mg antibody/ml separation matrix at 2.4 minutes residence time.
  • the separation matrix provides a dynamic binding capacity above 35 mg/ml, e.g. in the range of 35-50, such as about 39-40 mg/ml separation matrix.
  • the invention presents an increase of the gel phase distribution coefficient and decrease of the particle size.
  • the increase of the gel phase distribution coefficient i.e. the increase of the available particle volume
  • McCue et al Journal of Chromatography A, 989 (2003) 139-153: "Evaluation of protein A chromatography media”
  • decrease of the pore size increased dynamic binding capacity in the reported study.
  • the substantial increase in dynamic binding capacity of the present separation matrix is contradictory to the teachings of the prior art, and was consequently quite unexpected.
  • the most preferred format of the present separation matrix is particles, other formats are also encompassed by the invention such as a monolith; a filter or membrane; a chip, a surface, capillaries or the like.
  • the present invention relates to a chromatography column comprising a separation matrix as defined above.
  • the column may have been packed with the matrix according to conventional packing methods, or filled with matrix for operating in expanded bed mode.
  • the particles are preferable provided with a high density filler, as is well known in this field.
  • the column is made from any conventional material, such as a biocompatible plastic, e.g. polypropylene, stainless steel or glass.
  • the column may be of a size suitable for laboratory scale or large-scale purification and/or detection of antibodies.
  • the column according to the invention is provided with luer adaptors, tubing connectors, and domed nuts.
  • the present invention also encompasses a kit for purification of antibodies, which kit comprises, in separate compartments, a chromatography column packed with a separation matrix as defined above, one or more buffers and written instructions for large-scale capture of antibodies from feed.
  • the present kit also comprises luer adaptors, tubing connectors, and domed nuts.
  • the present invention relates to a method of purification of antibodies by affinity chromatography, which process comprises contacting a process feed with a separation matrix according to the invention to adsorb antibodies, an optional wash step of antibodies adsorbed to the separation matrix, adding an eluent that releases the anti- bodies from the separation matrix and recovery of antibodies from the eluate.
  • dynamic binding capacities above 35 mg antibody/ml separation matrix such as above 40 mg antibody/ml separation matrix, can be obtained.
  • the dynamic binding capacity when carrying out the present method may be in the range of 35-50 mg antibody/ml separation matrix, such as 39-40 mg antibody/ml separation matrix.
  • the present method may be used to isolate antibodies from culture liquids and super- natants.
  • the process feed comprises fermentation broth.
  • the antibodies are purified from host cell proteins, DNA, viruses, endotoxins, nutrients, components of a cell culture medium, such as antifoam agents and antibiotics, and product-related impurities, such as misfolded species and aggregates.
  • the feed has been subjected to mechanical filtration before its contact with the separation matrix, and consequently the mobile phase is a clarified cell culture broth. Suitable conditions for adsorption are well known to those of skill in the art.
  • the present method is useful to purify any kind of monoclonal or polyclonal antibodies, such as antibodies originating from mammalian hosts, such as mice, rodents, primates and humans, or antibodies originating from cultured cells such as hybridomas.
  • the antibodies recovered are human or humanised antibodies.
  • the antibodies are selected from antibodies originating from the group that consists of mouse, rat, rabbit, hamster, guinea pig, cow, sheep, goat, pig, and chicken.
  • the antibodies may be of any class, i.e. selected from the group that consists of IgA,
  • the antibodies recovered are immunoglobulin G (IgG).
  • the IgGs are selected from the group that consists of human IgGl, human IgG2, human IgG4, human IgGA, human IgGD, human IgGE, human IgGM, mouse IgGl, mouse IgG2a, mouse IgG2b, mouse IgG3, rabbit Ig, hamster Ig, guinea pig Ig, bovine Ig, and pig Ig, preferably human IgGl , human IgG2, human IgG4, mouse IgG2a, rabbit Ig, and guinea pig Ig.
  • the antibodies are monoclonal antibodies.
  • monoclonal antibody technology involves fusion of immortal cells, having the ability to replicate continuously, with mammalian cells to produce an antibody. The resulting cell fusion or 'hybridoma' will subsequently produce monoclonal antibodies in cell culture.
  • the term "antibodies” also includes antibody fragments and any fusion protein that comprises an antibody or an antibody fragment.
  • the present method is useful to isolate any immunoglobulin-like molecule, which presents the Protein A and/or Protein G and/or Protein L binding properties of an immunoglobulin.
  • the present method is operable as a conventional liquid chromatography process, wherein the mobile phases are passed through the separation matrix by impact of gravity and/or pumping.
  • the separation matrix is present in a chromatography column through which said process feed and eluent are passed.
  • this aspect of the invention relates to a method of purification of a liquid from one or more antibodies by affinity chromatography, which process comprises contacting a liquid with a separation matrix according to the invention to adsorb antibodies and recovering the purified liquid.
  • This embodiment is e.g. useful in the case where the liquid is blood or blood plasma, from which it is desired to remove one or more antibodies to obtain a safe blood product.
  • the antibodies are released from the separation matrix by adding an eluent to prepare the separation matrix for re-use.
  • the adsorption and elution of antibodies according to the present invention are easily released by standard conditions, such as those recommended for similar commercial products, see e.g. MabSelectTM application notes (Amersham Biosciences, Uppsala, Sweden).
  • the elution is e.g. gradient elution performed by adding an eluent of changing pH to the separation matrix.
  • the present invention relates to a multi-step process for the purification of antibodies, which process comprises a capture step as described above followed by one or more subsequent steps for intermediate purification and/or polishing of the antibodies.
  • the capture step is followed by hydrophobic interaction and/or ion exchange chromatography.
  • the capture step is followed by multimodal anion or cation exchange chromatography.
  • the capture step is carried out on MabSelectTM Xtra (Amersham Biosciences, Uppsala, Sweden). Detailed description of the drawing
  • FIG. 1 is a diagram wherein the dynamic binding capacity (DBC) (mg antibody/ml separation matrix) is shown on the Y axis, as a function of residence time (minutes) on the X axis, for a separation matrix according to the invention (upper line) and for a prior art product (lower dotted line). It appears clearly how the separation matrix according to the invention provides a substantially higher, in fact, about 30% higher, dynamic binding capacity.
  • DBC dynamic binding capacity
  • Example 1 Separation matrices
  • Agarose particles were prepared by suspension gelation as disclosed in US 6,602,990 (Amersham Biosciences). More specifically, particles having a K av of 0.69 were produced by the appropriate adjustment of solids content, according to well known principles in this field. Further, by adjusting the speed and duration of stirring, the median par- tide diameter was controlled to 80 ⁇ m.
  • the particles described above were epoxi-activated and recombinant Protein A (rProtein A) was coupled to the particles via C-terminal, following well known procedures as described e.g. in Hermanson, Greg T., Mallia, A. Krishna, Smith, Paul K. Immobilized Af- fmity Ligand Techniques, p. 118. Academic Press. ISBN 0-12-342330-9.
  • the rProtein A ligands were coupled to a ligand density of 7.3 mg/ml.
  • the comparative separation matrix was MabSelectTM, obtained from Amersham Biosciences, which according to the product note presents a median particle size of the cumula- tive volume distribution of 85 ⁇ m.
  • Example 2 Dynamic binding capacity
  • DRC dynamic binding capacity
  • Packing solution 2 20% (v/v) ethanol.
  • Adsorption buffer 0.020 M NaH 2 PO 4 containing 0.15 M NaCl adjusted to pH 7.4
  • Desorption buffer 0.1 M sodium citrate adjusted to pH 3.0 ⁇ 0.05 with hydrochloric acid.
  • Packing Mount the packing reservoir to the column with a connecting piece. Measure and mark desired bed height. Transfer quantitatively the gel and fill up with packing solution 1. Pack with 25 ml/minute with packing solution 2 for 5 minutes downward flow at a maximum pressure of 0.3 MPa. Mark the bed height during flow. Remove the packing reservoir, mount the top adaptor to the gel, and ran a flow of 10 ml/minute for 5 minutes more. Adjust or repack if necessary to a bed height of 10.0 ⁇ 0.3 cm.
  • the packing of the columns are checked by injecting a solution of acetone through the columns and calculating the symmetry of the resulting peak.
  • the peak asymmetry factor is then evaluated using the AKTA system, or calculated according to the following description:.
  • the peak asymmetry factor is calculated as the absolute value of B/A, where A and B are calculated as the retention volume at maximum peak height minus the retention volume at 10% peak height.
  • the column is approved if the symmetry is in the interval of 0.80 - 1.60.
  • the analysis should be performed on two columns at controlled room temperature, 23 ⁇ 1°C.
  • the breakthrough capacity is determined at a mobile phase velocity of 250 cm/hour.
  • Check the flow rate according to section 6.3. Run adsorption buffer through the bypass position until a stable baseline is reached. Autozero, and apply 35 ml of IgG solution also through bypass to obtain a stable 100% signal. It is important that the flow is the same as during the analysis. After a stable baseline with adsorption buffer is reached again at bypass position, the column is equilibrated with 5 column volumes of adsorption buffer. Autozero, and apply 100 column volumes of IgG solution to the column at a mobile phase velocity of 250 cm/h (8.38 ml/minute).
  • chromatographic system is thoroughly calibrated with respect to volume delivery. Calibrate regularly according to the manual for the instrument, and check the flow rate for the pump used for sample application before every analysis.
  • the dynamic binding capacity is evaluated at 10% breakthrough, q lo% .
  • UV absorbance is detected at 280nm.
  • the 100% UV signal (A 1O o % ) is determined and noted, as well as the UV signal (A SUb ) corresponding to the subclass of IgG that does not bind (determined at 60 ml from sample application start).
  • the column volume (Vc) and the concentration (C 0 ) of the sample feed (two decimals) are also used for the calculations.
  • Dynamic binding capacity is calculated as the amount of IgG loaded onto the column until the concentration of IgG in the column effluent is 10% of the IgG concentration in the feed. The loaded amount is corrected for the amount of IgG breaking through the column before the 10% breakthrough occurs.
  • V 0 is the column volume
  • V app is the volume applied until 10% breakthrough
  • V sys is the system dead volume (column dead volume not in- eluded)
  • the integral gives the total amount of IgG present in the effluent from the column up to the moment of 10% breakthrough
  • A(V) is the absorbance value at a given applied volume
  • a SUb is the absorbance contribution from the non-binding IgG subclass.
  • the difference in the dynamic capacities between the single columns should not exceed 1.2 mg/ml packed gel.
  • the gel phase distribution coefficient of a particle according to example 1 is determined by gel filtration. Two dextrans with different sizes are run through a packed HRl 6/30 column. Retention volumes for each dextran are detected, and used to calculate K av , a value describing the fraction of the particle volume available for a certain molecular weight. From the K av -values the K av -value for Mp 110000 is reported. EQUIPMENT Packing:
  • Mobile phase for packing is distilled water and for the selectivity test 0.20 M NaCl in distilled water.
  • the column packing is tested with an injection of 2% acetone in a distilled water mobile phase.
  • the dextrans used in the selectivity test are:
  • SAFETY DIRECTIONS No extra safety precautions need to be taken.
  • One analysis consists of packing of one column that is tested twice i.e. each dextran is injected twice.
  • W h peak- width at half height
  • the selectivity method can be run including the following steps: 1. Column equilibration, at least 1.5 CV 0.20 M NaCl.
  • Step 2 and 3 are then repeated for each dextran or dextran mix*.
  • the dextrans can be mixed according to the following protocol, but can also be injected one at a time.
  • V R retention volume for the eluted dextran adjusted for the extra column volume, ml
  • V 0 interstitial volume (the retention volume for native dextran) adjusted for the extra column volume (ml)
  • V c geometric volume of the column (bed height, cm • surface area of column, cm 2 )
  • K av - values are then plotted against log Mp of the dextrans. Two values from each dextran results in four values plotted in one diagram. A linear interpolation between the two dextrans gives the K av - value corresponding to the molecular mass of 110000 (Mp-value) which is reported.

Abstract

L'invention concerne une matrice de séparation comprenant des particules poreuses sur lesquelles ont été immobilisées des ligands de protéine de liaison aux anticorps, sachant que la densité de ligand se situe dans la gamme 5-10 mg/ml ; le coefficient de distribution de phase de gel des particules exprimé par Kav pour un dextrane ayant une taille de 110 kDa est supérieur à 0,65, et le diamètre de particule moyen se situe dans la gamme 65 - 84 µm. De préférence, le matériau en hydrate de carbone est de l'agarose hautement réticulé.
EP05815565A 2004-12-14 2005-12-12 Purification d'immunoglobulines Withdrawn EP1830947A4 (fr)

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Application Number Priority Date Filing Date Title
SE0403057A SE0403057D0 (sv) 2004-12-14 2004-12-14 Purification of immunoglobulins
US63831604P 2004-12-22 2004-12-22
PCT/SE2005/001900 WO2006065208A1 (fr) 2004-12-14 2005-12-12 Purification d'immunoglobulines

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EP1830947A4 EP1830947A4 (fr) 2012-04-18

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CA2586803A1 (fr) 2006-06-22
EP1830947A4 (fr) 2012-04-18
WO2006065208A1 (fr) 2006-06-22
JP2008523140A (ja) 2008-07-03
JP5787461B2 (ja) 2015-09-30
CA2586803C (fr) 2012-12-11
AU2005317279B2 (en) 2011-02-24
AU2005317279A1 (en) 2006-06-22

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