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EP1313838A2 - Laboration de l-thr onine par fermation - Google Patents

Laboration de l-thr onine par fermation

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Publication number
EP1313838A2
EP1313838A2 EP01984568A EP01984568A EP1313838A2 EP 1313838 A2 EP1313838 A2 EP 1313838A2 EP 01984568 A EP01984568 A EP 01984568A EP 01984568 A EP01984568 A EP 01984568A EP 1313838 A2 EP1313838 A2 EP 1313838A2
Authority
EP
European Patent Office
Prior art keywords
threonine
resistance
fermentation
process according
producing
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP01984568A
Other languages
German (de)
English (en)
Inventor
Thomas Hermann
Mechthild Rieping
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Evonik Operations GmbH
Original Assignee
Degussa GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from DE10103778A external-priority patent/DE10103778A1/de
Application filed by Degussa GmbH filed Critical Degussa GmbH
Publication of EP1313838A2 publication Critical patent/EP1313838A2/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • C12P13/00—Preparation of nitrogen-containing organic compounds
    • C12P13/04—Alpha- or beta- amino acids
    • C12P13/08—Lysine; Diaminopimelic acid; Threonine; Valine

Definitions

  • the invention provides a new process for the fermentative preparation of L-threonine with Enterobacteriaceae.
  • L-Threonine is used in animal nutrition, in human medicine and in the pharmaceuticals industry.
  • L-threonine can be prepared by fermentation of strains of the Enterobacteriaceae family, in particular Escherichia coli. Because of the great importance of this amino acid, work is constantly being undertaken to improve the preparation processes. Improvements to the process can relate to fermentation measures, such as e.g. stirring and supply of oxygen, or the composition of the nutrient media, such as e.g. the sugar concentration during the . fermentation, or the working up to the product form, by e.g. ion exchange chromatography, or the intrinsic output properties, i.e. those of genetic origin, of the microorganism itself.
  • fermentation measures such as e.g. stirring and supply of oxygen, or the composition of the nutrient media, such as e.g. the sugar concentration during the . fermentation, or the working up to the product form, by e.g. ion exchange chromatography, or the intrinsic output properties, i.e. those of genetic origin, of the microorganism itself.
  • the invention provides a fermentation process, which is characterized in that
  • a portion of the fermentation broth is separated off, 1 to 90 vol.%, in particular 1 to 50 vol.%, preferably 1 to 25 vol.% and particularly preferably 5 to 50 vol.% of the total volume of the fermentation broth remaining in the fermentation tank, subsequently
  • the remaining fermentation broth is topped up with growth medium and, preferably after a growth phase, a further fermentation is carried out by the feed process (fed batch) mentioned,
  • steps b) and c) are optionally carried out several times, and
  • the L-threonine is isolated from the fermentation broths collected.
  • the microorganisms with which the process according to the invention can be carried out can prepare L-threonine from glucose, sucrose, lactose, fructose, maltose, molasses, starch, or from glycerol and ethanol, the preparation from glucose, sucrose or molasses being preferred.
  • They are representatives of Enterobacteriaceae, in particular of the genera Escherichia, Serratia and Providencia.
  • the species Escherichia coli and of the genus Serratia the species Serratia marcescens are to be mentioned in particular.
  • Suitable L-threonine-producing strains of the genus Escherichia, in particular of the species Escherichia coli are, for example
  • Escherichia coli B-3996 (pMW: : THY)
  • Serratia in particular of the species Serratia marcescens, are, for example
  • Strains from the Enterobacteriaceae family which produce L- threonine preferably have, inter alia, one or more genetic or phenotypic features chosen from the group consisting of: resistance to ⁇ -amino- ⁇ -hydroxyvaleric acid, resistance to thialysine, resistance to ethionine, resistance to ⁇ - methylserine, resistance to diaminosuccinic acid, resistance to ⁇ -aminobutyric acid, resistance to borrelidin, resistance to rifampicin, resistance to valine analogues, such as, for example, valine hydroxa ate, resistance to purine analogues, such as, for example, 6- dimethylaminopurine, a need for L-methionine, optionally a partial and compensatable need for L-isoleucine, a need for meso-diaminopimelic acid, auxotrophy in respect of threonine-containing dipeptides, resistance to L-threonine, resistance
  • the strain 472T23 (US-A-5, 631, 157 ) has, inter alia, an enhanced, "feed back” resistant aspartate kinase I-homoserine dehydrogenase I, an attenuated threonine deaminase, a resistance to at least 5 g/1 L- threonine and the ability to utilize sucrose as a source of carbon.
  • the strain B-3996 (US-A-5, 175, 107 ) has, inter alia, an enhanced, "feed back” resistant aspartate kinase I-homoserine dehydrogenase I, an attenuated threonine deaminase, an attenuated threonine dehydrogenase, a resistance to at least 5 g/1 L-threonine and the ability to utilize sucrose as a source of carbon.
  • the strain kat-13 (US-A-5, 939, 307) has, inter alia, an enhanced, "feed back” resistant aspartate kinase I-homoserine dehydrogenase I, an attenuated threonine dehydrogenase, resistance to borrelidin and the ability to utilize sucrose as a source of carbon.
  • the strain KCCM-10132 (WO 00/09660) has a resistance to ⁇ -methylserine, a resistance to diaminosuccinic acid, sensitivity to fluoropyruvate, a resistance to L-glutamic acid and a resistance to at least 7% L-threonine.
  • the strain is also in need of the amino acids L-methionine and L-isoleucine.
  • enhancement in this connection describes the increase in the intracellular activity of one or more enzymes in a microorganism which are coded by the corresponding DNA, for example by increasing the number of copies of the gene or allele or of the genes or alleles, using a potent promoter or using a gene or allele which codes for a corresponding enzyme having a high activity, and optionally combining these measures.
  • the activity or concentration of the corresponding protein is in general increased by at least 10%, 25%, 50%, 75%, 100%, 150%, 200%, 300%, 400% or 500%, up to a maximum of 1000% or 2000%, based on the starting microorganism.
  • the term "attenuation" in this connection describes the reduction or elimination of the intracellular activity of one or more enzymes (proteins) in a microorganism which are coded by the corresponding DNA, for example by using a weak promoter or using a gene or allele which codes for a corresponding enzyme with a low activity or inactivates the corresponding gene or enzyme (protein) , and optionally combining these measures.
  • the activity or concentration of the corresponding protein is in general reduced to 0 to 50%, 0 to 25%, 0 to 10% or 0 to 5% of the activity or concentration of the wild-type protein.
  • the system output of a fermentation unit producing L-threonine is increased by a procedure in which after a first fermentation step a portion of the fermentation broth obtained in this way remains in the production fermenter and serves as the inoculum for one or more further fermentation steps (batches) .
  • 1 to 90 vol.% preferably 1 to 50 vol.%, preferentially 1 to 25 vol.%, 1 to 20 vol.%, 1 to 15 vol.% or 1 to 10 vol.%, and particularly preferably 5 to 20 vol.%, 5 to 15 vol.% or 1 to 10 vol.% of the total volume of the fermentation broth remains in the fermentation tank.
  • the broth remaining in the fermentation tank is preferably topped up with a growth medium.
  • a production medium is fed in.
  • the components of this medium can also be fed in separately.
  • 20 to 72 hours preferably 20 to 48 hours
  • the batch is ended and a portion of the fermentation broth, as described above, is separated off.
  • a new fermentation stage is then optionally started with the remainder.
  • the process can be repeated at least once, preferably approx. 2 to 6 times, depending on the stability of the strain used. Repetitions of approx. 2 to 8 times or 2 to 10 times or 2 to 4 times are also possible.
  • the growth medium typically comprises sugars, such as e.g. glucose, starch hydrolysate, sucrose or molasses, as the source of carbon.
  • Sugars such as e.g. glucose, starch hydrolysate, sucrose or molasses
  • Organic nitrogen-containing compounds such as peptones, yeast extract, meat extract, malt extract, corn steep liquor, soya bean flour and urea, or inorganic compounds, such as ammonium sulfate, ammonium chloride, ammonium phosphate, ammonium carbonate and ammonium nitrate, can be used as the source of nitrogen.
  • the sources of nitrogen can be used individually or as a mixture.
  • Phosphoric acid, potassium dihydrogen phosphate or dipotassium hydrogen phosphate or the corresponding sodium- containing salts can be used as the source of phosphorus.
  • the culture medium must furthermore comprise salts of metals, such as e.g. magnesium sulfate, manganese sulfate or iron sulfate, which are necessary for growth.
  • salts of metals such as e.g. magnesium sulfate, manganese sulfate or iron sulfate, which are necessary for growth.
  • essential growth substances such as amino acids (e.g. homoserine) and vitamins (e.g. thiamine), are employed in addition to the above-mentioned substances.
  • Antifoams such as e.g. fatty acid polyglycol esters, can be employed to control the development of foam.
  • the production medium comprises only one sugar, such as e.g. sucrose or glucose, and optionally an inorganic source of nitrogen, such as e.g. ammonium sulfate.
  • sugar such as e.g. sucrose or glucose
  • inorganic source of nitrogen such as e.g. ammonium sulfate.
  • these and other components can also be fed in separately.
  • the temperature is established in a range from 29°C to 42°C, preferably 33°C to 40°C. Temperatures in a range from 27°C to 39°C are also possible.
  • the fermentation can be carried out under normal pressure or optionally under increased pressure, preferably under an increased pressure of 0 to 1.5 bar.
  • the oxygen partial pressure is regulated at 5 to 50%, preferably approx. 20% atmospheric saturation. Regulation of the pH to a pH of approx. 6 to 8, preferably 6.5 to 7.5, can be effected with 25% aqueous ammonia.
  • the process according to the invention is distinguished with respect to conventional processes above all by an increased space/time yield or productivity.
  • a plasmid-free variant of the E. coli strain 472T23 was obtained from the American Type Culture Collection (Manasas, VA. , USA) as ATCC98082.
  • the strain ATCC98082 is described in the patent specification US-A-5, 631, 157.
  • the E. coli strain VL334/pYN7 was obtained from the Russian National Collection of Industrial Microorganisms (VKPM, Moscow, Russia) as CMIM B-1684.
  • the strain CMIM B-1684 is described in the patent specification US-A-4 , 278 , 765.
  • the plasmid pYN7 was isolated from the strain VL334/pYN7.
  • a DNA fragment 6.25 kbp long which carries the thrABC operon was isolated from plasmid pYN7 by preparative agarose gel electrophoresis with the aid of the restriction enzymes Hindlll and Ba HI .
  • the plasmid pBR322 (Bolivar et al., Gene 2, 95-113 (1977)) was obtained from Pharmacia Biotech (Uppsala, Sweden) and treated with the restriction enzymes Hindlll and BamHI.
  • the DNA fragment 4.3 kbp long was isolated by preparative agarose gel electrophoresis. The two DNA fragments were mixed, treated with T4 DNA ligase, and the strain DH5 ⁇ was transformed with the ligation mixture. After selection on a picillin-containing (50 ⁇ g/mL) LB agar, transformants which contained a plasmid which corresponded in its structure to the plasmid pYN7 were obtained.
  • the plasmid was isolated from a transformant, cleaved partly with the enzyme EcoRI and completely with the enzyme Hindlll and ligated with the parB gene region isolated.
  • the plasmid pKG1022 (Gerdes, Biotechnology (1988) 6:1402-1405) was cleaved with the enzymes EcoRI and Hindlll, the cleavage batch was separated in 1% agarose gel and the parB fragment 629 bp in size was isolated with the aid of the QIAquick Gel Extraction Kit (QIAGEN, Hilden, Germany) .
  • the ligation mixture was employed for transformation of strain ATCC98082.
  • Plasmid- carrying cells were carried out on LB agar (Lennox, Virology 1:190 (1955)), to which 50 ⁇ g/ml ampicillin had been added. Successful cloning of the parB gene region could be detected after isolation of the plasmid DNA, control cleavage with EcoRI and Hindlll and analysis of the cleavage batch by agarose gel electrophoresis.
  • the plasmid was designated pYN7parB.
  • the strain DM1265 has, inter alia, an enhanced, "feed back” resistant aspartate kinase I-homoserine dehydrogenase I, an attenuated threonine deaminase, a resistance to at least 5 g/1 L-threonine and the ability to utilize sucrose as a source of carbon.
  • This strain is distinguished by a high stability, in particular segregation stability.
  • An individual colony of the strain DM1265 was transinoculated on to minimal medium with the following composition: 3.5 g/1 Na 2 HP0 4 *2H 2 0, 1.5 g/1 KH 2 P0 4 , 1 g/1 NH 4 CI, 0.1 g/1 MgS0 4 *7H 2 0, 2 g/1 sucrose, 20 g/1 agar, 50 mg/1 ampicillin.
  • the culture was incubated at 37°C for approx. 5 days.
  • 10 ml preculture medium with the following composition: 2 g/1 yeast extract, 10 g/1 (NH 4 ) 2 S0 4 , 1 g/1 KH 2 P0 4 , 0.5 g/1 MgS0 4 *7H 2 0, 15 g/1 CaC0 3 , 20 g/1 sucrose,
  • a volume of 1 ml of this first preculture was inoculated into 1402 g of the nutrient medium Al-144.
  • the culturing fermentation was carried out in 2 1 stirred reactor fermenters from B. Braun (BBI, Germany, Melsungen, Biostat MD model) .
  • the nutrient medium Al-144 contained the constituents listed in Table 1.
  • This second preculture was cultured for 22.5 h at a temperature of 37°C, a volume- specific gassing of 0.71 vvm (volume per volume per minute) , an oxygen partial pressure of 10% of the atmospheric saturation and a pH of pH 7.0 until an optical density (OD) (660 nm) of 16.3 was reached.
  • OD optical density
  • the growth medium Ml-463 contained the constituents listed in Table 2.
  • the culture was cultured at a temperature of 37°C, an aeration of 1 1/min, a minimum stirring of 800 rpm and a pH of 7.0 and an oxygen partial pressure of 20% of the atmospheric saturation until a residual sugar concentration of approx. 3 g/1 was reached.
  • the broth obtained in this way was subsequently cultured for a further 30 h at a temperature of 37°C, an oxygen partial pressure of 20% of the atmospheric saturation and a pH of pH 7.0 until an OD (660 nm) of 33.4 was reached.
  • 450 g of a production medium comprising a sucrose solution with a concentration of 650 g/1 was fed in continuously.
  • optical density was then determined with a digital photometer of the LP1W type from Dr. Bruno Lange GmbH (Berlin, Germany) at a measurement wavelength of 660 nm and the concentration of L-threonine formed was determined by ion exchange chromatography and post-column reaction with ninhydrin detection with an amino acid analyzer from Eppendorf-BioTronik (Hamburg, Germany) ,
  • An individual colony of the strain DM1265 was transinoculated on to minimal medium with the following composition: 3.5 g/1 Na 2 HP0 4 *2H 2 0, 1.5 g/1 KH 2 P0 4 , 1 g/1 NH 4 C1, 0.1 g/1 MgS0*7H 2 0, 2 g/1 glucose, 20 g/1 agar, 50 mg/1 ampicillin.
  • the culture was incubated at 37°C for approx. 5 days.
  • 10 ml preculture medium with the following composition 2 g/1 yeast extract, 10 g/1 (NH) 2 S0 4 , 1 g/1 KH 2 P0 4 , 0.5 g/1 MgS0 4 *7H 2 0, 15 g/1 CaC0 3 , 20 g/1 glucose, 50 mg/1 ampicillin were inoculated with an inoculating loop and incubated for 16 h at 37°C and 180 rpm on an ESR incubator from K ⁇ hner AG (Birsfelden, Switzerland) .
  • a volume of 1 ml of this first preculture was inoculated into 1402 g of the nutrient medium Al-144.
  • the culturing fermentation was carried out in 2 1 stirred reactor fermenters from B. Braun (BBI, Germany, Melsungen, Biostat MD model) .
  • the nutrient medium Al-144 contained the constituents listed in Table 1.
  • This second preculture was cultured for 22.5 h at a temperature of 37 °C, a volume- specific gassing of 0.71 vvm, an oxygen partial pressure of 10% of the atmospheric saturation and a pH of pH 7.0 until an OD (660 nm) of 16.3 was reached.
  • the growth medium Ml-463 contained the constituents listed in Table 2.
  • the culture was cultured as described in Comparative Example A at a temperature of
  • the broth was then cultured for a further 31.25 h at a temperature of 37°C, an oxygen partial pressure of 20% of the atmospheric saturation and a pH of pH 7.0 until an OD (660 nm) of 35.7 was reached.
  • 450 g of a production medium comprising a sucrose solution with a concentration of 650 g/1 was fed in continuously.
  • 90% of the fermentation broth (1656 g) was removed from the fermenter by pumping off.
  • the remaining 10% of the total amount (184 g) was topped up with 1200 g of the growth medium Ml-474 and the fermentation was started again.
  • the growth medium Ml-474 contained the constituents listed in Table 3.
  • the culture of this third run was cultured as described in Comparative Example A at a temperature of 37°C, an aeration of 1 1/min, a minimum stirring of 800 rpm and a pH of 7.0 and an oxygen partial pressure of 20% of the atmospheric saturation until a residual sugar concentration of approx. 3 g/1 was reached after 5.25 h.
  • the culture was then cultured for a further 30.5 h at a temperature of 37°C, an oxygen partial pressure of 20% of the atmospheric saturation and a pH of pH 7.0 until an OD (660 nm) of 32.5 was reached. During this time, 450 g of a production medium comprising a sucrose solution with a concentration of 650 g/1 was fed in. At the end of each fermentation the OD and the concentration of L-threonine formed were determined as in Comparative Example A. The results of the particular runs are shown in Table 4.
  • space/time yield here describes the volumetric productivity, i.e. the quotient of the concentration of L- threonine at the end of the fermentation and the fermentation time.
  • An individual colony of the strain DM1265 was transinoculated on to minimal medium with the following composition: 3.5 g/1 Na 2 HP0 4 *2H 2 0, 1.5 g/1 KH 2 P0 4 , 1 g/1 NH 4 C1, 0.1 g/1 MgS0 4 *7H 2 0, 2 g/1 glucose, 20 g/1 agar, 50 mg/1 ampicillin.
  • the culture was incubated at 37°C for approx. 5 days.
  • 10 ml preculture medium with the following composition: 2 g/1 yeast extract, 10 g/1 (NH ) 2 S0, 1 g/1. KH 2 P0 4 , 0.5 g/1 MgS0 4 *7H 2 0, 15 g/1 CaC0 3 , 20 g/1 glucose,
  • a volume of 1 ml of this first preculture was inoculated into 1402 g of the nutrient medium Al-144.
  • the culturing fermentation was carried out in 2 1 stirred reactor fermenters from B. Braun (BBI, Germany, Melsungen, Biostat MD model) .
  • the nutrient medium Al-144 contained the constituents listed in Table 1.
  • This second preculture was cultured for 22.5 h at a temperature of 37°C, a volume- specific gassing of 0.71 vvm, an oxygen partial pressure of 10% of the atmospheric saturation and a pH of pH 7.0 until an OD (660 nm) of 16.3 was reached.
  • the growth medium Ml-463 contained the constituents listed in Table 2.
  • the culture was cultured as described in Comparative Example A at a temperature of 37 °C, an aeration of 1 1/min, a minimum stirring of 800 rpm and a pH of 7.0 and an oxygen partial pressure of 20% of the atmospheric saturation until a residual sugar concentration of approx. 3 g/1 was reached after 9.5 h.
  • the fermentation broth obtained in this way was then cultured for a further 32 h at a temperature of 37 °C, an oxygen partial pressure of 20% of the atmospheric saturation and a pH of pH 7.0 until an OD (660 nm) of 35.8 was reached.
  • 450 g of a production medium comprising a sucrose solution with a concentration of 650 g/1 was fed in continuously.
  • 75% of the fermentation broth of the fermenter contents was removed by pumping off.
  • the first fermentation (first run) was ended after 41.5 h and reached a titre of 67.1 g/1 threonine.
  • the remaining 25% of the total amount (453 g) was topped up with 700 g of the growth medium Ml-527 and the fermentation was started again.
  • the growth medium Ml-527 contained the constituents listed in Table 5.
  • the culture of this second run was cultured as described in Comparative Example A at a temperature of 37°C, an aeration of 1 1/min, a minimum stirring of 800 rpm and a pH of 7.0 and an oxygen partial pressure of 20% of the atmospheric saturation until a residual sugar concentration of approx. 3 g/1 was reached.
  • the culture was then cultured for a further 30 h at a temperature of 37 °C, an oxygen partial pressure of 20% of the atmospheric saturation and a pH of pH 7.0 until an OD (660 nm) of 36.2 was reached.
  • Total L-threonine formed relates to the L-threonine effectively formed or produced during the fermentation run.
  • the amount of L- threonine introduced by the inoculum is subtracted from the amount of L-threonine present in the fermentation tank at the end of the run.
  • the term "Productivity” designates the quotient of the total L-threonine formed per fermentation run and the fermentation time per run.
  • the L-threonine-producing E. coli strain kat-13 is described in US-A-5, 939, 307 and deposited at the Agriculture Research Service Patent Culture Collection (Peoria, Illinois, USA) as NRRL B-21593.
  • the strain kat-13 has, inter alia, an enhanced, "feed back” resistant aspartate kinase I-homoserine dehydrogenase I, an attenuated threonine dehydrogenase, resistance to borrelidin and the ability to utilize sucrose as a source of carbon.
  • An individual colony of the strain kat-13 was transinoculated on to minimal medium with the following composition: 3.5 g/1 Na 2 HP0 4 *2H 2 0, 1.5 g/1 KH 2 P0 4 , 1 g/1 NH 4 C1, 0.1 g/1 MgS0 4 *7H 2 0, 2 g/1 glucose, 20 g/1 agar.
  • the culture was incubated at 37°C for approx. 5 days.
  • a volume of 0.45 ml of this first preculture was inoculated into 1500 g of the nutrient medium Al-158.
  • the culturing fermentation was carried out in 2 1 stirred reactor fermenters from B. Braun (BBI, Germany, Melsungen, Biostat MD model) .
  • the nutrient medium Al-158 contained the constituents listed in Table 7.
  • This second preculture was cultured for 19.75 h at a volume-specific gassing of 1.16 vvm, an oxygen partial pressure of 20% of the atmospheric saturation and a pH of pH 6.9 until all the glucose had been consumed.
  • the fermentation was started at a temperature of 39°C, and after a fermentation time of 18 h the temperature was lowered to 37 °C.
  • the growth medium Ml-530 contained the constituents listed in Table 8.
  • the culture was cultured at a temperature of 37°C, an aeration of 1.3 1/min, a minimum stirring of 800 rpm and a pH of 7.0 and an oxygen partial pressure of 20% of the atmospheric saturation until all the glucose initially introduced had been consumed after 8 h.
  • the fermentation broth obtained in this way was then cultured for a further 57 h at a temperature of 37°C, an oxygen partial pressure of 20% of the atmospheric saturation, an aeration of 1.5 1/min and a pH of pH 7.0. During this time, 1000 g of a production medium comprising a glucose -H 2 0 solution with a concentration of 550 g/1 was fed in continuously.
  • An individual colony of the strain kat-13 was transinoculated on to minimal medium with the following composition: 3.5 g/1 Na 2 HP0 4 *2H 2 0, 1.5 g/1 KH 2 P0 4 , 1 g/1 NH 4 C1, 0.1 g/1 MgS0 4 *7H 2 0, 2 g/1 glucose, 20 g/1 agar.
  • the culture was incubated at 37°C for approx. 5 days.
  • a volume of 0.45 ml of this first preculture was inoculated into 1500 g of the nutrient medium Al-158.
  • the culturing fermentation was carried out in 2 1 stirred reactor fermenters from B. Braun (BBI, Germany, Melsungen, Biostat MD model) .
  • the nutrient medium Al-158 contained the constituents listed in Table 7.
  • This second preculture was cultured for 19.75 h at a volume-specific gassing of 1.16 vvm, an oxygen partial pressure of 20% of the atmospheric saturation and a pH of pH 6.9 until all the glucose had been consumed.
  • the fermentation was started at a temperature of 39°C, and after a fermentation time of 18 h the temperature was lowered to 37°C.
  • the growth medium Ml-530 contained the constituents listed in Table 8.
  • the culture was cultured at a temperature of 37°C, an aeration of 1.3 1/min, a minimum stirring of 800 rpm and a pH of 7.0 and an oxygen partial pressure of 20% of the atmospheric saturation until all the glucose initially introduced had been consumed after 8 h.
  • the fermentation broth obtained in this way was then cultured for a further 57 h at a temperature of 37°C, an oxygen partial pressure of 20% of the atmospheric saturation, an aeration of 1.5 1/min and a pH of pH 7.0 until an OD (660 nm) of 46.4 was reached.
  • 1000 g of a production medium comprising a glucose ⁇ 2 0 solution with a concentration of 550 g/1 was fed in continuously.
  • 90% of the fermentation broth (1651 g) of the fermenter contents was removed by pumping off.
  • the remaining 10% of the volume (184 g) was topped up with 650 g of the growth medium Ml-531 and the fermentation was started again.
  • the growth medium Ml-531 contained the constituents listed in Table 9.
  • the culture was cultured at a temperature of 37°C, an aeration of 1.5 1/min, a minimum stirring of 800 rpm and a pH of 7.0 and an oxygen partial pressure of 20% of the atmospheric saturation. During this time, 1000 g of a production medium comprising a glucose -H 2 0 solution with a concentration of 550 g/1 was fed in continuously.
  • Total L-threonine formed relates to the L-threonine effectively formed or produced during the fermentation run.
  • the amount of L- threonine introduced by the inoculum is subtracted from the amount of L-threonine present in the fermentation tank at the end of the run.
  • the term "Productivity” designates the quotient of the total L-threonine formed per fermentation run and the fermentation time per run.
  • the L-threonine-producing E. coli strain B-3996 is described in US-A-5, 175, 107 and deposited at the Russian National Collection for Industrial Microorganisms (VKPM, Moscow, Russia) .
  • the strain B-3996 has, inter alia, an enhanced, "feed back” resistant aspartate kinase I-homoserine dehydrogenase I, an attenuated threonine deaminase, an attenuated threonine dehydrogenase, a resistance to at least 5 g/1 L-threonine and the ability to utilize sucrose as a source of carbon.
  • An individual colony of the strain B-3996 was transinoculated on to minimal medium with the following composition: 3.5 g/1 Na 2 HP0 4 *2H 2 0, 1.5 g/1 KH 2 P0 4 , 1 g/1 NH 4 C1, 0.1 g/1 MgS0 4 *7H 2 0, 2 g/1 sucrose, 20 g/1 agar, 20 ⁇ g/ml streptomycin.
  • the culture was incubated at 37°C for approx. 5 days.
  • 10 ml preculture medium with the following composition: 2 g/1 yeast extract, 10 g/1 (NH 4 ) 2 S0, 1 g/1 KH 2 P0 4 , 0.5 g/1 MgS0 4 *7H 2 0, 15 g/1 CaC0 3 ,
  • a volume of 20 ml of this first preculture was inoculated into 1000 g of the nutrient medium Al-160.
  • the culturing fermentation was carried out in 2 1 stirred reactor fermenters from B. Braun (BBI, Germany, Melsungen, Biostat MD model) .
  • the nutrient medium Al-160 contained the constituents listed in Table 11.
  • This second preculture was cultured for 14 h at a temperature of 37°C, a volume- specific gassing of 1.00 vvm, an oxygen partial pressure of 10% of the atmospheric saturation and a pH of pH 6.9 until all the sucrose had been consumed.
  • the growth medium Ml-546 contained the constituents listed in Table 12.
  • the culture was cultured at a temperature of 37°C, an aeration of 1.0 1/min, a minimum stirring of 800 rpm and a pH of 6.9 and an oxygen partial pressure of 20% of the atmospheric saturation until all the sucrose initially introduced had been consumed after 7 h.
  • the fermentation broth obtained in this way was then cultured for a further 29 h at a temperature of 37°C, an oxygen partial pressure of 20% of the atmospheric saturation, an aeration of 1.0 1/min and a pH of pH 6.9.
  • a production medium comprising a sucrose solution with a concentration of 600 g/kg was fed in such that the sucrose concentration was always above 0.5 g/1.
  • optical density was then determined with a digital photometer of the LP1W type from Dr. Bruno Lange GmbH (Berlin, Germany) at a measurement wavelength of 660 nm and the concentration of L-threonine formed was determined by ion exchange chromatography and post-column reaction with ninhydrin detection with an amino acid analyzer from Eppendorf-BioTronik (Hamburg, Germany) ,
  • the growth medium Ml-546 which was contained in 2 1 stirred reactor fermenters from B. Braun (BBI, Germany, Melsungen, Biostat MD model), 100 g of the second preculture in nutrient medium Al-160 were added, as described in Example 7.
  • the growth medium Ml-546 contained the constituents listed in Table 12.
  • the culture was cultured at a temperature of 37°C, an aeration of 1.0 1/min, a minimum stirring of 800 rpm and a pH of 6.9 and an oxygen partial pressure of 20% of the atmospheric saturation until all the sucrose initially introduced had been consumed after 7 h.
  • the fermentation broth obtained in this way was then cultured for a further 29 h at a temperature of 37 °C, an oxygen partial pressure of 20% of the atmospheric saturation, an aeration of 1.0 1/min and a pH of pH 6.9. During this time, 411.8 g of a production medium comprising a sucrose solution with a concentration of 600 g/kg was fed in continuously.
  • the fermentation broth was then drained off to 10% of the total amount.
  • the remaining 10% of the total amount was topped up with growth medium Ml-546 to the starting weight of 1100 g and the fermentation was started again.
  • the growth medium Ml-546 contained the constituents listed in Table 13.
  • the culture of this third run was cultured as described in Example 7 at a temperature of 37°C, an aeration of 1 1/min, a minimum stirring of 800 rpm and a pH of 6.9 and an oxygen partial pressure of 20% of the atmospheric saturation until all the sucrose initially introduced had been consumed after 8 h.
  • the culture was then cultured for a further 28 h at a temperature of 37°C, an oxygen partial pressure of 20% of the atmospheric saturation and a pH of pH 6.9.
  • a production medium comprising a sucrose solution with a concentration of 600 g/kg was fed in such that the sucrose concentration in the fermenter was always above 0.5 g/1.
  • the fermentation run was ended. The draining off of the fermentation broth to 10% and the topping up of the fermenter with Ml-546 was repeated a total of five times.
  • Table 13 shows the results of the particular runs.
  • Total L-threonine formed relates to the L-threonine effectively formed or produced during the fermentation run. To calculate the total L-threonine formed, the amount of L- threonine introduced by the inoculum is subtracted from the amount of L-threonine present in the fermentation tank at the end of the run.
  • Productivity designates the quotient of the total L-threonine formed per fermentation run and the fermentation time per run.
  • the microorganism identified under I. above was accompanied by:
  • This International Depositary Authority accepts the microorganism identified under I. above, which was received by it on 199 9 - 04 - 29 (Date of the original deposit)'.
  • microorganism identified under I above was received by this International Depositary Authority on (date of original deposit) and a request to convert the original deposit to a deposit under the Budapest Treaty was received by it on (date of receipt of request for conversion).

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Abstract

Le procédé d'élaboration de L-thréonine par fermentation de la présente invention consiste à mettre en culture un micro-organisme de la famille des entérobactéries producteur de L-thréonine par nourrissage, puis à séparer une partie du bouillon de culture de façon à l'utiliser pour l'inoculation des milieux ultérieurs.
EP01984568A 2000-08-31 2001-07-25 Laboration de l-thr onine par fermation Withdrawn EP1313838A2 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE10042745 2000-08-31
DE10042745 2000-08-31
DE10103778 2001-01-27
DE10103778A DE10103778A1 (de) 2000-08-31 2001-01-27 Neues Fermentationsverfahren zur Herstellung von L-Threonin
PCT/EP2001/008603 WO2002018543A2 (fr) 2000-08-31 2001-07-25 Élaboration de l-thréonine par fermation

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EP1313838A2 true EP1313838A2 (fr) 2003-05-28

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KR100837842B1 (ko) * 2006-08-10 2008-06-13 씨제이제일제당 (주) 아스파테이트 세미알데히드 디하이드로게나아제 활성이증가된 ｌ-쓰레오닌 생산 미생물 및 이를 이용한ｌ-쓰레오닌 생산 방법
FI20065762A0 (fi) * 2006-11-30 2006-11-30 Oulun Yliopisto Menetelmä soluviljelmän kasvun kontrolloimiseksi
DE102007051024A1 (de) 2007-03-05 2008-09-11 Evonik Degussa Gmbh Verfahren zur Herstellung von L-Aminosäuren unter Verwendung von Stämmen der Familie Enterobacteriaceae
EP1975241A1 (fr) 2007-03-29 2008-10-01 Evonik Degussa GmbH Procédé de fabrication d'aminoacides L en utilisant des troncs améliorés de la famille des enterobacteriaceae
DE102007044134A1 (de) 2007-09-15 2009-03-19 Evonik Degussa Gmbh Verfahren zur Herstellung von L-Aminosäuren unter Verwendung von verbesserten Stämmen der Familie Enterobacteriaceae
DE102007052270A1 (de) 2007-11-02 2009-05-07 Evonik Degussa Gmbh Verfahren zur Herstellung von L-Aminosäuren unter Verwendung von verbesserten Stämmen der Familie Enterobacteriaceae
EP2060636A1 (fr) 2007-11-14 2009-05-20 Evonik Degussa GmbH Procédé de fabrication d'acides aminés L en utilisant des souches de la famille des Enterobacteriaceae améliorées
EP2098597A1 (fr) 2008-03-04 2009-09-09 Evonik Degussa GmbH Procédé de fabrication d'aminoacides L en utilisant des troncs améliorés de la famille des enterobacteriaceae
DE102008002309A1 (de) 2008-06-09 2009-12-10 Evonik Degussa Gmbh Verfahren zur Herstellung von L-Aminosäuren unter Verwendung von verbesserten Stämmen der Familie Enterobacteriaceae
DE102008040352A1 (de) 2008-07-11 2010-01-14 Evonik Degussa Gmbh Verfahren zur Herstellung von L-Tryptophan unter Verwendung von verbesserten Stämmen der Familie Enterobacteriaceae
DE102008044768A1 (de) 2008-08-28 2010-03-04 Evonik Degussa Gmbh Verfahren zur Herstellung von organisch-chemischen Verbindungen unter Verwendung von verbesserten Stämmen der Familie Enterobacteriaceae
EP3385275B1 (fr) 2017-04-07 2019-10-23 Evonik Degussa GmbH Procédé de fabrication d'aminoacides l aromatiques à l'aide de troncs améliorés de la famille des enterobacteriaceae
EP3608409A1 (fr) 2018-08-09 2020-02-12 Evonik Operations GmbH Procédé de préparation d'acides aminés l au moyen de souches améliorées de la famille des enterobacteriaceae
US11053526B2 (en) 2018-08-09 2021-07-06 Evonik Operations Gmbh Process for preparing L amino acids using improved strains of the enterobacteriaceae family
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EP3677594A1 (fr) 2019-01-07 2020-07-08 Evonik Operations GmbH Procédé de production de l-tryptophane utilisant des souches améliorées de la famille des entérobactéries
CN115181764A (zh) * 2022-08-11 2022-10-14 通辽梅花生物科技有限公司 一种制备l-苏氨酸的半连续发酵方法及其糖蜜营养液

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MXPA03000585A (es) 2003-06-06
CN1318574C (zh) 2007-05-30
WO2002018543A2 (fr) 2002-03-07
WO2002018543A3 (fr) 2003-01-03
AU2002220542A1 (en) 2002-03-13

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