PURIFICATION OF ERWINIA-L-ASPARAGINASE

Abstract: A process is provided for the purification of L-asparaginase by contacting a crude extract of L-asparaginase with a solid medium having cation exchange groups so as to adsorb L-asparaginase on the support and eluting adsorbed L-asparaginase from the support. The cation exchange groups comprise sulphonate groups and the elution step is carried out at a pH which is higher than the pH used in the contacting step.

Description: PURIFICATION OF ERWINIA-L-ASPARAGINASE This invention relates to a process for the purification of L-asparaginase. L-asparaginase has been reported to occur in a range of bacteria, fungi, plants and mammals and its presence in Gram-negative bacteria has been well documented (Wriston & Yellin, 1973; Wriston, 1985)- L-asparaginases have considerable commercial importance because some of these enzymes particularly those from Escherichia coli (asparaginase II) and Erwinia chTysanthemi are effective against acute lymphoblastic leukaemia (Wriston, 1985). The enzymes from Erwinia and E. coli show no immunological cross-reactivity and so can provide an alternative therapy for a patient who has become hypersensitive to one of these enzymes. (Cammack et al., 1982). The enzyme from Evwinia is a tetramer of relative molecular mass 140,000, with four identical subunits, and has an unusually high isoelectric point of pH 8.6. Hitherto, L-asparaginases have been prepared on a large scale by a combination of batch and column ion-exchange chromatography. A large number of stages are required to attain the necessary purity, with batch ion-exchange chromatography being particularly labour-intensive. Current commercial practice involves the growth of a cell culture, and then a crude protein extraction employing alkali disruption and acid precipitation. The resulting extract is then subjected to adsorption to and elution from CM-cellulose. There then follows a further acid precipitation step and chromatography steps using CM and DEAE-cellulose media One of the major problems of the system is its complexity, thus it is not readily automated and cannot be easily adapted for continuous operation. We have now developed a new method of L-asparaginase purification resulting-in a product of astonishing quality with a simplified process and the advantage of allowing for increased automation. According to the present invention there is provided a process for producing purified L-asparaginase which comprises (a) contacting a crude extract of L-asparaginase with a solid medium having cation exchange groups so as to adsorb L-asparaginase on the support and (b) eluting adsorbed L-asparaginase from the support, characterised in that the cation exchange groups comprise sulphonate groups and the elution step (b) is carried out at a pH which is higher than the pH used in step (a) and preferably is. less than 8.0. The cation sulphonate (-SO, ), groups may be provided, for example, by groups of the formula -(CH_) SO, wherein n is equal to 1 to 3- The nature of the matrix of the solid medium is not unduly critical, but in order to achieve a high flow rate in a continuous process a support with a high degree of porosity is preferred. Other desirable characteristics include rigidity, low non-specific binding of protein and general chemical stability. It has been found that these properties are provided by agarose or an agarose derivative. In carrying out the process of the invention, crude dilute extract of L-asparaginase is preferably applied to the solid medium at a pH of from 4.0 to 5-5t followed by a washing step at pH 6.0. Elution of adsorbed L-asparaginase may then be effected with a suitable buffer solution of pH in the range 6.0 to 7>5- This range is preferably between 6.5 to 7-0. The process of the invention may be advantageous applied to the purification of the L-asparaginase of E chrysanthemi . Although as mentioned above, L-asparaginases are fairly ubiquitous in prokaryotes and eukaryotes alike, that of E chrysanthemi is preferably used for this process because of its therapeutic utility. Thus the process of the invention may be employed to purify L-asparaginases extracted from cultures of E chrysanthemi or it may be employed to purify L-asparaginase from other sources. Examples include L-asparaginase having amino acid sequences related to that of the Erwinia enzyme. In order to retain a reasonably high specific activity it is desirable to retain a close sequence homology (e.g > 90 , most preferably >95#) with the wild type. The amino acid sequence of the wild type protein is depicted in Figure 1. This process may also be used for purification of L-asparaginase obtained from organisms subjected to transformation or other cloning techniques whereby the E chrysanthemi L-asparaginase gene is linked to systems promoting super-expression. The advantages of the process of the invention are apparent from the following Examples. EXAMPLE 1 - Preparation of Crude Extract 1. Bacterial cell culture. A 12 h seed culture of E chrysanthemi is grown at 37 * C and added to a stirred deep culture vessel in a medium containing yeast extract and sodium glutamate to a total volume of 400 litres, essentially as described by Elsworth et al (1969). The culture is harvested by centrifugation. 2. Extraction of protein from cells. Cell paste from 2.5 cultures are combined and suspended at a concentration of 1.5 g dry weight/100 ml of 6 mM EDTA. The suspension of 300-400 litres is stirred at l6 β C and the pH adjusted 11.3" 11-5 with 0.5 M NaOH. The mixture is stirred for 30 minutes and the pH is adjusted to 6.3 _ 6.7 with 12.5 v/v acetic acid. The precipitate is removed by centrifugation and the supernatant fluid is adjusted to pH 4.8 with 25% v/v acetic acid, then centrifuged to remove the deposit. EXAMPLE 2 - Purification Using a Matrix Bearing Sulphonate Groups Protein extracted from E chrysanthemi by the procedure described in Example 1 is purified as follows: Sodium acetate buffer is prepared by the addition of 25 v/v acetic acid to 4θ mM sodium acetate to pH 4.8. Sodium phosphate buffer, pH 6.0, is prepared by addition of 2 M NaOH to NaH-PO j ,. Absorbance of protein is monitored at 280 nm and cytochrome b-,-- is additionally monitored at 405 nm. The dilute extract at pH 4.8 is applied to a column of S-Sepharose Fast Flow equilibrated with 40 mM sodium acetate buffer, pH 4.8, at a linear flow rate of 300 cm/h. Unbound protein is washed from the column with equilibration buffer at the same linear flow rate. Bound protein, excluding asparaginase, but including cytochrome t _, is eluted from the column with about 20 column volumes of 40 mM sodium phosphate, pH 6.06.2, at a linear flow rate of 300 cm/h. This extensive wash is required to elute all the cytochrome b_^ 2 - L-asparaginase is eluted from the column at a linear flow rate of 100 cm/h with 40 mM sodium phosphate, pH 6.5 - 7-0. Successive fractions were analysed for L-asparaginase activity and the results are shown in the attached Figure 2. Fractions containing L-asparaginase are diafiltered into 20 mM sodium phosphate, pH 6.0, the conductivity reduced to less than 1.5 mS/cm and the solution concentrated and filter sterilised. In an alternative (and preferred) protocol, the pH was increased in a step-wise fashion and the enzyme was found to elute as a narrow peak immediately on introduction of a pH 6.8 buffer (see Figure 3). The results are given in the following Table 1. Table 1. Specific activity Yield (units/mg protein) (%) 17.4 100 19.7 91 88 76 609 70 615 59 /concentration EXAMPLE 3 (Comparative) Protein extracted from E chrysanthemi by the procedure described in Example 1 is purified in accordance with prior art protocols as follows: 1. Adsorption to CM-cellulose. The supernatant fluid (conductivity <6.5 mS/cm) is diluted with demineralised water to a conductivity of about 2.5 mS/cm and stirred at l4°C until all enzyme is adsorbed to 15 Kg CM-cellulose,- previously equilibrated with 40 mM sodium acetate buffer, pH 4.8. Fluid is removed from the suspension by continuous flow centrifugation. The CM-cellulose is washed in the centrifuge with demineralised water and the excess water removed by centrifugation. The cellulose is transferred to a plastic container and the enzyme eluted from the CM-cellulose with 18 litres 4θ mM NaOH containing 1 mM EDTA, pH 10.3. The CM- cellulose slurry is applied to a smaller continuous flow centrifuge and the eluate collected and retained. The CM-cellulose is recovered, added to 18 litres of elution buffer and the pH readjusted to 10.3 with 2M NaOH. The slurry is replaced in the centrifuge and the eluate collected and combined with the first eluate. 2 . Acid precipitation and concentration. The pH of the combined eluates is adjusted to 6.0 with 20% v/v orthophosphoric acid and the pH is checked after a further 45 minutes. The solution is passed through a continuous flow centrifuge, diluted to 80 litres, then concentrated to 30 litres. 45-85 litres of demineralised water is added to reduce the conductivity to below 1 mS/cm and the solution is concentrated to 3 litres. The concentration system is flushed with 7 litres of demineralised water. The concentrate is passed through a 0.5 um filtration membrane and the filtration system is flushed with 2 litres of filtered demineralised water. The solution is concentrated to 2 litres on a smaller system. If the conductivity is greater than 1.3 mS/cm demineralised water is added and the solution is again concentrated to 2 litres. The concentrator system is flushed with up to 1.5 litres of demineralised water. The pH of the solution is adjusted to 6.0 with 20% v/v orthophosphoric acid and if necessary is diluted to reduce the conductivity to below 1.3 ωS. Deposit is removed from the solution by centrifugation. The solution is sterile filtered and toluene added at 1 ml/litre. The above part of the process is repeated to provide sufficient enzyme (about 600 mega units) for the remainder of the process which is carried out under aseptic conditions. All remaining steps are carried out at 3*~ 6 * C unless otherwise indicated. 3. Chromatography on CM-cellulose. Unused CM 52-cellulose is treated with 60% v/v aqueous ethanol, extensively washed with filtered demineralised water and equilibrated against sodium phosphate buffer, pH 6.0. The cellulose is packed into a 25.2 x 60 cm column, washed with at least one bed volume of cooled equilibration buffer, and the extract of 18 litres applied to the column at a flow rate of approximately 4 litre/hour. The column is washed with at least one bed volume of the buffer. The enzyme is eluted from the column with 60 mM sodium phosphate buffer, pH 6.0, and the active fractions collected, filtered through a 0.2 um filter membrane and combined. The combined protein solution is concentrated to 40-60 mg/ml using a hollow fibre system and then adjusted to pH 8.5 with 1 M sodium hydroxide. The results are given in the following Table 2 Table 2 Stage Total enzyme Specific activity Yield (mega units) (units/mg protein) (%) EXAMPLE 4 - Finishing Steps Enzyme purified in the manner described in either of Examples 2 and 3 may be subjected to the following finishing steps: 1. Precipitation with ammonium sulphate. Ammonium sulphate is added to the protein solution to a final concentration of 40% w/v and the suspension stirred for 1-3 h at 18-25 * C. The precipitate is recovered by centrifugation (5986g, 30 min) , ,dissolved in sterile distilled water and diafiltered against sterile distilled water using a hollow fibre system until the conductivity of the solution is in the range of 0.9 to 1.15 mS/cm. The solution is concentrated so the enzyme activity is in the range 65,000 to 85,000 U/ml. The pH is adjusted to 8.7 with 1 M sodium hydroxide and the conductivity to between 1.2 and 1.6 mS/cm with 0.25 M sodium borate buffer pH 8.7- 2. Passage through CM-cellulose. CM 52-cellulose is treated with 60% v/v aqueous ethanol, then equilibrated with 20 mM sodium borate buffer, pH 8.7. and packed into a 25.2 x 45 cm column. The enzyme is applied to the column at a flow rate of approximately 5 litres/hour. The enzyme does not bind, but passes through the column. The active fractions are filtered and combined. 3. Passage through DEAE-cellulose. DEAE 52 cellulose is equilibrated with sodium borate buffer, pH 8.7, and packed into a 25-2 x 60 cm column. The enzyme solution is applied to the column at a flow rate of approximately 6 litres/hour and fractions collected, filtered and combined. 4. Crystallisation. The concentration of the enzyme solution is adjusted to between 25,000 and 35.000 U/ml by dilution with 20 mM sodium borate buffer, pH 8.7. and 0.66 volumes of ethanol is added. The solution is adjusted to pH 8.5 with 1 M acetic acid and the suspension stirred for a further 1 hour at 18-25°C. The precipitate is removed by centrifugation (5968g for 45 mins) , and 0.09 volumes ethanol is added. The solution is stored at -2°C for 24 h before the crystals are resuspended, a further 0.1 volumes of ethanol added and the solution returned to -2 β C for at least 48 h. The supernatant fluid is decanted from the crystals, and the crystals are centrifuged (5986g for 20 min) . The sedimented crystals are dissolved in a minimum volume of sterile distilled water, and dialysed extensively against sterile distilled water at 2-4 β C. The combined dialysed enzyme solution is then made 10 mM with respect to sodium chloride and the resultant bulk enzyme solution frozen at -20°C to await final processing. 5. Preparation of vials A sufficient amount of bulk enzyme solution is thawed and combined to provide material for a batch of 10,000 vials filled to 1 ml. The protein concentration is adjusted to 30 to 50 mg/ml with sterile distilled water, separated into conveniently sized batches, adjusted to pH 6.0 with 1.0 M acetic acid and treated at 18-25 β C with 0.5 volumes Alhydrogel. After stirring for 30 mins. the solutions are centrifuged (5986g for 45 min) to remove the aluminium oxide and the supernatant fluids combined. The solution is adjusted to pH 7-4 with 1.0 M sodium hydroxide and diluted to 14,000 U/ml with sterile distilled water. Sterile sodium chloride and glucose monohydrate are added to final concentrations of 10 mM and 0.5% w/v respectively. The solution is finally diluted with sterile distilled water to give an enzyme activity of 10.500 U/ml and filtered through a 0.2 um positively charged membrane filter into a sterile collection vessel. The sterile bulk product is-filled into 3 ml glass vials, freeze dried and capped and crimpled under 0.5 atmosphere nitrogen. The results are shown in the following Table 4 Table 4 Stage Total enzyme Specific activity Yield (mega units) (units/mg protein) (%) Ammonium sulphate 558 650 (100) precipitation CM-cellulose passage 530 700 95-7 DE-cellulose passage 524 723 94.2 Crystallisation 468 700 84.2 Bulk enzyme 433 700 77-1 Depyrogenation 4ll 700 72.8 It can be seen from Table 1 (Example 2) that the process of the invention achieved a degree of purification resulting in a specific activity >600 units/mg at a yield of 60-70% after only three purification steps (alkaline extract, acid precipitation, adsorption/elution) . On the other hand (see Table 2 Comparative Example 3) an equivalent degree of purification (specific activity >600 units/mg is achieved only after six purification steps (alkaline extract, acid precipitation, CM-cellulose adsorption, acid precipitation, ultrafiltration/concentration, CM-cellulose adsorption). Also in the prior art procedure, in reaching the aforementioned specific activity, the yield had dropped to 40%.

Claims: CLAIMS : 1. A process for producing purified L-asparaginase which comprises (a) contacting a crude extract of L-asparaginase with a solid medium having cation exchange groups so as to adsorb L-asparaginase on the support and (b) eluting adsorbed L-asparaginase from the support, characterised in that the cation exchange groups comprise sulphonate groups and the elution step (b) is carried out at a pH which is higher than the pH used in step (a). 2. A process according to Claim 1 wherein step (b) is carried out at a pH of less than 8.0. 3. A process according to Claim 2 wherein the sulphonate groups form part .of groups of the formula -(CH_) S03 wherein n = 1 to 3« 4. A process according to any preceding claim wherein the support is derived from agarose. 5. A process according to any preceding claim wherein the contacting of the crude extract with the solid medium in step (a) is effected at a pH of from 4.0 to 5.5- 6. A process according to any preceding claim wherein the eluting of adsorbed L-asparaginase in step (b) is effected at a pH of from 6.0 to 7.5 7. A process according to Claim 6 wherein the pH in step (b) is within the range 6.6 to 7-0. 8. A process according to any preceding claim comprising the steps (i) extracting L-asparginase from disrupted cells at a pH of 11.3 to 11.5. (ii) adjusting the pH to within the range 6.3 to 6.7. (iii) separating supernatant from precipitated impurities, (iv) subjecting supernatant from step (c) to adsorption on said solid medium having cation exchange groups, and (v) eluting adsorbed L-asparaginase. 9. A process according to any preceding claim wherein the L-asparaginase subjected to purification has substantially the amino acid sequence of E chrysanthemi L-asparaginase. 10. A process according to any preceding claim wherein the L-asparaginase subjected to purification has at least 90% sequence homology with that amino acid sequence depicted in Figure 1. 11. A process according to Claim 10 wherein the L-asparaginase subjected to purification has at least 95% sequence homology with that amino acid sequence depicted in Figure 1. 12. A process according to Claim 11 wherein the L-asparaginase subjected to purification has at least 99% sequence homology with that amino acid sequence depicted in Figure 1. 13. Aprocess according to any preceding claim wherein the crude extract is produced by culturing a transformed microorganism containing a recombinant plasmid having a DNA insert coding for said L-asparaginase. 14. A process according to any of Claims 1 to 9 wherein the crude extract is obtained by culturing E chrysanthemi . SUB

Inventors: GOWARD CHRISTOPHER RODERICK, GOWARD, CHRISTOPHER, RODERICK
Applicants: HEALTH LAB SERVICE BOARD, PUBLIC HEALTH LABORATORY SERVICE BOARD
Application year: 1991
Main classification: C12N9
IPC codes: C12N9