Title of Invention	PRODUCTION PROCESS FOR RECOMBINANT PLACENTAL GROWTH FACTOR
Abstract	The invention discloses a process for extracting and purifying the recombinant Placental Growth Factor (PLGF) expressed in inducible prokaryotic expression systems comprising the following steps: I) fermentation of the bacterial cells, II) extraction and purification of the inclusion bodies, III) renaturation of the expressed protein, IV) ion-exchange chromatography, V) reverse-phase chromatography.

Title of Invention

PRODUCTION PROCESS FOR RECOMBINANT PLACENTAL GROWTH FACTOR

Abstract

The invention discloses a process for extracting and purifying the recombinant Placental Growth Factor (PLGF) expressed in inducible prokaryotic expression systems comprising the following steps: I) fermentation of the bacterial cells, II) extraction and purification of the inclusion bodies, III) renaturation of the expressed protein, IV) ion-exchange chromatography, V) reverse-phase chromatography.

Full Text	PRODUCTION PROCESS OF RECOMBINANT PLACENTAL GROWTH FACTOR DESCRIPTION Field of the invention The present invention relates to a process for extracting and purifying the recombinant Placental Growth Factor from genetically modified cells. State of Art The Placental Growth Factor {PLGF) is a homodimeric glycoprotein with a structure similar to the Vascular Endothelial Growth Factor (VEGF). The complete polynucleotide sequence codifying the PLGF protein was described by Maglione and Persico in patent EP-B-550 519 (WO-A-92/06194) claiming Italian priority of 27.09.1990. Alternative processes of splicing the ARN of PLGF generate three homologue forms of the Placental Growth Factor, precisely PLGF-1, PLGF-2 and PLGF-3, having different polypeptide sequences, and all described in literature. The above-mentioned patent also describes a method for producing the PLGF factor comprising the use of an inducible prokaryotic expression system characterised by host cells modified with an expression vector, in which the human PLGF gene is integrated under the control of an inducible promoter (directly or indirectly). After inducing the PLGF expression with appropriate activator, the cells are incubated, isolated and submitted to lysis. The so-obtained raw lysate is a complex mixture of proteins containing low quantities of the expressed PLGF protein and having low specific activity. In fact, in the known process, the protein expression is induced in cultures containing low cellular density, as it is evident from the low optical density at time of induction, that is between 0.2 and 0.6 OD at 600 ran. Furthermore, the process described in the preceding document does not comprise additional purification stages of the expressed protein. For this reason, the lysates obtained according to the application WO-A-92/06194 are inappropriate as such to be used directly in the preparation of medicaments. A more complex method for purifying the same placental factor is envisaged by Maglione et al. in "I1 Farmaco" 55 (2000), pages 165 to 167. Nevertheless, the method disclosure merely gives a simple listing of known applicable techniques, without describing conditions and experimental details thereof, which are essential for obtaining the PLGF protein in the purity and quantity necessary for a pharmaceutical use. The scope of the present invention is to provide a new method for extracting and purifying the recombinant PLGF expressed in bacterial cells, allowing to obtain PLGF at high level of purity and with yields suitable to be industrially used in the preparation of medicaments. A further scope of the invention is to obtain the PLGF protein in essentially active form (greater than 98.5%), that is mainly composed by dimeric (not less than 70%) and multimeric forms and containing residues of the monomeric form (little or not active) not greater than 1.5%. Summary of the invention The invention is based upon the identification of a sequence of purification techniques particularly appropriate for the extraction and purification of human PLGF expressed in bacterial cells. The invention is further based upon the determination of the optimum operative conditions with respect to the single techniques and to the chemical-physical features of the substance to be purified. Then, object of the present invention is a process for extracting and purifying the recombinant Placental Growth Factor (PLGF) expressed by means of an inducible prokaryotic expression system comprising the steps of: I) fermentation of the bacterial cells, II) extraction and purification of the inclusion bodies, III) renaturation of the expressed protein, IV) ion-exchange chromatography, V) reverse-phase chromatography, and optionally VI) final stages of ultrafiltration, formulation and lyophilization. According to such method, the fermentation (step I) is performed until obtaining a high bacterial density in the medium, as it is shown by the high optical density in the medium, before proceeding with the induction step. The step (II) comprises bacterial lysis, rupture of DNA and isolation of the inclusion bodies. The renaturation of the expressed protein (step III) is obtained by solubilizing the inclusion bodies in denaturant buffer, and by transforming, at least partially, the expressed protein in the dimeric form. At last, in the step (IV) and (V) the dimeric and multimeric forms of the expressed protein are separated from the monomeric form and isolated in pure form, to be subsequently ultrafiltrated and lyophilised in presence of usual lyophilisation and formulation additives. A specific object of the invention is the above- mentioned process for extracting and purifying the PLGF-1 protein of human origin, but substantially valid also for PLGF-1 of animal origin. The claimed process advantageously allows the obtaining of production yields of expressed protein from 30 to 50 times higher than the yields obtained according to the method described in the preceding state of art. The claimed process furthermore allows the obtaining of the highly pure protein, with high specific activity and in substantially dimeric form. Further object of the invention is the active Placental Growth Factor obtainable by means of the process of the invention, free from any residual protein or other bacterial contaminant and containing residues of monomeric form not higher than 1.5%. Description of the accompanying drawings Figure 1: The figure shows the results obtained by electrophoresis SDS-PAGE under reducing conditions for monitoring step I. Prel and Pre2 represent the pre- induction checks, prepared as follows. Soon before the induction, about 0,064 units of optical absorption measured at 600nm (OD600) are taken and diluted 5 times with water. Of this dilution 2 0 ul are taken which are added to 2 0 ul of reducing buffer and submitted to boiling. 20 ul of this last solution are loaded onto the SDS PAGE matrix. Postl and Post2 represent the post- induction checks prepared as above. M designates the mixture of markers of molecular weight. In the post- induction columns (Postl and Post2) a band is noted just above the indicator of molecular weight 14.3 substantially absent in the pre-induction columns (Prel and Pre2) corresponding to the PLGF-1 protein expressed and segregated within the inclusion bodies. Figure 2: The figure shows the monitoring chromatogram of the anionic-exchange chromatography on Q- Sepharose Fast Flow resin. X-axis shows the elution volume (ML), y-axis shows the optical absorption units (OD) . The first elution peak obtained by eluting by 20% with buffer B (NaCl 200 mM) corresponds to the PLGF-1 protein in substantially dimeric form, but it comprises impurities and the monomeric form. The following peak, eluted by 100% with buffer B (NaCl 1M) contains impurities which are eliminated. Figure 3: The figure shows the monitoring chromatogram of the first elution stage in reverse-phase chromatography on RP Source 3 0 resin. X-axis shows the elution volume (ml), y-axis shows the optical absorption units (OD). The first abundant elution peak corresponds to the various impurities, which do not bond to the resin. The second elution peak corresponds to the PLGF protein in monomeric form eluted under isochratic conditions (experimentally found at about 10%-15% of buffer B). Figure 4: The figure shows the monitoring chromatogram of the second elution stage in reverse-phase chromatography on RP Source 3 0 resin. X-axis shows the elution volume (ml), y-axis shows the optical absorption units (OD) . The elution peak corresponds to the PLGF protein in dimeric-multimeric form. Figure 5: The figure shows the results obtained in electrophoresis on SDS-PAGE for the final monitoring of the whole process. Prerefol and Postrefol represent the checks preceding and following the renaturation of the expressed protein (step III) . QFF represents the peak eluted from the Q Sepharose fast flow resin, containing the protein mainly in dimeric form. Mon represents the peak containing the monomeric form. Dim represents the peak eluted in the second substep of the reverse-phase chromatography on RP Source 30 resin. It is noted that before the renaturation, the expressed protein is mainly in monomeric form. After the renaturation, part of the protein is in dimeric form. The following purification on QFF and RF 30 chromatography allow the obtaining of PLGF- 1 protein with high purity degree. Detailed description of the invention The genetic modification of the bacterial host cells is described by Maglione et al. in the preceding patent EP-B-0550519 (WO-A-92/06194) . For this purpose, bacterial cells are transformed introducing of an expression vector comprising an insert corresponding to the" human gene coding for PLGF-1 factor. The complete gene sequence is known in literature and it is freely accessible. A plasmid containing such sequence was deposited with the ATCC under accession number ATCC No 40892. The expression is performed under the control of the system of RNA polymerase of T7 phage and it is induced with IPTG (isopropyl-ß-D-tiogalactopyranoside). Nevertheless, other inducible prokaryotic expression systems may be utilised. Examples of such systems, obtainable on the market, are represented by: 1) pBAD expression system (In vitrogen BV) wherein the synthesis of a protein is placed under the control of the araBAD promoter and it may be induced in different strains of E.Coli by means of arabinose. 2) T7 Expression System (In vitrogen BV or Promega) wherein the synthesis of a protein is controlled by the promoter of RNA polymerase of T7 phage and it may be induced by means of lactose or the analogues thereof (IPTG) . In this case it is required the use of E.Coli derivatives of DE3 (B12KDE3) or JM109(DE3)) type containing, namely, a copy of the gene of Rna polymerase of T7 phage placed under the control of a lactose- inducible promoter. 3) Trc expression system (In vitrogen BV) wherein the synthesis of a protein is placed under the control of the trc hybrid promoter. Such promoter has been obtained by melting the trp promoter and the lac promoters and it may be induced in different strains of E.Coli by means of lactose or the analogues thereof (IPTG). 4) Tac expression system (Amerham biosciences) wherein the synthesis of a protein is placed under the control of the tac promoter. In this system the protein synthesis is induced in strains of E.Coli laclq (type JM105) by means of lactose or the analogues thereof (IPTG) . 5) Px, expression system wherein the synthesis of a protein is placed under the control of the PL promoter and it may be induced by adding tryptophan. In this case it is required the use of E.Coli derivatives (GI724) containing a copy of the codifying gene for the cI repressor of the Lambda phage placed under the control of a tryptophan-inducible promoter. Step I: Fermentation and induction The first stage of the claimed process consists in the fermentation of a functionally-modified bacterial strain equivalent to the strain described in the preceding European patent (above). In a preferred embodiment the micro-organism is a derivative of Escherichia Coli modified with an expression plasmid comprising the human gene of PLGF. A preferred micro- organism is the one called [B12(DE3)pLysS PLGF-1] obtained by integrating in the commercially available strain [B12(DE3)pLysS] (Promega Corporation USA) the gene of the human PLGF-1. The present invention, nevertheless, is not limited to the human PLGF-1 factor, but it also relates to the one of animal origin (monkey, mouse, rabbit etc.). The present invention is not limited so much the less to the use of a E. Coli derivative, but it includes the use of any prokaryotic micro-organism susceptible to be genetically modified and able to express heterologous proteins under the form of inclusion bodies. The strains utilised as inoculum in the process of the invention are kept before using them in the lyophilised form to preserve the expression capacity thereof. Upon use, the lyophilised material is brought again in solution by utilising an appropriate buffer. Although there is a wide range of known culture media available on the market and which may be effectively used, the fermentation step according to the invention is preferably performed in a medium free from any material of animal or human origin in order to avoid any infection risk. Yeast"s extracts (Difco) added with one or more suitable antibiotics represent the most suitable means for the process. In the preferred embodiment a medium is used which has been obtained by mixing under sterility conditions a first solution (A) containing yeast"s extracts, glycerol and ammonium sulphate with a second solution- (B) containing a phosphate buffer. The mixture is then integrated with ampicillin and chloramphenicol or equivalent antibiotics. Appropriate antibiotic concentrations are from 50 to 300 ug/ml of ampicillin, preferably from 100 to 200 ug/ml and from 10 to 100 ug/ml of chloramphenicol, preferably from 30 to 40 ug/ml. The fermentation step may be preceded by a preinoculum step wherein the lyophilised micro-organism is suspended in the medium and submitted to consecutive incubation and dilution steps aimed at having in culture the optimum quantity of micro-organism cells. Preferably, the micro-organism is incubated for one night at 37°C, then diluted and incubated again for some hours. The chosen pre-inoculum volume is subsequently centrifuged, suspended again in the culture solution enriched with ampicillin and inoculated in the fermentation vessel for the fermentation step. The fermentation is performed in the above-mentioned medium added with ampicillin and chloramphenicol at the temperature suitable for the micro-organism, usually at about 37°C, in presence of a percentage of dissolved 02, with respect to the saturation with air, from 20% to 40%, preferably 30%. The pH during fermentation is kept at neutral or weakly acid values (6.4 to 7.4). Furthermore, since the fermentation process takes place under stirring, antifoam agents are preferably to be used. The fermentation progress is accompanied by the increase in the optical density of the medium. For this reason, the optical density is the parameter utilised according to the invention to monitor the progress degree of the fermentation. Readings at 600 nm are particularly appropriate. Essential feature of the invention is the high cellular density achieved in the culture at time of the expression induction. Optical densities at 600 nm (OD600) from 1 to 50 may be achieved thanks to culture media of the invention. Densities higher than 18, nevertheless, are preferred to obtain the high production levels typical of the claimed method. Densities between 16 and 2 0 are particularly preferred to induce the producing bacterial strain and gave optimum results. The fermentation, then, is kept at the above-mentioned conditions until achieving such values of optical density, then one proceeds to induce the protein expression. Any agent or chemical-physical condition able to induce in the cells of the used micro-organism the machinery of expression of the heterologous protein may be advantageously utilised. In the specific case wherein the bacterial strain BL21(DE3)pLysS modified with an expression plasmid containing the promoter of 11 phage is used, the expression is induced with lactose or the derivatives thereof, such as isopropyl-b- tiogalactopyranoside (IPTG) with a proper concentration, namely about l mM. The induction duration may vary according to need. Good results are obtained for periods of some hours, preferably from 3 to 4 hours; in the optimum process the induction is kept for 3 hours and 2 0 minutes by using a percentage of dissolved 02 equal to about 10%. Cell samples are taken before and after induction and submitted to analytical techniques of control such as electrophoresis on SDS-PAGE, to determine the induction outcome. When the protein expression reaches the desired levels, the culture is centrifuged and the cells are moved to the following step. Step II; Extraction and purification. The expressed heterologous protein in bacterial strains is segregated inside the cell itself in the form of inclusion bodies. Therefore, the process of the invention provides passages of lysis of the cells, rupture of the extracted nucleic material (DNA) and recovery and washing of the inclusion bodies. The cells are washed, although not necessarily, and suspended in solutions containing emnulsifier agents in appropriate concentration, preferably Triton X100 in concentrations from 0.5% to 1%, then they are submitted to lysis of the cellular membrane. The lysis process may be performed by means of freezing/thawing, French Press, sonication or other similar known techniques. Nevertheless, the preferred, method for the bacterial strain BL21(DE3)pLysS is the freezing/thawing method, which in the most preferred embodiment is repeated at least for two consecutive cycles. After the mechanical lysis, the lysis stage is continued for a few minutes in the lysis solution at room temperature under stirring. The release in the lysis medium of the inclusion bodies is accompanied by the release of micro-organism different components and cellular substances, above all the nucleic materials. These substances could interfere with and jeopardise the following protein purification process. Therefore, the suspension/solution obtained by lysis is submitted to rupture of such nucleic material, specifically DNA, by means of enzymatic agents such-as DNAse (natural or recombinant such as the Benzonase), chemical agents, such as deoxycholic acid, or physical- mechanical agents, such as sonication or high energy stirring by means of blades, for example, in a mixer. The rupture of DNA, carried out for example in a mixer, is performed on lysed cells re-suspended in appropriate volumes of washing solutions containing chelating and deterging agents, for example EDTA and Triton X100. It is preferably repeated for more cycles, preferably 2, alternated with stages of dilution, in washing solution, centrifugation and elimination of tne supernatant in order to remove components and cellular substances from the fraction containing the inclusion bodies. Step III Renaturation (refolding) of the protein The fraction containing the purified inclusion bodies of PLGF-1 is then solubilised in denaturing buffer containing known denaturant agents such as urea, guanidine isothiocyanate, guanidine-hydrochloride. Preferably, the denaturant solution is a urea solution in denaturant concentration, for example 8M. In order to accelerate the solubilisation process, the fraction may advantageous be submitted to homogenisation or sonication. After solubilizing the inclusion bodies, the solution is diluted with the same denaturant buffer until obtaining an optical density measured at 280 nm of about 0,8 (OD280 0.8). Subsequently, the solution is further diluted with a dilution buffer until 0.5 OD280. Suitable dilution solutions contain salts and polyethylene glycol (PEG) and have basic pH (about 8) . The renaturation of the PLGF-1 protein in diluted solution is obtained by adding to the solution appropriate concentrations of oxidising/reducing pairs, followed by an incubation of 10 to 30 hours, preferably 18 to 20 at a temperature of 10°C to 30°C, preferably 20°C, under stirring. Examples of such pairs are: Cystine/Cysteine, Cystamine/ Cysteamine, 2-hydroxyethyldisulphide/2-mercapto-ethanol. Preferred example of oxidising/reducing pair is the glutathione in its oxidised and reduced forms, respectively at concentrations between 0.1 mM and 2.5 mM (preferably 0.5 mM) and between 0.25 mM and 6.25 mM (preferably 1.25 mM). By means of renaturation, the PLGF-1 protein expressed essentially in monomeric form is partially brought back to the dimeric form (Figure 5). Step IV: anionic-exchange chromatography The solution coming from the preceding step, preferably through centrifugation and/or filtration and containing the protein in mainly monomeric and partially dimeric form, is loaded onto anion-exchange resin in order to enrich the mixture with the dimeric form and to purify it from bacterial contaminants. Any commercially available matrix suitable for anion-exchange chromatography may be likewise used to the extent that its features of capacity, loading and flow speed be similar to those of the Q Sepharose Fast Flow resin (Amersham biosciences) , apart from being suitable for an industrial process. In a preferred embodiment a high-flow resin is used, for example Q-sepharose Fast Flow (Amersham biosciences) or equivalent. The resin is washed and equilibrated with solutions having low ionic strength. An example of such solution comprises ethanolamine-HCl pH 8.5 with.low or absent salt content. The same solution may be utilised for loading, absorbing and washing the protein mixture to be purified. The used resins allow loading of large volumes of protein solution with ratios Volume loaded/Volume column varying from 1:1 to 10:1. Ratios Vol./Vol. next to 10:1 are preferred since they allow optimising the use of the column. However, ratios higher than 10:1 are to be avoided since, due to the saturation of the adsorbing capacity of the matrix, they lead to high loss in the dimeric form of the protein. Whereas the PLGF-1 protein in monomeric form already percolates in the stages of washing with low ionic strength, the elution of the dimeric and multimeric forms is obtained by increasing the ionic strength of the starting solution. Such increase is obtained by mixing the equilibration solution with increasing and pre- established percentages of a second solution containing NaCl 1M. In a preferred embodiment, the protein in dimeric form is eluted with solutions containing from 15% to 25% of NaCl 1 M solution, which corresponds to a NaCl concentration from 150 to 250 mM. In the best embodiment, the protein is eluted in isochratic conditions at NaCl concentration of 200 mM. The elution of the various species is automatically monitored by measuring the optical absorption at 280nm (figure 2) . The collected fractions containing the PLGF-1 protein in dimeric form are subsequently controlled by electrophoresis SDS-PAGE (figure 5). Advantageously, the whole chromatography process is automatically performed by a computerised system operating under the control of a suitable programme, for example the Software FPCL Director system (Amersham biosciences). Step V: Reverse-phase chromatography The fractions coming from the preceding step containing the PLGF-1 protein enriched with the active forms are collected, diluted with appropriate buffer and loaded onto an reverse-phase chromatography column in order to further purify the protein in active form. The quantity of loaded solution corresponds to OD280 between 4.5 and 5.5 per millilitre of chromatographic matrix. Such quantities are to be considered maximum quantities. Any commercially available chromatographic matrix suitable for the intended use may be utilised to the extent that its features of loading capacity and flow speed are compatible with the process requirements. In a preferred embodiment, a resin is used having such bead- sizes so as to guarantee the best exploitation of the absorbing capability together with the easiness in packing the column itself. Examples of such matrixes are the RP Source 15 or RP Source 30 (Amersham biosciences) resins. All the solutions for equilibration, loading, resin washing and elution are hydro-organic solutions comprising different percentages of organic solvent. Examples of such solutions are solutions comprising ethanol, methanol or acetonitrile. Preferably, hydro- alcoholic solutions comprising increasing percentages of ethanol are utilised. In an embodiment of the invention appropriate quantities of two buffer solutions are mixed, the former comprising buffer A, i.e. ethanol 40% and TFA (trifluoroacetic acid) 0.1%, the latter comprising buffer B, i.e. ethanol 70% and TFA 0.1%. The protein material loaded onto the resin and properly washed is then eluted through an elution process comprising two subsequent stages wherein elution solutions containing an increasing gradient of organic solvent are utilised. The first stage is performed under conditions of rising gradient of organic solvent until obtaining the elution peak of the monomeric form. Such gradient is obtained by adding the buffer B to the buffer A in percentages from 4% to 40%, with an increasing rate of buffer B of 3% for each eluted column volume. As soon as the elution peak corresponding to the monomeric form of the protein appears, the elution is continued under isochratic conditions until. exhaustion of the elution peak of the monomeric form. The so-set isochratic conditions cause the largest possible separation of the chromatographic peaks corresponding to the two monomeric and dimeric forms and, then, the best obtainable resolution for a process of industrial, and not analytical type. The second stage is performed again under condition of increasing gradient of organic solvent until whole elution of the protein mainly in dimeric form is achieved. In this second stage, the gradient is obtained by adding the buffer B to the buffer A in percentages from 10% to 100%, with an increasing rate of buffer B of 40.9% for each eluted column volume. The elution of the various forms of PLGF-1 protein is automatically monitored by measuring the optical absorption at 280nm (figure 3 and figure 4) . The collected fractions containing the PLGF-1 protein essentially in dimeric form are subsequently controlled by electrophoresis SDS-PAGE (figure 5) . Advantageously, the whole reverse-phase chromatography process is automatically performed by a computerised system operating under the control of a suitable programme, for example the Software FPCL Director system (Amersham biosciences). The results of the electrophoresis show that PLGF-1 protein obtained from the second stage of the reverse- phase chromatography is in highly pure active form, namely it comprises the protein in dimeric and partially multimeric form, but it is essentially free from any contamination of the monomeric form. The so-obtained product comprises not less than 98.5% of active form, preferably not less than 99.5%, wherein not less than 70% is in dimeric form. The residual of monomeric form is not higher than 1.5%. The protein in active form is obtained in average amounts of 160 mg per litre of bacterial culture. The pure protein obtained according to the above-described method may be submitted to additional working stages such as ultrafiltration on membrane. In this case the product is filtered on membrane having cut- off limit lower than, or equal to 3 0kD and it is submitted to diafiltration against TFA acidulated water until a dilution factor of 1:106. The so-obtained final product may be properly formulated with lyophilisation additives and lyophilised to keep its best biological activity. The invention is here below described by means of examples having, however, only illustrating and not limiting purposes. Example 1: Fermentation The following procedure relates to the method of fermentation and induction of the genetically modified micro-organism (MOGM) [B121(DE3)pLysS PlGF-1] in a fermentation vessel using 1 mM IPTG. Materials: Solution SBM constituted by: Solution A (per 1 litre) Bacto yeast extract(Difco) 34 g Ammonium sulphate 2 .5 g Glycerol 100 ml H20 q.s. at: 900 ml Solution B (10 X)(per 100 ml) KH2PO4 1.7 g K2HPO4 -3H2O 20 g, or K2HPO4 15.26 g H20 q.s. at 100 ml The solutions A and B are separately autoclaved and mixed upon use under sterile conditions. Alternatively, the solutions A and B are mixed and filtered under sterile conditions. IPTG 200mM (200X) is produced by dissolving 5 g of pure substance in 100 ml of distilled water. The solution is filtered by means of 0.22-um filters, subdivided into aliquots and frozen at -20°C. The utilised antifoam agent is Antifoam O-10 (not siliconic) Sigma Cat A-8207. The used bacterial strain is [BL21pLysS PlGF-1 WCB] (working cell bank). Preinoculum: A tube of lyophilised genetically modified micro-organism (MOGM) WCB is taken and it is suspended in 1 ml of SBM + 100 ug/ml Ampicillin + 34 ug/ml of chloramphenicol. The suspension is diluted in 3 0 ml of SBM + 100 ug/ml Ampicillin + 34 ug/ml of chloramphenicol. The suspension is incubated at 37°C for one night (O/N) . The day after the 3 0 ml of the O/N culture are diluted in 800 ml of SBM + 100 ug/ml Ampicillin + 34 ug/ml of chloramphenicol and they are subdivided into 4 1-liter Erlenmeyer flasks, each containing 200 ml. The content of each flask is incubated at 37°C for 24 hours. The content of the 4 flasks is mixed and the OD600 are read by diluting 1/20 in water (50 ul + 950 ul of water). An established volume of preinoculum is then centrifuged for 10 min. at 7.500 x g at 4°C in sterile tubes. The bacteria are then re-suspended in 20 ml of SBM + 200 ug/ml of Ampicillin + 10 ug/ml chloramphenicol per each litre of fermentation by stirring at 420 rpm at R.T. for 20 minutes. At the same time the fermentation vessel is prepared and the oxygen probes are calibrated. The oxygen probes are calibrated at 37°C temperature at 0% with nitrogen, then at 100% with air without antifoam under stirring at 600 RPM. The fermentation is carried out under the following experimental conditions: Medium: SBM + 200ug/ml of ampicillin and 10 ug/ml of chloramphenicol Temperature: 37°C % dissolved 02: 30% (with respect to saturation with air) pH: from 6.4 to 7.4. Antifoam: 1:10 is diluted in water; strongly stirring before adding it in quantities of 140 ul per 750 ml of medium. Induction: The induction is carried out under the following experimental conditions: OD600 of induction: 16-20. Inducing agent: IPTG lmM final. % dissolved 02: 10% (with respect to saturation with air). Induction length: 3 hours and 2 0 minutes. Just before the induction 2 0 ul of bacteria are taken, added to 80 ul of water and kept for the pre- induction check. At time of induction, IPTG is added to the final concentration of 1 mM. The percentage of dissolved 02 is brought to 10%. At the end of the induction the final OD600 are read and the overall volume is measured. Then, 10 ul of bacteria are taken, added to 90 ul of water and kept for the post-induction check. The induction is controlled by way of a SDS-PAGE electrophoresis by loading 20 m1 of the 2 previously boiled samples. The medium containing the induced bacteria is then centrifuged at 7.500 x g for 10 min. or at 3000 x g for 25 min. at 4°C and the supernatant is eliminated. Results: The induction results are checked by SDS- PAGE electrophoresis as shown in figure 1. Example 2: Extraction and purification of the inclusion bodies. The following procedure relates to the preparation and refolding of the inclusion bodies of PlGF-1. By means of refolding the PLGF-1 bacterial protein is partially brought back to the dimeric form. Material: Mixer with appropriate capacity. Lysis solution: 1 mM Mg2SO4 + 20mM Tris-HCl pH8 + Triton X100 by 1%. Washing solution: 0.5% triton X100 + 10 mM EDTA pH 8. BD (denaturing buffer): 8 M urea, 50 mM Tris pH 8, Ethylenediamine 20mM. Dissolving and bringing to volume in H2O. Oxidised glutathione 200x: 100 mM in H2O; Reduced glutathione 20Ox: 25 0 mM in H2O. Dilution buffer: 600 uM final PEG 4000 (2.4g/l), 50 mM Tris-HCl pH 8, 20 mM NaCl. Antifoam: Antifoam O-10 (not siliconic) Sigma. Preparation of the PLGF-1 inclusion bodies. The lysis and washing solutions are equilibrated at room temperature (RT). Two cycles of freezing/thawing at -80/37°C are performed. The bacterial pellet is lysed in 1 ml of lysis solution per each 450 OD600 of bacteria. It is then incubated at RT 3 0 min. under stirring (250 RPM). The solution is poured into a mixer with appropriate capacity and a quantity of washing solution of 3 ml for each 450 OD600 of bacteria is added. If necessary, 0.4 ul of not-diluted antifoam per each millilitre of sample are added. The solution is spun at the maximum speed for 1 minute or until the sample is well homogeneous. The content of the mixer is then transferred into a container with appropriate capacity and 6,5 ml of washing solution per each 450 OD600 of bacteria are added. It is incubated for 45 min. at RT under stirring. The so-obtained suspension is centrifuged at 13.000 x g for 45 min. at 25°C and the supernatant is discharged. The settled pellet is re-suspended in 4 ml of washing solution per each 450 OD600 of bacteria and the cycle in the mixer is repeated for the second time. The suspension is transferred into a container with appropriate capacity, diluted with 6.5 ml of washing solution per each 450 OD600 and incubated for 30 min. at RT under stirring. The centrifugation under the above seen conditions is then repeated and the supernatant is eliminated. Example 3: Renaturation of the protein. The inclusion bodies are solubilised in 7 ml of denaturing buffer BD (containing urea 8M) and further diluted in BD until OD280 of 0,8. Subsequently, 0.6 volumes of dilution buffer are added in order to bring the final urea concentration to 5M. Afterwards 1/200 of reduced glutathione 200X (final concentration of 1,25 mM) and 1/2 00 of oxidised glutathione 200X (final concentration of 0.5 mM) are added. A 15 ml sample for checking (prerefol) is taken and the solution is then incubated at 20°C for 18-20 hours under stirring. At the end of the incubation, the medium is centrifuged for 10 min. at 20°C, 10.000 x g, filtered by means of 0.45 or 0.8 mm filters and a 15 ml sample is taken for checking (postrefol). Results: The 15-ml samples of the pre,- and post- refolding solutions are analysed by means of SDS-PAGE electrophoresis (figure 5). Example 4: Anion-exchange chromatography The following procedure relates to the first step of purification of the PlGF-1 protein after refolding. Upon loading of the sample onto the column, there will be a high loss of not-absorbed PlGF-1 monomer. The loaded quantity must not exceed 10 times the volumes of the column, since this would cause a significant loss in the PLGF-1 dimer. The elution is performed under isochratic conditions at 20% of buffer B (see below) , which corresponds to a NaCl concentration of 200 mM. The eluted peak still contains the glutathiones .used for refolding, which contribute by about 50% of OD280. Material and parameters: FPLC system: Amersham-biosciences handled by the software called FPLC Director. Monitoring parameters U.V.: Wavelength = 280 nm; scale top - 2. Temperature: 20°C (minimum 15, maximum 25) Resin: Q-sepharose Fast Flow (Amersham- biosciences) . Column volume/height: Volume: 1/10 of volume of the sample to be loaded; height: between 13 and 16 cm. Equilibration: 2 Column Volume (CV) of buffer B, then 1.5 CV of buffer A. Sample: Renatured, centrifuged and/or filtrated PlGF-1. Load no more than 10 CV thereof. Buffer A: 20 mM Ethanolamine-HCl pH 8.5. Buffer B: Buffer A + 1M NaCl. Injection speed: 1 cm/min (maximum speed tested on small columns = 1.887 cm/min; minimum tested speed = 0.5 cm/min.). Elution speed: 1 cm/min (maximum speed tested on small columns = 1.887 cm/min; minimum tested speed = 0.5 cm/min.). Washings after injection: 1.5 CV with 0% of buffer B. Peak collected: Peak eluted at isochratic conditions at 20% of buffer B, running for about 3 CV. Final washing: 2 CV at 100% B. Procedure: The peak eluted under isochratic conditions at 20% of buffer B is collected, then 0.271 water volumes, 0.0045 TFA volumes and 0.225 ethanol volumes are added thereto. In this way the sample results to be diluted 1.5 times and contains 15% ethanol and 0.3% TFA. The addition of these 2 substances facilitates the bounding of PlGF-1 to the reverse-phase resin (see example 5). Results: The chromatography step is continuously- controlled by monitoring the optical densities at 280 nm as illustrated by figure 2 . The purity of the isolated protein material is analysed by means of SDS-PAGE electrophoresis (figure 5). Example 5: Reverse-phase chromatography. The following procedure may be performed with RP source resin with 15 micron or 30 micron average particle diameter. However, the 30-micron RP source resin, while not involving any alteration in the purification process, allows an economical saving of the resin itself (about 50%) , a greater easiness in the packaging procedure of the column and a lower backpressure. The procedure relates to the second phase of the purification of the PlGF-1 protein after passing on the QFF resin. During the sample injection, a high adsorbance is apparent and corresponds to the not adsorbed peak of the glutathiones which do not bound to the resin. This procedure consists of 2 sub-stages, the former called RPCmon, is used to eliminate most of the monomeric component of PlGF-1, whereas the latter is used to elute the essentially dimeric component of the protein and it is called RPCdim. First sub-stage (RPCmon) Material and parameters: FPLC system: Amersham-biosciences handled by the software called FPLC Director. Monitoring parameters U.V. : Wavelength = 280 nm; full scale = 0.05. Temperature: 20°C (minimum 15, maximum 25) Resin: Reverse Phase Source 3 0 (Amersham- biosciences) . Resin volume/height: Volume: 1/5 - 1/6 of the overall OD280 of the sample to be loaded; height: between 27 and 33 cm. Equilibration: 2 Column Volume (CV) of buffer B, then 2 CV of buffer A. Sample: P1GF-1 coming from the preceding step (example 4), diluted 1.5 times and containing ethanol 15% and TFA 0.3%. Loading max. 4.5 to 5.5 OD280 per ml of resin. Buffer A: Ethanol 40% + TFA 0.1%. Buffer B: Ethanol 70% + TFA 0.1%. Injection speed: 1.887 cm/min. Elution speed: 1.887 cm/min. Washings after injection: 1.5 CV with 4% buffer B. Monomer peak: Gradient ranging from 4 to 40% of B in 12 CV (3%B/CV) . Just after starting the elution of the peak, by OD280 reaching 25% of the full scale, the elution is continued with isochratic conditions with the buffer B concentration reached in that moment until the peak elution is complete (about 2.5 -3.5 CV). Operations A suitable quantity of the solution corresponding to the "monomer" peak is taken and it is concentrated for checking (mon in Fig. 5). Second sub-stage (RPCdim) Material and parameters: Without re-equilibrating the column, but by simply shifting the scale range of the UV monitor to the value 2, a gradient ranging from 10 to 100%-of the buffer B is run in 2.2 CV (40.9%B/CV). Operations: The fractions corresponding to the "Dimer" peak are taken. Figure 4 illustrates an example thereof. They are collected and the volume and the optical density at 280 nm are measured. The overall yield (expressed in mg) obtained before the lyophilisation is calculated by multiplying the OD280 times the volume times the dilution. The average value of such yield is 164 mg of pure PLGF-1 per litre of bacterial culture with a standard deviation of 23.21. It may also be expressed in mg per 1000 OD600 of fermented bacteria, resulting to 5.58 mg of pure PLGF-1 each 1000 OD600 of fermented bacteria with a standard deviation of 0.8. The so-obtained dimer solution is kept at -2 0°C until ultradiafiltration and lyophilisation. A sample of such solution is submitted to SDS-PAGE electrophoresis as illustrated in figure 5. We claim : 1. A process for extracting and purifying recombinant Placental Growth Factor (PLGF) in dimeric and multimeric active form containing no more than 1.5% of monomeric form, by expression in an inducible expression system in modified prokaryotic cells such as herein described comprising the following steps: I) fermentation of the prokaryotic cells, II) extraction and purification of the inclusion bodies, III) renaturation of the expressed protein, IV) ion-exchange chromatography, V) reverse-phase chromatography, characterised in that step (I) is performed until obtaining optical density of the culture medium from 14 to 50 at 600 nm (OD600 14- 50) followed by induction, that step (II) comprises lysis of the culture cells, rupture of the DNA and isolation of the inclusion bodies, that in step (III) the inclusion bodies are solubilised into denaturing buffer and the expressed protein is brought, at least partially, back to the dimeric form, that in step (IV) the dimeric and multimeric forms of the expressed protein are separated from the monomeric form by anion exchange chromatography that in step (V) the dimeric and multimeric forms of the expressed protein are further separated from the monomeric form by reverse-phase chromatography with two subsequent elution stages with increasing gradient of organic solvent separated by an elution stage under isochratic conditions and finally isolated. 2. The process as claimed in claim 1, characterised in that the Placental Growth Factor (PLGF) is human PLGF-1 or of animal origin. 3. The process as claimed in claim 1 or 2 characterised in that the prokaryotic cells are bacterial cells. 4. The process as claimed in any of the claims 1 to 3, characterised in that step I is performed in a medium allowing the obtaining of a high bacterial density in the fermentation step and free of any material of animal or human origin. 5. The process as claimed in any of the preceding claims, characterised in that step I is performed in a medium comprising one or more selection agents, yeast extract, glycerol and ammonium salts. 6. The process as claimed in any of the preceding claims, characterised in that the inducible expression system is the expression system 77. 7. The process as claimed in any of the preceding claims, characterised in that the bacterial cells are a strain derived from E.Coli. 8. The process as claimed in any of the preceding claims, characterised in that the bacterial strain is E. Coli {B121(DE3)pLysS}. 9. The process as claimed in any of the preceding claims, characterised in that the expression is induced by means of lactose, isopropyl-P-D- thiogalactopyranoside (IPTG) or functionally equivalent analogues. 10. The process as claimed in any of the preceding claims, characterised in that the optical density of the culture at time of the induction is 14 to 30 OD at 600 nm (14-30 OD600), preferably 16 to 20 (16-20 OD600). 11. The process as claimed in any of the preceding claims, characterised in that step I comprises a preliminary step of preinoculation. 12. The process as claimed in any of the preceding claims, characterised in that in step II the cell lysis is performed by means of freezing/thawing, French Press or other equivalent techniques. 13. The process as claimed in any of the preceding claims, characterised in that in step II the DNA rupture is performed by means of DNAse of extraction or recombinant origin, preferably the benzonase, or by chemical-mechanical action. 14. The process as claimed in any of the preceding claims, characterised in that in step II the DNA rupture is performed by means of a mixer. 15. A process as claimed in any of the preceding claims, characterised in that in step II the inclusion bodies are isolated by means of at least two cycles of centrifugation and washing into a suitable buffer. 16. The process as claimed in any of the preceding claims, characterised in that in step III the inclusion bodies are solubilised into denaturing buffer containing urea, guanidine isothiocyanate, guanidine-hydrochloride or any other denaturing agent and are optionally homogenised or sonicated. 17. The process as claimed in any of the preceding claims, characterised in that in step III, after the solubilisation of the inclusion bodies, the solution is diluted and the protein material is renatured by adding to the solution oxidising/reducing agents and by incubating for 10 to 30 hours, preferably 18 to 20 at temperature 10°C to 30°C, preferably 20°C under stirring. 18. The process as claimed in claim 17, characterised in that the solution is diluted until obtaining an optical density at 280 nm (OD280) from 0.01 to 2, preferably 0.5, that the oxidising/reducing agents are glutathione reduced and oxidised in such proportions and concentrations that it allows the maximum formation of dimeric form. 19. The process as claimed in any of the preceding claims, characterised in that in step IV the solution coming from the preceding step is loaded onto an anionic- exchange column with a ratio Volume loaded/Volume column ratio from 1:1 to 10:1. 20. The process as claimed in claim 19 characterised in that the ratio Volume loaded/Volume column is 10:1. 21. The process as claimed in claims 19 or 20, characterised in that the protein is eluted with ethanolamine-HCl, NaCl buffer and that the protein in monomeric form is mainly comprised in the fractions containing the material not bound to the resin, whereas the protein in dimeric form is essentially comprised in the subsequent fractions eluted at NaCl concentration from 150 to 250 raM. 22. The process as claimed in any of the preceding claims, characterised in that in step V the solution eluted in the preceding step at NaCl concentration from 150 to 250 raM is diluted and loaded onto reverse-phase chromatography column in amount corresponding to an optical density from 4.5 to 5.5 OD at 280 nm per ml of resin. 23. The process as claimed in claims 1 and 22, characterised in that the first elution stage is performed under conditions of increasing gradient of organic solvent until the elution peak of the monomeric form appears, it is prosecuted under isochratic conditions until exhaustion of the elution peak of the monomeric form, and that the second stage is performed under conditions of increasing gradient of organic solvent until complete elution of the protein in mainly dimeric form. 24. The process as claimed in any of the claims 22 to 23 characterised in that the elution buffer contains ethanol, methanol or acetonitrile. 25. The process as claimed in any of the claims 22 to 24 characterised in that the elution buffer is a hydroalcoholic solution containing increasing percentages of ethanol. 26. The process as claimed in any of the claims 22 to 25 characterised in that the reverse-phase chromatography is performed on resin having 30-micron particles with medium diameter. 27. The process as claimed in any of the preceding claims comprising an additional ultrafiltration step followed by lyophilisation in presence or absence of appropriate additives. 28. Placental Growth Factor in active form obtainable by means of the process as claimed in any of the claims 1 to 24, characterised in that it is pure from contaminants of the host strain and that it contains the monomeric form in percentage not higher than 1.5% and that it is essentially in dimeric and multimeric form. The invention discloses a process for extracting and purifying the recombinant Placental Growth Factor (PLGF) expressed in inducible prokaryotic expression systems comprising the following steps : I) fermentation of the bacterial cells, II) extraction and purificatin of the inclusion bodies, III) renaturation of the expressed proteing, IV) ion-exchange chromatography, V) reverse-phase chromatography.

Full Text

PRODUCTION PROCESS OF RECOMBINANT PLACENTAL GROWTH FACTOR
DESCRIPTION
Field of the invention
The present invention relates to a process for
extracting and purifying the recombinant Placental Growth
Factor from genetically modified cells.
State of Art
The Placental Growth Factor {PLGF) is a homodimeric
glycoprotein with a structure similar to the Vascular
Endothelial Growth Factor (VEGF). The complete
polynucleotide sequence codifying the PLGF protein was
described by Maglione and Persico in patent EP-B-550 519
(WO-A-92/06194) claiming Italian priority of 27.09.1990.
Alternative processes of splicing the ARN of PLGF
generate three homologue forms of the Placental Growth
Factor, precisely PLGF-1, PLGF-2 and PLGF-3, having
different polypeptide sequences, and all described in
literature.
The above-mentioned patent also describes a method
for producing the PLGF factor comprising the use of an
inducible prokaryotic expression system characterised by
host cells modified with an expression vector, in which
the human PLGF gene is integrated under the control of an
inducible promoter (directly or indirectly). After
inducing the PLGF expression with appropriate activator,
the cells are incubated, isolated and submitted to lysis.
The so-obtained raw lysate is a complex mixture of
proteins containing low quantities of the expressed PLGF
protein and having low specific activity. In fact, in the
known process, the protein expression is induced in
cultures containing low cellular density, as it is
evident from the low optical density at time of
induction, that is between 0.2 and 0.6 OD at 600 ran.
Furthermore, the process described in the preceding
document does not comprise additional purification stages
of the expressed protein. For this reason, the lysates
obtained according to the application WO-A-92/06194 are
inappropriate as such to be used directly in the
preparation of medicaments.
A more complex method for purifying the same
placental factor is envisaged by Maglione et al. in "I1
Farmaco" 55 (2000), pages 165 to 167. Nevertheless, the
method disclosure merely gives a simple listing of known
applicable techniques, without describing conditions and
experimental details thereof, which are essential for
obtaining the PLGF protein in the purity and quantity
necessary for a pharmaceutical use.
The scope of the present invention is to provide a
new method for extracting and purifying the recombinant
PLGF expressed in bacterial cells, allowing to obtain
PLGF at high level of purity and with yields suitable to
be industrially used in the preparation of medicaments.
A further scope of the invention is to obtain the
PLGF protein in essentially active form (greater than
98.5%), that is mainly composed by dimeric (not less than
70%) and multimeric forms and containing residues of the
monomeric form (little or not active) not greater than
1.5%.
Summary of the invention
The invention is based upon the identification of a
sequence of purification techniques particularly
appropriate for the extraction and purification of human
PLGF expressed in bacterial cells. The invention is
further based upon the determination of the optimum
operative conditions with respect to the single
techniques and to the chemical-physical features of the
substance to be purified.
Then, object of the present invention is a process
for extracting and purifying the recombinant Placental
Growth Factor (PLGF) expressed by means of an inducible
prokaryotic expression system comprising the steps of: I)
fermentation of the bacterial cells, II) extraction and
purification of the inclusion bodies, III) renaturation
of the expressed protein, IV) ion-exchange
chromatography, V) reverse-phase chromatography, and
optionally VI) final stages of ultrafiltration,
formulation and lyophilization. According to such method,
the fermentation (step I) is performed until obtaining a
high bacterial density in the medium, as it is shown by
the high optical density in the medium, before proceeding
with the induction step. The step (II) comprises
bacterial lysis, rupture of DNA and isolation of the
inclusion bodies. The renaturation of the expressed
protein (step III) is obtained by solubilizing the
inclusion bodies in denaturant buffer, and by
transforming, at least partially, the expressed protein
in the dimeric form. At last, in the step (IV) and (V)
the dimeric and multimeric forms of the expressed protein
are separated from the monomeric form and isolated in
pure form, to be subsequently ultrafiltrated and
lyophilised in presence of usual lyophilisation and
formulation additives.
A specific object of the invention is the above-
mentioned process for extracting and purifying the PLGF-1
protein of human origin, but substantially valid also for
PLGF-1 of animal origin.
The claimed process advantageously allows the
obtaining of production yields of expressed protein from
30 to 50 times higher than the yields obtained according
to the method described in the preceding state of art.
The claimed process furthermore allows the obtaining of
the highly pure protein, with high specific activity and
in substantially dimeric form.
Further object of the invention is the active
Placental Growth Factor obtainable by means of the
process of the invention, free from any residual protein
or other bacterial contaminant and containing residues of
monomeric form not higher than 1.5%.
Description of the accompanying drawings
Figure 1: The figure shows the results obtained by
electrophoresis SDS-PAGE under reducing conditions for
monitoring step I. Prel and Pre2 represent the pre-
induction checks, prepared as follows. Soon before the
induction, about 0,064 units of optical absorption
measured at 600nm (OD600) are taken and diluted 5 times
with water. Of this dilution 2 0 ul are taken which are
added to 2 0 ul of reducing buffer and submitted to
boiling. 20 ul of this last solution are loaded onto the
SDS PAGE matrix. Postl and Post2 represent the post-
induction checks prepared as above. M designates the
mixture of markers of molecular weight. In the post-
induction columns (Postl and Post2) a band is noted just
above the indicator of molecular weight 14.3
substantially absent in the pre-induction columns (Prel
and Pre2) corresponding to the PLGF-1 protein expressed
and segregated within the inclusion bodies.
Figure 2: The figure shows the monitoring
chromatogram of the anionic-exchange chromatography on Q-
Sepharose Fast Flow resin. X-axis shows the elution
volume (ML), y-axis shows the optical absorption units
(OD) . The first elution peak obtained by eluting by 20%
with buffer B (NaCl 200 mM) corresponds to the PLGF-1
protein in substantially dimeric form, but it comprises
impurities and the monomeric form. The following peak,
eluted by 100% with buffer B (NaCl 1M) contains
impurities which are eliminated.
Figure 3: The figure shows the monitoring
chromatogram of the first elution stage in reverse-phase
chromatography on RP Source 3 0 resin. X-axis shows the
elution volume (ml), y-axis shows the optical absorption
units (OD). The first abundant elution peak corresponds
to the various impurities, which do not bond to the
resin. The second elution peak corresponds to the PLGF
protein in monomeric form eluted under isochratic
conditions (experimentally found at about 10%-15% of
buffer B).
Figure 4: The figure shows the monitoring
chromatogram of the second elution stage in reverse-phase
chromatography on RP Source 3 0 resin. X-axis shows the
elution volume (ml), y-axis shows the optical absorption
units (OD) . The elution peak corresponds to the PLGF
protein in dimeric-multimeric form.
Figure 5: The figure shows the results obtained in
electrophoresis on SDS-PAGE for the final monitoring of
the whole process. Prerefol and Postrefol represent the
checks preceding and following the renaturation of the
expressed protein (step III) . QFF represents the peak
eluted from the Q Sepharose fast flow resin, containing
the protein mainly in dimeric form. Mon represents the
peak containing the monomeric form. Dim represents the
peak eluted in the second substep of the reverse-phase
chromatography on RP Source 30 resin. It is noted that
before the renaturation, the expressed protein is mainly
in monomeric form. After the renaturation, part of the
protein is in dimeric form. The following purification on
QFF and RF 30 chromatography allow the obtaining of PLGF-
1 protein with high purity degree.
Detailed description of the invention
The genetic modification of the bacterial host cells
is described by Maglione et al. in the preceding patent
EP-B-0550519 (WO-A-92/06194) . For this purpose, bacterial
cells are transformed introducing of an expression vector
comprising an insert corresponding to the" human gene
coding for PLGF-1 factor. The complete gene sequence is
known in literature and it is freely accessible. A
plasmid containing such sequence was deposited with the
ATCC under accession number ATCC No 40892. The expression
is performed under the control of the system of RNA
polymerase of T7 phage and it is induced with IPTG
(isopropyl-ß-D-tiogalactopyranoside).
Nevertheless, other inducible prokaryotic expression
systems may be utilised. Examples of such systems,
obtainable on the market, are represented by:
1) pBAD expression system (In vitrogen BV) wherein
the synthesis of a protein is placed under the control of
the araBAD promoter and it may be induced in different
strains of E.Coli by means of arabinose.
2) T7 Expression System (In vitrogen BV or Promega)
wherein the synthesis of a protein is controlled by the
promoter of RNA polymerase of T7 phage and it may be
induced by means of lactose or the analogues thereof
(IPTG) . In this case it is required the use of E.Coli
derivatives of DE3 (B12KDE3) or JM109(DE3)) type
containing, namely, a copy of the gene of Rna polymerase
of T7 phage placed under the control of a lactose-
inducible promoter.
3) Trc expression system (In vitrogen BV) wherein
the synthesis of a protein is placed under the control of
the trc hybrid promoter. Such promoter has been obtained
by melting the trp promoter and the lac promoters and it
may be induced in different strains of E.Coli by means of
lactose or the analogues thereof (IPTG).
4) Tac expression system (Amerham biosciences)
wherein the synthesis of a protein is placed under the
control of the tac promoter. In this system the protein
synthesis is induced in strains of E.Coli laclq (type
JM105) by means of lactose or the analogues thereof
(IPTG) .
5) Px, expression system wherein the synthesis of a
protein is placed under the control of the PL promoter
and it may be induced by adding tryptophan. In this case
it is required the use of E.Coli derivatives (GI724)
containing a copy of the codifying gene for the cI
repressor of the Lambda phage placed under the control of
a tryptophan-inducible promoter.
Step I: Fermentation and induction
The first stage of the claimed process consists in
the fermentation of a functionally-modified bacterial
strain equivalent to the strain described in the
preceding European patent (above). In a preferred
embodiment the micro-organism is a derivative of
Escherichia Coli modified with an expression plasmid
comprising the human gene of PLGF. A preferred micro-
organism is the one called [B12(DE3)pLysS PLGF-1]
obtained by integrating in the commercially available
strain [B12(DE3)pLysS] (Promega Corporation USA) the gene
of the human PLGF-1. The present invention, nevertheless,
is not limited to the human PLGF-1 factor, but it also
relates to the one of animal origin (monkey, mouse,
rabbit etc.). The present invention is not limited so
much the less to the use of a E. Coli derivative, but it
includes the use of any prokaryotic micro-organism
susceptible to be genetically modified and able to
express heterologous proteins under the form of inclusion
bodies.
The strains utilised as inoculum in the process of
the invention are kept before using them in the
lyophilised form to preserve the expression capacity
thereof. Upon use, the lyophilised material is brought
again in solution by utilising an appropriate buffer.
Although there is a wide range of known culture
media available on the market and which may be
effectively used, the fermentation step according to the
invention is preferably performed in a medium free from
any material of animal or human origin in order to avoid
any infection risk. Yeast"s extracts (Difco) added with
one or more suitable antibiotics represent the most
suitable means for the process. In the preferred
embodiment a medium is used which has been obtained by
mixing under sterility conditions a first solution (A)
containing yeast"s extracts, glycerol and ammonium
sulphate with a second solution- (B) containing a
phosphate buffer. The mixture is then integrated with
ampicillin and chloramphenicol or equivalent antibiotics.
Appropriate antibiotic concentrations are from 50 to 300
ug/ml of ampicillin, preferably from 100 to 200 ug/ml and
from 10 to 100 ug/ml of chloramphenicol, preferably from
30 to 40 ug/ml.
The fermentation step may be preceded by a
preinoculum step wherein the lyophilised micro-organism
is suspended in the medium and submitted to consecutive
incubation and dilution steps aimed at having in culture
the optimum quantity of micro-organism cells. Preferably,
the micro-organism is incubated for one night at 37°C,
then diluted and incubated again for some hours. The
chosen pre-inoculum volume is subsequently centrifuged,
suspended again in the culture solution enriched with
ampicillin and inoculated in the fermentation vessel for
the fermentation step.
The fermentation is performed in the above-mentioned
medium added with ampicillin and chloramphenicol at the
temperature suitable for the micro-organism, usually at
about 37°C, in presence of a percentage of dissolved 02,
with respect to the saturation with air, from 20% to 40%,
preferably 30%. The pH during fermentation is kept at
neutral or weakly acid values (6.4 to 7.4). Furthermore,
since the fermentation process takes place under
stirring, antifoam agents are preferably to be used.
The fermentation progress is accompanied by the
increase in the optical density of the medium. For this
reason, the optical density is the parameter utilised
according to the invention to monitor the progress degree
of the fermentation. Readings at 600 nm are particularly
appropriate.
Essential feature of the invention is the high
cellular density achieved in the culture at time of the
expression induction. Optical densities at 600 nm (OD600)
from 1 to 50 may be achieved thanks to culture media of
the invention. Densities higher than 18, nevertheless,
are preferred to obtain the high production levels
typical of the claimed method. Densities between 16 and
2 0 are particularly preferred to induce the producing
bacterial strain and gave optimum results. The
fermentation, then, is kept at the above-mentioned
conditions until achieving such values of optical
density, then one proceeds to induce the protein
expression.
Any agent or chemical-physical condition able to
induce in the cells of the used micro-organism the
machinery of expression of the heterologous protein may
be advantageously utilised. In the specific case wherein
the bacterial strain BL21(DE3)pLysS modified with an
expression plasmid containing the promoter of 11 phage is
used, the expression is induced with lactose or the
derivatives thereof, such as isopropyl-b-
tiogalactopyranoside (IPTG) with a proper concentration,
namely about l mM. The induction duration may vary
according to need. Good results are obtained for periods
of some hours, preferably from 3 to 4 hours; in the
optimum process the induction is kept for 3 hours and 2 0
minutes by using a percentage of dissolved 02 equal to
about 10%.
Cell samples are taken before and after induction
and submitted to analytical techniques of control such as
electrophoresis on SDS-PAGE, to determine the induction
outcome.
When the protein expression reaches the desired
levels, the culture is centrifuged and the cells are
moved to the following step.
Step II; Extraction and purification.
The expressed heterologous protein in bacterial
strains is segregated inside the cell itself in the form
of inclusion bodies. Therefore, the process of the
invention provides passages of lysis of the cells,
rupture of the extracted nucleic material (DNA) and
recovery and washing of the inclusion bodies.
The cells are washed, although not necessarily, and
suspended in solutions containing emnulsifier agents in
appropriate concentration, preferably Triton X100 in
concentrations from 0.5% to 1%, then they are submitted
to lysis of the cellular membrane. The lysis process may
be performed by means of freezing/thawing, French Press,
sonication or other similar
known techniques.
Nevertheless, the preferred, method for the bacterial
strain BL21(DE3)pLysS is the freezing/thawing method,
which in the most preferred embodiment is repeated at
least for two consecutive cycles. After the mechanical
lysis, the lysis stage is continued for a few minutes in
the lysis solution at room temperature under stirring.
The release in the lysis medium of the inclusion
bodies is accompanied by the release of micro-organism
different components and cellular substances, above all
the nucleic materials. These substances could interfere
with and jeopardise the following protein purification
process. Therefore, the suspension/solution obtained by
lysis is submitted to rupture of such nucleic material,
specifically DNA, by means of enzymatic agents such-as
DNAse (natural or recombinant such as the Benzonase),
chemical agents, such as deoxycholic acid, or physical-
mechanical agents, such as sonication or high energy
stirring by means of blades, for example, in a mixer. The
rupture of DNA, carried out for example in a mixer, is
performed on lysed cells re-suspended in appropriate
volumes of washing solutions containing chelating and
deterging agents, for example EDTA and Triton X100. It is
preferably repeated for more cycles, preferably 2,
alternated with stages of dilution, in washing solution,
centrifugation and elimination of tne supernatant in
order to remove components and cellular substances from
the fraction containing the inclusion bodies.
Step III Renaturation (refolding) of the protein
The fraction containing the purified inclusion
bodies of PLGF-1 is then solubilised in denaturing buffer
containing known denaturant agents such as urea,
guanidine isothiocyanate, guanidine-hydrochloride.
Preferably, the denaturant solution is a urea solution in
denaturant concentration, for example 8M. In order to
accelerate the solubilisation process, the fraction may
advantageous be submitted to homogenisation or
sonication. After solubilizing the inclusion bodies, the
solution is diluted with the same denaturant buffer until
obtaining an optical density measured at 280 nm of about
0,8 (OD280 0.8). Subsequently, the solution is further
diluted with a dilution buffer until 0.5 OD280. Suitable
dilution solutions contain salts and polyethylene glycol
(PEG) and have basic pH (about 8) . The renaturation of
the PLGF-1 protein in diluted solution is obtained by
adding to the solution appropriate concentrations of
oxidising/reducing pairs, followed by an incubation of 10
to 30 hours, preferably 18 to 20 at a temperature of 10°C
to 30°C, preferably 20°C, under stirring. Examples of
such pairs are: Cystine/Cysteine, Cystamine/ Cysteamine,
2-hydroxyethyldisulphide/2-mercapto-ethanol. Preferred
example of oxidising/reducing pair is the glutathione in
its oxidised and reduced forms, respectively at
concentrations between 0.1 mM and 2.5 mM (preferably 0.5
mM) and between 0.25 mM and 6.25 mM (preferably 1.25 mM).
By means of renaturation, the PLGF-1 protein expressed
essentially in monomeric form is partially brought back
to the dimeric form (Figure 5).
Step IV: anionic-exchange chromatography
The solution coming from the preceding step,
preferably through centrifugation and/or filtration and
containing the protein in mainly monomeric and partially
dimeric form, is loaded onto anion-exchange resin in
order to enrich the mixture with the dimeric form and to
purify it from bacterial contaminants. Any commercially
available matrix suitable for anion-exchange
chromatography may be likewise used to the extent that
its features of capacity, loading and flow speed be
similar to those of the Q Sepharose Fast Flow resin
(Amersham biosciences) , apart from being suitable for an
industrial process. In a preferred embodiment a high-flow
resin is used, for example Q-sepharose Fast Flow
(Amersham biosciences) or equivalent. The resin is washed
and equilibrated with solutions having low ionic
strength. An example of such solution comprises
ethanolamine-HCl pH 8.5 with.low or absent salt content.
The same solution may be utilised for loading, absorbing
and washing the protein mixture to be purified. The used
resins allow loading of large volumes of protein solution
with ratios Volume loaded/Volume column varying from 1:1
to 10:1. Ratios Vol./Vol. next to 10:1 are preferred
since they allow optimising the use of the column.
However, ratios higher than 10:1 are to be avoided since,
due to the saturation of the adsorbing capacity of the
matrix, they lead to high loss in the dimeric form of the
protein.
Whereas the PLGF-1 protein in monomeric form already
percolates in the stages of washing with low ionic
strength, the elution of the dimeric and multimeric forms
is obtained by increasing the ionic strength of the
starting solution. Such increase is obtained by mixing
the equilibration solution with increasing and pre-
established percentages of a second solution containing
NaCl 1M. In a preferred embodiment, the protein in
dimeric form is eluted with solutions containing from 15%
to 25% of NaCl 1 M solution, which corresponds to a NaCl
concentration from 150 to 250 mM. In the best embodiment,
the protein is eluted in isochratic conditions at NaCl
concentration of 200 mM. The elution of the various
species is automatically monitored by measuring the
optical absorption at 280nm (figure 2) . The collected
fractions containing the PLGF-1 protein in dimeric form
are subsequently controlled by electrophoresis SDS-PAGE
(figure 5). Advantageously, the whole chromatography
process is automatically performed by a computerised
system operating under the control of a suitable
programme, for example the Software FPCL Director system
(Amersham biosciences).
Step V: Reverse-phase chromatography
The fractions coming from the preceding step
containing the PLGF-1 protein enriched with the active
forms are collected, diluted with appropriate buffer and
loaded onto an reverse-phase chromatography column in
order to further purify the protein in active form. The
quantity of loaded solution corresponds to OD280 between
4.5 and 5.5 per millilitre of chromatographic matrix.
Such quantities are to be considered maximum quantities.
Any commercially available chromatographic matrix
suitable for the intended use may be utilised to the
extent that its features of loading capacity and flow
speed are compatible with the process requirements. In a
preferred embodiment, a resin is used having such bead-
sizes so as to guarantee the best exploitation of the
absorbing capability together with the easiness in
packing the column itself. Examples of such matrixes are
the RP Source 15 or RP Source 30 (Amersham biosciences)
resins. All the solutions for equilibration, loading,
resin washing and elution are hydro-organic solutions
comprising different percentages of organic solvent.
Examples of such solutions are solutions comprising
ethanol, methanol or acetonitrile. Preferably, hydro-
alcoholic solutions comprising increasing percentages of
ethanol are utilised. In an embodiment of the invention
appropriate quantities of two buffer solutions are mixed,
the former comprising buffer A, i.e. ethanol 40% and TFA
(trifluoroacetic acid) 0.1%, the latter comprising buffer
B, i.e. ethanol 70% and TFA 0.1%.
The protein material loaded onto the resin and
properly washed is then eluted through an elution process
comprising two subsequent stages wherein elution
solutions containing an increasing gradient of organic
solvent are utilised. The first stage is performed under
conditions of rising gradient of organic solvent until
obtaining the elution peak of the monomeric form. Such
gradient is obtained by adding the buffer B to the buffer
A in percentages from 4% to 40%, with an increasing rate
of buffer B of 3% for each eluted column volume. As soon
as the elution peak corresponding to the monomeric form
of the protein appears, the elution is continued under
isochratic conditions until. exhaustion of the elution
peak of the monomeric form. The so-set isochratic
conditions cause the largest possible separation of the
chromatographic peaks corresponding to the two monomeric
and dimeric forms and, then, the best obtainable
resolution for a process of industrial, and not
analytical type. The second stage is performed again
under condition of increasing gradient of organic solvent
until whole elution of the protein mainly in dimeric form
is achieved. In this second stage, the gradient is
obtained by adding the buffer B to the buffer A in
percentages from 10% to 100%, with an increasing rate of
buffer B of 40.9% for each eluted column volume. The
elution of the various forms of PLGF-1 protein is
automatically monitored by measuring the optical
absorption at 280nm (figure 3 and figure 4) . The
collected fractions containing the PLGF-1 protein
essentially in dimeric form are subsequently controlled
by electrophoresis SDS-PAGE (figure 5) . Advantageously,
the whole reverse-phase chromatography process is
automatically performed by a computerised system
operating under the control of a suitable programme, for
example the Software FPCL Director system (Amersham
biosciences).
The results of the electrophoresis show that PLGF-1
protein obtained from the second stage of the reverse-
phase chromatography is in highly pure active form,
namely it comprises the protein in dimeric and partially
multimeric form, but it is essentially free from any
contamination of the monomeric form. The so-obtained
product comprises not less than 98.5% of active form,
preferably not less than 99.5%, wherein not less than 70%
is in dimeric form. The residual of monomeric form is not
higher than 1.5%. The protein in active form is obtained
in average amounts of 160 mg per litre of bacterial
culture. The pure protein obtained according to the
above-described method may be submitted to additional
working stages such as ultrafiltration on membrane. In
this case the product is filtered on membrane having cut-
off limit lower than, or equal to 3 0kD and it is
submitted to diafiltration against TFA acidulated water
until a dilution factor of 1:106. The so-obtained final
product may be properly formulated with lyophilisation
additives and lyophilised to keep its best biological
activity.
The invention is here below described by means of
examples having, however, only illustrating and not
limiting purposes.
Example 1: Fermentation
The following procedure relates to the method of
fermentation and induction of the genetically modified
micro-organism (MOGM) [B121(DE3)pLysS PlGF-1] in a
fermentation vessel using 1 mM IPTG.
Materials:
Solution SBM constituted by:
Solution A (per 1 litre)
Bacto yeast extract(Difco) 34 g
Ammonium sulphate 2 .5 g
Glycerol 100 ml
H20 q.s. at: 900 ml
Solution B (10 X)(per 100 ml)
KH2PO4 1.7 g
K2HPO4 -3H2O 20 g, or
K2HPO4 15.26 g
H20 q.s. at 100 ml
The solutions A and B are separately autoclaved and
mixed upon use under sterile conditions. Alternatively,
the solutions A and B are mixed and filtered under
sterile conditions.
IPTG 200mM (200X) is produced by dissolving 5 g of
pure substance in 100 ml of distilled water. The solution
is filtered by means of 0.22-um filters, subdivided into
aliquots and frozen at -20°C.
The utilised antifoam agent is Antifoam O-10 (not
siliconic) Sigma Cat A-8207.
The used bacterial strain is [BL21pLysS PlGF-1 WCB]
(working cell bank).
Preinoculum: A tube of lyophilised genetically
modified micro-organism (MOGM) WCB is taken and it is
suspended in 1 ml of SBM + 100 ug/ml Ampicillin + 34
ug/ml of chloramphenicol.
The suspension is diluted in 3 0 ml of SBM + 100
ug/ml Ampicillin + 34 ug/ml of chloramphenicol.
The suspension is incubated at 37°C for one night
(O/N) . The day after the 3 0 ml of the O/N culture are
diluted in 800 ml of SBM + 100 ug/ml Ampicillin + 34
ug/ml of chloramphenicol and they are subdivided into 4
1-liter Erlenmeyer flasks, each containing 200 ml.
The content of each flask is incubated at 37°C for
24 hours. The content of the 4 flasks is mixed and the
OD600 are read by diluting 1/20 in water (50 ul + 950 ul
of water).
An established volume of preinoculum is then
centrifuged for 10 min. at 7.500 x g at 4°C in sterile
tubes.
The bacteria are then re-suspended in 20 ml of SBM +
200 ug/ml of Ampicillin + 10 ug/ml chloramphenicol per
each litre of fermentation by stirring at 420 rpm at R.T.
for 20 minutes. At the same time the fermentation vessel
is prepared and the oxygen probes are calibrated.
The oxygen probes are calibrated at 37°C temperature
at 0% with nitrogen, then at 100% with air without
antifoam under stirring at 600 RPM.
The fermentation is carried out under the following
experimental conditions:
Medium: SBM + 200ug/ml of ampicillin and 10 ug/ml
of chloramphenicol
Temperature: 37°C
% dissolved 02: 30% (with respect to saturation
with air)
pH: from 6.4 to 7.4.
Antifoam: 1:10 is diluted in water; strongly
stirring before adding it in quantities of 140 ul per 750
ml of medium.
Induction:
The induction is carried out under the following
experimental conditions:
OD600 of induction: 16-20.
Inducing agent: IPTG lmM final.
% dissolved 02: 10% (with respect to saturation
with air).
Induction length: 3 hours and 2 0 minutes.
Just before the induction 2 0 ul of bacteria are
taken, added to 80 ul of water and kept for the pre-
induction check.
At time of induction, IPTG is added to the final
concentration of 1 mM.
The percentage of dissolved 02 is brought to 10%.
At the end of the induction the final OD600 are read
and the overall volume is measured.
Then, 10 ul of bacteria are taken, added to 90 ul of
water and kept for the post-induction check.
The induction is controlled by way of a SDS-PAGE
electrophoresis by loading 20 m1 of the 2 previously
boiled samples.
The medium containing the induced bacteria is then
centrifuged at 7.500 x g for 10 min. or at 3000 x g for
25 min. at 4°C and the supernatant is eliminated.
Results: The induction results are checked by SDS-
PAGE electrophoresis as shown in figure 1.
Example 2: Extraction and purification of the
inclusion bodies.
The following procedure relates to the preparation
and refolding of the inclusion bodies of PlGF-1. By means
of refolding the PLGF-1 bacterial protein is partially
brought back to the dimeric form.
Material:
Mixer with appropriate capacity.
Lysis solution: 1 mM Mg2SO4 + 20mM Tris-HCl pH8
+ Triton X100 by 1%.
Washing solution: 0.5% triton X100 + 10 mM EDTA pH
8.
BD (denaturing buffer): 8 M urea, 50
mM Tris pH 8, Ethylenediamine 20mM.
Dissolving and bringing to volume in H2O.
Oxidised glutathione 200x: 100 mM in H2O;
Reduced glutathione 20Ox: 25 0 mM in H2O.
Dilution buffer: 600 uM final PEG 4000 (2.4g/l),
50 mM Tris-HCl pH 8, 20 mM NaCl.
Antifoam: Antifoam O-10 (not siliconic) Sigma.
Preparation of the PLGF-1 inclusion bodies.
The lysis and washing solutions are equilibrated at
room temperature (RT).
Two cycles of freezing/thawing at -80/37°C are
performed.
The bacterial pellet is lysed in 1 ml of lysis
solution per each 450 OD600 of bacteria.
It is then incubated at RT 3 0 min. under stirring
(250 RPM).
The solution is poured into a mixer with appropriate
capacity and a quantity of washing solution of 3 ml for
each 450 OD600 of bacteria is added.
If necessary, 0.4 ul of not-diluted antifoam per
each millilitre of sample are added.
The solution is spun at the maximum speed for 1
minute or until the sample is well homogeneous.
The content of the mixer is then transferred into a
container with appropriate capacity and 6,5 ml of washing
solution per each 450 OD600 of bacteria are added. It is
incubated for 45 min. at RT under stirring.
The so-obtained suspension is centrifuged at 13.000
x g for 45 min. at 25°C and the supernatant is
discharged.
The settled pellet is re-suspended in 4 ml of
washing solution per each 450 OD600 of bacteria and the
cycle in the mixer is repeated for the second time.
The suspension is transferred into a container with
appropriate capacity, diluted with 6.5 ml of washing
solution per each 450 OD600 and incubated for 30 min. at
RT under stirring.
The centrifugation under the above seen conditions
is then repeated and the supernatant is eliminated.
Example 3: Renaturation of the protein.
The inclusion bodies are solubilised in 7 ml of
denaturing buffer BD (containing urea 8M) and further
diluted in BD until OD280 of 0,8. Subsequently, 0.6
volumes of dilution buffer are added in order to bring
the final urea concentration to 5M.
Afterwards 1/200 of reduced glutathione 200X (final
concentration of 1,25 mM) and 1/2 00 of oxidised
glutathione 200X (final concentration of 0.5 mM) are
added. A 15 ml sample for checking (prerefol) is taken
and the solution is then incubated at 20°C for 18-20
hours under stirring.
At the end of the incubation, the medium is
centrifuged for 10 min. at 20°C, 10.000 x g, filtered by
means of 0.45 or 0.8 mm filters and a 15 ml sample is
taken for checking (postrefol).
Results: The 15-ml samples of the pre,- and post-
refolding solutions are analysed by means of SDS-PAGE
electrophoresis (figure 5).
Example 4: Anion-exchange chromatography
The following procedure relates to the first step of
purification of the PlGF-1 protein after refolding. Upon
loading of the sample onto the column, there will be a
high loss of not-absorbed PlGF-1 monomer. The loaded
quantity must not exceed 10 times the volumes of the
column, since this would cause a significant loss in the
PLGF-1 dimer.
The elution is performed under isochratic conditions
at 20% of buffer B (see below) , which corresponds to a
NaCl concentration of 200 mM. The eluted peak still
contains the glutathiones .used for refolding, which
contribute by about 50% of OD280.
Material and parameters:
FPLC system: Amersham-biosciences handled by the
software called FPLC Director.
Monitoring parameters
U.V.: Wavelength = 280 nm; scale top - 2.
Temperature: 20°C (minimum 15, maximum 25)
Resin: Q-sepharose Fast Flow (Amersham-
biosciences) .
Column volume/height: Volume: 1/10 of volume of
the sample to be loaded; height: between 13 and 16 cm.
Equilibration: 2 Column Volume (CV) of buffer
B, then 1.5 CV of buffer A.
Sample: Renatured, centrifuged and/or filtrated
PlGF-1. Load no more than 10 CV thereof.
Buffer A: 20 mM Ethanolamine-HCl pH 8.5.
Buffer B: Buffer A + 1M NaCl.
Injection speed: 1 cm/min (maximum speed tested
on small columns = 1.887 cm/min; minimum tested speed =
0.5 cm/min.).
Elution speed: 1 cm/min (maximum speed tested on
small columns = 1.887 cm/min; minimum tested speed = 0.5
cm/min.).
Washings after
injection: 1.5 CV with 0% of buffer B.
Peak collected: Peak eluted at isochratic
conditions at 20% of buffer B, running for about 3 CV.
Final washing: 2 CV at 100% B.
Procedure:
The peak eluted under isochratic conditions at 20%
of buffer B is collected, then 0.271 water volumes,
0.0045 TFA volumes and 0.225 ethanol volumes are added
thereto. In this way the sample results to be diluted 1.5
times and contains 15% ethanol and 0.3% TFA. The addition
of these 2 substances facilitates the bounding of PlGF-1
to the reverse-phase resin (see example 5).
Results: The chromatography step is continuously-
controlled by monitoring the optical densities at 280 nm
as illustrated by figure 2 .
The purity of the isolated protein material is
analysed by means of SDS-PAGE electrophoresis (figure 5).
Example 5: Reverse-phase chromatography.
The following procedure may be performed with RP
source resin with 15 micron or 30 micron average particle
diameter. However, the 30-micron RP source resin, while
not involving any alteration in the purification process,
allows an economical saving of the resin itself (about
50%) , a greater easiness in the packaging procedure of
the column and a lower backpressure.
The procedure relates to the second phase of the
purification of the PlGF-1 protein after passing on the
QFF resin. During the sample injection, a high adsorbance
is apparent and corresponds to the not adsorbed peak of
the glutathiones which do not bound to the resin. This
procedure consists of 2 sub-stages, the former called
RPCmon, is used to eliminate most of the monomeric
component of PlGF-1, whereas the latter is used to elute
the essentially dimeric component of the protein and it
is called RPCdim.
First sub-stage (RPCmon)
Material and parameters:
FPLC system: Amersham-biosciences handled by the
software called FPLC Director.
Monitoring parameters
U.V. : Wavelength = 280 nm; full scale = 0.05.
Temperature: 20°C (minimum 15, maximum 25)
Resin: Reverse Phase Source 3 0 (Amersham-
biosciences) .
Resin volume/height: Volume: 1/5 - 1/6 of the
overall OD280 of the sample to be loaded; height: between
27 and 33 cm.
Equilibration: 2 Column Volume (CV) of buffer B,
then 2 CV of buffer A.
Sample: P1GF-1 coming from the preceding step
(example 4), diluted 1.5 times and containing ethanol 15%
and TFA 0.3%. Loading max. 4.5 to 5.5 OD280 per ml of
resin.
Buffer A: Ethanol 40% + TFA 0.1%.
Buffer B: Ethanol 70% + TFA 0.1%.
Injection speed: 1.887 cm/min.
Elution speed: 1.887 cm/min.
Washings after
injection: 1.5 CV with 4% buffer B.
Monomer peak: Gradient ranging from 4 to 40% of B in
12 CV (3%B/CV) . Just after starting the elution of the
peak, by OD280 reaching 25% of the full scale, the
elution is continued with isochratic conditions with the
buffer B concentration reached in that moment until the
peak elution is complete (about 2.5 -3.5 CV).
Operations
A suitable quantity of the solution corresponding to
the "monomer" peak is taken and it is concentrated for
checking (mon in Fig. 5).
Second sub-stage (RPCdim)
Material and parameters:
Without re-equilibrating the column, but by simply
shifting the scale range of the UV monitor to the value
2, a gradient ranging from 10 to 100%-of the buffer B is
run in 2.2 CV (40.9%B/CV).
Operations:
The fractions corresponding to the "Dimer" peak are
taken. Figure 4 illustrates an example thereof. They are
collected and the volume and the optical density at 280
nm are measured.
The overall yield (expressed in mg) obtained before
the lyophilisation is calculated by multiplying the OD280
times the volume times the dilution. The average value of
such yield is 164 mg of pure PLGF-1 per litre of
bacterial culture with a standard deviation of 23.21. It
may also be expressed in mg per 1000 OD600 of fermented
bacteria, resulting to 5.58 mg of pure PLGF-1 each 1000
OD600 of fermented bacteria with a standard deviation of
0.8.
The so-obtained dimer solution is kept at -2 0°C
until ultradiafiltration and lyophilisation. A sample of
such solution is submitted to SDS-PAGE electrophoresis as
illustrated in figure 5.
We claim :
1. A process for extracting and purifying recombinant Placental Growth
Factor (PLGF) in dimeric and multimeric active form containing no more than 1.5%
of monomeric form, by expression in an inducible expression system in modified
prokaryotic cells such as herein described comprising the following steps: I)
fermentation of the prokaryotic cells, II) extraction and purification of the inclusion
bodies, III) renaturation of the expressed protein, IV) ion-exchange chromatography,
V) reverse-phase chromatography, characterised in that step (I) is performed until
obtaining optical density of the culture medium from 14 to 50 at 600 nm (OD600 14-
50) followed by induction, that step (II) comprises lysis of the culture cells, rupture of
the DNA and isolation of the inclusion bodies, that in step (III) the inclusion bodies
are solubilised into denaturing buffer and the expressed protein is brought, at least
partially, back to the dimeric form, that in step (IV) the dimeric and multimeric forms
of the expressed protein are separated from the monomeric form by anion exchange
chromatography that in step (V) the dimeric and multimeric forms of the expressed
protein are further separated from the monomeric form by reverse-phase
chromatography with two subsequent elution stages with increasing gradient of
organic solvent separated by an elution stage under isochratic conditions and finally
isolated.
2. The process as claimed in claim 1, characterised in that the Placental
Growth Factor (PLGF) is human PLGF-1 or of animal origin.
3. The process as claimed in claim 1 or 2 characterised in that the prokaryotic
cells are bacterial cells.
4. The process as claimed in any of the claims 1 to 3, characterised in that
step I is performed in a medium allowing the obtaining of a high bacterial density in
the fermentation step and free of any material of animal or human origin.
5. The process as claimed in any of the preceding claims, characterised in
that step I is performed in a medium comprising one or more selection agents, yeast
extract, glycerol and ammonium salts.
6. The process as claimed in any of the preceding claims, characterised in
that the inducible expression system is the expression system 77.
7. The process as claimed in any of the preceding claims, characterised in
that the bacterial cells are a strain derived from E.Coli.
8. The process as claimed in any of the preceding claims, characterised in
that the bacterial strain is E. Coli {B121(DE3)pLysS}.
9. The process as claimed in any of the preceding claims, characterised in
that the expression is induced by means of lactose, isopropyl-P-D-
thiogalactopyranoside (IPTG) or functionally equivalent analogues.
10. The process as claimed in any of the preceding claims, characterised in
that the optical density of the culture at time of the induction is 14 to 30 OD at 600
nm (14-30 OD600), preferably 16 to 20 (16-20 OD600).
11. The process as claimed in any of the preceding claims, characterised in
that step I comprises a preliminary step of preinoculation.
12. The process as claimed in any of the preceding claims, characterised in
that in step II the cell lysis is performed by means of freezing/thawing, French Press
or other equivalent techniques.
13. The process as claimed in any of the preceding claims, characterised in
that in step II the DNA rupture is performed by means of DNAse of extraction or
recombinant origin, preferably the benzonase, or by chemical-mechanical action.
14. The process as claimed in any of the preceding claims, characterised in
that in step II the DNA rupture is performed by means of a mixer.
15. A process as claimed in any of the preceding claims, characterised in that
in step II the inclusion bodies are isolated by means of at least two cycles of
centrifugation and washing into a suitable buffer.
16. The process as claimed in any of the preceding claims, characterised in
that in step III the inclusion bodies are solubilised into denaturing buffer containing
urea, guanidine isothiocyanate, guanidine-hydrochloride or any other denaturing
agent and are optionally homogenised or sonicated.
17. The process as claimed in any of the preceding claims, characterised in
that in step III, after the solubilisation of the inclusion bodies, the solution is diluted
and the protein material is renatured by adding to the solution oxidising/reducing
agents and by incubating for 10 to 30 hours, preferably 18 to 20 at temperature 10°C
to 30°C, preferably 20°C under stirring.
18. The process as claimed in claim 17, characterised in that the solution is
diluted until obtaining an optical density at 280 nm (OD280) from 0.01 to 2,
preferably 0.5, that the oxidising/reducing agents are glutathione reduced and
oxidised in such proportions and concentrations that it allows the maximum
formation of dimeric form.
19. The process as claimed in any of the preceding claims, characterised in
that in step IV the solution coming from the preceding step is loaded onto an anionic-
exchange column with a ratio Volume loaded/Volume column ratio from 1:1 to 10:1.
20. The process as claimed in claim 19 characterised in that the ratio Volume
loaded/Volume column is 10:1.
21. The process as claimed in claims 19 or 20, characterised in that the
protein is eluted with ethanolamine-HCl, NaCl buffer and that the protein in
monomeric form is mainly comprised in the fractions containing the material not
bound to the resin, whereas the protein in dimeric form is essentially comprised in
the subsequent fractions eluted at NaCl concentration from 150 to 250 raM.
22. The process as claimed in any of the preceding claims, characterised in
that in step V the solution eluted in the preceding step at NaCl concentration from
150 to 250 raM is diluted and loaded onto reverse-phase chromatography column in
amount corresponding to an optical density from 4.5 to 5.5 OD at 280 nm per ml of
resin.
23. The process as claimed in claims 1 and 22, characterised in that the first
elution stage is performed under conditions of increasing gradient of organic solvent
until the elution peak of the monomeric form appears, it is prosecuted under
isochratic conditions until exhaustion of the elution peak of the monomeric form, and
that the second stage is performed under conditions of increasing gradient of organic
solvent until complete elution of the protein in mainly dimeric form.
24. The process as claimed in any of the claims 22 to 23 characterised in that
the elution buffer contains ethanol, methanol or acetonitrile.
25. The process as claimed in any of the claims 22 to 24 characterised in that
the elution buffer is a hydroalcoholic solution containing increasing percentages of
ethanol.
26. The process as claimed in any of the claims 22 to 25 characterised in that
the reverse-phase chromatography is performed on resin having 30-micron particles
with medium diameter.
27. The process as claimed in any of the preceding claims comprising an
additional ultrafiltration step followed by lyophilisation in presence or absence of
appropriate additives.
28. Placental Growth Factor in active form obtainable by means of the
process as claimed in any of the claims 1 to 24, characterised in that it is pure from
contaminants of the host strain and that it contains the monomeric form in percentage
not higher than 1.5% and that it is essentially in dimeric and multimeric form.
The invention discloses a process for extracting and purifying the recombinant
Placental Growth Factor (PLGF) expressed in inducible prokaryotic expression
systems comprising the following steps : I) fermentation of the bacterial cells,
II) extraction and purificatin of the inclusion bodies, III) renaturation of the
expressed proteing, IV) ion-exchange chromatography, V) reverse-phase
chromatography.

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Patent Number

217419

Indian Patent Application Number

01130/KOLNP/2004

PG Journal Number

13/2008

Publication Date

28-Mar-2008

Grant Date

26-Mar-2008

Date of Filing

09-Aug-2004

Name of Patentee

GEYMONAT S.P.A.

Applicant Address

VIA S. ANNA, 2, I-03012 ANAGNI

Inventors:

#	Inventor's Name	Inventor's Address
1	MAGLIONE DOMENICO	VIA DELLA PESCHIERA 20,, I-03012, ANAGNI
2	BATTISTI MAURO	VIALE DEGLI EROI 16, I-00032 CARPINETO
3	CONTI ETTORE	VIA TOSCANA 1-RES. 'COLLI DEL VIV ARO", I-00040 ROCCA DI PAPA
4	SALVIA GIUSEPPE	VIA ANDREA DORIA, 39, I-95123 CATANIA
5	TUCCI MARINA	VIA SANITA 40, I-03012 ANAGNI

PCT International Classification Number

C 12 N 15/12

PCT International Application Number

PCT/IT02/00065

PCT International Filing date

2002-02-05

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1			NA