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WO1997031947A1 - Procede de production d'albumine a haut degre de purete - Google Patents

Procede de production d'albumine a haut degre de purete Download PDF

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Publication number
WO1997031947A1
WO1997031947A1 PCT/GB1996/000448 GB9600448W WO9731947A1 WO 1997031947 A1 WO1997031947 A1 WO 1997031947A1 GB 9600448 W GB9600448 W GB 9600448W WO 9731947 A1 WO9731947 A1 WO 9731947A1
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WO
WIPO (PCT)
Prior art keywords
albumin
solution
matrix
process according
affinity
Prior art date
Application number
PCT/GB1996/000448
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English (en)
Inventor
Andrew Robert Goodey
Darrell Sleep
Hendrik Van Urk
Stephen Berezenko
John Rodney Woodrow
Richard Alan Johnson
Patricia Carol Wood
Stephen James Burton
Alan Victor Quirk
Original Assignee
Delta Biotechnology Limited
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Application filed by Delta Biotechnology Limited filed Critical Delta Biotechnology Limited
Priority to AU48379/96A priority Critical patent/AU4837996A/en
Priority to PCT/GB1996/000448 priority patent/WO1997031947A1/fr
Publication of WO1997031947A1 publication Critical patent/WO1997031947A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K14/00—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof
    • C07K14/435—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof from animals; from humans
    • C07K14/76—Albumins
    • C07K14/765—Serum albumin, e.g. HSA

Definitions

  • the present invention relates to purifying the protein human serum albumin (HSA) extracted from serum or recombinant human albumin (rHA) produced by transforming a microorganism with a nucleotide coding sequence encoding the amino acid sequence of human serum albumin.
  • HSA human serum albumin
  • rHA recombinant human albumin
  • albumin refers generically to HSA and/or rHA.
  • Albumin is used to treat patients with severe burns, shock or blood loss. It is also used to supplement media used for growing higher eukaryotic cells and as an excipient in the formulation of therapeutic proteins. At present, the demand for the product is satisfied by albumin extracted from human blood. Examples of extraction and separation techniques include those disclosed in: JP 03/258 728 on the use of a cation exchanger; EP 428 758 on the use of anion exchange followed by cation exchange; and EP 452 753 on the use of heating, adding salt and diafiltering.
  • rHA in microorganisms has been disclosed in EP 330 451 and EP 361 991.
  • Purification techniques for rHA have been disclosed in: WO 92/04367. removal of matrix-derived dye; EP 464 590, removal of yeast-derived colorants: and EP 319 067, alkaline precipitation and subsequent application of the rHA to a lipophilic phase having specific affinity for albumin.
  • the present invention provides highly purified albumin.
  • One aspect of the present invention provides a process for purifying albumin, the process comprising the steps of applying a relatively impure albumin solution to a chromatographic material for which the albumin has no specific affinity such that albumin binds to the material, and eluting the bound albumin from the material by applying a solution of a compound having a specific affinity for albumin.
  • the chromatographic material is a cation exchanger, such as SP-Sepharose FF, SP- Spherosil etc, as listed below in Example 2.
  • the compound with specific affinity for albumin may be octanoate (eg sodium octanoate), other long chain (C 6 to CA fatty acids, salicylate, octylsuccinate, N-acetyltryptophan or a mixture of two or more of these.
  • octanoate eg sodium octanoate
  • other long chain C 6 to CA fatty acids
  • salicylate octylsuccinate
  • N-acetyltryptophan a mixture of two or more of these.
  • a second aspect of the invention provides a process for purifying albumin, the process comprising the steps of subjecting an albumin solution to cation exchange chromatography in which the albumin is bound to a cation exchange material and then anion exchange chromatography in which the albumin is bound to an anion exchange material.
  • the albumin which is eluted from the cation exchange material may be subsequently treated by one or more of affinity chromatography, ultrafiltration and gel permeation before being subjected to the said anion exchange chromatography.
  • the process comprises the steps of:
  • albumin which is eluted from the cation exchange material may be applied to the said anion exchange material without any intervening treatment (other than dilution).
  • a second preferred embodiment provides a process for purifying albumin, comprising the steps of:
  • the albumin solution is conditioned by adding octanoate and/or other albumin stabiliser (eg sodium acetyltryptophanate) thereto to a final concentration of from about 1-10 mM and adjusting the pH to about 4.0-5.0.
  • albumin stabiliser eg sodium acetyltryptophanate
  • the albumin retained in the cation exchange step is washed with a high salt solution (eg 0.5-2.0 M NaCl buffered at pH 4.0 with 10-100 mM, preferably 20-40 mM, for example 27 mM sodium acetate) before being eluted.
  • a high salt solution eg 0.5-2.0 M NaCl buffered at pH 4.0 with 10-100 mM, preferably 20-40 mM, for example 27 mM sodium acetate
  • the albumin is eluted in the cation exchange step using a buffer containing a compound having a specific affinity for albumin, especially an acid or salt thereof, for example octanoate or any other long chain ( -Cr>) fatty acid, salicylate, octylsuccinate or N-acetyltryptophan.
  • the albumin is eluted from the anion exchanger with a buffer containing a high level (eg at least 50 mM, preferably 50-200 M, for example 80-150 mM) of a boric acid salt, for example sodium or potassium tetraborat ⁇ .
  • the albumin purified in accordance with the invention may then, with or without intervening process steps, be subjected to chromatography on a resin containing an immobilised compound which will selectively bind glycoconjugates and saccharides, such as aminophenylboronic acid (PBA).
  • PBA aminophenylboronic acid
  • the affinity chromatography preferably uses a resin comprising an immobilised albumin-specific dye, such as a Cibacron Blue type of dye, preferably immobilised on the resin via a spacer such as 1 ,4-diaminobutane or another spacer of C,. g , preferably C,. 6 , eg C I 5 and most preferably C 4 length, preferably having ⁇ . ⁇ -diamino substitution.
  • a spacer such as 1 ,4-diaminobutane or another spacer of C,. g , preferably C,. 6 , eg C I 5 and most preferably C 4 length, preferably having ⁇ . ⁇ -diamino substitution.
  • the purified albumin solution prepared by the process of the invention may be further processed according to its intended utility. For example, it may be ultrafiltered through an ultrafiltration membrane to obtain an ultrafiltration retentate having an albumin concentration of at least about 80g albumin per litre, with the ultrafiltration retentate being diafiltered against at least 5 retentate equivalents of water.
  • ammonium ions are relatively tightly bound to the albumin. It is preferable for such ammonium ions to be removed from the albumin and we have found that this can be achieved by use of a counter-ion. The desirability of exposing the albumin to a counter-ion would not have occurred to those in this art since prior processes have not involved ammonium ions and there was no reason to suppose that ammonium ions would be bound by the albumin.
  • a further aspect of the invention provides a method of purifying an albumin solution comprising exposing the solution to a solution of a counter-ion such that ammonium ions are displaced from the albumin and can be removed from the solution.
  • the counter-ion (preferably a metal ion such as sodium ions) can be added to the albumin solution and the ammonium ions removed by dialysis, or the ammonium ion can be diafiltered away across a semi-permeable membrane separating the albumin from the solution of the counter-ion, or they can be removed by gel permeation chromatography. Diafiltration against at least five retentate volumes of 50 mM sodium chloride is generally suitable.
  • the albumin obtained has been found to have extremely low levels of, or to be essentially free of, colorants, lactate, citrate, metals, human proteins such as immunoglobulins, pre-kallikrein activator, transferrin, ⁇ ,-acid glycoprotein, haemoglobin and blood clotting factors, prokaryotic proteins, fragments of albumin, albumin aggregates or polymers, endotoxin, bilirubin, haem, yeast proteins and viruses.
  • colorant as used herein means any compound which colours albumin.
  • a pigment is a colorant which arises from the organism, especially yeast, which is used to prepare recombinant albumin
  • a dye is a colorant which arises from chromatographic steps to purify the albumin.
  • At least 99%, preferably at least 99.9%, by weight of the protein in the albumin preparations purified by the process of the invention is albumin.
  • Such highly pure albumin is less likely to cause adverse side effects.
  • the albumin produced by the process of the invention has been found to be at least 99.5% monomeric, preferably substantially 100% monomeric by reducing SDS PAGE, and is characterised by one or more of the following characteristics. It has an aluminium ion content of less than 150 ng, preferably less than 100 ng; an iron ion content of less than 3,000 ng, preferably less than 1,000 ng; a copper ion level of less than 10,000 ng, preferably less than 5,000 ng; a magnesium ion level of less than 3,000 ng, preferably less than 1,500 ng; a zinc ion level of less than 5,000 ng, preferably less than 3,000 ng, a manganese ion level of less than 50 ng, all based on one gram of albumin; a glycation level of less than 0.6, preferably less than 0.15 (more preferably less than 0.05), moles hexose/mole protein; a level of low molecular weight contaminants of below 20 V.sec,
  • the starting material may be an albumin-containing fermentation medium, or the impure albumin solution may be a solution obtained from serum by any of the plethora of extraction and purification techniques developed over the last 50 years, for example those disclosed in Stoltz et al (1991) Pharmaceut. Tech. Int. June 1991 , 60-65 and More & Harvey (1991) in "Blood Separation and Plasma Fraaionation” Ed. Harris, Wiley-Liss. 261-306.
  • the process does not normally comprise a heat treatment step as part of the purification process (in contrast to EP 428 758 and EP 658 569). Similarly, if it is prepared from microorganisms (rather than from humans) it does not normally require a final pasteurisation step (typically 60° C for one hour).
  • the final product may be formulated to give it added stability.
  • the highly pure albumin product of the invention contains at least 100 g, more preferably 1 kg or 10 kg of albumin, which may be split between a plurality of vials.
  • the process of the present invention can be utilised to obtain more purified albumin from an impure albumin solution from a number of sources, such as serum, it is particularly applicable to purifying recombinant human albumin (rHA).
  • the albumin produced in accordance with the invention may be any mammalian albumin, such as rat, bovine or ovine albumin, but is preferably human albumin. DNA encoding albumin may be expressed in a suitable host to produce albumin.
  • DNA may be used in accordance with known techniques to construct an expression vector, which is then used to transform an appropriate host cell for the expression and production of albumin.
  • Such techniques include those disclosed in EP-A-73 646, EP-A-88 632, EP-A-201 239 and EP-A-387 319.
  • yeasts for example Saccharomyces cerevisiae, Pichia pastoris and Kluyveromyces laais
  • filamentous fungi for example Aspergillus
  • plant cells animal cells and insect cells.
  • insect cells for example E. coli and Bacillus subtilis
  • yeasts for example Saccharomyces cerevisiae, Pichia pastoris and Kluyveromyces laais
  • filamentous fungi for example Aspergillus
  • plant cells animal cells and insect cells.
  • insect cells for example E. coli and Bacillus subtilis
  • yeast Saccharomyces cerevisiae for example Saccharomyces cerevisiae, Pichia pastoris and Kluyveromyces laais
  • filamentous fungi for example Aspergillus
  • plant cells animal cells and insect cells.
  • insect cells for example E. coli and Bacillus subtilis
  • yeast Saccharomyces cerevisiae for example Saccharomyces cerevisiae, Pichia pastoris
  • Exemplary genera of yeast contemplated to be useful in the practice of the present invention are Pichia (Hansenula), Saccharomyces, Kluyveromyces, Candida, Torulopsis, Torulaspora, Schizosaccharomyces, Citeromyces, Pachysolen, Debaromyces, Metschunikowia, Rhodosporidium, Leucosporidium, Botryoascus, Sporidiobolus, Endomycopsis, and the like.
  • Preferred genera are those selected from the group consisting of Pichia (Hansenula), Saccharomyces, Kluyveromyces, Yarrowia and Hansenula. Examples of Saccharomyces spp. are S.
  • Y. lipolytica is an example of a suitable Yarrowia species.
  • a yeast strain which is deficient in one or more proteases.
  • Such strains include the well-known pep4 ⁇ 3 mutants and strains with mutations in the PRA1 and/or PRB1 genes, as in Woolford et al (1993) J. Biol. Chem. 268, 8990- 8998, Cabez ⁇ n et al (1984) P.N.A.S. 81, 6594-6598. EP-A-327 797 and Jones et al (1982) Genetics 102, 665-677.
  • the proteases in the fermentation medium may be inactivated by heating. The existence of proteases reduces the yield of the albumin during the overall process.
  • the yeast has a low (or zero) level of the Yap3p protease and/or of the hspl50 heat shock protein, for example as a result of having the respective genes disrupted, as is taught in our patent applications published as WO 95/23857 and WO 95/33833, respectively.
  • Yap3p can cause the formation of the 45 kD albumin fragment referred to below, and hspl50 co-purifies with albumin in some separation steps.
  • Yeast may be transformed with an expression plasmid based on the Saccharomyces cerevisiae 2 ⁇ m plasmid.
  • the plasmid contains bacterial replication and selection sequences, which may be excised, following transformation, by an internal recombination event in accordance with the teaching of
  • the plasmid may also contain an expression cassette comprising: a yeast promoter (such as the Saccharomyces cerevisiae PRB1 promoter), as taught in EP 431 880; a sequence encoding a secretion leader, for example one which comprises most of the natural HSA secretion leader, plus a small portion of the 5. cerevisiae ⁇ -mating factor secretion leader, as taught in WO 90/01063; the HSA coding sequence, obtainable by known methods for isolating cDNA corresponding to human genes, and also disclosed in. for example, EP 73 646 and EP 286 424; and a transcription terminator, for example the terminator from Saccharomyces ADHI, as taught in EP 60 057.
  • a yeast promoter such as the Saccharomyces cerevisiae PRB1 promoter
  • a sequence encoding a secretion leader for example one which comprises most of the natural HSA secretion leader, plus a small portion of the 5. cerevisi
  • Figure 1 shows schematically a fermenter used to produce rHA
  • Figure 2 is a UV trace from a CI8 PTH Reverse Phase HPLC column (Applied Biosystems Inc), showing the low level of low molecular weight contaminants in the albumin of the invention
  • Figure 3 is similar to Figure 2 but shows low molecular weight contaminants in prior art albumin
  • Figure 4 is a gas chromatogram showing the fatty acid content of commercially available albumin
  • FIG 5 corresponds to Figure 4 but shows albumin of the invention.
  • Figures 6a and 6b show electrospray mass spectrometry for albumin of the invention and prior art albumin, respectively.
  • Plasmid pAYE316 was introduced into a (MATa, leu2, pep4-3, [cir * ]) Saccharomyces cerevisiae strain by the method described by Hinnen et al, (1978) P.N. A.S. 75, 1929. Transformants were selected on a minimal medium lacking leucine (Yeast nitrogen base, Difco).
  • a stock master cell culture in defined liquid medium (Buffered Minimal Medium (BMM) salts medium: Yeast Nitrogen Base [without amino acids and (NH 4 ) 2 SO 4 , Difco], 1.7g/L; citric acid monohydrate 6.09g/L; anhydrous Na ⁇ HPO,, 20.16g/L, pH 6.5+0.2, sucrose is added to 20g L) is used to prepare running stocks (manufacturer's working cell bank) of process yeast suitable for the preparation of shake flask cultures by freezing aliquots of the culture in the presence of 20% (w/v) trehalose.
  • BMM Bactas medium
  • This section relates to the production of rHA from stock culture through to the final fermentation and is a general definition of an rHA fermentation process which is not limited to the specific detail of particular equipment or scale.
  • the yeast [cir 0 , pAYE316] is grown as an axenic culture physiologically suited for inoculation of the seed vessel. If timing of the seed vessel is to be reproducible, it is necessary to define the phase of growth (primary carbohydrate excess) and inoculum biomass (12 ⁇ 2mg/L which requires a 100ml inoculum per 10 litres of medium).
  • One stock vial is inoculated into a shake flask containing lOOmL of BMM +2%(w/v) sucrose and the flask is incubated at 30°C on an orbital shaker (200rpm revolutions per minute) until a cell dry weight (cdw) of 0.6-1.2g/L (assessed by optical density at 600nm) is obtained.
  • This culture is then used to inoculate a seed fermentation vessel to a level of 12+2mg/L.
  • the inoculum for the main production fermenter is provided by growing the production organism, preferably S. cerevisiae [cir 0 , pAYE316], in a seed fermenter (in this example, 20 L working volume) to a high cell dry weight (cdw) of approx. lOOgL '.
  • a fed-batch regime is followed so as to minimise the accumulation of ethanol and acetate and thus to maximise cell yield.
  • the whole of each fermentation is monitored and controlled via a computer control system, such as the Multi-Fermenter Computer System (MFCS) software available from B. Braun (Germany), The software supplied by B. Braun is a Supervisory Control and Data Acquisition Package; similar packages are available from other companies.
  • MFCS Multi-Fermenter Computer System
  • the feed control algorithm is intended to control the addition of sucrose so that maximum biomass is achieved by avoiding the Crabtree effect, thereby minimising the production of ethanol and/or acetate.
  • the fermentation vessel is subjected to a hot NaOH wash and pyrogen-free water (PFW) rinse.
  • PFW pyrogen-free water
  • the heat sterilised vessel will contain approximately 10 L of sterile MWIO medium (Table 1) batch salts plus trace elements.
  • the medium for rHA production can be ultrafiltered (10,000 Mol. Wt. cut-off) to remove endotoxins.
  • the trace elements are added to demineralised water, acidified with 35ml/L of 98 % H 2 SO 4 .
  • Sucrose/L is added to the batch medium at the 20L seed fermenter stage.
  • Any convenient method of sterilisation may be used, as may any depyrogenation method, for example ultrafiltration.
  • the vitamins are always filter sterilised.
  • the operating temperature of 30°C is set, as well as the minimum stirrer speed, typically 400-500 rpm.
  • the initial pH is adjusted with ammonia solution (specific gravity 0.901) using a pH controller set at 5.7 ⁇ 0.2. 2M H 2 SO 4 is also used as a pH corrective agent.
  • Sucrose to 20gL " ⁇ MW10 batch vitamins, and Breox FMT30 antifoam to 0.04gL ' are added to the vessel.
  • Sterile filtered air is introduced into the vessel at 0.5 v/v/m (ie 0.5 litre non- compressed air per litre of medium per minute), the medium is inoculated to 12 ⁇ 2mg cell dry weight L ' from an axenic shake flask culture and the MFCS computer system is initiated. Following completion of the batch phase of growth (signalled by a dissolved oxygen tension increase of > 15% in 30 min), addition of the feed medium is initiated, under control of the MFCS system.
  • the control strategy is effectively the same as described below for the production fermentation.
  • the air flow is increased in two steps in order to maintain a flow of approximately I v/v/m.
  • the dissolved oxygen tension (DOT) is controlled at 20% air saturation by changing the stirrer speed. Once the stirrer speed cannot be increased further and the air flow rate has reached its maximum value, the feed control algorithm controls the feed rate to minimise the formation of fermentation products.
  • the culture is transferred to a production vessel.
  • An axenic culture of the yeast [cir" , pAYE316] is produced by fed-batch fermentation to a high cdw ( > 80gL ') for the production of extracellular rHA.
  • the production fermenter in this example a fermenter with a working volume of 8.000L, is inoculated with the culture grown in the seed fermenter, the cell dry weight of which is preferably >80g.L " '.
  • the initial cell dry weight concentration in the production fermenter on transfer of the seed fermenter culture is preferably 0.25-1.00 g.L '1 . Although it is preferred to initiate feeding within one hour, it can be delayed if necessary.
  • the feed regime is intended to minimise the accumulation of ethanol and acetate, so as to maximise the cell and product yield.
  • the fermentation is carried out in a fermenter such as that shown in Fig. 1. designed to give optimum gas dissolution and bulk mixing.
  • the vessel which is subjected to a hot NaOH wash and PFW rinse, will contain approximately 4000 L of sterile MW10 (Table 1). batch salts and trace elements.
  • This medium may be sterilised independently of the vessel either by heat or filter sterilisation. It has been found in accordance with the present invention that it is advantageous for the fermentation medium, such as MW10. to be free of ethylene diamine tetraacetic acid (EDTA), or a salt thereof or other strong metal-chelating agents, since their presence results in a significantly higher degree of coloured contaminants in the albumin produced.
  • EDTA ethylene diamine tetraacetic acid
  • the operating temperature is set at 30°C, and the stirrer speed regulated to be sufficient to maintain a homogeneous solution, typically about 50 rpm.
  • the initial pH is adjusted with ammonia solution (SG 0.901) (controller set to 5.7 ⁇ 0.2). 2M H 2 SO 4 may be used as a second pH corrective agent.
  • the MWIO batch vitamins are added, as is a suitable antifoam, as required (eg Breox FMT30 to 0.125 g 1 )-
  • Sterile filtered air is added to the vessel at 0.5 v/v/m initially to maximise sensitivity of exhaust gas analysis, and the MFCS computer system is initiated.
  • the exhaust gas is analysed, for instance by use of a continuous mass spectrometer (eg a Fisons VG gas analyzer).
  • the vessel is inoculated with the whole of the seed vessel culture (minimum 0.4% v/v).
  • MW10 feed in a volume equal to the batch volume.
  • the feed is started and the RQ override control disabled until OUR and CER values are sufficiently high to make control effective.
  • the feed rate is adjusted manually during the period without RQ control if RQ is consistently > 1.2.
  • the feed rate is increased, via computer control, according to the following algorithm:
  • Feed rate (FR) ke* 1 '
  • k is the initial feed rate
  • ⁇ is the exponential growth rate
  • t is time.
  • the value k is determined empirically as the initial feed rate that is necessary to achieve a growth rate that minimises the accumulation of ethanol and acetate.
  • k has been determined as having a value 0.08 mL of MW10 feed medium per minute per liter of culture.
  • the value ⁇ is related to the maximum growth rate of a fully respirative organism, in this example 0.1 h " '.
  • t is a counter variable that starts at 0 (zero) and then increases by 1 every minute, unless RQ> 1.2 or DOT ⁇ 15% . In these cases, the value of t is reduced.
  • the vessel can be overpressured as necessary to enhance OTR.
  • the culture is held for downstream processing at the end of the feed.
  • This hold time should be kept to a minimum, but can be extended up to 48 hours and beyond if necessary.
  • the temperature of the culture is mnt O 97/31
  • the DOT is allowed to fall to 0% .
  • the feed is stopped, the aeration turned off and the overpressure reduced.
  • the pH control is maintained. Sufficient agitation is maintained to retain the cells in suspension and facilitate cooling and pH homogeneity, preferably about 50 rpm.
  • rHA > 1.5g monomer/L culture determined by SDS-PAGE, related to the whole culture.
  • the microorganism cells are removed from the fermentation culture medium. While it is preferred that the cells be removed prior to beginning of the purification process as described, it can be carried out simultaneously with the first step under certain conditions, eg where the first purification step is carried out in a fluidised bed.
  • the fermentation culture which has been cooled in the fermenter during the hold phase to less than 15 'C without aeration, is transferred to a tank where it is diluted to give a biomass concentration of 180-210g/kg and cooled further if necessary.
  • the diluted culture should be held for as short a time as possible without aeration at reduced temperature with sufficient agitation to prevent yeast cell deposition.
  • Cells and supernatant are subjected to a primary separation step, for example microfiltration or ce ⁇ trifugation in any appropriate centrifuge such as an Alfa Laval BTUX510 continuous discharge nozzle run at 5700 rpm. Centrate so produced may be filtered in line, for example using a depth filter (l ⁇ m pore size), supplied by Cuno, to remove residual whole and broken yeast cells and other particles. At least 75% of the rHA present in the diluted culture is recovered in a single pass centrifugation operation. Optionally, the cell slurry from this operation may be resuspended in water or buffer and re-centrifuged to provide a second centrate, thus enhancing product recovery. The resultant solution is then treated by the process of the invention to purify the albumin contained therein as shown in Example 2.
  • a primary separation step for example microfiltration or ce ⁇ trifugation in any appropriate centrifuge such as an Alfa Laval BTUX510 continuous discharge nozzle run at 5700 rpm. Centrate so produced may be filtered
  • the centrate from a fermentation (such as described in Example 1), or an impure albumin solution from any other source (such as plasma), is prepared, or conditioned, for chromatography on a cation exchange matrix while protecting the albumin from polymerisation (by including octanoate) and protease activity (by heating or by choosing yeast without damaging levels of proteases).
  • sodium octanoate is added (Chromatography Solution 13 (CS13) - Table 2) to a final concentration of 1-lOmM, for example approximately 5mM, to stabilise the albumin.
  • the pH is adjusted with acetic acid (CS09) to 4.3-4.8. preferably 4.50 ⁇ 0.1 (most preferably ⁇ 0.05), and the conductivity is checked to be ⁇ 5.5mS cm '.
  • the culture supernatant from some host strains or species contains proteases that can degrade rHA during subsequent processing. In such instances, this protease activity can be destroyed by heat treatment of the culture supernatant containing the rHA.
  • 1-lOmM sodium octanoate is sufficient to protect the rHA from heat denaturation, and 30 seconds up to 10 minutes at temperatures of 60-80°C is adequate to inactivate the proteases.
  • the supernatant can be further conditioned as described previously. If degradation by proteases is not encountered, then the heat treatment is preferably omitted.
  • the albumin loads (g albumin/L matrix) for the chromatography columns are determined from titres of albumin (g/L) by either SDS-PAGE (in the case of the SP-FF column) or GP-HPLC (for all other columns).
  • the progress of each step is monitored by measuring UV absorbance on line, for example at 254 or 280 nm.
  • the sequence of chromatographic steps as described here is novel and inventive in a number of aspects.
  • a cationic matrix for the first purification step allows the majority of low molecular weight pigmented species derived from the yeast fermentation to pass directly through the column, whereas those that do bind to the matrix are bound weakly and can be removed by a high ionic strength salt clean such as 1M NaCl.
  • the cationic matrix unlike an anionic matrix which adsorbs these type of molecules irreversibly, can be regenerated and used for multiple cycles of chromatography as the first step in the purification. Hence, this step forms the basis for a robust commercial chromatography process.
  • Cibacron Blue type of column as the second step in this example is novel in that it is used specifically to remove a 45kDa fragment of albumin which is very difficult to remove from albumin as its physicochemical properties, eg size and pi, are similar to the intact molecule. Surprisingly, the fragment binds more strongly to the dye than full length albumin does, thus allowing their separation.
  • tetraborate ions in CS06 and CS10 is particularly advantageous since they perform a specific role in complexing with carbohydrate moieties in macromolecules and binding them tightly to the anionic groups on the matrix. This results in an enhanced purity of albumin in the eluate.
  • Chromatography can be performed using either axial flow columns, such as those available from Pharmacia, or using radial flow columns, such as those available from Sepragen. In this example, the columns are all axial.
  • the buffer solutions can be prepared at the concentrations described below, or concentrated stock solutions can be prepared and mixed or diluted on-line for immediate use.
  • Albumin is concentrated and purified with respect to at least yeast proteins (if the albumin is rHA from a yeast fermentation) and other antigens, low molecular weight contaminants and pigmented compounds by cation exchange chromatography.
  • the method uses a commercial cation exchange matrix such as SP-Sepharose FF, SP-Spherosil, CM-Sepharose FF, CM-Cellulose, SE-Cellulose or S-Spherodex.
  • the matrix is SP-Sepharose FF (Pharmacia) at a bed height of 5 to 25cm, preferably 10 to 15cm and in this example 12.5 cm, with a column loading of 10 to 50g albumin/L, preferably 40 ⁇ lOg albumin/L matrix.
  • T e matrix is equilibrated with a buffer to remove the alkali storage solution; preferably the buffer should be strong enough to reduce the pH to approximately pH ⁇ .O.
  • a buffer such as CS01 is used to remove storage solution CS07 from the column; however, any buffer with a pH ⁇ 6.0 could be used. Equilibration is judged to be complete when the pH of the column effluent is approximately pH6.0.
  • the conditioned centrate is then loaded onto the column at a flow rate of, for example 1.0-8.0cm/min, preferably 4.0-7.0cm/min, in this example, 6.36cm/min. and then the column is washed with a solution to remove residual contaminants.
  • This wash solution should have a pH ⁇ 6.0 and a conductivity less than 5mS cm "1 , preferably less than 3mS cm '1 , to prevent the elution of albumin.
  • a suitable solution is CS01.
  • the preceding steps are all run at 6.36cm/min; for elution and all subsequent steps the flow rate is reduced to 0.5-5.
  • Ocm/min preferably 2.0- 4.0cm/min, in this example 3.18cm/min, in order to reduce the volume of eluate.
  • Elution of albumin is effected by increasing the ionic strength; a solution with a conductivity in the range 5-10 mS cm ' , preferably 6-8mS cm '1 , for example CS02, is used.
  • the collection of albumin starts when the UV signal rises above 1.0 A 280 /cm, and collection continues until the UV signal falls below 0.6 A 280 /cm or a maximal volume of 6.5 column volumes has been collected.
  • the column is then cleaned using CS03 and 04, and then stored in CS07. T)
  • the affinity matrix may comprise any Cibacron Blue type of dye which binds albumin, for example Reactive Blue 2, Procion Blue HB, Blue Sepharose, Blue Trisacryl and other anthraquinone-type compounds.
  • the matrix is the "Delta Blue Agarose” matrix described below. This has been found to reduce the levels of Blue leachates generated by the matrix and to enhance the alkaline stability of the matrix to facilitate cleaning and depyrogenation.
  • a further improvement of the matrix compared to commercially available matrices is the incorporation of a spacer, 1 ,4-diaminobutane. between the dye (Reactive Blue 2) and the matrix. This was found to be the optimal length of spacer with respect to eluate albumin purity.
  • Reactive Blue 2 has the chemical structure represented below.
  • the ortho, meta or para isomer, or any mixture thereof, can be used.
  • the preferred isomer is the ortho-SO; form but, as it is difficult to make to the desired purity, the meta isomer is used.
  • the aminobutyl-Reactive Blue 2 is prepared to a minimum purity of 98% total peak area as determined by analytical HPLC. This can be achieved either by using crude commercially available dye, which will necessitate purification of the aminobutyl derivative dye, or using a pure synthesised dye. In the latter method, the starting dye material should be a minimum of 98% pure by analytical HPLC at 280nm. Such material is available from ACL, Isle of Man. Reactive Blue 2 is reacted with 1 ,4-diaminobutane in water by heating the mixture to O 9
  • the derivatised dye is purified from the mixture, for instance by precipitation.
  • the aminobutyl-Reactive Blue 2 is then coupled to the matrix, for instance to epichlorhydrin-activated Sepharose CL-6B (Pharmacia, Sweden). See Porath et al (1971) J. Chromatog. 60, 167-177.
  • the dye content of such a Delta Blue Agarose (DBA) matrix should, preferably, be 50 ⁇ 5 mmole/g dry weight.
  • the method uses DBA at a bed height of 10-30cm, preferably 20-30cm (in this example 25cm), with a column loading of 7-14g rHA/1 matrix, preferably 8-I2g/l (in this example 10 ⁇ lg albumin/L matrix); all steps are run at a flow rate of 0.3-2. Ocm/min. preferably 1.0-2. Ocm/min, in this example 1.53cm/min.
  • the DBA is equilibrated in CS01 from CS07; equilibration is complete when the pH of the column effluent is approximately pH9.5.
  • the SP-FF eluate Prior to chromatography, the SP-FF eluate is adjusted to approximately pH8.5-9.5, preferably pH 9.0, with ammonia, and then loaded onto the column. When loading is complete, the column is washed to remove contaminants with 1-5 volumes of buffer 10-30mS cm '1 , preferably 15-25 mS cm "1 , for example CSI2, preferably 5 column volumes.
  • the albumin is eluted using a high ionic strength buffer of > 100mS cm 1 , preferably 125-165mS cm 1 , for example CS03. Eluate collection is started when the UV signal (A 280 /cm) rises above 0.4, and stops when the signal falls below 0.4 again. The column is then cleaned using CS04 and stored in CS07.
  • This step concentrates the albumin for gel permeation chromatography.
  • a cellulose-type membrane (nominal molecular weight cut off less than or equivalent to 30.000, for example 10.000) in an ultrafiltration apparatus is used to concentrate DBA eluate to a retentate concentration of 20-120g/L albumin, preferably 80-110g /L.
  • the membranes are treated, post-use, by flushing out residual protein with water, or CS03 or CS05 from Table 3, and cleaning with 0.1M sodium hydroxide.
  • the membranes may then be stored in 20mM sodium hydroxide.
  • This step purifies the albumin with respect to yeast antigens (if the albumin is rHA from a yeast fermentation), pigment and dimerised albumin and performs a buffer exchange step.
  • the method uses a commercial gel permeation matrix such as Sephadex G100, G150, G250, Sephacryl S-100, S-200 or S-300, Toyopearl HW50S or Superose 6 or 12.
  • the matrix is Sephacryl S-200 HR (Pharmacia) at a bed height of greater than 60cm, preferably 90 ⁇ cm (3 x 30 cm).
  • the column is equilibrated in CS05 and run at 0.1- 1.5cm/min, preferably 0.5-1.
  • the column is then loaded with albumin from the intermediate UF step when pH 9.5 is reached.
  • the load volume is equivalent to approximately 2-9% of the coiumn volume, preferably 5-8% , for example 7.5% of the column volume.
  • the albumin fraction is collected in three parts: an initial small amount of albumin dimer goes to waste until the A 2g0 /cm reaches 10% full scale deflection (FSD) on the way up; at this point collection of a recycle fraction starts and continues until 90% FSD and then the albumin is collected as the primary product fraction. This continues until the A 280 falls through 5% FSD, after which the effluent stream is directed to waste again. The recycle and primary product fractions are collected separately. This step is repeated until all the material has been loaded onto the column.
  • FSD full scale deflection
  • a cellulosic type membrane nominal molecular weight cut-off equal to or less than 30,000, or as used in this example 10,000, in an ultrafiltration apparatus, is used to concentrate the pooled recycle fraction to a retentate concentration of 20-120g/L albumin, preferably 80-110g/L.
  • the membranes are treated, post-use as described above under Intermediate Ultrafiltration.
  • polyethersulfone or PVDF membranes with a cut-off of ⁇ 30.000 may be used instead of the cellulose-type membranes.
  • Such membranes are available from Amicon and Millipore. It is preferable to use membranes which are compatible with NaOH, used for storage and 25
  • the aim of this step is to purify albumin with
  • the method uses an anion exchange matrix such as QMA- Spherosil, DEAE-Spherodex, Q-Hyper D, DEAE-cellulose, QAE-cellulose, or TMAE, DMAE, or DEAE Fractogel.
  • the matrix is the commercial anion exchange matrix DEAE Sepharose-FF (Pharmacia) at any convenient bed
  • the sequence of purification steps is: cation exchange, affinity chromatography, ultrafiltration, gel permeation (with ultrafiltration of recycle fraction) and anion exchange.
  • the eluate from the DE-FF column has been found to have less than 0.1 % (w/w) albumin dimer and an undetectable level of albumin polymers or aggregates as analysed by GP HPLC using a TSK SW3000XL column, loaded with 25.0 ⁇ l of eluate containing 10.0 mg/ml of albumin.
  • Example 3 Formulation of purified albumin into a final product
  • This Example illustrates the concentration, diafiltration and formulation of the highly purified albumin into a suitable product, in this instance 25 %(w/v) albumin.
  • This procedure is carried out in two stages, namely final ultrafiltration (UF) and formulation.
  • Final UF begins with transfer of the DEAE eluate (adjusted to pH 7.0 ⁇ 0.3 with phosphoric acid) to the Final UF feed vessel and terminates after retentate and washings, if any, are transferred to the formulation vessel.
  • the albumin-containing process stream is sequentially subjected to primary concentration, diafiltration and secondary concentration in an ultrafiltration system fitted with cellulosic or, more preferably, polyethersulphone membranes with a nominal molecular weight cut off limit of 10,000.
  • the initial concentration step increases the albumin concentration to approximately lOOg.L ' and is immediately followed by the continuous diafiltration phase where the albumin is diafiltered against at least 5, preferably at least 7, retentate volume equivalents of water- for-injection.
  • ammonium ions may be present at this stage. Surprisingly, we have found that these ammonium ions are bound quite tightly by the albumin and cannot be completely removed by diafiltration against 11
  • the salt may be added to the albumin retentate or, more usually, will be added to the diafiltration water.
  • a solution of approx 100 g/1 may be recovered directly from the diafiltration step.
  • a solution of approx 275-325 g/1 is obtained following a further concentration step (UF). Finally, the solution is transferred to the bulk product formulation vessel.
  • the formulation step produces albumin in an appropriate chemical environment and at an appropriate concentration suitable for bulk product sterile filtration (0.22 ⁇ m hydrophilic polyvinylidene-difluoride) and filling.
  • the transferred solution is analysed to determine concentrations of albumin, sodium and octanoate. These quantities are taken into account and any necessary further amounts of stock sodium chloride and sodium octanoate excipient solutions and appropriate grade water added to achieve the bulk formulation specification.
  • the final albumin concentration may be 235-265g.L ' (ie about 25%), with a sodium concentration of 130-160mM.
  • albumin concentration may be made, however, with, for example, a minimum concentration of at least 4% (w/v), preferably 4 - 25 % (w/v).
  • Formulation is complete following addition of appropriate conventional pharmaceutically acceptable excipients, such as those specified in the US or European Pharmacopoeias for human albumin, and diluting water.
  • a final concentration of 0.08 mmoles sodium octanoate per gram of albumin may be desirable.
  • the product is sterile and non-pyrogenic. There may be about 1 % (w/w) dimeric albumin but no larger polymers or aggregates are detectable as analysed by GP HPLC using a TSK SW3000XL column.
  • Example 4 Cation exchange followed directly by anion exchange
  • the initial cation exchanger step was essentially the same as in Example 2, but with the following variations.
  • the bed flow path length was 11.0 ⁇ 1.0 cm.
  • the chromatography was then carried out as follows.
  • An SP-FF (Pharmacia) column was equilibrated in four volumes of 10-100 mM acetate, preferably 20-40 mM, for example 30 mM as in CS20, and the albumin solution was loaded at a flow rate of 0.07 to 0.75 bed volumes per min, preferably 0.3-0.6, in this example 0.5 bed volumes per minute.
  • the column was washed with eight volumes of 10-100 mM, preferably 30-70, for example 50 mM acetate (CS21) and then ten volumes of CS20 and the albumin eluted with, and collected in, an acetate/octanoate buffer (for example 40-120. preferably 60-100.
  • the flow rate for the equilibration, loading and washing steps is 0.5 bed volumes per minute.
  • a flow rate of 0.04-0.6 bed vol/min, preferably 0.15-0.35, in this example 0.25 bed vol/min is used.
  • the anticipated recovery of rHA monomer is between 46 and 66% .
  • the albumin was therefore eluted from the cation exchange column with a solution of octanoate, achieving a novel biospecific elution of rHA from a cation exchanger.
  • the pH is close to the pi of the albumin so that the binding of the octanoate causes a significant overall charge difference; for example, the pH is at least 4.5, preferably about pH 5.5.
  • the eluate from the cation exchanger is then loaded directly (ie instead of after affinity and gel permeation chromatography as in Example 2, but preferably after dilution) onto the anion exchange resin at a pH of 4.5-6.5, preferably about 5.5. and a conductivity preferably in the range 1.5 to 5.0 mS.c '. for example 2.5 ⁇ 0.5 S.cm "1 .
  • This has been found to result in any dimeric albumin that was formed during the cation exchange chromatography being converted back to monomeric albumin under the conditions of the anion exchange chromatography. A yield of approximately 1 10% for albumin monomer has been achieved over this step.
  • an 11.0 ⁇ 1.0 cm bed flow path length column of DEAE-Sepharose Fast Flow (Pharmacia) is pre-equilibrated with the cation exchange elution buffer (CS23) and then equilibrated with an acetate buffer (for example CS20) before being loaded with 30.0 ⁇ 10.0 g monomeric albumin per litre of matrix.
  • CS23 cation exchange elution buffer
  • acetate buffer for example CS20
  • the column is then washed with a borate solution as in Example 2 (CS27), eluted as in Example 2 (CS06), and cleaned with salt/detergent (CS24), caustic (CS25) and stored in dilute caustic (CS26) all as for the cation exchange column.
  • the flow rate for all the steps is 0.07 to 0.75 bed vol/min, preferably 0.3-0.6, in this example 0.5 bed volumes per minute.
  • the eluate from the anion exchange resin still contains impurities and is then applied directly to the affinity matrix (eg Delta Blue Agarose as described in Example 2).
  • the bed height was reduced from 25 cm in Example 2 to 11.0 ⁇ 1.0 cm which allowed a higher flow rate within normal operating pressure. Therefore, a bed height of 1 1.0 cm was preferred and does not adversely affect recovery of albumin or albumin purity.
  • the column was equilibrated in ammonium acetate (100- 300 mM. preferably 200-275, for example 250 mM as in CS29) and the albumin was applied at 7.0-14.0 g/1, preferably 8.0-12.0 g/1, in this example 10.0 ⁇ 1.0 g per litre of matrix.
  • the column was washed with 5 column volumes of the ammonium acetate buffer (CS29), and the albumin was eluted with strong salt and phosphate solution (1.0-3.0 M NaCl, for example 1.5-2.5 M or 2.0 M NaCl, and 5-100 mM, eg 50 mM phosphate, as in CS30).
  • strong salt and phosphate solution 1.0-3.0 M NaCl, for example 1.5-2.5 M or 2.0 M NaCl, and 5-100 mM, eg 50 mM phosphate, as in CS30).
  • the pH of the eluant in this variant of the process was changed to pH7.0 from pH9.2.
  • the buffer was changed accordingly from 50 mM ammonium acetate to 50 mM sodium phosphate which was preferred because of its buffering at pH7.0, and its relative cost.
  • the lower pH eluant was responsible for an increase in DBA eluate albumin monomer recovery.
  • a pH lower than 7.0 increased the fragment levels, and above pH7.0 the albumin monomer recovery was reduced.
  • the pH which can be in the range 5.5-9.0, is therefore preferably pH7.0.
  • the column was cleaned and stored in caustic (CS25, CS26) as above.
  • the DBA eluate (optionally after ultrafiltration with a cellulosic type membrane (nominal cut off MW30,000) to give 80-110 g/1 of albumin) was then applied to the gel permeation resin, for example S-200 (HR).
  • the S-200 running buffer was changed to 40 mM sodium phosphate pH7.0.
  • the sodium octanoate was omitted from this buffer for cost reasons, and instead was added to the solution prior to diafiltration (added to a concentration of l-20mM, preferably 5mM).
  • the phosphate conferred a higher conductivity on the running buffer which improved the purity.
  • a high salt concentration can be used to increase conductivity but it is still preferable to buffer the solution.
  • the pH7.0 was preferable since this was the desired pH for formulation.
  • the sequence of purification steps is: cation exchange (eluting with a molecule specifically bound by albumin), anion exchange, affinity chromatography and gel permeation.
  • the diafiltration step prior to formulation may be assisted by starting with albumin at pH7.0.
  • the albumin was more concentrated at the final eluate than with the process of Example 2, assisting the final ultrafiltration step prior to formulation (Example 3).
  • Example 2 or 4 the process of Example 2 or 4 was followed except as follows. Following loading of the albumin on to the cation exchange column (for example SP-Sepharose FF, Pharmacia), the column was washed with CS21 (50 mM sodium acetate, pH 3.9-4.1, 0.6-0.8 mS.cm '), then further washed with a high salt buffer containing 1-3M NaCl, preferably 2M NaCl, in sodium acetate buffer (for example 10-50mM sodium acetate, preferably about 27mM, pH 3.5-4.5, preferably pH4.0) before the final wash in CS20.
  • CS21 50 mM sodium acetate, pH 3.9-4.1, 0.6-0.8 mS.cm '
  • a high salt buffer containing 1-3M NaCl, preferably 2M NaCl, in sodium acetate buffer (for example 10-50mM sodium acetate, preferably about 27mM, pH 3.5-4.5, preferably pH4.0) before the final wash
  • This more stringent washing procedure results in an eluate containing a lower level of non-albumin proteins and may be especially useful if the albumin is rHA from a yeast fermentation.
  • the albumin was eluted as described in Example 4. The lowering of the pH prior to the high salt wash helps to retain the albumin on the column during that wash, and the final wash also maximises albumin recovery. It is probable that neither step has a major effect on the purity of the albumin recovered.
  • Example 2 or 4 (with or without the variation in Example 5) was varied as follows.
  • the eluate from the cation exchange column was diluted to below lOmS.cm "1 , preferably less than 5mS.cm "1 , and then loaded on to an anion exchange matrix (for example DEAE Sepharose FF, Pharmacia).
  • an anion exchange matrix for example DEAE Sepharose FF, Pharmacia.
  • the anion exchange matrix was then washed with dilute tetraborate buffer (for example 15- 25mM potassium tetraborate or sodium tetraborate), which has the effect of raising the pH to approximately 9.2, and then the albumin was eluted with a more concentrated tetraborate buffer (for example 80-150mM potassium tetraborate, preferably HOmM potassium tetraborate).
  • dilute tetraborate buffer for example 15- 25mM potassium tetraborate or sodium tetraborate
  • albumin was eluted with a more concentrated tetraborate buffer (for example 80-150mM potassium tetraborate, preferably HOmM potassium tetraborate).
  • the albumin was eluted with 20mM tetraborate, lOOmM NaCl; elution with 80-150mM tetraborate (eg 33.6 g/1) results in an eluate with a lower content of carbohydrate-containing contaminants, for example yeast glycoproteins, due to an increased affinity of these species for the anion exchange matrix under these conditions.
  • Potassium tetraborate is used in preference to sodium tetraborate because of its higher solubility at room temperature.
  • the eluate from the anion exchange matrix was dealt with as in Example 2 or 4. For example, in the Example 4 process, it was then directly loaded onto an affinity matrix, eg Delta Blue Agarose (DBA), which was run as described in Example 4.
  • DBA Delta Blue Agarose
  • a gel permeation step is then carried out as in Example 2 or 4.
  • the eluate from the DBA matrix may be applied to a gel permeation medium, for example Sephacryl S-200 (HR) (Pharmacia), equilibrated in an ammonium acetate buffer (for example 10-lOOmM, preferably about 30mM), containing sodium chloride (20-2000mM, preferably about lOOmM) and octanoate (1 -20 mM, preferably about 5mM octanoate at pH 9.0-9.5, preferably 9.2).
  • HR Sephacryl S-200
  • the S-200 step is run as follows.
  • the S-200 is run at a minimum bed height of 90.0 ⁇ 3 cm (eg 3 x 30 cm in series),
  • (a) The retentate from intermediate ultrafiltration is loaded onto the column. Recycle and product fractions are collected. This step is repeated until all the material has been loaded onto the column,
  • (b) The pooled recycle fractions are concentrated to 80-110 g rHA/L by ultrafiltration as above,
  • the retentate from recycle ultrafiltration is loaded onto the same column and a product fraction collected from each peak. This step is repeated until all the material has been loaded onto the column,
  • (d) The product fractions from the primary and secondary gel permeation chromatography steps ((a) and (c)) are pooled as the S-200 eluate.
  • the final step consists of an affinity step to remove glycoconjugates, such as glycoproteins and glycolipids, and poly-, oligo- and monosaccharides.
  • This step uses immobilised aminophenylboronic acid (PBA) as the ligand.
  • PBA immobilised aminophenylboronic acid
  • US Patent No 4 562 251 (incorporated herein by reference) describes suitable methods for making diborotriazine agarose or monoborotriazine agarose: (1) Triazine is O-linked to agarose first and then linked with 3-aminophenylboronic acid (APBA) in a second reaction. If the X on the triazine is replaced with chlorine then the disubstituted resin is produced.
  • APBA 3-aminophenylboronic acid
  • Triazine is reacted with APBA first to produce either mono or diborotriazine. These are then O-linked via the free chlorine on the triazine to the -ONa activated agarose to produce either mono or disubstituted agarose. All of the examples and descriptions in this patent use -ONa activated agarose which results in O-linkages.
  • the albumin collected from the S-200 column was chromatographed through the PBA matrix, having been pre-equilibrated in S-200 running buffer (see above); under these conditions, the albumin does not bind appreciably to the matrix, whereas the carbohydrate-based contaminants are retarded sufficiently to separate them from the albumin as it passes through the column.
  • the chromatography is thus in the negative mode with respect to the albumin. Further details were as follows:
  • the phenyl boronate matrix had a flow path length of 11.0 ⁇ 1.0 cm and was equilibrated with a buffer containing ammonium ions (10-50 mM), acetate (10-50 M) and 1.0-10.0 mM octanoate (eg CS36 - see table below).
  • the column was then loaded at 35 ⁇ 15 g of rHA/L matrix.
  • the PBA is run as a negative step and therefore the product collected is the flow through during loading and the subsequent wash with the equilibration buffer. All chromatographic steps can be performed at flow rates in the range 0.005-0.3 bed vol/min.
  • equilibration and cleaning of the column are carried out at a higher flow rate, eg 0.19 bed vol/min. than load and collection of the albumin solution, which is preferably carried out at a flow rate of 0.01-0.05, preferably 0.025 bed vol/min.
  • the column is then cleaned with a borate buffer (as in CS37), salt (CS38) and caustic (CS25) and then stored in the borate buffer (CS37).
  • the pH of the collected flow through and wash is adjusted to 7.0 ⁇ 0.1 with phosphoric acid solution (CS35).
  • Example 2 (2) Yeast fermentation as in Example 1. (2) Centrate conditioning as in Example 2.
  • Example 7 Dilution and anion exchange with concentrated tetraborate elution as in Example 6.
  • DBA Affinity chromatography
  • S-200 Intermediate ultrafiltration and then gel permeation (S-200), with recycle ultrafiltration, as in Example 7.
  • the step involving immobilised phenylboronate may be used earlier in the process, for instance in a process in which the steps are ordered: cation exchanger - anion exchanger - affinity material - ultrafiltration/diafiltration - immobilised phenylboronate - gel permeation.
  • the conditions for each step are as in Examples 4 to 7. except as follows.
  • the DBA eluate is concentrated to 80-110 g/1 albumin and the pH is adjusted to 9.2 by diafiltering (5 volumes) against an ammonium acetate of the kind used in Example 7.
  • the concentrated DBA eluate is then chromatographed on PBA and the flowthrough is collected and applied directly to the gel permeation (eg S200) column.
  • the gel permeation step is now the last step, it may run in a buffer which is suited to the formulation step, for example 20-130 mM (preferably 50-100 mM) NaCl, at pH 7.0.
  • This Example illustrates the analysis that is carried out to establish the purity of albumin purified in accordance with the present invention. Unless stated otherwise, all of the assays are performed on albumin which has been formulated as described in Example 3 to yield the final product.
  • a microassay for glycated protein has shown that (rHA) purified in accordance with the invention is not modified by non-enzymic glycosylation (glycation).
  • the microassay measures the stable Amadori product (AP) form of glycated protein, by oxidation of the C-l hydroxyl groups of AP with periodate.
  • the formaldehyde released by periodate oxidation is quantitated by conversion to a chromophore, diacetyldihydrolutidine (DDL), by reaction with acetylacetone in ammonia. DDL is then detected colorimetrically at 405 nm.
  • Batches A-K were rHA purified according to Example 2.
  • Batches L-O were samples of commercially available human serum albumin from differing sources.
  • Eight batches of rHA purified according to Example 7 had a negligible level of glycation (0.042 ⁇ 0.018 moles/mole) compared to HSA (0.387 ⁇ 0.012).
  • Rationale - The aim of this assay is to remove non-covalently bound low molecular weight contaminants (LMC) from rHA and HSA using acidic organic solvents.
  • An HPLC "fingerprint" chromatogram can then be produced for comparison of samples.
  • Method - To 100 ⁇ l of final product (20 mg; rHA or HSA) is added sequentially 50 ⁇ l formic acid (98% v/v), 100 ⁇ l chloroform and 50 ⁇ l ethanol with vortexing after each addition. The samples are kept at room temperature for 5 mins with regular mixing. Protein is then precipitated by the addition of 1 ml acetone (30 mins, -20°C).
  • the protein samples are pelleted by centrifugation and the supematants are decanted off and dried by rotary evaporation under vacuum.
  • the dried samples are resuspended in 25% acetonitrile/0.1 % trifluoroacetic acid.
  • the samples were monitored at 214nm using a Shimadzu UV monitor.
  • the peak at 2.15 mins is thought to be due to insoluble or partially soluble material passing through the column, and the large peak at 56.5 mins is also present in the trace of a water blank and thus is regarded as an artefact.
  • the quality of the albumin of the invention in terms of non-covalently bound LMCs is clearly superior to that of clinical HSA.
  • the total peak area between 10 mins and 55 mins for the albumin of the invention was about 6.4 V.sec whereas the total peak area between the same two times for commercially available material was about 39.7 V.sec.
  • CE Capillary electrophoresis
  • An important aspect of the quality control of recombinant proteins is the confirmation and stability of the pre-determined primary structure.
  • HSA from a commercial source - one sample stored at -20°C and one stored at 30°C for 12 weeks
  • rHA purified according to the invention stored at 4°C and 30°C for 6 months
  • Des-Leu rHA a truncated form of rHA minus the C-terminal leucine (1 mg each) were reduced with 5 mM dithiothreitol (Calbiochem) for 120 min 37°C, then alkylated with 10 M iodoacetamide (Sigma) for 90 mins at 37 °C in 6M guanidine HCl in 0.5M Tris HCl pH 8.0.
  • N-terminal Sequencing Performed on an ABI 477A protein sequencer.
  • FAB-MS Fast Atom Bombardment - Mass Spectrometry
  • the signals at 1028 and 1140 may be fragment ions; they were not peptides that could be detected by sequence analysis.
  • the Des-Leu C-terminal tryptic peptide was detected in commercial HSA at approximately 5-10% (not quantitative), but could not be detected in the rHA of the invention, even after 6 months at 30°C.
  • the Des-Leu peptide could not be detected in the HSA 12 weeks at 30 C C, and the peak for the full length C-terminal peptide at 37.5 minutes (though not isolated) was very diminished compared to the other samples, indicating that perhaps this has undergone further C-terminal degradation.
  • DTNB 5.5'-Dithiobis (2-nitrobenzoic acid) DTNB, Sigma Product No D8130. TRIS PRE-SET pH crystals pH8.0, Sigma Product No T4753. EDTA. disodium, Sigma Product No ED2SS. Sodium dihydrogen phosphate dihydrate, Analar grade. Disodium hydrogen phosphate dihydrate, Analar grade.
  • Buffer 1 0.1M (12.1g) Tris-HCl; 0.01M (3.72g) EDTA Na 2 .2H 2 O, pH8.0. PRE ⁇ SET pH crystals. Dissolve in 500ml water and make up to 1 litre exact volume. Stable for one month at room temperature.
  • Buffer 2 0.05M Sodium phosphate pH7.0. Na 2 HPO 4 .2H 2 O (5.45g), 3.04g NaH 2 PO 4 .2H 2 O. Dissolve in 500ml water, and make up to 1 litre exact volume. Stable for 1 month at room temperature.
  • Reagent 0.01 M (39.4mg) DTNB in phosphate buffer. Dissolve in 10ml buffer 2. Prepare fresh each day.
  • Sample Dilute albumin to about 10.3 ⁇ M in buffer 1 (0.66mg/ml).
  • Aluminium was measured using a Perkin Elmer M2100 atomic absorption spectrophotometer, a Perkin Elmer HGA-700 graphite furnace, a Perkin Elmer AS- 70 Autosampler with sample cups and an aluminium hollow cathode lamp.
  • the reagents were AR grade magnesium nitrate, an aluminium standard solution (1000 ppm) and AR grade concentrated nitric acid.
  • a 1.00% w/v magnesium nitrate solution was made up with Milli-Q water.
  • 15 ⁇ l of aluminium standard solution was pipetted into the autosampler and diluted to 1500 ⁇ l with 0.20% nitric acid solution. The procedure is repeated with 15 ⁇ l of the solution obtained and then with 150 ⁇ L of the solution subsequently obtained, to give a 10 ppb ( ⁇ g/L) aluminium solution.
  • An albumin sample is diluted with 0.20% nitric acid solution to give an aluminium concentration within the limits of the calibration graph. A 1:2 dilution is usually sufficient.
  • Magnesium is measured similarly, using a Perkin Elmer AS-51 flame autosampler and a magnesium hollow cathode lamp.
  • a Magnesium Standard solution of 1000 ppm is diluted with Milli-Q water to give 0.1 , 0.2, 0.5 and 1.0 ppm standard solutions.
  • the atomic absorption of the sample is detected at 285.2 n .
  • Copper, iron, manganese and zinc are measured in the same way as aluminium except that, for zinc, a 1.0 ppb ( ⁇ g/1) standard solution is used instead of a 10 ppb solution.
  • concentration of metal ions was determined in ng/L and then related to the concentration of albumin (ng metal ion g albumin). These data are presented in Table 9.
  • Table 10 shows the corresponding levels of metal ions in commercial HSA.
  • the average level of aluminium in the product of the invention was about 60 ng/g whereas the commercial sources had 155-3190 ng/g.
  • the product of the invention had an average of about 948 ng/g iron (compare 1850- 41,200 ng/g in prior art material), an average of 2,990 ng/g of copper (compare 580- 23,840 ng/g in prior art material), an average of 1 , 120 ng/g of magnesium (compare 500-54,000 ng/g in prior art material), an average of 2,390 ng/g of zinc (compare 930-7,230 ng/g in prior art material, and an average of 48 ng/g manganese (compare 65 to 940 ng/g in prior art material).
  • fatty acids profiles of albumin according to the invention and commercially available HSA were analysed by acidic solvent extraction and gas chromatography of the free fatty acids using a C17:0 internal standard.
  • Gas chromatograph eg Shimadzu GC 9A with flame ionisation detector
  • Autoinjector eg Shimadzu AOC 14
  • Integrator/Printer eg Shimadzu CR4A: HP-FFA 30 x 0.53 mm, 1.0 ⁇ m phase column (Hewlett Packard Ltd); Megabore Installation kit (J & W Scientific 220-1150 for GC 9A) with direct injection liner.
  • Reagents Water (Milli-Q); Dichloromethane Super Purity Solvent (Romil Chemicals, Loughborough, Leics.); Sodium Acetate Trihydrate Analar (BDH Ltd, Poole): Acetic Acid Glacial Analar (BDH Ltd, Poole): Human Serum Albumin Solution (ZenalbTM20, Bio Products Laboratory, Elstree, Herts.); Sodium Sulphate Anhydrous (Analytical Reagent); standard fatty acids from Sigma.
  • Free Fatty Acid standard mixtures Weigh 5 mg of each fatty acid into separate glass vials. Dissolve each fatty acid in 1 ml Dichloromethane and transfer to three 12 ml Pyrex culture tubes respectively for short chain (C6-C14), medium chain (C16-C18) and long chain (C20-C22:l) fatty acids. Dry down mixture under a stream of nitrogen and dissolve in 1 ml Dichloromethane. Transfer 50 ⁇ l aliquots of mixture into labelled glass vials, dry under nitrogen, cap and store at -20°C.
  • Detector Flame ionisation; Carrier Gas: Nitrogen at 30 ml min "1 ; Injection Volume: 0.5 ⁇ l; Column initial temperature: 70°C; Hold: 1.5 min; Gradient 1 : 20°C min 1 to 150°C; Gradient 2: 4°C min 1 to 240°C; Hold: 7 min; Detector Temperature: 280°C; Setting Specific to Shimadzu GC9A are:
  • Peak Area Ratio Peak Area
  • Example results are presented for a batch of albumin prepared according to Example 2 (FIG. 4) and commercial HSA (FIG. 5).
  • No abnormal fatty acids have been detected in the former by this method although the profiles for the two proteins showed significant differences.
  • both showed large amounts of the added stabiliser, octanoate (C8:0).
  • commercial HSA was characterised by predominantly C16:0, C16: l , C18:0, C18:l and C18:2 whilst the albumin of the invention contained mainly C10:0, C12:0.
  • C16: l and occasionally C14:0 Further experiments showed that the levels of C10:0 and C12:0 in rHA final product correlated with the levels of these contaminants in the octanoate used for the latter stages of the purification process.
  • the total level of C18 fatty acids does not exceed 1.0% (mole/mole) of the level of octanoate. and preferably does not exceed 0.5 % of that level.
  • the level of C18:2, C18:3 and C20 fatty acids is generally undetectable. In commercial HSA, there may typically be about 0.4 moles CIO to C20 fatty acids per mole of albumin. In the product of the invention, there is typically no detectable C20 fatty acids and only about 0.01 to 0.02 moles C18 fatty acids per mole of albumin.
  • the absorbance of a 5% (w/v) solution of the final product in a 1 cm cuvette was measured at 350nm, 403nm and 500nm and calculated in terms of absorbances per gram of albumin/litre per cm pathlength (ie A L.g '.cm ').
  • the albumin of the invention has the following values:
  • the albumin of the invention does not exceed respective absorbances of 6.0 x 10 3 , 2.5 x 10 3 and 0.75 x 10 3 at the said three wavelengths.
  • SDS reducing polvacrylamide gel electrophoresis This assay is performed to show that rHA consists of a single polypeptide chain which when treated with a reducing agent ( .-mercaptoethanol) migrates as a single band (monomer) on SDS reducing polyacrylamide electrophoresis (PAGE).
  • a reducing agent .-mercaptoethanol
  • 2 ⁇ g rHA of albumin prepared by the process of the invention was subject to two- dimensional electrophoresis using a Millipore Investigator system.
  • the separation in the first dimension was a pH 3-10 isoelectric focusing gel and was followed by a 10% polyacrylamide/SDS gel in the second dimension.
  • Coomassie Blue On staining of the gel with Coomassie Blue, only one spot was visible, indicating the presence of only one protein species.
  • Electrospray mass spectrometry was performed using a VG Quattro electrospray mass spectrometer, calibrated with horse heart myoglobin (16951 Da. obtained from Sigma) over m/z range 950-1750 Da/e.
  • Samples of commercially available HSA and samples of rHA purified according to the invention were desalted prior to analysis by reverse phase HPLC using an acetonitrile gradient containing trifluoroacetic acid.
  • Figures 6a and b show the spectra for albumin of the invention and prior art HSA, respectively. The latter shows peaks representing blocked free thiol and N-terminal degradation.
  • the albumin of the invention can be seen to be substantially homogeneous in this assay, in other words it shows a single defined peak, occurring at a mass of about 66441 Da. Long term stability

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Abstract

Procédé d'élaboration d'albumine renfermant des quantités extrêmement faibles ou étant essentiellement exempte de colorants, d'ions métalliques, de protéines humaines, de protéines hôtes, de fragments d'albumine, de polymères ou d'agrégats d'albumine et de virus, et qui est essentiellement non glycosylée, à forte teneur en thiols libres et comporte une terminaison C intacte. Le procédé consiste à soumettre l'albumine (de préférence exprimée et sécrétée par une levure transformée) à une chromatographie par échange cationique à mode positif puis par échange anionique à mode positif. D'autres étapes peuvent être appliquées, comme par exemple l'ultrafiltration, la chromatographie par perméation sur gel, la chromatographie d'affinité pour l'albumine (par exemple en utilisant des colorants bleus) et la chromatographie d'affinité pour les polluants (comme par exemple en utilisant une résine d'acide aminophénylborique). L'invention porte également sur l'élution de l'albumine à l'aide d'un composé présentant une affinité pour l'albumine, à partir d'une matière ne présentant pas d'affinité pour celle-ci, ainsi que sur l'extraction des ions ammonium par un contre-ion.
PCT/GB1996/000448 1996-02-29 1996-02-29 Procede de production d'albumine a haut degre de purete WO1997031947A1 (fr)

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Cited By (10)

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WO2000044772A3 (fr) * 1999-01-30 2000-11-30 Delta Biotechnology Ltd Technique
EP1656954A1 (fr) * 2004-07-26 2006-05-17 Grifols, S.A. Solutions d'albumine humaine thérapeutiques ayant une faible activité de l'activateur de la prékallikréine (PKA) et procédés de production
US7223561B2 (en) 1995-05-25 2007-05-29 Novozymes Delta, Limited Process of high purity albumin production
AU2007200939B2 (en) * 1999-01-30 2010-03-04 Albumedix Ltd. Process
US7998986B2 (en) 2001-12-21 2011-08-16 Exelixis Patent Company Llc Modulators of LXR
US8013001B2 (en) 2001-12-21 2011-09-06 Exelixis, Inc. Modulators of LXR
WO2015164320A1 (fr) * 2014-04-23 2015-10-29 Synageva Biopharma Corp. Traitement de blanc d'oeuf
CN111620937A (zh) * 2020-03-09 2020-09-04 烟台双塔食品股份有限公司 一种高纯度白蛋白的提取方法
CN113735963A (zh) * 2021-09-10 2021-12-03 山东健通生物科技有限公司 一种重组人血清白蛋白纯化过程去除色素的方法
CN118271424A (zh) * 2024-06-03 2024-07-02 中国农业科学院农产品加工研究所 一种鲜奶级高纯度α-乳白蛋白的分离制备方法

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US7223561B2 (en) 1995-05-25 2007-05-29 Novozymes Delta, Limited Process of high purity albumin production
US9555344B2 (en) 1999-01-30 2017-01-31 Albumedix A/S Process for the purification of recombinant albumin
CN1810834B (zh) * 1999-01-30 2013-04-17 诺维信生物制药丹麦公司 制备高纯度白蛋白溶液的方法
WO2000044772A3 (fr) * 1999-01-30 2000-11-30 Delta Biotechnology Ltd Technique
JP2002542761A (ja) * 1999-01-30 2002-12-17 デルタ バイオテクノロジー リミテッド 方 法
US9029102B2 (en) 1999-01-30 2015-05-12 Novozymes Biopharma Dk A/S Process for the purification of recombinant albumin
EP2048234A1 (fr) * 1999-01-30 2009-04-15 Novozymes Biopharma UK Limited Procédé chromatographique de purification de l'albumine
JP2013135675A (ja) * 1999-01-30 2013-07-11 Novozymes Biopharma Dk As 方法
CN1526732B (zh) * 1999-01-30 2010-06-16 诺维信生物制药英国有限公司 制备高纯度白蛋白溶液的方法
JP2010246551A (ja) * 1999-01-30 2010-11-04 Novozymes Biopharma Uk Ltd 方法
US7993877B2 (en) 1999-01-30 2011-08-09 Novozymes Biopharma Dk A/S Process for the purification of recombinant albumin
AU763899B2 (en) * 1999-01-30 2003-07-31 Albumedix Ltd. Process
AU2007200939B2 (en) * 1999-01-30 2010-03-04 Albumedix Ltd. Process
US8013001B2 (en) 2001-12-21 2011-09-06 Exelixis, Inc. Modulators of LXR
US7998986B2 (en) 2001-12-21 2011-08-16 Exelixis Patent Company Llc Modulators of LXR
US7332577B2 (en) 2004-07-26 2008-02-19 Grifols, S.A. Therapeutic human albumin solutions with low prekallikrein activator (PKA) activity and process for obtaining them
US8084580B2 (en) 2004-07-26 2011-12-27 Grifols, S.A. Therapeutic human albumin solutions with low prekallikrein activator (PKA) activity and process for obtaining them
EP1656954A1 (fr) * 2004-07-26 2006-05-17 Grifols, S.A. Solutions d'albumine humaine thérapeutiques ayant une faible activité de l'activateur de la prékallikréine (PKA) et procédés de production
WO2015164320A1 (fr) * 2014-04-23 2015-10-29 Synageva Biopharma Corp. Traitement de blanc d'oeuf
US9938319B2 (en) 2014-04-23 2018-04-10 Alexion Pharmaceuticals, Inc. Egg white processing
CN111620937A (zh) * 2020-03-09 2020-09-04 烟台双塔食品股份有限公司 一种高纯度白蛋白的提取方法
CN111748023A (zh) * 2020-03-09 2020-10-09 烟台双塔食品股份有限公司 一种环保节能提取白蛋白的方法
CN111793120A (zh) * 2020-03-09 2020-10-20 烟台双塔食品股份有限公司 一种绿色循环提取白蛋白的方法
CN113735963A (zh) * 2021-09-10 2021-12-03 山东健通生物科技有限公司 一种重组人血清白蛋白纯化过程去除色素的方法
CN118271424A (zh) * 2024-06-03 2024-07-02 中国农业科学院农产品加工研究所 一种鲜奶级高纯度α-乳白蛋白的分离制备方法

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