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WO2010115838A1 - Procédé de fermentation - Google Patents

Procédé de fermentation Download PDF

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Publication number
WO2010115838A1
WO2010115838A1 PCT/EP2010/054401 EP2010054401W WO2010115838A1 WO 2010115838 A1 WO2010115838 A1 WO 2010115838A1 EP 2010054401 W EP2010054401 W EP 2010054401W WO 2010115838 A1 WO2010115838 A1 WO 2010115838A1
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WO
WIPO (PCT)
Prior art keywords
source
fermentation
process according
repressing
growth rate
Prior art date
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Ceased
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PCT/EP2010/054401
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English (en)
Inventor
Van Wouter Adrianus Winden
Van Anton Bernard Putten
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DSM IP Assets BV
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DSM IP Assets BV
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Priority to CN201080014358XA priority Critical patent/CN102369290A/zh
Priority to EP10713893A priority patent/EP2414530A1/fr
Publication of WO2010115838A1 publication Critical patent/WO2010115838A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P35/00—Preparation of compounds having a 5-thia-1-azabicyclo [4.2.0] octane ring system, e.g. cephalosporin
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P17/00—Preparation of heterocyclic carbon compounds with only O, N, S, Se or Te as ring hetero atoms
    • C12P17/18—Preparation of heterocyclic carbon compounds with only O, N, S, Se or Te as ring hetero atoms containing at least two hetero rings condensed among themselves or condensed with a common carbocyclic ring system, e.g. rifamycin
    • C12P17/188—Heterocyclic compound containing in the condensed system at least one hetero ring having nitrogen atoms and oxygen atoms as the only ring heteroatoms
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P37/00—Preparation of compounds having a 4-thia-1-azabicyclo [3.2.0] heptane ring system, e.g. penicillin

Definitions

  • the present invention relates to an industrial process for the production of a valuable compound. This process allows high production levels of valuable compounds, such as primary or secondary metabolites, pharmaceutical proteins or peptides, or industrial enzymes, in an economically attractive yield.
  • C-source which is usually also the energy source
  • a very common C-source is glucose.
  • the C-source may also influence the production rate of the valuable compound.
  • the production rate depends on the concentration of the C-source, such that an increase of C-source concentration leads to an increase in the production rate.
  • a critical concentration the C-source often results in a reduced production rate. This phenomenon is called "repression".
  • a repressing C-source is as defined herein below. It is well known that glucose is a repressing sugar for production of metabolites by many microorganisms under various conditions. For instance Change et al. (J. Industrial Microbiol. (1990), 6, 165-169) describe that excess glucose results in lower penicillin V production in fermentation processes with wild type
  • Penicillium chrysogenum strains The fact that glucose is a less favourable carbon source for penicillin production in batch cultures than, for example, lactose, was already discovered in the first years of penicillin production process development (e.g. Moyer and Coghill in J. Bacteriol. (1946), 51 , 57-78).
  • Another way is that to keep repressing C-sources below the critical concentration during the course of the fermentation. This may be achieved by feeding the C-source to the fermentor under such conditions that the concentration of the C-source during fermentation remains below values where the repressing effect occurs.
  • Robin et al. used a glucose feed under limiting conditions for the production of adipyl-7-ADCA by a Penicillium chrysogenum strain transformed with the gene encoding the expandase gene (Metabolic Engineering (2003), 5, 42048 and Biotechnology and Bioengineering
  • a disadvantage of a low concentration of C-source is that the biomass-specific growth rate (as defined herein below) of the microorganism is limited by the availability of C-source, resulting in slow formation of biomass and hence a long fermentation time to reach the desired level of valuable compound.
  • Another disadvantage of using a low concentration of C-source is that the biomass-specific production rate (as defined herein below) by the microorganism is also low, again resulting in a low production rate.
  • a third way is to completely avoid the use of the repressing C-sources which are known to be repressing in fermentation processes using certain microorganisms for the production of selected valuable compounds but instead to use a C-source which is known to be non-repressing.
  • a non-repressing C- source instead of a repressing C-source, since non-repressing C-sources have no negative effect on the production rate and can advantageously be used at high concentrations from the onset of the fermentation without the need to limit the concentration.
  • Viscosity is generally determined by two factors, namely by the amount (concentration) of the biomass in the fermentation broth, and by the morphology of the microorganism (called “biomass-specific viscosity").
  • filamentous microorganisms like filamentous bacteria such as Actinomycetes or filamentous fungi such as Penicillium or Aspergillus, typically have a dispersed mycelium with very long and branched hyphae which leads to undesirably high biomass-specific broth viscosity.
  • biomass-specific viscosity can build up rapidly, leading to poor oxygen transport in the broth.
  • a low (biomass-specific) viscosity of the fermentation broth is therefore advantageous for the production rate.
  • An alternative method is to limit the growth rate by the supply of another nutrient than the C-source.
  • Oh et al Biotechnology and Bioengineering (1988), 32, 569-573) demonstrated that phosphate limitation in a batch fermentation of Penicillium chrysogenum in the presence of a high concentration of a non-repressing sugar (i.e. 3% lactose) results in a 2-fold increase in the biomass-specific production rate of penicillin.
  • a great disadvantage of this batch fermentation system is that the volumetric production rate of the phosphate limited fermentation is much lower compared to the control (see Figure 1 in Oh et al.).
  • Biomass-specific production rate also referred to as “production rate” is defined herein as the amount of valuable compound (based on dry matter) produced per amount of biomass (based on dry matter) per amount of time (in reciprocal time)
  • Volumetric production rate is the amount of valuable compound (based on dry matter) produced per bioreactor volume (in reciprocal cubic meters) per amount of time (in reciprocal time).
  • Biomass specific growth rate also referred to as “growth rate” is defined herein as the amount of biomass (based on dry matter) produced per amount of biomass (based on dry matter) per amount of time (in reciprocal time).
  • Growth rate limiting nutrient is defined herein as the nutrient which is the dominant growth rate governing factor.
  • a "repressing C-source” is a C-source which, at increasing concentration in the fermentor, results in an initial increase of the biomass-specific production rate, but which, above a critical concentration of the C-source, results in a decrease of the biomass-specific production rate.
  • a “non-repressing C-source” is a C-source which, at increasing concentration, results in an increase of the biomass-specific production rate, until, above a certain concentration, the biomass-specific production rate reaches a plateau value.
  • a non-repressing C-source therefore does not, above a critical concentration, result in a decrease of the biomass-specific production rate.
  • Non-repressing C-sources may therefore advantageously be used in fermentation processes at high concentrations.
  • the present invention provides a process for the production of a valuable compound, comprising fermentation of a microbial strain on an industrial scale in a medium comprising a non-repressing C-source and feeding at least one growth rate limiting nutrient, whereby the production of penicillin-G by semi-continuous fermentation of Penicillium chrysogenum with biomass retention is excluded.
  • the process for the production of a valuable compound is subject to repression by a repressing C-source as defined.
  • the non-repressing C-source may be any assimilable C-source which is non- repressing for the microorganism producing said valuable compound.
  • the non-repressing C-source may be present at high concentrations during any time point in the fermentation process.
  • the total amount of non-repressing C-source required for the entire fermentation process may be added at the beginning of the fermentation process, resulting in high concentrations which, in case a repressing C-source would be used, would result in significant repressing conditions.
  • the non-repressing C-source may also be added at certain time intervals during the fermentation or as a continuous feed. The skilled person is very well capable of designing the fermentation process for a given microorganism and valuable compound in order to get optimal results.
  • the non-repressing C-source may be selected from the group consisting of carbohydrates, polyols, oils and triglycerides, alcohols, organic acids, amino acids and proteins.
  • Carbohydrates may include for example monosaccharides such as glucose, fructose and galactose; disaccharides such as sucrose, lactose and maltose; polysaccharides such as starch, dextrin, maltodextrin, inulin, and cellulose.
  • Polyols may include for example glycerol, sorbitol, and mannitol.
  • Oils may include for example soybean oil and rape seed oil.
  • Alcohols may include for example methanol, ethanol, propanol and higher alcohols.
  • Organic acids may include for example formic acid, acetic acid, propionic acid, citric acid and benzoic acid.
  • Proteins may include peptides of any size, for example dipeptides, tripeptides, oligopeptides and polypeptides, including (partially) hydrolyzed proteins (so-called protein hydrolysates).
  • the growth rate limiting nutrient may be any nutrient provided it is required for growth and may be fed at growth rate limiting conditions.
  • the growth rate limiting nutrient is not the C-source.
  • the growth rate limiting nutrient is selected from the group consisting of a phosphorous source, a nitrogen source, a sulphur source, an oxygen source, one or more vitamins and one or more trace elements.
  • the growth rate limiting nutrient is the phosphorus source or preferably the growth rate limiting nutrient is the nitrogen source or preferably the growth rate limiting nutrient is the sulphur source.
  • the growth rate limiting nutrient is the phosphorus source.
  • a suitable phosphorous source that may be added as the growth rate limiting nutrient is well known in the art and may for example be phosphoric acid or a phosphate- containing salt such as ortho-phosphate, hydrogen phosphate, dihydrogen phosphate and/or pyrophosphate.
  • a phosphate- containing salt such as ortho-phosphate, hydrogen phosphate, dihydrogen phosphate and/or pyrophosphate.
  • the skilled person is very well capable of selecting the appropriate phosphorus source.
  • a suitable nitrogen source that may be added as the growth rate limiting nutrient is well known in the art and may for example be urea, ammonia, nitrate, and/or ammonium salts such as ammonium sulphate, ammonium phosphate and/or ammonium nitrate, and amino acids such as glutamate and/or lysine.
  • the skilled person is very well capable of selecting the appropriate nitrogen source.
  • a suitable sulphur source that may be added as the growth rate limiting nutrient is well known in the art and may for example be sulphuric acid, sulphate and/or thiosulphate. The skilled person is very well capable of selecting the appropriate sulphur source.
  • the growth rate limiting nutrient is not the exclusive source of elements (i.e. atoms) which are incorporated into the valuable compound.
  • the growth rate and the production rate are uncoupled. This is advantageous because feeding such nutrient results in limitation of the growth rate (and hence of biomass-specific viscosity) but not of the production rate.
  • the skilled man knows how to select nutrients that are not the exclusive source of elements composing the valuable compound. For example, if the valuable compound contains (in addition to O and H) N, C, and S, the growth rate limiting nutrient in this embodiment should not be the only source of N, C, and S.
  • the growth rate limiting nutrient is preferable selected from the group of nutrients that are not the exclusive source of the elements C, H, N and S.
  • a preferred embodiment in this case would be to use a suitable phosphorous source as the growth rate limiting nutrient.
  • the production rate in the process of the invention is higher than the production rate in the same process but without feeding at least one growth rate limiting nutrient.
  • Feeding at least one growth rate limiting nutrient advantageously provides a tool to limit the growth rate and hence the biomass-specific viscosity.
  • an industrial scale fermentation process or an industrial process may be understood to encompass a fermentation process on a volume scale which is > 10 m 3 , preferably > 25 m 3 , more preferably > 50 m 3 , most preferably > 100 m 3 , preferably less than 5000 m 3 .
  • the process of the invention may be performed as a fed-batch, a repeated fed- batch, a semi-continuous fed batch or a continuous fermentation process.
  • either none or part of the fermentation media compounds are added to the media before the start of the fermentation and either all or the remaining part, respectively, of the compounds is fed during the fermentation process.
  • the compounds which are selected for feeding can be fed together or separate from each other to the fermentation process.
  • the complete starting medium is additionally fed during fermentation.
  • part of the fermentation broth comprising the biomass is removed at regular time intervals, whereas in a continuous process, the removal of part of the fermentation broth occurs continuously.
  • the fermentation process is thereby replenished with a portion of fresh medium corresponding to the amount of withdrawn fermentation broth.
  • the process of the invention is suitable for the fermentative production of any valuable compound of interest, including primary or secondary metabolites, pharmaceutical proteins or peptides, or industrial enzymes.
  • Primary metabolites are biomolecules that are essential to the growth, development or reproduction, and are shared by many species. Primary metabolites are for example intermediates of the main metabolic pathways such as the glycolytic pathway or the TCA cycle. Examples of primary metabolites are amino acids and nucleic acids.
  • Secondary metabolites are not essential for growth, development, or reproduction, but instead have an ecological function.
  • Examples of secondary metabolites are antibiotics or ⁇ -lactam compounds, especially ⁇ -lactam antibiotics.
  • a preferred valuable compound is a ⁇ -lactam compound.
  • Examples of ⁇ -lactam compounds are clavulanic acid, penicillin (e.g. penicillin-G, penicillin-V or 6-aminopenicillinic acid) and semisynthetic penicillins such as amoxicillin and cephalosporins such as cephalosporin C.
  • the ⁇ -lactam compound is an N-acylated derivative of ⁇ -lactam intermediates such as 7-ADCA, 7-ACA, 7-ADAC, 7-ACCA, 7-PACA or 7-amino-3-carbamoyloxymethyl-3-cephem-4-carboxylic acid.
  • the acyl-group at the 7- amino position is preferably adipic acid yielding the corresponding adipoyl-derivate as disclosed in WO93/05158, WO93/08287 or WO 2004/106347.
  • Alternative suitable side chains have been disclosed in WO95/04148, WO95/04149, WO96/38580, WO98/48034 and WO98/48035
  • a suitable microbial strain for the process of the invention may be any wild type strain producing a valuable compound of interest.
  • a suitable microbial strain of the invention may be a strain which has been obtained and/or improved by subjecting a parent or wild type strain of interest to a classical mutagenic treatment or to recombinant
  • the microbial strain which is suitable for the process of the invention is a yeast, a fungus, a protozoa or a bacterium.
  • the microbial strain may include filamentous and non-filamentous strains.
  • the microbial strain is a filamentous strain, preferably a bacterium or a fungus.
  • a preferred filamentous bacterium is an Actinomycete.
  • the Actinomycete is Streptomyces clavurigerus. Which preferably produces clavulanic acid as the valuable compound.
  • a filamentous fungus is preferably selected from the group consisting of Aspergillus, Trichoderma, Penicillium and Acremonium.
  • Preferred examples are Penicillium chrysogenum for the production of PenG or PenV, Acremonium chrysogenum for the production of cephalosporin C and Aspergilli such as Aspergillus niger or Aspergillus oryzae either as wild type or classically improved strains producing, or genetically modified to overexpress genes encoding, enzymes such as amylases, lipases, phospholipases, galactolipases, hemicellulases, xylanases, cellulases, proteases and other enzymes known to be used in industry.
  • the fungus is Penicillium chrysogenum and the secondary metabolites are adipoyl-7-ADCA, adipoyl-7-ADCA, adipoyl-7-ACA, adipoyl-7- ADAC, adipoyl-7-ACCA, V7-PACA or adipoyl ⁇ -amino-S-carbamoyloxymethyl-S-cephem ⁇ - carboxylic acid, most preferred is adipoyl-7-ADCA.
  • the secondary metabolites are adipoyl-7-ADCA, adipoyl-7-ADCA, adipoyl-7-ACA, adipoyl-7- ADAC, adipoyl-7-ACCA, V7-PACA or adipoyl ⁇ -amino-S-carbamoyloxymethyl-S-cephem ⁇ - carboxylic acid, most preferred is adipoyl-7-ADCA.
  • Penicillium chrysogenum strain is transformed with and expressing a gene encoding an expandase.
  • This engineered Penicillium chrysogenum strain when grown in the presence of adipic acid as the side chain precursor in the fermentation vessel, produces and excretes adipoyl-7-ADCA.
  • FIG. 1 Phosphate concentration during fermentation. Solid line, fermentation A; bold solid line, fermentation B; dashed line, fermentation C. Fermentation A and
  • FIG. 1 Adipoyl ⁇ -aminodeacetoxycephalosporinic acid production. Solid line, fermentation A; bold solid line, fermentation B; dashed line, fermentation C.
  • FIG. 1 Phosphate concentration during fermentation. Solid line, fermentation D; dashed line, fermentation E. Figure 5. Adipoyl-7-ADCA concentration during fermentation. Solid line, fermentation D; dashed line, fermentation E.
  • adipoyl-7-ADCA concentration was determined via HPLC as described in US 6,410,259.
  • Penicillium chrysogenum CBS 455.95 which has been transformed with an expandase expression cassette wherein the expandase coding region is provided with the IPNS promoter, as described in WO93/05158, was fermented in media according to Table 1. Three separate fermentations (A-C) were carried out. Trace element solution is according to Table 2. The fermentation conditions are listed in Table 3. The fermentations were inoculated at an inoculation strength of 5 vol% with inoculum grown in the same medium as given for fermentation A in Table 1 , except that the concentration of glucose was 50 g/kg and no potassium adipate was present.
  • Figure 1 shows the phosphate concentration during the fermentation.
  • Figure 2 shows the relative stirrer speed during the fermentation. Higher stirring speeds correspond to higher viscosity.
  • Figure 3 shows the adipoyl-7-ADCA production.
  • Example 2 Two fermentations D and E were carried out as described in Example 1 except that the composition of the media was according to Table 5. Phosphate is not present in the initial media but is instead fed as a solution containing 2.76 g/kg KH 2 PO 4 and 1.96 g/kg K 2 HPO 4 according to the feed profile as listed in Table 4.
  • Figure 4 shows the phosphate concentration during the fermentation.
  • Figure 5 shows the adipoyl-7-ADCA acid production.
  • Penicillium chrysogenum CBS 455.95 was fermented in media according to Table 1. Three fermentations F, G and H were carried out as described in Example 1 for A, B and C respectively, except that the media (Table 1) did not contain potassium adipate, but instead contained 1 g/kg of potassium phenylacetic acid. Another difference with Example 1 was that the untransformed Penicillium chrysogenum CBS 455.95 was used. The fermentation conditions were identical to Example 1 (Table 6) except that the concentration of phenylacetic acid was kept between 0.6 and 2.0 g/kg by analysing the concentration in the broth every 4 hours and dosing an adequate amount of a concentrated solution of potassium phenylacetic acid to the broth.

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Abstract

La présente invention porte sur un procédé de fabrication d'un composé précieux comprenant la fermentation à une échelle industrielle d'une souche microbienne comprenant une source de carbone (C) favorable et l'introduction d'au moins un élément nutritif limitant la vitesse de croissance. Le procédé comprend des souches fongiques, de levure, de protozoaire et de bactéries.
PCT/EP2010/054401 2009-04-03 2010-04-01 Procédé de fermentation Ceased WO2010115838A1 (fr)

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CN201080014358XA CN102369290A (zh) 2009-04-03 2010-04-01 发酵工艺
EP10713893A EP2414530A1 (fr) 2009-04-03 2010-04-01 Procédé de fermentation

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EP09157313.9 2009-04-03
EP09157313 2009-04-03

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Cited By (5)

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CN107164420A (zh) * 2017-07-07 2017-09-15 精晶药业股份有限公司 一种l‑丙氨酸半连续发酵的方法
US10030225B2 (en) * 2012-11-14 2018-07-24 Merck Patent Gmbh Cell culture media
US11162115B2 (en) 2017-06-30 2021-11-02 Inv Nylon Chemicals Americas, Llc Methods, synthetic hosts and reagents for the biosynthesis of hydrocarbons
US11505809B2 (en) 2017-09-28 2022-11-22 Inv Nylon Chemicals Americas Llc Organisms and biosynthetic processes for hydrocarbon synthesis
US11634733B2 (en) 2017-06-30 2023-04-25 Inv Nylon Chemicals Americas, Llc Methods, materials, synthetic hosts and reagents for the biosynthesis of hydrocarbons and derivatives thereof

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