• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention describes the use of chemical synthetic media for the industrial scale fermentative production of valuable compounds. Microbial strains suitable for industrial scale fermentation using chemical synthetic media include fungal, yeast and bacterial strains. Suitable strains can be obtained as wild type strains or by screening and selection after mutagenesis treatment and DNA transformation.
    公开号:KR20000075487A
    申请号:KR1019997007546
    申请日:1998-02-20
    公开日:2000-12-15
    发明作者:드라아트빌헬머스시어도러스안토니우스마리아；프레우스팅요하네스코르넬리스제라더스；코에크만버투스피터
    申请人:윌리암 로엘프 드 보에르；디에스엠 엔.브이；
    IPC主号:
    专利说明:

    Fermentational Production of Valuable Compounds Using Chemical Synthesis Medium TECHNICAL FIELD OF VALUABLE COMPOUNDS ON AN INDUSTRIAL SCALE USING CHEMICALLY DEFINED MEDIA}
    Many valuable compounds are generally produced by fermentative production in industrial scale fermenters, ie fermenters in which microorganisms produce the desired valuable compounds under controlled conditions in fermenters of 10 to 300 m 3. In modern industrial scale fermentation processes, the producing organism is typically fermented on a complex fermentation medium. Complex medium is understood as a medium comprising complex nitrogen and / or carbon sources such as soy flour, cotton seed flour, corn steep liqueur, yeast extract, casein hydrolyzate, molasses and the like.
    The advantage of the composite medium is that the composite natural materials that make up are inexpensive and readily available and form a complete or nearly complete nutritional source for microorganisms containing vitamins and minerals as well as carbon and nitrogen sources. In addition, mixtures of biological polymers such as proteins, carbohydrates, lipids, etc. present in composite natural materials need to be degraded by enzymes secreted by microorganisms before their consumption. The result is that small molecules that are evenly consumable throughout the fermenter and during the fermentation process are useful and thereby avoid the problem of mixing with the concentration gradient and remain below concentrations that inhibit the levels of these consumable small molecules. In addition, such polymers as well as organic acids are present in the complex medium to provide a buffer function in this way to promote pH control in the medium.
    In addition to these advantages, the composite fermentation medium has several important disadvantages. Most importantly, composite natural materials have a composition and variable quality that are not chemically defined due to seasonal variation and other geographic origins. Composite natural materials are a major cause of process variability because the composition of the fermentation medium has a significant effect on fermentation parameters such as viscosity, heat transfer and oxygen transfer. In addition, they interfere with downstream processing and adversely affect the quality of the final product. For example, fermented broth, specifically filamentous microorganisms, shows reduced filtration when using composite natural materials.
    Composite natural materials also contain compounds that inadvertently accumulate in the final product or separate with the final product. Heavy metals, pesticides or herbicides are examples of unwanted compounds present in composite natural materials. Composite natural materials may also contain poisons or cause the formation of poisons.
    Another disadvantage is that the complex medium produces undesirable odors during sterilization, producing unwanted pollution.
    Notwithstanding the above-described disadvantages associated with the use of complex media, such media are still preferred for large scale industrial fermentation processes. There are various reasons why media that do not contain composite natural materials, ie chemical synthetic media, have not been considered for use in industrial scale fermentation processes. One obvious reason is found in the advantages associated with the use of complex media. More importantly, the yields of products obtained using chemical synthetic media on an industrial scale were thought to be essentially lower than those obtained using media containing composite natural materials. In addition, high-producing microbial strains developed for industrial processes in complex media do not possess their good performance in chemical synthetic media. One reason for unsatisfactory performance in chemical synthesis media is that recent industrial strains perform various sequences of mutagenesis and selection without considering their performance on chemical synthesis media.
    Therefore, chemical synthetic media have been applied for research purposes only, ie, in laboratory cultures in Petri dishes and / or shake flasks or only on relatively small fermentation scales, typically not exceeding about 20-40 L volume. Penicillin (Jarvis and Johnson, J. Am. Chem. Soc. 69, 3010-3017 (1947); Stone, and Farrell, Science 104, 445-446 (1946); White et al., Arch. Biochem. 8, 303 -309 (1945)), clavulanic acid (Romero et al., Appl. Env. Microbiol. 52, 892-897 (1986)) and erythromycin (Bushell et al., Microbiol. 143, 475-480 ( See examples of fermentative production of secondary metabolites, 1997).
    However, investigations of the use of chemical synthetic media on such small scales of research have not provided any information to those skilled in the art regarding the usefulness of such media in large industrial fermentation processes for production purposes typically having a volume scale of about 10 m 3 or more.
    In recent industrial practice it is desirable to apply chemical synthesis methods to industrial scale fermentation to avoid problems associated with the use of conventional methods for composite media.
    Here we use chemical synthetic media for industrial scale fermentation processes that enable the production of valuable compounds such as primary or secondary metabolites, pharmaceutical proteins or peptides, or industrial enzymes in economical yield in combination with suitable strains. Describe it.
    The present invention relates to fermentation ie fermentative production of valuable compounds such as primary or secondary metabolites, pharmaceutical proteins or peptides, or industrial enzymes.
    Figure 1. Overview of pWGx.GIT
    Figure 2. Changes in Total Glucose Isomerase Produced During Fermentation
    The present invention discloses an industrial process for the production of valuable compounds comprising the steps of fermentation of microbial strains in a fermentation broth, a chemical synthetic medium consisting essentially of chemically defined components, and recovery of valuable compounds from the fermentation broth. .
    The present invention discloses a process for the preparation and / or amelioration of microbial strains that produce valuable compounds of interest that can be fermented on an industrial scale in a chemical synthetic medium comprising the following steps:
    Mutagenesis treatment and / or DNA transformation selected from physical means and chemical mutagens,
    Screening the resulting mutants and / or transformants for their growth performance on chemical synthesis medium and the desired productivity level of their said valuable compound,
    Selecting mutants having a similar or improved growth performance and / or having an improved productivity level of said valuable compound of interest when compared to said parent strain on a chemical synthetic medium.
    The present invention describes the use of chemical synthetic fermentation media for industrial scale fermentation of suitable microbial strains capable of producing valuable compounds.
    Throughout the description of the present invention, the industrial scale fermentation process or the industrial process means 10m 3 or more, preferably 25m 3 or more, more preferably 50m 3 or more, and most preferably 100m 3 or more to complete the fermentation process. It is understood that.
    The term "chemically defined" is understood to be used for fermentation medium consisting essentially of chemically defined components. Fermentation media consisting essentially of chemically defined components include media that do not contain complex carbon and / or nitrogen sources, ie, do not contain complex natural materials with compositions that are not chemically defined. Fermentation media consisting essentially of chemically defined components typically contain small amounts of complex nitrogen and / or carbon sources in amounts as defined below that are not sufficient to maintain microbial growth and / or to ensure sufficient biomass formation. Also included are essentially media.
    In that sense, the composite natural materials have a composition that is not chemically defined because of the fact that such natural materials contain many different compounds among the complex heteropolymeric compounds and have various compositions due to seasonal variation and differences in geographical origin. Typical examples of composite natural materials that function as complex carbon and / or nitrogen sources in fermentation include soy flour, cotton seed flour, corn stew liqueur, yeast extract, casein hydrolyzate, molasses and the like.
    In essence, small amounts of complex carbon and / or nitrogen sources are present in the chemical synthesis medium according to the present invention, for example from inoculum for main fermentation. Inoculum for its main fermentation is not necessarily obtained by fermentation on chemical synthetic media. Most often what comes from the inoculum will be detectable through the presence of small amounts of complex nitrogen sources in chemical synthetic media for the main fermentation.
    It is beneficial to use complex carbon and / or nitrogen sources in the fermentation process of the inoculum for the main fermentation, for example to accelerate the formation of biomass, ie to increase the growth rate of the microorganisms and / or to promote internal pH control. Do. For that reason, it is beneficial to add a small amount of complex carbon and / or nitrogen sources, such as yeast extracts, essentially to the initial stages of the main fermentation, in particular to accelerate biomass formation in the early stages of the fermentation process.
    The small amount of complex carbon and / or nitrogen source essentially present in the chemical synthesis medium according to the invention is 10% or less of the total amount of carbon and / or nitrogen (Kjeldahl N) present in the chemical synthesis medium, preferably carbon and / or nitrogen The amount is limited to 5% or less of the total amount, more preferably 1% or less of the total amount of carbon and / or nitrogen. Most preferably no complex carbon and / or nitrogen source is present in the chemical synthesis medium according to the present invention.
    As used herein, the term “chemical synthesis medium” includes a medium in which all essential ingredients have been added to the medium prior to the start of the fermentation process and also some of the essential ingredients are added before the start of the fermentation process and some of the medium during the fermentation process. Medium added thereto.
    The present invention further discloses that microbial strains can convert simple natural materials of a chemical synthesis medium into economical amounts of valuable products. It has been surprisingly found that the productivity of microbial strains in chemical synthesis media is, or in some cases even higher than that, in a composite medium as measured on an industrial scale.
    Another advantage of using a chemical synthesis medium is that the oxygen transfer from the gas phase to the liquid phase and the carbon dioxide transfer from the liquid phase to the gas phase are inherently improved compared to using a composite medium. As is known to those skilled in the art, the concentrations of dissolved oxygen and dissolved carbon dioxide are important factors in scaling up the fermentation process and can determine the economic feasibility of industrial processes. Improved mass transfer obtained using chemical synthetic media can contribute to the absence of essential amounts of compounds that promote the fusion of gas bubbles in such media. Fusion-promoting compounds can be found, for example, between any hydrophobic and / or polymeric compounds present in composite natural materials. Fusion of gas droplets typically results in lower mass transfer coefficients (van't Riet and Tramper, in: Basic Bioreactor Design, pp 236-273 (1991)).
    Oxygen transfer is often a limiting factor in the fermentation process, especially in fermentation of filamentous microorganisms. The improved oxygen transfer capacity obtained when the fermentation is performed using the chemical synthesis medium according to the present invention provides a cheaper way to optimize productivity than investments in hardware such as power input, oxygen enrichment of inlet air or fermentor pressure.
    In industrial fermentation processes filamentous microorganisms, such as filamentous bacteria such as Actinomycetes or filamentous fungi such as Penicillium or Aspergillus, typically grow in pellet morphology. In that respect, proteins and peptides present in the complex fermentation medium typically have a tendency to make fluffy pellets that are easily shaken into dispersed mycelium with very long and branched mycelium as a result of high growth rates obtained using the complex medium. . The downy pellet form therefore generally leads to undesirably high juicy viscosity. The use of chemical synthetic media has a desirable effect on morphology, such as to produce more robust pellets that do not break easily during fermentation. In this way, a significant reduction in filamentous fermentation broth viscosity can be obtained using chemical synthetic media. Since the low viscosity of the fermented broth is beneficial for product formation, control of viscosity is of paramount importance for industrial scale fermentation processes.
    Another advantage of using chemical synthetic media is found in the downstream processing of the product. For certain strain-product combinations, downstream processing is markedly enhanced by using chemical synthetic media, especially when filamentous strains are fermented.
    Chemical synthesis media used in the process of the present invention typically must contain so-called structural and so-called catalytic elements.
    Structural elements are the constituents of the microorganism's polymers: hydrogen, oxygen, carbon, nitrogen, phosphorus and sulfur. The structural elements hydrogen, oxygen, carbon and nitrogen are typically contained in carbon and nitrogen sources. Phosphorus and sulfur are typically added as phosphate and sulfate and / or thiosulfate ions.
    The type of carbon and nitrogen source used in the chemical synthesis medium is not particularly defined in the present invention as long as the carbon and nitrogen source has essentially chemically defined characteristics.
    Preferably, the carbon source is glucose, lactose, fructose, sucrose, maltodextrins, carbohydrates such as starch and inulin, glycerol, vegetable oils, hydrocarbons, alcohols such as methanol and ethanol, acetates and higher alkanoic acids, and the like. It is selected from the group which consists of organic acids. More preferably the carbon source is selected from the group consisting of glucose, sucrose and soybean oil. The most preferred carbon source is glucose. The term "glucose" is understood to include glucose syrups, ie glucose compositions containing glucose oligomers in limited amounts.
    The nitrogen source is preferably selected from the group consisting of urea, ammonia, nitrate, ammonium sulfate, ammonium phosphate and ammonium salts such as ammonium nitrate and amino acids such as glutamate and lysine. More preferably the nitrogen source is selected from the group consisting of ammonia, ammonium sulfate and ammonium phosphate. Most preferably the nitrogen source is ammonia. The use of ammonia as a nitrogen source has the advantage that ammonia can additionally function as a pH-regulator. Some or all of the sulfur and / or phosphorus needs of the microorganism are met when ammonium sulfate and / or ammonium phosphate are used as the nitrogen source.
    Catalytic elements are components that are enzymes or cofactors of enzymes. These elements are for example magnesium, iron, copper, calcium, manganese, zinc, cobalt, molybdenum, selenium, boron.
    In addition to these structural and catalytic elements, cations such as potassium and sodium ions must be present to function as counter ions and to regulate pH and osmotic pressure in the cell.
    Compounds which may optionally be included in the chemical synthesis medium are chelating agents such as citric acid, mono- and phosphate mono- and potassium carbonates and buffers. Buffers are preferably added when handling the process without external pH adjustment. In addition, antifoams may be administered prior to and / or during the fermentation process.
    Polymers and organic acids present in the composite medium provide buffering capacity in such media. Due to the absence of these compounds in chemical synthetic media, pH control is more difficult in chemical synthetic media than in composite media. The present invention shows that pH control, in which acids or bases are administered depending on the pH of the broth, allows for an appropriate pH profile in chemically defined industrial scale processes.
    Vitamins are a group of structurally unrelated organic compounds required for normal metabolism of microorganisms. Microbes are known to vary greatly in their ability to synthesize the vitamins they need. Vitamins should be added to the fermentation medium of microorganisms unable to synthesize the vitamins. Typically, chemically synthetic fermentation media for certain lower fungi such as yeast or bacteria or Mucorales are supplied with one or more vitamins. Higher fungi most often do not require vitamins.
    Vitamins are selected from the group of thiamine, riboflavin, pyridoxal, nicotinic acid or nicotinamide, pantothenic acid, cyanocobalamine, folic acid, biotin, lipoic acid, purine, pyrimidine, inositol, choline and hemin.
    Structural and catalytic elements and optionally vitamins are required for the growth of microorganisms, ie the formation of biomass.
    The amount of essential compounds added to the chemical synthesis medium, ie structural and catalytic elements and optionally including vitamins, depends primarily on the amount of biomass formed in the fermentation process. The amount of biomass formed varies widely and is typically about 10 to about 150 g / l fermentation broth. In general, fermentations producing amounts of biomass less than about 10 g / l are not industrially suitable.
    In addition, the optimal amount of each component of the synthetic medium, as well as essential and non-essential compounds, will depend on the type of microorganism to be fermented in the synthetic medium, the amount of biomass and the product formed. For this reason, the use of a chemical synthetic medium allows for the variation of the concentration of each medium component independently of the other components, thus facilitating optimization of the medium composition.
    It is necessary to supply additional compounds to the chemical synthesis medium for product formation and / or to increase the concentration of certain compounds already present in the chemical synthesis medium above the level necessary for microbial growth. The function of these compounds is to induce and / or promote the production of the desired compound by the microorganism or to function as a precursor of the desired compound.
    Examples of compounds fed to the chemical synthesis medium and / or added in increased amounts are increased amounts of sulfates for the production of β-lactam compounds, increased amounts of nitrogen-containing compounds for the production of amino acids, in particular basic amino acids, penicillin G Phenylacetic acid for production, phenoxyacetic acid for penicillin V production, adipic acid for adifil-7-ADCA and adiphyl-7-ACA production, propionic acid for erythromycin production.
    The total amount of carbon source added to the chemical synthesis medium in the industrial fermentation process according to the present invention is expressed as the amount of carbon per liter of medium, which varies from 10 to 200 gC / l, preferably 20 to 200 gC / l.
    The total amount of nitrogen source added to the chemical synthesis medium varies from 0.5 to 50 gN / l, preferably 1 to 25 gN / l, where N is expressed as Kjeldahl nitrogen.
    The ratio between carbon and nitrogen sources in fermentation varies considerably, with one determinant for the appropriate ratio being the composition of the components of the product to be formed.
    Additional compounds required for microbial growth, such as phosphates, sulfates or trace elements, are added using the concentration ranges described in Table 1 as guidelines. The concentration range of these additional compounds differs between different classes of microorganisms, namely fungi, yeasts and bacteria.
    Vitamin concentrations are generally in the range of 0.1 (biotin) to 500 (myo-inositol) mg / l.
    Typically the amount of media components required for microbial growth is determined in terms of the amount of carbon source used for fermentation since the amount of biomass formed is primarily determined by the amount of carbon source used.
    Typical concentration ranges (g / l) of media components necessary for the growth of various classes of microorganisms in addition to carbon and nitrogen sourcesFungus leaven Bacteria (Actinomycetes) PO4 1,5SO4 2,5 1-20 MgSO 4 · 7aq 3 0.5-10 0.5-2 0.5-2 CaCl22aq3 0.01-0.1 0.1-1 0.05-0.5 FeSO 4 · 7aq 3 0.1-1.0 0.1-0.5 0.1-0.5 ZnSO47ag3 0.0005-0.1 0.002-1 0.002-0.1 MnSO41ag3 0.0005-0.1 0.002-1 0.002-0.1 CuSO45aq3,4 ≤0.005 0.001-0.01 0.001-0.01 CoSO47aq3,4 ≤0.01 ≤0.01 ≤0.01 Na2MoO42aq4 ≤0.0005 0.001-0.005 0.001-0.005 H3BO3 4 ≤0.0005 0.001-0.005 0.001-0.005 KI 4 ≤0.002 ≤0.002OneThe basic required amount of phosphate salt will be 0.5-1% of the dry weight of biomass. In relatively small batch processes, external phosphate will be required for pH control.2Sulfates are also administered via titrants such as K + and Na +.3Sulphates can be (partly) substituted for chlorides as counter ions in trace elements or vice versa.4For some trace elements it is difficult to define a lower limit. The demand is met by their presence in other media components, such as ferrous sulfate, water, small amounts of yeast extracts, for example.5Phosphates and sulphates K> NH4> As preference for Na as potassium, ammonium and / or sodium salts Is added.
    The industrial fermentation process according to the invention using a chemical synthetic medium can be carried out as a batch, repeated ash, oil value, repeated oil value or continuous fermentation process.
    In a batch process, all medium components are added directly to the medium as a whole before the start of the fermentation process.
    In a batch ash process, a partial harvest of gravy, optionally accompanied by a partial supply of complete medium, occurs several times, optionally.
    In a fed-batch process, compounds containing one or more structural and / or catalytic elements are not added to the medium at all prior to the start of fermentation, or some are added and compounds containing one or more structural and / or catalytic elements during the fermentation process, respectively. All or the residue is fed. Compounds selected for feeding may be fed together or separately with the fermentation process.
    In particular in a fermentation process in which the original fermentation medium is diluted about twice or more by feeding of compounds comprising one or more structural elements, the feeding further comprises catalytic elements and additional medium components in addition to the structural elements.
    In a recurrent feed or continuous fermentation process, the complete starting medium is additionally fed during fermentation. The starting medium can be fed with or separately from structural element feeding. Some of the fermentation broth containing the biomass is removed at regular time intervals in a repetitive fed process, while some of the fermentation broth is continuously removed in a continuous process. The fermentation process is thereby replenished with fresh medium corresponding to the amount of fermented broth taken out.
    In a preferred embodiment of the present invention an oil or repetitive oil addition process is applied in which carbon and / or nitrogen sources and / or phosphates are fed into the fermentation process. In more preferred embodiments the carbon and nitrogen sources are further fed to the fermentation process. Most preferably, phosphate as well as carbon and nitrogen sources are fed. In that respect the preferred carbon source is glucose and the preferred nitrogen source is ammonia and / or ammonium salts.
    The use of a fed-in process typically allows the use of significantly higher amounts of carbon and nitrogen sources than those used in batch processes. Specifically, the amount of carbon and nitrogen sources applied to the oil value process can be at least about twice the highest amount applied to the batch process. This results in significantly higher amounts of biomass formed in the oil value process.
    Another aspect of the invention relates to the selection of downstream processing of fermented gravy. After the fermentation process is finished, valuable products can be selectively recovered from the fermentation broth using standard techniques developed for valuable compounds of interest. Suitable downstream processing techniques applied in this way depend on the properties of the valuable compounds and the positioning of the cells. First of all, the biomass is separated from the fermentation broth using, for example, centrifugation or filtration. If a valuable product accumulates inside or is associated with a cell, the valuable compound is recovered from the biomass. Otherwise when the valuable product is secreted from the microbial cells it is recovered from the fermentation broth.
    The use of chemical synthetic media in the industrial fermentative production of compounds of interest is of great benefit for downstream processing, since the amount of by-products is essentially less than when using complex media. In addition, the quality of the product is improved because unwanted by-products are not co-separated with the compound of interest.
    In another aspect of the invention suitable strains for industrial fermentation processes using chemical synthetic media are identified.
    Suitable microbial strains for industrial fermentation processes using chemical synthesis media can be any wild type strain that produces compounds of interest as long as they have good growth performance on the chemical synthesis medium. In addition, suitable microbial strains for industrial fermentation processes using chemically synthesized media can also be used to treat the parental strain of interest if the resulting mutant or transformed microbial strain has good growth performance on the chemically synthesized media. And / or improved strains obtained by recombinant DNA transformation. Whether the resulting mutant or transformed strains have growth performance on the chemical synthesis medium is improved or comparable to that of the parent strain will depend on the growth performance of the parent strain on the chemical synthesis medium.
    When the strain is gateul to 0.05h -1 or more, preferably at least 0.1h -1, more preferably at least 0.2h -1, the specific growth rate (μ) less than 0.4h -1 and most preferably on a chemical synthetic medium chemically It is understood that it has good growth performance on synthetic medium. The growth performance of microbial strains on chemical synthetic media can be conveniently analyzed by fermenting the strains in chemical synthetic media on a relatively small scale, such as, for example, shake flask culture and / or 10 L bench fermentation. In the growth performance analysis it is preferred to include 10L bench fermentation with pH, temperature and oxygen concentration control.
    In one embodiment of the invention the parental strain of interest is subjected to classical mutagenesis using a suitable means such as UV irradiation, physical means such as N-methyl-N'-nitro-N-nitrosoguanidine or ethylmethane sulfonate The treatment yields and / or ameliorates microbial strains that can be fermented in chemical synthetic media. In another embodiment of the present invention, a parent strain of interest is obtained by applying DNA technology to obtain and / or improve microbial strains that can be transformed with one or more functional genes of interest and fermented in chemical synthetic media. .
    In general, the present invention envisions two groups of parental strains of interest for classical mutagenesis and / or DNA transformation. In one embodiment of the invention the parental strain of interest is selected from the group of strains that have good growth performance on chemical synthetic media but need to be improved with respect to the productivity level of the desired compound. In another embodiment of the invention, the parent strain of interest is selected from the group of strains with high productivity levels of the desired compound but relatively poor growth performance on chemical synthetic media. It is understood that microbial strains having a specific growth rate of less than about 0.05 h −1 have relatively poor growth performance on chemical synthetic media.
    Both the classical mutagenesis treatment as well as the DNA transformation process then screen the resulting mutants or transformants for both their growth performance on the chemical synthetic medium as well as the productivity level of their desired compound. Mutant strains or transformants are selected that have good growth performance on the chemical synthetic medium and / or improved productivity levels of the compound of interest as compared to the parent strain.
    It should be noted that some microbial strains, particularly industrial strains that have already been subjected to extreme mutagenesis to improve productivity levels, exhibit poor or no growth in chemical synthetic media. Poor growth performance or lack of such mutagenic strains results from the fact that growth on chemical synthetic media cannot be applied as a criterion for the selection of appropriate mutants. For example, mutated strains are likely to have mutations that cause unknown growth demands (unknown nutrogenic mutations).
    Microbial strains suitable for industrial fermentation using chemical synthetic media include filamentous and non-cephaly strains. Microbial strains suitable for fermentation, for example in chemical synthetic media, include fungal strains such as Aspergillus, Penicillium or Mucorales, yeast strains such as Saccharomyces, Pichia, Phaffia or Kluyveromyces, and bacterial strains such as Actinomycetes. The use of the chemical synthetic medium according to the invention is particularly advantageous for the industrial fermentation of filamentous microorganisms.
    The process according to the invention using chemical synthetic media is suitable for fermentative production on industrial scale of any valuable compound of interest, including primary or secondary metabolites, pharmaceutical proteins or peptides or industrial enzymes. Preferred valuable compounds are secondary metabolites such as antibiotics or β-lactam compounds, in particular β-lactam antibiotics.
    Examples of strain-product combinations include A. niger for amyloglucosidase such as A. niger CBS 513.88, A. oryzae for α-amylase, A. terreus for Alova terin such as A. terreus CBS 456.95 , Mortierella alpina for lipids containing arachidonic acid or harakidonic acid, Mucor miehei for protease, P. chrysogenum for β-lactam compounds (penicillin G or V) such as P. chrysogenum CBS 455.95 or other suitable strains, Streptomyces clavuligerus for clavulanic acid such as S. clavuligerus ATCC 27064, Pichia ciferrii for tetraacetylpytosphingosine such as P. ciferrii NRRL Y-1031 F-60-10, Phaffia rhodozyma for astaxanthin such as P. rhodozyma CBS 6938, Eric Contains Saccharopolyspora erythraea for thromycin, K. lactis for lactase, Streptomyces natalensis for natamycin.
    The invention also provides for one or more desired functional genes that result in a transformed strain overexpressing a product already produced by said strains or a transformed strain expressing a product not naturally produced by said strain. The use of microbial strains transformed to have is envisioned.
    As a result, if the selected strain has good growth performance on the chemical synthetic medium, it remains only for those skilled in the art to select the selected strain for transformation. For example, a strain that has already been subjected to one or more mutagenesis treatments may be selected for transformation. Otherwise non-mutated or wild type strains may be selected. After analysis of the expression level of the desired compound, the transformants obtained after transformation of the selected strains with the desired one or more functional genes should be analyzed for their growth performance on chemical synthetic medium.
    Examples of recombinant strains that produce products that are not naturally produced by the strains are as follows.
    Streptomyces lividans such as S. lividans TK21, which has a gene encoding for example glucose isomerase originating from Actinoplanes missouriensis, which contains an expression cassette allowing expression of glucose isomerase.
    Acremonium, which allows the production of cephalosporin compounds such as 7-ADCA or 7-ACA using adipic acid (see EP 532341) or 3-carboxymethylthio-propionic acid (see WO95 / 04148) as side chain precursors. one or more expressions having genes encoding expandases, hydroxylases and acetyltransferases derived from chrysogenum or Streptomyces clavuligerus and the like to enable expression of the expandase and optionally hydroxylase and / or acetyltransferase Penicillium chrysogenum containing cassettes such as P. chrysogenum CBS 455.95.
    Aspergillus niger such Aspergillus niger CBS 513.88 containing an expression cassette allowing expression of human lactoferrin (see WO93 / 22348) or bovine chymosin.
    * Kluyveromyces lactis containing an expression cassette allowing expression of bovine chymosin or phospholipase A 2 , insulin or recombinant human albumin.
    Examples of recombinant strains that overproduce the enzyme already produced by the strain are:
    A. niger such as A. niger CBS 513.88 containing an expression cassette allowing overexpression of phytase (see EP 420358) or endoxylalanase I (see EP 463706).
    The present invention is an example of an industrial scale fermentation process using a chemical synthetic medium for the production of glucose isomerase by a recombinant Streptomyces strain and the beneficial use of the chemical synthetic medium for fermentation of a jarge scale Penicillium compared to a complex medium. Holding
    Additional examples are used to measure the growth performance and productivity of desired strains when grown on small scale in such media to identify microbial strains suitable for fermentative production of valuable compounds on an industrial scale in chemical synthetic media. It relates to a chemical synthesis medium that can be.
    Example 1
    Industrial Production of Glucose Isomerase Using Streptomyces lividans
    Composition of Streptomyces Strains Producing Glucose Isomerase
    The glucose isomerase gene of Actinoplanes missouriensis was first cloned in E. coli K12 strain JM101 as a 5.0 kb DNA fragment.
    It was found that the 1.7 kb fragment inside the 5.0 kb fragment showed the complete coding sequence of glucose isomerase of A. missouriensis and its upstream regulatory region (see Amore and Hollenberg (1989), Nucl. Acids Res. 17, 7515). ).
    A glucose isomerase mutant showing increased thermal stability was obtained by replacing a triplet AAG encoding lysine at position 253 of the glucose isomerase protein with a CGG encoding arginine in the glucose isomerase gene (Quax et al. (1991), Bio / Technology 9, 738-742.
    Plasmid pIJ486 (Ward et al. (1986), Mol. Gen. Genet. 203, 468-478) was used as a vector for cloning in Streptomyces. A DNA fragment of 1737 bp A. missouriensis encoding glucose isomerase was combined with a large PstI DNA fragment of pIJ486. The resulting plasmid pWGx.GIT essentially contained an A. missouriensis DNA fragment encoding the replication region, thiostrepton resistance gene and GIT of plasmid pIJ101. A schematic map of pWGx.GIT is shown in FIG.
    Glucose isomerase producing strains were constructed by the transformation of Streptomyces lividans strain TK21 with plasmid pWGx.GIT (Hopwood et al. (1985), Genetic Manipulation of Streptomyces: A Laboratory Manual.The John Innes Foundation, Norwich, England) It became.
    Industrial Production of Glucose Isomerase
    Refer to Example 1 by picking up thiostrepton resistant colonies and growing in 20 ml Tryptone Soytone Broth containing thiostreptone (50 mg / L) in 100 ml shake flask for 40-48 hours at 30 ° C. and shaking incubation at 280 rpm. A working cell bank of the production strain constructed as described was prepared.
    16 g / L Bactopeptone (Difco 0123/01), 4 g / L Bacto soytone (Difco 0436/01), 20 g / L of the mycelium equivalent to 1 ml of the working cell bank (fresh or stored as frozen mycelium at -80 ° C) Casein hydrolysate (Merck 2239), 10 g / L dipotassium phosphate. 3 aq (Merck, Anal.Reagent), 16.5 g / L glucose. 1 aq, 0.6 g / L soybean oil and 50 mg / L thiostrepton Was inoculated into 100 ml of inoculum growth medium in a 500 ml shake flask. The pH of the medium was adjusted to 7.0 with sodium hydroxide and / or sulfuric acid prior to sterilization. Glucose and thiostrepton were added after sterilization separately. Thiostrepton was dissolved in DMSO at a concentration of 50 g / l and sterilized by filtration with a 0.2 μm Nalgene filter. The culture was grown at 280 rpm in an incubator shake incubator at 30 ° C. for 24 hours.
    50 ml of the grown culture was added to the above-mentioned medium except for the double glucose concentration (33 g / L glucose.laq), extra antifoaming agent (SAG5693, 0.6 g / L; silicon antifoaming agent purchased from Basildon company) and thiostrepton Transfer to 6 L of the second phase inoculum growth medium having a composition similar to. Glucose was again sterilized individually into a 50% solution and added after sterilization of the medium (60 minutes, 121 ° C.). The culture was incubated for 36 hours in a sterile air column sterilized with 840 L per hour with a nozzle comprising four holes with a diameter of 2 mm and maintained at a temperature of 22 ° C. Alternatively this phase can be performed in shake flasks (eg 12 × 500 ml medium in Erlenmeyer flasks with 2 L of flap) at similar inoculation rates and shaken at 280 rpm in an orbital shaker incubator.
    16.3 kg citric acid. 1 aq, 70.8 g of sulfuric acid-iron. 7 aq., 109 g of sulfuric acid-zinc. 7 aq, 109 g of sulfuric acid-manganese. 1 aq, 32.7 g of dichloride-cobalt. 6 aq, 5.45 g of sodium molybdate. 2aq, 5.45g boric acid, 5.45g sulfuric acid-copper. 5aq, 10.9kg sulfuric acid-diammonium, 10.9kg sulfuric acid-magnesium. 7aq, 463g calcium chloride.2aq, 1090g soybean oil, 21.8kg phosphoric acid- Cultures were grown with an inoculum fermenter containing 4.5 m 3 of inoculum medium containing monopotassium and 139 kg of glucose. 1 aq and 5.9 kg of yeast extract (beer yeast with 10% Kjeldahl nitrogen based on dry weight). Transferred aseptically. The medium was prepared as follows: All components except glucose were introduced into the order indicated in about 2700 L of tap water. The pH was adjusted to 4.5 with sodium hydroxide and / or phosphoric acid and the medium was sterilized at 122 ° C. for 60 minutes. Glucose was sterilized in a separate vessel at 120 ° C. for 60 minutes in 1000 L of water at pH4.5. After cooling both portions the glucose was aseptically transferred to the inoculum-container. After mixing the two parts, the pH was adjusted to 7.0 with ammonia and the volume was adjusted to 4.5m 3 with sterile water. The fermentation temperature was adjusted to 30 ° C., the pH was maintained at 7.0 +/− 0.1 with gaseous ammonia and the excess pressure was maintained at 1.3 to 1.4 bar while the fermentor was aerated at 0.5 to 1.0 vvm. The foam was adjusted to a sterilized mixture of soybean oil and silicon antifoaming agents such as SAG5693 in a 3: 1 ratio if necessary. The oxygen concentration maintained at least 25% air-saturation by optimizing the stirrer speed (0.5-3 Kw / m 3). The culture was transferred to the main fermentation before all the glucose was consumed (as in all the above growth phases) and before the oxygen uptake exceeded the level of 30 mmole per one volume of juice per hour.
    The main fermentation medium is 245.1 kg of citric acid. 1 aq, 1062 g of sulfuric acid-iron. 7 aq, 1634 g of sulfuric acid-zinc. Sodium. 2 aq, 82 g boric acid, 82 g sulfuric acid-copper. 5 aq, 163.4 kg sulfuric acid-ammonium, 163.4 kg magnesium sulfate. 7 aq, 6.94 kg calcium dichloride. 2 aq, 16.3 kg soybean oil, 327 kg phosphoric acid Contains monopotassium, 880 kg of brewer's yeast extract (10% Kj-N based on dry weight) and 556 kg of glucose.1aq. The medium was prepared as described for inoculum fermentation (glucose was sterilized individually). For glucose, DE-95 sugar syrup can be used as an alternative. The volume of the medium before inoculation is 65 m 3 after the pH is adjusted to 7.0 with ammonia.
    Glucose. Glucose feeds were prepared from 275 to 550 g of glucose / L feed solution as glucose equivalents from 1aq or 90-DE-syrup. The pH was adjusted to 4.5-5.0 with phosphoric acid solution. Sterilization was carried out batchwise (122 ° C., 45 minutes) or continuously via heat shock or filtration set.
    Main fermentation was controlled by 30 ° C. +/− 0.5 and pH 7.0 +/− 0.1 (pH adjustment with ammonia and phosphoric acid). The airflow is set at 0.5 to 1.5 vvm, preferably 0.7 vvm, the excess pressure is 0.5 to 1.5 bar and the fermenter is used to reduce the oxygen concentration to less than 0.2 mmol / L as measured at the bottom of the stirrer using Rushton turbines. In order to prevent it, the mixture was stirred at an intensity of 0.5 to 3 Kw / m 3. The glucose feed was started when the oxygen uptake suddenly dropped and when the dissolved oxygen concentration increased, as well as when the pH was between 6.9 and 7.1. The glucose concentration in the gravy should be << 0.2 g / L at this point.
    The glucose feed rate initially corresponded to 93 kg glucose / h, then increased linearly to 64 kg after starting 64 hours. It was increased to 298 kg glucose / h until a feed rate of 186 kg / h after 100 blood hours was about 200 feed hours.
    Foaming was controlled with sterile soybean oil administered at 5.5 kg / h or else with an input of 45 kg every 8 hours during the first 100 hours of fermentation. If necessary, another foam control was carried out in a mixture of soybean oil and silicon antifoaming agent (Basildon silicon antifoaming agent) such as SAG471 in a ratio of 3: 1.
    The ammonia concentration was measured every 12 hours and maintained between 750 and 1500 mg / L by adding aseptic ammonium sulfate equivalent to 500 mg ammonia / L as soon as the level dropped to less than 1000 mg / L.
    The phosphate concentration of the culture filtrate should be kept higher than 500 mg PO 4 / L by the addition of sterile potassium phosphate equivalent to 500 mg / L.
    The productivity of glucose isomerase can be obtained from gravy and purified protein as determined by protein measurement methods known in the art or analyzed by enzymatic analysis applied on stabilized gravy samples. The gravy samples were stabilized by adding 5 ml of a stabilizer solution containing 12 g / L tris-hydroxymethylaminomethane and 2.4 g / L CoCl 2 .6aq to 2 g gravy and then heating at 73 ° C. for 30 minutes. After cooling, 0.42 ml of the stabilized sample was added to 0.8 ml glucose solution (27.25 g / L Tris / HCl buffer pH 8.2, glucose 67.56 g / L, MaCl 2 .6aq, 22.33 g / L Na 2 -EDTA.2aq and 5 mg / L of Triton X-100) and incubated at 60 ° C. The activity was determined by measuring glucose to fructose conversion and expressed in GU / g (1GU is the amount of enzyme required for the formation of 1 μmole fructose per minute). The specific activity of 12 units per mg of protein was used to determine the amount of protein per kg of gravy.
    The total amount of enzyme produced in Figure 2 is shown.
    As demonstrated in this example, 850 kg of enzyme can be produced in one oil production run.
    Example 2
    Production of Penicillin V
    Conidia spores of P. chrysogenum CBS 455.95 (or another suitable strain derived from Wisconsin 54.1255, preferably by mutations and selection for higher productivity, preferably in the manner described below) (g / l) ) Was inoculated into production medium at 10E5 to 10E6 conidia / ml: glucose. H 2 O, 5; Lactose. H 2 O, 80; (NH 2 ) 2 CO, 4.5; (NH 4 ) 2 SO 4 , 1.1; Na 2 SO 4 , 2.9; KH 2 PO 4 , 5.2; K 2 HPO 4 .3H 2 O, 4.8; Trace elements solution (citric acid .H 2 O, 150; FeSO 4 .7H 2 O, 15; MgSO 4 .7H 2 O, 150; H 3 BO 3, 0.0075; CuSO 4 .5H 2 O, 0.24; CoSO 4 .7H 2 0, 0.375; ZnSO 4 .7H 2 0, 1.5; MnSO 4 .H 2 0, 2.28; CaCl 2 H 2 0, 0.99), 10 (ml / l); 10% potassium phenoxyacetate solution, pH 7, 75 (ml / l). (PH 6.5 before sterilization).
    The culture was incubated at 25 ° C. for 144-168 hours at 280 rpm in an orbital shaker. At the end of fermentation, the mycelium was removed by centrifugation or filtration to quantify the amount and the medium was analyzed for penicillin produced by HPLC methods well known in the art.
    Example 3
    Large Scale Penicillium Fermentation Using Combined and Synthetic Media
    Penicillium chrysogenum Wisconsin 54.1255 was optimized for growth and penicillin production on chemical synthetic media by mutations and selection on synthetic media as described in Example 2. Crude fermentation was carried out by Hersbach et al. Containing 50 kg / m 3 corn steep solids (Biotechnology pp 45-140 of industrial antibiotics, Marcel Dekker Inc. 1984, Table 4, medium B containing salts as mentioned under medium A). ) Was performed on 60 m 3 -scale with the composite medium described by. In parallel with this, fermentation was carried out in the synthetic medium given in Example 2, while lactose and urea were eliminated while the dose was doubled due to the high cell density characteristics of this fed fermentation. Glucose was fed to the fermentor while maintaining a glucose concentration of less than 2 g / L to avoid glucose inhibition. Ammonium, sulfuric acid-diammonium and acetic acid-phenyl were fed to the fermentor to adjust the pH and concentrations of ammonium, sulfate and phenylacetic acid to the desired range (Hersbach 1984).
    Since oxygen transfer is an important parameter that determines the economics of industrial fermentation processes, the performance of the fermentation process was analyzed by measuring the degree of oxygen transfer in each process.
    A good measure for oxygen delivery from the fermentation process is the relative k L a value measured in one system. k L a is defined as the oxygen transfer coefficient and calculated according to van't Riet and Tramper (Basic Biorector Design, Marcel Dekker Inc. (1991), pp. 236-273).
    The oxygen transfer capacity calculated by its k L a value was found to be 10-20% higher in the chemical synthesis medium than in the complex medium during the main part of the fermentation.
    Example 4
    Production of 7-ADCA
    The process described in Example 2 was subjected to P. chrysogenum CBS 455.95 (or to mutations and selection for higher productivity) transformed with an expander expression cassette with an expander coding region with an IPNS promoter as described in EP 532341. , Another suitable strain derived from Wisconsin 54.1255, preferably in the manner described below, using 10% potassium adipic acid solution in place of phenoxyacetate and 10% adipe in pH 5.5 instead of phenoxyacetate Modification was made by using a modification of the medium containing 400 ml of potassium acid (the pH of the medium before sterilization was 5.5 instead of 6.5).
    The resulting adipoyl-7-ADCA was then converted to 7-ADCA essentially using an enzymatic deacylation process such as described in Example 4 or 5 of WO95 / 04148.
    Example 5
    Production of lovastatin
    Conidia spores or Aspergillus terreus strain CBS 456.95 (or strains derived by mutation and selection for higher productivity, preferably in one of the methods to be described below) in a production medium containing (g / l) Inoculated with 10E5-10E6 conidia / ml: dextrose, 40; CH 3 COONH 4 , 2.2; Na 2 SO 4 , 4; KH 2 PO 4 , 3.6; K 2 HPO 4 .3H 2 O, 35.1; Trace element solution (see Example 2 above), 10 (ml / l).
    The culture was incubated at 28 ° C. at 220 rpm in an orbital shake incubator for 144-168 hours. At the end of the fermentation, the mycelium was removed by centrifugation or filtration to quantify the amount and the medium was analyzed for lovastatin produced by HPLC methods well known in the art.
    Example 6
    Production of clavulanic acid
    Streptomyces clavuligerus strain ATCC 27064 or its mutants were inoculated in preculture medium consisting of (g / l): (NH 4 ) 2 SO 4 , 2.75; KH 2 PO 4 , 0.5; MgSO 4 .7H 2 O, 0.5; CaCl 2 H 2 O, 0.01; 3- (N-morpholino), propanesulfonic acid, 21; Glycerol, 19.9; Sodium succinate, 5.5; Trace elements solution (ZnSO 4 .7H 2 O, 2.8 ; iron ammonium citrate, 2.7; CuSO 4 .5H 2 O , 0.125; MnSO 4 .H 2 O, 1; CoCl 2 .6H 2 O, 0.1; Na 2 B 4 O 7 .10H 2 O, 0.16; Na 2 MoO 4 .2H 2 O, 0.054), 0.06 (ml / l).
    The cultures were incubated in an orbital shake incubator at 220 rpm for 48-72 hours at 28 ° C. and inoculated into 20 volumes of production medium containing (g / l): (NH 4 ) 2 SO 4 , 2; Asparagine, 4; KH 2 PO 4 , 1.5; MgSO 4 .7H 2 O, 0.5; CaCl 2 H 2 O, 0.01; 3- (N-morpholino), propanesulfonic acid, 21; Glycerol, 19.9; Sodium succinate, 5.5; Trace element solution (see above), 0.06 (ml / l); FeSO 4 .7H 2 O, 0.5; MnCl 2 .4H 2 O, 0.1; ZnSO 4 .7H 2 O, 0.1.
    The incubation was continued for 144 hours in 500 ml Erlenmeyer flasks, preferably with a stopper plate containing 50 ml of culture. At the end of the fermentation the mycelium was removed by centrifugation or filtration and the amount was quantified and the filtrate was analyzed by HPLC methods well known in the art.
    Example 7
    Production of Amyloglucosidase
    Aspergillus niger strain CBS 513.88 or its mutants were inoculated with 10 5 to 10 6 conidia spores / ml in development medium containing (g / l): K 2 HPO 4 .3H 2 O, 0.75; KH 2 PO 4 , 6.6; Na 3 citrate. 3 H 2 O, 5.3; Citric acid. H 2 O, 0.45; Glucose. H 2 O, 25; (NH 4 ) 2 SO 4 , 8; NaCl, 0.5; MgSO 4 .7H 2 O, 0.5; FeSO 4 .7H 2 O, 0.1; ZnSO 4 .7H 2 O, 0.05; CaCl 2 , 0.005; CuSO 4 .5H 2 O, 0.0025; MnSO 4 H 2 O, 0.0005; H 3 BO 3 , 0.0005; Na 2 MoO 4 .2H 2 O, 0.0005; EDTA, 0.13; Tween 80, 3. If necessary, 50 μg / ml of arginine and / or proline may be added to improve development.
    The culture was incubated in an orbital shake incubator at 295 rpm for 48-72 hours at 33 ° C. and inoculated into 10-20 volumes of production medium containing (g / l): KH 2 PO 4 , 1-5; NaH 2 PO 4 .H 2 O, 0.5; Na 3 citrate. 3 H 2 O, 53; Citric acid. H 2 O, 4.05; Dextrose polymer 70; (NH 4 ) 2 SO 4 , 8; (NaCl, MgSO 4 .7H 2 O , FeSO 4 .7H 2 O, ZnSO 4 .7H 2 O, CaCl 2, CuSO 4 .5H 2 O, MnSO 4 .4H 2 O, H 3 BO 3, Na 2 MoO 4 .2H 2 O, EDTA): Same as the development medium.
    The incubation was continued for 96 hours in a 500 ml Erlenmeyer flask containing preferably 100 ml of medium. After the fermentation, the mycelium was removed by centrifugation or filtration to quantify the amount and the filtrate was analyzed for the activity of starch decomposition.
    Example 8
    Production of Astaxanthin
    Phaffia rhodozyma strain CBS 6938 or a mutant thereof in yeast extract, 10; Peptone, 20; 25 ml of preculture medium containing glucose, 20 (g / l): The cultures were incubated in 100 ml Erlenmeyer flasks with a stopper in an orbital shake incubator at 275 rpm for 72 hours at 20 ° C.
    1 ml of preculture was inoculated into 100 ml of production medium containing (g / l): glucose, 30; NH 4 Cl, 4.83; MgSO 4 .7H 2 O, 0.88; NaCl, 0.06; CaCl 2 H 2 O, 0.15; A trace element solution (0.4NH 2 SO 4; citric acid .H 2 O, 50; (NH 4) 2 Fe (SO 4) 2 .6H 2 O, 90; ZnSO 4 .7H 2 O, 16.7; CuSO 4 .5H 2 O, 2.5; MnSO 4 .4H 2 O, 2; H 3 BO 3, 2; Na 2 MoO 4 .2H 2 O, 2; KI, 0.5), 0.3 (ml / l); Vitamin solution (0.07 N in H 2 SO 4 ; myo-inositol, 40; nicotinic acid, 2; Ca-D-pantothenate, 2; vitamin B1, 2; p.aminobenzoic acid, 1.2; vitamin B6, 0.2; biotin 0.008 ) 1-5 (ml / l); Pluronic, 0.04; KH 2 PO 4 , 1; Potassium hydrogen phthalate, 20 (pH 5.4 before sterilization).
    The incubation was continued for 96 hours in a 500 ml Erlenmeyer flask, preferably with a check valve. After fermentation, the astaxanthin content (quantified amount) of the biomass was determined by solvent extraction and measuring the optical density of the extract at 470-490 nm.
    Example 9
    Production of arachidonic acid
    One 1 ml vial, a suspension of Mortierella alpina strain ATCC 16266 stored at −80 ° C., was aseptically opened and the contents were inoculated into 500 ml of production medium containing (g / l): glucose, 70; Yeast extract 0.5; Na 4 NO 3 , 3.0; KH 2 PO 4 , 7.2; MgSO 4 .7H 2 O, 1.5; A trace element solution (0.4NH 2 SO 4; citric acid .H 2 O, 50; (NH 4) 2 Fe (SO 4) 2 .6H 2 O, 90; ZnSO 4 .7H 2 O, 16.7; CuSO 4 .5H 2 O, 2.5; MnSO 4 .4H 2 O, 2; H 3 BO 3, 2; Na 2 MoO 4 .2H 2 O, 2; KI, 0.5), 0.3 (ml / l); (Pre-sterilization pH 7.0).
    The cultures were incubated at 25 ° C. for 72 hours at 250 rpm in 2 liter shake flasks with a stop plate in an orbital shake incubator. After fermentation, the amount of biomass and arachidonic acid content of the biomass were determined by GC method well known in the art after centrifugation, freeze drying and solvent extraction.
    Example 10
    Production of erythromycin
    Saccharopolyspora erythraea strain NRRL2338 or a mutant thereof (selected for increased productivity, preferably in the manner described below) was inoculated into (g / l) 25 ml of preculture medium containing: soluble starch, 15; NaCl, 5; Soy flour, 15; CaCO 3 , 10; Yeast extract, 5; Cone steep solid, 5; CoCl 2 .6H 2 O, 1 g / l solution 670 μl.
    The cultures were incubated in 100 ml shake flasks without plates in shake incubator-incubators at 32-34 ° C. for 3 days at 250 rpm.
    0.4 ml of the culture was inoculated into 25 ml of sterile production medium (g / l) containing: citric acid. H 2 O, 2; (NH 4 ) 2 SO 4 , 2; MgSO 4 .7H 2 O, 2; CaCl 2 H 2 O, 0.085; KH 2 PO 4 , 0.25; HEPES (= N- (2-hydroxyethyl) piperazine-N '-(2-ethanesulfonic acid)), 5; Glucose, 1.5; Soluble starch, 20; Soybean oil, 0.4; Trace elements solution (gram present in 250ml of distilled water: Citric acid .H 2 O, 62.5; FeSO 4 .7H 2 O, 0.8215; CuSO 4 .5H 2 O, 0.0625; CoCl 2 .H 2 O, 0.375; H 3 BO 3 , 0.0625; ZnSO 4 .7H 2 O , 1.25; MnSO 4 .H 2 O, 1.25; Na 2 MoO 4 .2H 2 O, 0.0625), 3.6ml / l. pH = 7.0. To each flask was added 0.25 ml of n-propanol.
    The culture was incubated in a 100 ml shake flask with a check plate in a shaker-incubator at 300-34 ° C. for 5 days. After the fermentation was finished, the juice was centrifuged and the amount of biomass was measured. The erythromycin content of this clarification liquid was measured by the HPLC method known in the art.
    Example 11
    Production of β-carotene
    Spore suspensions of Blakeslea trispora CBS 130.59 were inoculated in 114 ml preculture medium (10 g / l yeast extract; 20 g / l peptone; 20 g / l glucose) in a 500 ml shake flask. The preculture was incubated for 42 hours on a rotary shaker at 250 ° C. at 26 ° C. The biomass was obtained by filtration and washed three times with 100 ml of sterile demineralized water to remove the components of the preculture medium. The biomass was then homogenized by blending and resuspended in 40 ml of demineralized water until only small fragments remained.
    The production medium was prepared in 100 ml portions of a 500 ml shake flask with a check valve. The composition of the production medium is as follows (g / l): glucose, 40; Asparagine monohydrate, 2; KH 2 PO 4 , 0.5; MgSO 4 .7H 2 O, 0.25. As well as a microelement solution (g / l) having the following composition (0.3 ml / l): 0.4NH 2 SO 4 ; Citric acid. H 2 O, 50; (NH 4) 2 Fe (SO 4) 2 .6H 2 O, 90; ZnSO 4 .7H 2 O, 16.7; CuSO 4 .5H 2 O, 2.5; MnSO 4 H 4 O, 2; H 3 BO 3 , 2; Na 2 MoO 4 .2H 2 O, 2; KI, 0.5. The pH of the medium was adjusted to 6.2 before sterilization. The flask was sterilized at 120 ° C. for 20 minutes and after sterilization, 0.05 ml of a 1 mg / ml solution of thiamine hydrochloride in demineralized water was added (sterile by filtration).
    The production culture was inoculated with 0.5 to 10 ml of the suspension of the fragmented mycelium prepared above. The culture was incubated for 139 hours on a rotary shaker (250 rpm; 26 ° C.). The fungus biomass was obtained by filtration and then washed with demineralized water to remove media components and weighed.
    The amount of β-carotene produced was determined by measuring the absorbance at 450 nm of the acetone fraction by acetone extraction and spectrophotometer.
    权利要求:
    Claims (35)
    [1" claim-type="Currently amended] A method of preparing a valuable compound comprising fermenting a microbial strain on an industrial scale in a chemically synthetic fermentation medium consisting essentially of chemically defined components and recovering the valuable compound from the fermentation broth.
    [2" claim-type="Currently amended] The method of claim 1, wherein the chemical synthesis medium contains essentially a small amount of complex carbon and / or nitrogen sources.
    [3" claim-type="Currently amended] The chemically defined constituents of the chemical synthesis medium are carbohydrates such as glucose, lactose, fructose, sucrose, maltodextrin, starch and inulin, glycerol, vegetable oils, hydrocarbons, Carbon sources selected from the group consisting of alcohols such as methanol and ethanol, organic acids such as acetate and higher alkanoic acid, ammonium salts such as urea, ammonia, nitrate, ammonium sulfate, ammonium phosphate and ammonium nitrate and amino acids such as glutamate and lysine And a nitrogen source selected from the group consisting of.
    [4" claim-type="Currently amended] The method of claim 3 wherein the carbon source is glucose and the nitrogen source is ammonia and / or ammonium salts.
    [5" claim-type="Currently amended] The process according to any of claims 1 to 4, wherein the fermentation takes place via a batch, repeated batch, fed fed, repeated fed or continuous fermentation process.
    [6" claim-type="Currently amended] 6. The method of claim 5 wherein the fermentation occurs through a fed-batch process.
    [7" claim-type="Currently amended] 7. The method of claim 6, wherein a carbon and / or nitrogen source is fed to the process.
    [8" claim-type="Currently amended] 8. The method of claim 7, wherein the carbon source is glucose and the nitrogen source is ammonia and / or ammonium salts.
    [9" claim-type="Currently amended] The method according to claim 1, wherein the valuable compound is a pharmaceutical protein or peptide, a primary or secondary metabolite, or an industrial enzyme.
    [10" claim-type="Currently amended] 10. The method of claim 9, wherein the valuable compound is a secondary metabolite.
    [11" claim-type="Currently amended] The method of claim 10 wherein the secondary metabolite is a β-lactam compound.
    [12" claim-type="Currently amended] 10. The method of claim 9, wherein the valuable compound is an enzyme.
    [13" claim-type="Currently amended] 10. The method according to any one of claims 1 to 9, wherein the microbial strain is yeast.
    [14" claim-type="Currently amended] The method of claim 13, wherein the yeast is Phaffia rhodozyma and the valuable compound is astaxanthin.
    [15" claim-type="Currently amended] 10. The method according to any one of claims 1 to 9, wherein the microbial strain is a filamentous microbial strain.
    [16" claim-type="Currently amended] The method of claim 15, wherein the filamentous strain is a fungus.
    [17" claim-type="Currently amended] The method of claim 16 wherein the fungus is an Aspergillus strain.
    [18" claim-type="Currently amended] 18. The method of claim 17, wherein the fungus is Aspergillus terreus and the valuable compound is lovastatin.
    [19" claim-type="Currently amended] The method of claim 16 wherein the fungus is a Penicillium strain.
    [20" claim-type="Currently amended] 20. The method of claim 19, wherein the fungus is Penicillium chrysogenum and the valuable compound is a β-lactam compound.
    [21" claim-type="Currently amended] The method of claim 16 wherein the fungus is a Mucorales strain.
    [22" claim-type="Currently amended] The method of claim 21, wherein the Mucorales strain is a Mortierella strain.
    [23" claim-type="Currently amended] The method of claim 22 wherein the Mucorales strain is Mortierella alpina and the valuable compound is a lipid comprising arachidonic acid.
    [24" claim-type="Currently amended] 24. The method of claim 23, wherein the lipid comprising arachidonic acid is triglycerides.
    [25" claim-type="Currently amended] The method of claim 21, wherein the Mucorales strain is a Blakeslea strain.
    [26" claim-type="Currently amended] The method of claim 25, wherein the Mucorales strain is Blakeslea trispora and the valuable compound is β-carotene.
    [27" claim-type="Currently amended] The method of claim 15, wherein the filamentous strain is a bacterium.
    [28" claim-type="Currently amended] The method of claim 27, wherein the bacterium is Actinomycete.
    [29" claim-type="Currently amended] 29. The method of claim 28, wherein Actinomycete is a Streptomyces strain and the valuable compound is glucose isomerase.
    [30" claim-type="Currently amended] 29. The method of claim 28, wherein Actinomycete is Streptomyces clavuligerus and the valuable product is clavulanic acid.
    [31" claim-type="Currently amended] 29. The method of claim 28, wherein Actinomycete is Saccharopolyspora erythraea and the valuable compound is erythromycin.
    [32" claim-type="Currently amended] A method of preparing and / or improving microbial strains that produces desired valuable compounds that can be fermented on an industrial scale in a chemical synthetic medium, comprising the following steps:
    Mutagenesis treatment and / or DNA transformation selected from the group consisting of physical means and chemical mutagens,
    Screening the resulting mutants and / or transformants for their growth performance on chemical synthetic medium and the productivity level of said valuable compound desired,
    Selecting mutants and / or transformants with better growth performance on the chemical synthesis medium and / or improved productivity levels of the desired valuable compound as compared to said parent strain.
    [33" claim-type="Currently amended] 33. The method of claim 32, wherein the parent strain is selected from the group consisting of strains that have good growth performance on chemical synthetic media but need to improve productivity levels.
    [34" claim-type="Currently amended] 33. The method of claim 32, wherein the parent strain is selected from the group consisting of strains with a high level of productivity of the desired compound but relatively poor growth performance on chemical synthetic media.
    [35" claim-type="Currently amended] Use of a chemical synthetic fermentation medium to produce valuable compounds on an industrial scale by fermentation of microbial strains.
    类似技术:
    公开号 | 公开日 | 专利标题
    Finogenova et al.2005|Organic acid production by the yeast Yarrowia lipolytica: a review of prospects
    Adrio et al.2010|Recombinant organisms for production of industrial products
    Hujanen et al.2001|Optimisation of media and cultivation conditions for L |-lactic acid production by Lactobacillus casei NRRL B-441
    Demain2000|Small bugs, big business: the economic power of the microbe
    ES2285757T3|2007-11-16|Procedure to produce dicarboxyl acids.
    Hajjaj et al.1999|Improvement of red pigment/citrinin production ratio as a function of environmental conditions by Monascus ruber
    CN1330750C|2007-08-08|Fermentation production process for phosphoglyceric acid family amino-acid and amino-acid derivative
    Boze et al.1992|Production of food and fodder yeasts
    US6365381B2|2002-04-02|Method for producing optically active compound
    US5521075A|1996-05-28|Method for making succinic acid, anaerobiospirillum succiniciproducens variants for use in process and methods for obtaining variants
    EP2115135B1|2012-12-05|A microorganism of corynebacterium genus having enhanced l-lysine productivity and a method of producing l-lysine using the same
    KR100838038B1|2008-06-12|- - a microorganism of corynebacterium genus having enhanced l-lysine productivity and a method of producing l-lysine using the same
    FI104836B|2000-04-14|Process for the preparation of amino acids by fermentation
    RU2491345C2|2013-08-27|Fermentation medium and method of production of recombinant proteins
    US5792631A|1998-08-11|Microbial process for the production of ascorbic acid using Chlorella protothecoides
    US7794990B2|2010-09-14|Microorganism of corynebacterium genus having enhanced L-lysine production ability and method of producing L-lysine using the same
    Adrio et al.2006|Genetic improvement of processes yielding microbial products
    EP0824595B1|2001-12-05|Process for making 1,3-propanediol from carbohydrates using mixed microbial cultures
    RU2208644C2|2003-07-20|Method for preparing n-deacylated cephalosporin
    CN102517239B|2014-08-13|A microorganism having enhanced L-valine productivity and process for preparing L-valine using the same
    Parekh et al.1999|Pilot-scale production of butanol by Clostridium beijerinckii BA101 using a low-cost fermentation medium based on corn steep water
    JP4162774B2|2008-10-08|Protein production method
    US8114626B2|2012-02-14|Yeast strain and method for using the same to produce nicotinamide riboside
    US20070178564A1|2007-08-02|Microorganism of the genus corynebacterium having enhanced l-lysine productivity and method of producing l-lysine using the microorganism of the genus corynebacterium
    Yegneswaran et al.1991|Effect of dissolved oxygen control on growth and antibiotic production in Streptomyces clavuligerus fermentations
    同族专利:
    公开号 | 公开日
    EP2345734A2|2011-07-20|
    PL335227A1|2000-04-10|
    EP2256211A3|2011-02-16|
    PT970236E|2006-08-31|
    ID23995A|2000-06-14|
    DE69834630T2|2007-04-19|
    EP2256211A2|2010-12-01|
    AT327340T|2006-06-15|
    CZ295499A3|2000-04-12|
    CN1127571C|2003-11-12|
    US20140342396A1|2014-11-20|
    EP0970236B1|2006-05-24|
    JP4469401B2|2010-05-26|
    DE69834630D1|2006-06-29|
    ES2262228T3|2006-11-16|
    SI0970236T1|2006-10-31|
    US20070092955A1|2007-04-26|
    EP1690945A2|2006-08-16|
    JP2008200053A|2008-09-04|
    JP2001512970A|2001-08-28|
    EP0970236A2|2000-01-12|
    CN1495259A|2004-05-12|
    CN1248294A|2000-03-22|
    JP2014087365A|2014-05-15|
    JP4217277B2|2009-01-28|
    KR100576576B1|2006-05-04|
    WO1998037179A3|1999-01-14|
    WO1998037179A2|1998-08-27|
    US20020039758A1|2002-04-04|
    AU6400098A|1998-09-09|
    BR9807362A|2000-04-18|
    EP1690945A3|2009-06-03|
    CZ299290B6|2008-06-11|
    EP2345734A3|2012-03-21|
    JP2009195254A|2009-09-03|
    CN100351386C|2007-11-28|
    RU99120113A|2002-12-27|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    法律状态:
    1997-02-20|Priority to EP97200494
    1997-02-20|Priority to EP97200494.9
    1998-02-20|Application filed by 윌리암 로엘프 드 보에르, 디에스엠 엔.브이
    1998-02-20|Priority to PCT/EP1998/001122
    2000-12-15|Publication of KR20000075487A
    2006-05-04|Application granted
    2006-05-04|Publication of KR100576576B1
    优先权:
    申请号 | 申请日 | 专利标题
    EP97200494|1997-02-20|
    EP97200494.9|1997-02-20|
    PCT/EP1998/001122|WO1998037179A2|1997-02-20|1998-02-20|Fermentative production of valuable compounds on an industrial scale using chemically defined media|
    [返回顶部]