CA2184619A1 - Novel process for the isolation of clavulanic acid and of pharmaceutically acceptable salts thereof from the fermentation broth of streptomyces sp. p 6621 ferm p 2804 - Google Patents

Abstract

Disclosed is a novel and improved process for the isolation of clavulanic acid and of pharmaceutically acceptable salts thereof such as potassium clavulanate from the aqueous fermentation broth of Streptomyces sp. P 6621 FERM P 2804, wherein from the fermentation broth the mycelium, a major part of proteins and other suspended solid particles are removed by microfiltration at a pH value of the medium between 5.8 and 6.2 and at a temperature between about 20.degree.C and 40.degree.C, the purified broth (the aqueous phase) is optionally additionally purified by ultrafiltration, and the thus purified broth is concentrated by reverse osmosis, then it is directly extracted in a countercurrent in centrifugal extractors with a water-immiscible organic solvent at a pH value of the medium between 1 and 3, whereat the still remaining proteins are simultaneously removed, from the obtained organic phase the water-soluble impurities are removed by washing the organic phase with water, the organic phase is dried in vacuo in a rectification column to a water content under 0.1 vol % and then concentrated by evaporation, decolourized by a treatment with active carbon and then the clavulanic acid present in the dry organic phase, most suitably in the ethyl acetate phase, is isolated and purified by a reaction with N,N'-diisopropylethylenediamine at a temperature of about room temperature to the intermediary N,N'-diisopropylethylenediammonium diclavulanate, which is isolated and then reacted with potassium 2-ethyl hexanoate in isopropanol to yield potassium salt of clavulanic acid having high purity.

Description

WO 95/23870 P~ S~C_2 Novel Process for the Isolation of Clavulanic Acid and of Pharmaceutically Acceptable Salts Thereof from the Fermentation Broth of Streptolllyces sp. P 6621 FERM P 2804 Technical Field (IPC C 12 P 17/18, C 07 D 498/04) The present invention belongs to the field of pharmaceutical industry and relates to a novel and imploved process for the isolation of clavulanic acid and of pharmaceuti-cally acceptable salts thereof from the fermentation broth of Streptomyces sp. P 6621 FERM P 2804.

Technical Problem There exists a cQIlc~ l need for a novel and i~loved process for ~rc;~a~ g pure clavulanic acid and pharmaceutically acceptable salts thereof such as potassium clavlll~n~te by the isolation from the fermentation broth obtained by means of aclavulanic acid-producing microolg~ .", in which process sophisticated conven-tional isolation methods and chromatographic purific~tinn of the desired productwould be avoided.

PnorArt Clavulanic acid is the common name for (2R,SR,Z)-3-(2-hydroxyethylidene)-7-oxo-4-oxa-1-azabicyclo[3.2.0]heptane-2-calbu~lic acid of the following formula H 1'' \=C
H
~N /~
O H COOH

wo gs/23870 2 1 8 ~ 6 1 ~ PCr/~S~ 2 Alkali metal salts and esters thereof are activé as inhibitors of beta-lactamases produced by some Gram positive as well as some Gram negative :rnicroorganisms.

In addition to the action of inhibiting beta-lact~m~es, clavulanic acid and alkali metal salts thereof also have a synergistic action in combination with beta-lactam antibiotics of penicillin and cephalosporin series. Therefore clavulanic acid and salts thereof are used in galenic l,le~,arations to ~lcvellt the deactivation of beta-lactam antibiotics. Commercial preparations contain a more stable potassium salt of clavulanic acid (the acid alone is rather unstable) in combination with amoxicillin trihydrate.

Clavulanic acid is prepared by the fermentation of a clavulanic acid-producing microorganism such as various microorg7lni~m~ belonging to dirrelcllt Streptomyces strains such as S. clavuligerus NRRL 3585, S. jumoninensis NRRL 5741, S. katsura-hamanus IFO 13716 and Streptomyces sp. P 6621 FERM P 2804.

The aqueous culture broth obtained after fermentation may be purified and con-centrated according to conventional processes comprising e.g. filtration and chromatographic purification as illustrated in GB 1,508,977 prior to the extraction of the aqueous solution with the organic solvent to obtain a solution of impure clavulanic acid in an organic solvent.

GB 1,508,977 teaches, inter alia, that salts of clavulanic acid may be obtained by the adsorption of the clavulanate anion in the filtered broth onto an anionic exchange resin and are eluted therefiolll with an electrolyte, the solution formed is desalted and then the solvent is removed. This process may be used to achieve acceptable yields of the desired substance, yet it requires sophisticated purifications by chromatographic methods and the use of resin columns demands important invest-ments, which limits production operations on a large scale.

GB 1,543,563 discloses a modified fermentation process using the strain S.
clavuligerus NRRL 3585, wherein the pH value of the medium is maintained in the range between 6.3 and 6.7 and thus the yield of the desired compound increases.
Salts of clavulanic acid such as potassium clavulanate are prepared by re-salting from lithium clavulanate, whereby the desired compound is also purified.

- 218~61~
EP-A-0 026 044 illustrates the use of tert-butylamine salt of clavulanic acid as a use-ful intermediate in the preparation of clavulanic acid. The salt is known from BE 862 211, but only as an ingredient in pharmaceutical formulations.

EP-B-0 182 522 discloses a method of prepa~ g clavulanic acid by the fermentation of microorganism S. clavuligerus. An important improvement of the process was achieved by the addition of a carbon source such as glycerol into the fermentation medium in the course of the process either continually or intellllil~elltly, whereat it is very important that the carbon level is maintained in a sufficiently low concentration, namely under 0.5% (w/v) and by no means exceeds 2%. The Examples illustrate thatthe essential h~ uvelllent of the increased yield of clavulanic acid was observed when the carbon source was added during fermentation. It is stated that the con-centration of clavulanic acid in the fermentation broth after 160 hours was about 1400,ug/ml, this being a noticeable illl~luvelllent over previous processes.

A further illl~luvelllent was also a novel process of yuliryillg clavulanic acid from solution as its lithium salt. However, to achieve a higher purity of lithium clavulanate a concentrated solution of another lithium salt such as lithium chloride was added.
The obtained recrystallized lithium clavulanate could be further purified and then optionally converted into other salts such as potassium clavulanate, in a mannerknown from the above literature.

The mycelium, proteins and other solids are removed by known methods such as centrifugation or filtration with a possible prior treatment of the fermentation broth with a selected aggregation agent to aggregate the mycelium and thus make possible an easier filtration. The filtered fermentation broth is further treated with ion ex-change resins or by precipitation with a solvent such as acetone in order to remove proteins and the precipitate is separated by repeated centrifugation and filtration.
This separation of the mycelium, proteins and other accompanying particles in the suspension originally present in the fermentation broth, is time-consuming and requires several working steps.

These time-consuming methods of removing the mycelium, proteins and other suspended particles and subsequent isolation from the obtained transparent fermen-tation broth as well as preparation of pure clavulanic acid and salts thereof were avoided in a manner as disclosed in the published EP-A-0 385 552 and EP-A-0 387 178.

~184619 4 The whole process comprises three steps, i.e. ~ulirylllg the fermentation broth of the mycelium"~lroteills and other solid particles, purifying the clavulanic acid present in an impure form in the broth of a purified filtrate of Slle~ulo~llyces clavuligerus by using one of the primary, secondary or tertiary amines forming stable intermediary salts of clavulanic acid, whereby the major part of accompanying iLu~ulilies in clavulanic acid are separated, and as the last step, the conversion of intermediary amine salts of clavulanic acid (of 85% purity) into the desired alkali metal salt such as potassium clavlll~n~te.

The first step is disclosed in more detail in EP-A-O 385 552, wherein from the aqueous culture broth obtained by the fermentation of the microorganism Strep-tomyces clavuligerus, by means of a physico-chemical process of coagulation-flocculation, the mycelium, proteins and other solid particles are removed. The floc-culi obtained in this process are sufficiently large and compact so that an easysedimentation and separation is made possible, which is best achieved by using roll-ing sieves. Thus a transparent broth is obtained, which may be optionally con-centrated by reverse c,smosi~

In this manner a purified fermentation broth is obtained, the collvelllional ~uliryh~g methods such as cellllirugation, adsorption on active carbon, filtration with coad-juvants etc. having been avoided.

In all known processes it is also necessary (which is dirrelellt from the disclosed floc-culation method) that the purified broth of the culture is treated by means of various processes of deproteinization and ion exchange, which causes significant total losses in the final yield of the desired substance. In contrast to well-known methods, the to-tal yields in the flocculation method amount to 85 to 90%.

The disclosed method of coagulation-flocculation from the fermentation broth of Streptomyces clavuligerus is based upon adding an inorganic electrolyte into th~broth culture to increase the coagulant action, applying the inorganic coagulant as in-itiator of the coagulation process under stirring and at a pH value of the medium be-tween 6 and 8, adding an organic electrolyte when the flocculation begins, and then separating the obtained flocculi from the fermentation broth using rolling sieves or filtration and, optionally, when flocculation takes place in the presence of a water-immiscible solvent, decanting the phases, separating the flocculi and, optionally, con-centrating the liquid by reverse osmosis or evaporation.

EP-A-0 562 583 discloses the use of salts of clavulanic acid with organic diamines such as N,N'-diisopropylethylenediammonium diclavulanate as useful intermediatesfor the isolation and preparation of pure clavulanic acid or alkali metal salts thereof such as potassium clavulanate from ethyl acetate e~tract obtained after the solvent extraction of the obtained aqueous culture broth formed after fermentation, wherein clavulanic acid is present.

Technical Solu~ion The aim of the invention is to i~ uve the process of isolation of clavulanic acid from the fermentation broth obtained by means of a clavulanic acid-producing micro-organism such as SllG~Io~llyces sp. P 6621 FERM P 2804, in which process time-consuming conventional methods of removing the mycelium, proteins and other suspended solid particles present in the aqueous culture broth would be avoided, fol-lowed by the ~re~aration of salts of high purity such as potassium clavulanate.

Suitable salts according to the present invention are pharmaceutically acceptable alkali metal and alkaline earth metal salts such as sodium, potassium, calcium and magnesium salts. Among these salts sodium and potassium salt, especially potassium salt are the most suitable.

The present invention is generally useful for ~uliryillg fermentation broths obtained by means of a clavulanic acid-producing microor~nis,l,.

It is evident from the above Prior Art that known processes have col,l~,ised time-consuming isolation methods and only EP-A-0 385 552 discloses an i",proved process, wherein a completely transparent broth is obtained. However, it is a disad-vantage of this process that, in order to achieve the desired aim, several reagents such as inorganic electrolytes, coagulants, organic polyelectrolytes have to be used and that flocculation, sedimentation or filtration of the fermentation broth require a.
relatively long production time, which affects the purity of the desired product.

On page 2, column 2, lines 22 to 35, some possibilities of puliryi~g the fermentation broth are given, yet said methods would lead to a significant decrease of the yield of c!avulanic acid. It is further stated that the use of several sophisticated techniques in the process of isolation and purification such as ultrafiltration and reverse osmosis WO 95t23870 2 1 8 4 6 1 9 PCI/Slg5100002 would not simplify the process because the use of those methods would require prior filtrations on active carbon or ionic resins.

Con~laly to these statements it has ~ulplisillgly been found that it may be possible to avoid the use of several reagents as used in the process disclosed in EP-A-0 385 552, as well as other time-consuming ways of purification of the aqueous fermentationbroth, which ways are disclosed in the literature, when according to the present in-vention a microfiltration method is used, wherein the mycelium, a major part of proteins (at least 80% of those present in the broth) and other suspended particles are removed.

To this purpose there a multi-stage device for continuous microfiltration is used, which makes possible to carry out the process of separating the mycelium and aqueous filtrate in a dwell time of less than half an hour, the device being composed of several (five) serially connected independent segments (filtration loops). Each seg-ment has its own circulation pump which permits the desired velocity of the fermen-tation broth (5 to 8 m/s) through charmels of ceramic filtering elements having a pore size of 0.05,um. In the microfiltration process taking place at a temperature between about 20 C and 40 C (the telll~uel~tule should not exceed 40 C), tangentionalvelocities are regulated in such a way that in a solid fraction the molecules of a molecular weight over 30,000 are retained. In such a way we succeeded in removing about 80 to 90% of the ~loteills present. The mycelium separated in the microfiltra-tion process was also washed with water in order to increase the yield of clavulanic acid in the combined filtrate. By the disclosed method of purifying the aqueous fer-mentation broth by microfiltration, over 95% of clavulanic acid are retained in the purified aqueous phase, which even exceeds the results of the flocculation method of EP-A-0 385 552 and represents a further hll~lovelllent of the present invention.
After microfiltration the filtrate may be optionally purified by an ultrafiltration process. The purpose of that purification is to separate a major part of the rem~inin~
protein impurities and other accompanying i~u~ulilies having a higher molecular weight than clavulanic acid. In such a way undesired impurities are successfullyremoved, which may precipitate upon extraction with a water-immiscible organic sol-vent, whereby the colouring of the aqueous filtrate obtained after purification with microfiltration is essentially reduced and the purity of the desired product is further illl~luved.

In the ultrafiltration device a polymeric membrane having a high resolution rate of about 20,000 daltons (between 10,000 and 30,000 daltons) is used. The process iscarried out continuously so that the dwell t*mes are as short as possible, and over two serially connected ultrafiltration devices (which increases the separation selectivity of impurities and clavulanic acid); by adding pure washing water as well as by counter-current COllvt;yillg of the retentate (aqueous phase) obtained in the ultrafiltration process, the losses of clavulanic acid in the aqueous phase are reduced to less than 5%.

The combined aqueous filtrate is then concentrated in a reverse osmosis device at a temperature about room temperature to about 1/5 of the original volume to obtain a concentrated aqueous phase of *mpure calvulanic acid and then the obtained con-centrate (retentate) is directly extracted at temperatures between 15 C and 25 C
(extraction may also take place at a temperature under 15 C) with a water-immiscible organic solvent such as ethyl acetate, in an acidic medium *n the pH range of the medium between 1 and 3, which is adjusted by add*ng inorganic acid such as sulfuric acid. Besides ethyl acetate, also other water-immi~cible organic solvents may be used such as methyl acetate, methyl isobutyl ketone or n-butyl alcohol.

Since by the microfiltration process we succeeded to remove the mycelium and a major part of the proteins present, a d*ect extraction of the purified and con-centrated aqueous fermentation broth with an adequate water-immiscible organic solvent such as ethyl acetate is possible without the use of time-cosuming purification methods as applied in known ways disclosed in the above literature and there is avoided the use of additional reagents as applied in the coagulation-flocculation method for the ~uliryillg of the fermentation broth. Thus, in addition to the above hlll~ruve"lent, the process according to the invention also provides a reduction of costs of the method of broth purification. To avoid a denaturation of the rem~ining proteins in the aqueous phase concentrate because of an interaction with the organic solvent or sulfuric acid in the course of the extraction of the impure clavulanic acid from the aqueous phase into the organic phase, it is best to carry out the extraction in a series of centrifugal extractors, wherein in one of them, namely in a self-enl~yillg centrifugal separator, the separated proteins are removed simultaneously and con-tinuously.

In the obtained extract of the impure clavulanic acid in a water-immiscible organic solvent there may be also present water-soluble illl~ulilies such as various decom-218~fil~ 8 ~

position products of clavulanic acid that are more polar than clavulanic acid alone,hence water-soluble i~ uliLies are removed by washing the combined organic phase with water. In this manner a purified extract of clavulanic acid in organic phase such as ethyl acetate extract is obtained.

Clavulanic acid may be isolated from the organic phase and purified so as disclosed in the process of our EP-A-0 562 583. The best way of isolating clavulanic acid as described in this patent application is carried out by a reaction of the ethyl acetate extract of the clavulanic acid with N,N'-diiso~lo~ylethylene~ mine at a temperature of about room temperature and by a subsequent conversion of the obtained inter-mediary N,N'-diiso~ro~ylethylenediammonium diclavulanate with potassium 2-ethyl hexanoate in an aqueous isopropanol solution and at room temperature to obtain potassium clavulanate, which is isolated with a high purity.

Now it has been found that the ~le~alation of the intermediary N,N'-diisu~lol~yl-ethylenediammonium diclavlll~n~te is best carried out in such a way that in the reac-tion between a water-immiscible organic phase such as ethyl acetate extract of the clavulanic acid and N,N'-diiso~royylethylenediamine there is used an organic phase whercfiulll water has been completely removed since already small water amounts may disturb the ~lepal~tion of the intermediary salt as the separated salt dissolves in the water present in the organic phase and pitched by-products may be obtained, which makes the drying more difficult.

If water is completely removed from the organic phase, the stability of the organic phase or of the extract increases since it is well-known that the stability of clavulanic acid in aqueous solutions and in an acidic pH medium in the extraction process is very poor. Therefore for the drying of the organic phase such as ethyl acetate extract of clavulanic acid, drying in a rectification column (principle of fractional distillation) in vacuo was used because of the poor stability of the intermediary salt at higher tem-peratures. It is an essential feature of this method that the organic phase such as.
ethyl acetate and water form an azeotrope having a lllillilUUlll boiling point and thus the organic phase such as ethyl acetate extract is completely dried in the disclosed manner. Thus the organic phase such as ethyl acetate extracts always has a watercontent of less than 0.1 vol.%, averagely from 0.03 to 0.05 vol.%. The completely anhydrous organic phase such as ethyl acetate extract of clavulanic acid is then, within a very short dwell time, concentrated by evaporation to a 1/20 of the original volume to be subsequently reacted with N,N'-diisopropylethylenediamine.

W095/23870 2I X~Cl g g PCT/~5/~D_2 The subsequent reaction of N,N'-diisopropylethylenediammonium diclavulanate withpotassium 2-ethyl hexanoate to potassium clavulanate of high purity may be carried out as disclosed in our EP-A-0 562 583 and best in such a way as disclosed in the Ex-amples and illustrated by the above hll~l,Jvelnents.

The invention is illustrated but in no way limited by the following Examples.

wo gs/23870 PCT/~ 2 218~619 Example 1 ~ i Continuous preparation of a concentrate of ethyl acetate extract co~ inillg impure clavulanic acid An aqueous fermentation broth (10,000 1) obtained by the fermentation of the microorganism Streptomyces sp. P 6621 FERM P 2804 (concentration of clavulanic acid amounted to 3580 mg/l) was added to a 33% aqueous solution (5 1) of sulfuric acid in a vessel (capacity 50 m3) under stirring and cooling so that the pH value of the medium was maintained between 5.8 and 6.2. Then the broth was conlilluously added to a microfiltration device with a flow rate of 1200 Vh, which device was com-posed of five serially connected segments. Each segment had its own circulation pump to provide for the velocity of the fermentation broth through the channels of ceramic filtering elements with a pore size of 0.05 ~m to be 8 m/s. By the microfiltra-tion process, wherein care was taken that the temperature did not exceed 40 C, the mycelium and a major part of proteins and of other suspended solid particles were removed.

The separated solids were washed with water having the flow rate of 300 Vh and then the combined filtrate (permeate) after microfiltration was added continuously with the flow rate of 1500 l/h into a reverse osmosis device, wherein the permeate was concentrated to 1/5 of the original volume.

To the concentrate (retentate) obtained after the reverse osmosis with a flow rate of 300 l/h, a 33~o aqueous solution (4 Vh) of sulfuric acid was added so that the pH
value of the medium was maintained between 1.5 and 2.0, then ethyl acetate was added at a flow rate of 900 l/h to extract an acidic retentate at room temperature in the countercul,ellt in a series of five cellllirugal extractors, whereat in the second -self-elllplyillg - centrifugal separator the still rem~ining separated proteins were simultaneously removed.

The combined ethyl acetate extract from the series of the centrifugal extractors was washed in the first centrifugal extractor with demineralized water having a flow rate of 30 l/h and thus the still rem~ining water-soluble illl~uliLies were removed.

The ethyl acetate extract having the flow rate of 900 l/h was dried in vacuo at the temperature of 30 C in the rectification column so that the water content of 0.03 Wo 95/23s70 218 4 6 I 9 11 PCT/SI95/00002 vol.% was achieved, then the extract was evaporated in a thin-layer evaporator in vacuo at the temperature of 30 C to a lt20 of the original volume. The obtained con-centrated ethyl acetate extract (concentration of the impure clavulanic acid amounted to 50 g/l) having the flow rate of 45 Vh was decolourized by a continuous addition of active carbon tO.45 kg), the ~ Lule was stirred for 30 minutes and then the carbon was filtered off from the suspension of the concentrate of the ethyl acetate extract on a ples~ure filter under nitrogen pressure of 1 bar to obtain a dry concentrate (45 l) of the ethyl acetate extract containing impure clavulanic acid.

Example 2 Preparation of N~N~-diiso~lo~ylethylenerli~mmonium diclavlll~n~te To a dry concentrate (45 l) of ethyl acetate extract obtained in the colllilluous process of E~ample 1 (the clavulanic acid content amounted to 50 g/l), N,N'-diiso-propylethylenediamine (1.41) was added for 5 minutes under vigorous stirring at the temperature of 25 C. The obtained suspension was filtered off, the obtained crystals were resuspended in acetone (451) and, at stirring and cooling the suspension at a temperature under 10 C, crystals of the desired substance were separated, whichcrystals were filtered off, washed with acetone and dried in vacuo at the temperature of 30 C. Crystals of N,N'-diiso~ro~ylethylenediammonium diclav~ n~te (3.3 kg; the clavulanic acid content amounted to 60%) were obtained.

Example 3 Preparation of potassium clavulanate N,N'-diisopropylethylenediammonium diclavulanate (3.3 kg) from Example 2 was dissolved in an isopropanol/water mL~Lule (82.5 1; the water portion amounted to1.5~o) and to the obtained solution active carbon (1.5 kg) and potassium 2-ethylhexanoate (0.51; 2 M) were added for 30 minutes under stirring at room tempera-ture. Then the carbon and the obtained precipitate were filtered off. To the obtained filtrate (80 1) a solution (61) of potassium 2-ethyl hexanoate (2 M) in isopropanol was added for 20 minutes during stirring at room temperature. The obtained suspension was then stirred under cooling at a temperature between 0 C and 5 C for another 2 hours, then the separated crystals were filtered off, washed with isopropanol and acetone and dried in vacuo at the temperature of 30 C. Potassium clavulanate (2 kg;

WO95t23870 PCT/SI5S~C 2 2i~ 2 USP grade, the clavulanic acid content 80.6%, determined by HPLC method) was obtained.

Claims (5)

1. Process for the isolation of clavulanic acid and of pharmaceutically acceptable salts thereof from the aqueous fermentation broth of Streptomyces sp. P 6621 FERM P 2804, characterized in that from the fermentation broth the mycelium, a major part of proteins and other suspended solid particles are removed by microfiltration at a pH value of the medium between 5.8 and 6.2 and at a tempera-ture between about 20°C and 40°C, the purified broth (the aqueous phase) is op-tionally additionally purified by ultrafiltration, and the thus purified broth is con-centrated by reverse osmosis, then it is directly extracted in a countercurrent in a series of centrifugal extractors with a water-immiscible organic solvent at a pH value of the medium between 1 and 3, whereat the still remaining separated proteins are simultaneously removed, the organic phase is washed with water, dried in vacuo in a rectification column to a water content of under 0.1 vol.% and then concentrated by evaporation, decolourized by the treatment with active carbon and then the clavulanic acid present in the completely dry organic phase is isolated and purified by the reaction with N,N'-diisopropylethylenediamine at a temperature of about roomtemperature to N,N'-diisopropylethylenediammonium diclavulanate, which is iso-lated and then reacted with potassium 2-ethyl hexanoate in isopropanol to yield the potassium salt of clavulanic acid having high purity.

2. Process according to claim 1, characterized in that the pH value of the medium is adjusted with sulfuric acid.

3. Process according to claim 1, characterized in that as water-immiscible or-ganic solvent in direct extraction ethyl acetate is used.

4. Process according to claim 1, characterized in that the direct countercurrentextraction of the purified aqueous fermentation broth is carried out with ethyl acetate at a temperature between 15°C and 25°C.

5. Process according to claim 1, characterized in that the water content at the drying of the organic phase amounts to between 0.03 and 0.05 vol.%.