WO2017159764A1 - 化学品の製造方法および微生物の培養方法 - Google Patents
化学品の製造方法および微生物の培養方法 Download PDFInfo
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- WO2017159764A1 WO2017159764A1 PCT/JP2017/010555 JP2017010555W WO2017159764A1 WO 2017159764 A1 WO2017159764 A1 WO 2017159764A1 JP 2017010555 W JP2017010555 W JP 2017010555W WO 2017159764 A1 WO2017159764 A1 WO 2017159764A1
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
- C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
- C12P7/06—Ethanol, i.e. non-beverage
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Definitions
- the present invention relates to a method for producing a chemical product by continuous culture using a fermentation raw material containing Kane molasses as a main component.
- Biomass-derived chemicals such as biodegradable polymer raw materials such as lactic acid and biofuels such as ethanol have become sustainable (sustainable) as well as carbon dioxide emissions into the atmosphere and the emergence of energy problems. It is attracting a great deal of attention as a life cycle assessment (LCA) compatible product.
- These biodegradable polymer raw materials and biofuel production methods include glucose, which is a hexose refined from edible biomass such as corn, and molasses (Kane molasses) produced in the process of refining sugar from sugarcane, Generally, it is obtained as a fermentation product by a microorganism. Cane molasses is consumed in large quantities as a raw material for ethanol fermentation in sugar producing countries such as Brazil and Thailand, and is an important raw material for fermentation.
- a batch culture method, a fed-batch culture method, or a continuous culture method is used as a method for producing a chemical product by microbial culture.
- Patent Document 1 production of a chemical product that is a fermentation product by a continuous culture method using a separation membrane is used. It is disclosed that speed and yield are improved.
- Patent Document 2 there is no description regarding use of a cane molasses containing raw material.
- patent document 2 the recovery rate by the membrane
- the present invention has an object to provide a method capable of realizing continuous culture using a separation membrane similar to the case of using a fermentation raw material not containing cane molasses even when using a fermentation raw material containing cane molasses as a main component.
- the present inventor has included microorganism-derived particles having an average particle diameter of 100 nm or more in the centrifugal supernatant of a culture solution in continuous fermentation using a separation membrane using a fermentation raw material containing Kane molasses as a main component.
- the present inventors have found that the above-mentioned problems can be solved by culturing the microorganisms to be caused to arrive at the present invention.
- the present invention is as follows (1) to (5).
- Microorganisms are cultured with a fermentation raw material containing Kane molasses as a main component, the culture solution is filtered through a separation membrane to collect a filtrate containing chemicals from which microorganisms have been separated, and an unfiltered solution containing microorganisms
- the microorganism is allowed to contain particles having an average particle diameter of 100 nm or more in the centrifugal supernatant of the culture solution.
- a method for producing a chemical product is produced.
- the microorganism is cultured with a fermentation raw material containing Kane molasses as a main component, the culture solution is filtered through a separation membrane, and an unfiltered solution containing the microorganism is retained or refluxed in the culture solution, and the fermentation raw material is used as the culture solution.
- a method for culturing microorganisms wherein microorganisms that contain particles having an average particle diameter of 100 nm or more in the centrifugal supernatant of the culture solution are cultured.
- the membrane of the separation membrane can be prevented and the chemical product can be produced efficiently.
- the present invention cultivates microorganisms with fermentation raw materials mainly composed of cane molasses, collects the filtrate containing the chemical product from which the microorganisms have been separated by filtering the culture solution through a separation membrane, A method for producing a chemical product in which a filtrate is retained or refluxed in a culture solution, and a fermentation raw material is added to the culture solution to perform continuous fermentation, and particles having an average particle size of 100 nm or more in the centrifugal supernatant of the culture solution.
- the present invention relates to a method for producing a chemical product and a method for culturing microorganisms, which are characterized by culturing microorganisms containing sucrose.
- the microorganism used in the present invention is a microorganism having the ability to produce a chemical product, and when the microorganism is cultured with a fermentation raw material mainly containing cane molasses, There is no particular limitation as long as it is a microorganism that contains particles having a particle diameter of 100 nm or more.
- Specific examples of such microorganisms include yeast belonging to the genus Shizosaccharomyces. As the yeast belonging to the genus Shizosaccharomyces, Shizosaccharomyces pombe, Shizosaccharomyces japonicus, Shizosaccharomyces octosporus or Shizosaccharomyces can be used.
- the particle in the present invention means an insoluble granular substance other than microorganisms contained in the culture solution.
- Measurement of the average particle size of the particles present in the culture solution is performed by a dynamic light scattering method (DLS, photon correlation method). Specifically, an autocorrelation function is obtained by cumulant analysis from the fluctuation of the scattering intensity obtained by measurement by the dynamic light scattering method, converted to a particle size distribution with respect to the scattering intensity, and then the analysis range minimum value is set to 1 nm. The maximum value is converted to an average particle diameter with 5000 nm.
- ELS-Z2 manufactured by Otsuka Electronics Co., Ltd. is used.
- microorganisms also exist as particles in the culture solution
- the microorganisms are precipitated by centrifuging the culture solution at room temperature under conditions of 1000 ⁇ G for 10 minutes, and the particles contained in the centrifugation supernatant The average particle size is measured.
- the average particle size of the particles is 100 nm or more, preferably 300 nm or more, more preferably 300 to 1500 nm.
- a separation membrane is used.
- the membrane occlusion can be remarkably suppressed.
- the upper limit of the average particle diameter of the particles is not particularly limited as long as the filtration flux is not reduced due to the occurrence of membrane clogging, but the upper limit is the average particle diameter of particles that do not precipitate with microorganisms even by centrifugation, and is preferably the upper limit.
- the value is 1500 nm.
- Kane molasses is a by-product produced during sugar production from sugarcane juice or crude sugar. That is, it refers to a crystallization mother liquor containing a sugar component remaining after crystallization in the crystallization step in the sugar making process.
- the crystallization process is usually performed a plurality of times, and the first sugar, which is the crystal component obtained by the first crystallization, and the remaining liquid (No. 1 molasses) of the first sugar are crystallized. Crystallization was repeated as in the case of No. 2 sugar, which is the crystal component obtained, and No. 3 sugar obtained by crystallization of the remaining liquid of No. 2 sugar (No. 2 molasses).
- the final stage molasses obtained as the analysis mother liquor is called Kane molasses.
- the cane molasses used in the present invention is preferably a cane molasses after a large number of crystallizations, and is preferably a cane molasses remaining after crystallization at least twice or more, more preferably three times or more. preferable.
- the sugar component contained in cane molasses contains sucrose, glucose, and fructose as main components, and may contain some other sugar components such as xylose and galactose.
- the sugar concentration in cane molasses is generally about 200 to 800 g / L.
- the sugar concentration in cane molasses can be quantified by a known measurement technique such as HPLC.
- the fermentation raw material contains all the nutrients necessary for the growth of microorganisms.
- the fermentation raw material used in the present invention only needs to contain cane molasses as a main component.
- a carbon source, a nitrogen source, inorganic salts, and if necessary, organic micronutrients such as amino acids and vitamins are appropriately added. May be.
- the fermentation raw material which contains cane molasses as a main component means that 50 weight% or more is a cane molasses among the substances (except water) contained in a fermentation raw material.
- Carbon sources include sugars such as glucose, sucrose, fructose, galactose, lactose, starch saccharified solution containing these sugars, sweet potato molasses, sugar beet molasses, high test molasses, and organic acids such as acetic acid, alcohols such as ethanol Cellulose-containing biomass-derived sugar solutions are preferably used in addition to glycerin and glycerin.
- cellulose-containing biomass examples include plant biomass such as bagasse, switchgrass, corn stover, rice straw, and straw, and woody biomass such as trees and waste building materials.
- Cellulose-containing biomass contains cellulose or hemicellulose, which is a polysaccharide obtained by dehydrating and condensing sugar, and a sugar solution that can be used as a fermentation raw material is produced by hydrolyzing such a polysaccharide.
- the method for preparing a cellulose-containing biomass-derived sugar solution is not particularly limited, and as a method for producing such sugar, a method for producing a sugar solution by acid hydrolysis of biomass using concentrated sulfuric acid (Japanese Patent Publication No. 11-506934).
- JP 2005-229821 A discloses a method for producing a sugar solution by hydrolyzing biomass with dilute sulfuric acid and then further treating with an enzyme such as cellulase (A. Aden et al., “Lignocellulosic”). Biomassto Ethanol Process Design and Economics Customizing Co-Current Dilute Acid Prehydration and Enzymatic Hydrology for Corn Saver EL Technical Report (2002)).
- a method not using an acid a method of hydrolyzing biomass using subcritical water at about 250 to 500 ° C. to produce a sugar solution (Japanese Patent Laid-Open No. 2003-212888), or treating the biomass with subcritical water Later, a method for producing a sugar solution by further enzyme treatment (Japanese Patent Application Laid-Open No. 2001-95597), a biomass solution by hydrolyzing biomass with pressurized hot water at 240 to 280 ° C. and further enzyme treatment Is disclosed (Japanese Patent No. 3041380). After the treatment as described above, the obtained sugar solution and Kane molasses may be mixed and purified. The method is disclosed, for example, in WO2012 / 118171.
- Nitrogen sources include ammonia gas, aqueous ammonia, ammonium salts, urea, nitrates, and other supplementary organic nitrogen sources such as oil cakes, soybean hydrolysates, casein degradation products, other amino acids, vitamins, corn Steep liquor, yeast or yeast extract, meat extract, peptides such as peptone, various fermented cells and hydrolysates thereof are used.
- inorganic salts phosphates, magnesium salts, calcium salts, iron salts, manganese salts and the like can be appropriately added.
- the nutrient can be added and used as a standard or a natural product containing it.
- the separation membrane used in the present invention is not particularly limited as long as it has a function of separating and filtering a culture solution obtained by microbial culture from microorganisms.
- the material include porous ceramic membranes and porous glass.
- a membrane, a porous organic polymer membrane, a metal fiber woven fabric, a non-woven fabric, and the like can be used. Among these, a porous organic polymer membrane or a ceramic membrane is particularly preferable.
- the configuration of the separation membrane is preferably, for example, a separation membrane including a porous resin layer as a functional layer from the viewpoint of stain resistance.
- the separation membrane including the porous resin layer preferably has a porous resin layer that acts as a separation functional layer on the surface of the porous substrate.
- the porous substrate supports the porous resin layer and gives strength to the separation membrane.
- the porous resin layer does not penetrate into the porous substrate even if the porous resin layer penetrates into the porous substrate. But either is fine.
- the average thickness of the porous substrate is preferably 50 to 3000 ⁇ m.
- the material of the porous substrate is made of an organic material and / or an inorganic material, and an organic fiber is preferably used.
- the preferred porous substrate is a woven or non-woven fabric made of organic fibers such as cellulose fiber, cellulose triacetate fiber, polyester fiber, polypropylene fiber and polyethylene fiber. More preferably, the density control is relatively easy and the production is easy. Inexpensive nonwoven fabric is used.
- An organic polymer film can be suitably used for the porous resin layer.
- the material of the organic polymer film include polyethylene resin, polypropylene resin, polyvinyl chloride resin, polyvinylidene fluoride resin, polysulfone resin, polyethersulfone resin, polyacrylonitrile resin, cellulose resin, and the like. Examples thereof include cellulose triacetate resins.
- the organic polymer film may be a mixture of resins mainly composed of these resins.
- the main component means that the component is contained in an amount of 50% by weight or more, preferably 60% by weight or more.
- the organic polymer film is made of a polyvinyl chloride resin, a polyvinylidene fluoride resin, a polysulfone resin, a polyethersulfone resin, which is easy to form a film with a solution and has excellent physical durability and chemical resistance.
- Polyacrylonitrile-based resins are preferable, and polyvinylidene fluoride-based resins or resins containing them as the main components are most preferably used.
- polyvinylidene fluoride-based resin a homopolymer of vinylidene fluoride is preferably used.
- polyvinylidene fluoride resin a copolymer of a vinyl monomer copolymerizable with vinylidene fluoride is also preferably used.
- vinyl monomers copolymerizable with vinylidene fluoride include tetrafluoroethylene, hexafluoropropylene, and ethylene trichloride fluoride.
- the separation membrane used in the present invention only needs to have a pore size through which microorganisms used in fermentation cannot pass, but clogging occurs due to secretions of microorganisms used in fermentation and fine particles in fermentation raw materials. It is difficult and it is desirable that the filtration performance is within a stable range for a long time. Therefore, the average pore diameter of the porous separation membrane is preferably 0.01 to 5 ⁇ m. More preferably, when the average pore diameter of the separation membrane is 0.01 to 1 ⁇ m, both a high exclusion rate at which microorganisms do not leak and high water permeability can be achieved, and water permeability can be maintained for a long time. Can be held.
- the average pore diameter of the separation membrane is preferably 1 ⁇ m or less.
- the average pore diameter of the separation membrane is preferably not too large compared to the size of the microorganism in order to prevent leakage of the microorganism, that is, the occurrence of a problem that the rejection rate decreases.
- the average pore diameter is preferably 0.4 ⁇ m or less, more preferably 0.2 ⁇ m or less, and further preferably 0.1 ⁇ m or less.
- the average pore diameter of the separation membrane in the present invention is preferably 0.01 ⁇ m or more. Yes, more preferably 0.02 ⁇ m or more, and still more preferably 0.04 ⁇ m or more.
- the average pore diameter can be obtained by measuring and averaging the diameters of all pores that can be observed within a range of 9.2 ⁇ m ⁇ 10.4 ⁇ m in a scanning electron microscope observation at a magnification of 10,000 times. it can.
- the average pore diameter or the membrane surface was photographed at a magnification of 10,000 times using a scanning electron microscope, and 10 or more, preferably 20 or more pores were randomly selected. It can also be obtained by measuring and number average.
- a circle having an area equal to the area of the pores (equivalent circle) is obtained by an image processing device or the like, and the equivalent circle diameter is obtained by the method of setting the diameter of the pores.
- the standard deviation ⁇ of the average pore diameter of the separation membrane used in the present invention is preferably 0.1 ⁇ m or less.
- the standard deviation ⁇ of the average pore diameter is N (the number of pores that can be observed within the above-mentioned range of 9.2 ⁇ m ⁇ 10.4 ⁇ m), each measured diameter is Xk, and the average pore diameter is X (ave) It is calculated by the following (Formula 1).
- the permeability of the fermentation broth is one of the important performances.
- the pure water permeability coefficient of the separation membrane before use can be used as an index of the permeability of the separation membrane.
- the pure water permeation coefficient of the separation membrane is 5.6 ⁇ 10 ⁇ 10 m 3 when calculated by measuring the water permeation amount at a head height of 1 m using purified water at a temperature of 25 ° C. by a reverse osmosis membrane.
- the pure water permeability coefficient is 5.6 ⁇ 10 ⁇ 10 m 3 / m 2 / s / pa or more 6 ⁇ 10 ⁇ 7 m 3 / m 2 / s / If it is less than pa, a practically sufficient amount of permeated water can be obtained.
- the surface roughness is an average value of heights in a direction perpendicular to the surface.
- the membrane surface roughness is one of the factors for facilitating separation of microorganisms adhering to the separation membrane surface by the membrane surface cleaning effect by the liquid flow by stirring or a circulation pump.
- the surface roughness of the separation membrane is not particularly limited, and may be in a range in which microorganisms attached to the membrane and other solid substances are peeled off, but is preferably 0.1 ⁇ m or less. When the surface roughness is 0.1 ⁇ m or less, microorganisms adhering to the film and other solid substances are easily peeled off.
- the membrane surface roughness of the separation membrane is 0.1 ⁇ m or less, the average pore diameter is 0.01 to 1 ⁇ m, and the pure water permeability coefficient of the separation membrane is 2 ⁇ 10 ⁇ 9 m 3 / m 2 / It has been found that by using a separation membrane of s / pa or more, an operation that does not require excessive power necessary for membrane cleaning can be performed more easily.
- the surface roughness of the separation membrane is 0.1 ⁇ m or less, the shearing force generated on the membrane surface can be reduced in the filtration of microorganisms, the destruction of microorganisms is suppressed, and the clogging of the separation membrane is also suppressed. By doing so, stable filtration for a long period of time becomes easier.
- the surface roughness of the separation membrane is preferably as small as possible.
- the membrane surface roughness of the separation membrane was measured under the following conditions using the following atomic force microscope (AFM).
- FAM atomic force microscope
- Device Atomic force microscope device (“Nanoscope IIIa” manufactured by Digital Instruments)
- Condition probe SiN cantilever manufactured by Digital Instruments
- Scan mode Contact mode in-air measurement
- Underwater tapping mode underwater measurement
- Scanning range 10 ⁇ m, 25 ⁇ m square (measurement in air) 5 ⁇ m
- 10 ⁇ m square underwater measurement
- Scanning resolution 512 ⁇ 512 -Sample preparation The membrane sample was immersed in ethanol at room temperature for 15 minutes, then immersed in RO water for 24 hours, washed, and then air-dried.
- the RO water refers to water that has been filtered using a reverse osmosis membrane (RO membrane), which is a type of filtration membrane, to exclude impurities such as ions and salts.
- RO membrane reverse osmosis membrane
- the pore size of the RO membrane is approximately 2 nm or less.
- the film surface roughness “drough” is calculated by the following (Formula 2) from the height of each point in the Z-axis direction by the above-described atomic force microscope (AFM).
- the shape of the separation membrane used in the present invention is not particularly limited, and a flat membrane or a hollow fiber membrane can be used, but a hollow fiber membrane is preferred.
- the inner diameter of the hollow fiber is preferably 200 to 5000 ⁇ m, and the film thickness is preferably 20 to 2000 ⁇ m.
- a woven fabric or a knitted fabric in which organic fibers or inorganic fibers are formed in a cylindrical shape may be included in the hollow fiber.
- the above-mentioned separation membrane can be manufactured by the manufacturing method described in WO2007 / 097260, for example.
- a microorganism culture solution is filtered through a separation membrane to collect a filtrate containing a chemical product from which microorganisms have been separated, and an unfiltered solution containing microorganisms is retained or refluxed in the culture solution.
- continuous fermentation which collect
- the transmembrane pressure difference during filtration is not particularly limited as long as the fermentation broth can be filtered.
- the organic polymer membrane is filtered at a transmembrane differential pressure higher than 150 kPa to filter the culture solution, the structure of the organic polymer membrane is likely to be destroyed, and the ability to produce chemicals is increased. May decrease.
- the transmembrane pressure is lower than 0.1 kPa, the permeated water amount of the fermentation broth is often not sufficiently obtained, and the productivity when producing a chemical product tends to decrease.
- the permeated water amount of the fermentation broth is increased by setting the transmembrane differential pressure, which is the filtration pressure, preferably in the range of 0.1 to 150 kPa. Further, since there is no decrease in chemical production capacity due to destruction of the film structure, it is possible to maintain a high ability to produce chemical products.
- the transmembrane pressure difference is preferably in the range of 0.1 to 50 kPa and more preferably in the range of 0.1 to 20 kPa in the case of the organic polymer film.
- the temperature in yeast fermentation may be set to a temperature suitable for the yeast to be used, and is not particularly limited as long as the microorganism grows, but the temperature is in the range of 20 to 75 ° C.
- continuous fermentation filtration of the culture solution
- continuous fermentation may be started after batch culture or fed-batch culture is performed at the initial stage of culture to increase the microorganism concentration. Moreover, you may seed
- the concentration of microorganisms in the culture solution is preferably maintained in a state where the productivity of chemicals is high in order to obtain efficient productivity. For example, good production efficiency can be obtained by maintaining the concentration of microorganisms in the culture solution as a dry weight of 5 g / L or more.
- culture is performed by removing a part of the culture solution containing microorganisms from the fermenter and supplying and diluting the fermentation raw material as necessary during the continuous fermentation.
- the number of fermenters is not limited.
- the continuous fermentation apparatus used in the present invention filters a yeast culture solution through a separation membrane, collects a product from the filtrate, holds or refluxs an unfiltered solution containing microorganisms in the culture solution, and a fermentation raw material.
- a yeast culture solution through a separation membrane
- collects a product from the filtrate holds or refluxs an unfiltered solution containing microorganisms in the culture solution
- a fermentation raw material Is not particularly limited as long as it is an apparatus for producing a chemical product by continuous fermentation in which the product in the filtrate is recovered by adding the above to the culture solution, but specific examples are described in WO2007 / 097260 and WO2010 / 038613. Can be used.
- Examples of chemical products produced by the present invention include substances that are mass-produced in the fermentation industry, such as alcohols and organic acids.
- alcohol ethanol, 1,3-propanediol, 1,3-butanediol, 2,3-butanediol, 1,4-butanediol, glycerol, butanol, isobutanol, 2-butanol, isopropanol, etc.
- Examples of the organic acid include acetic acid, lactic acid, adipic acid, pyruvic acid, succinic acid, malic acid, itaconic acid, and citric acid.
- the present invention can also be applied to the production of substances such as enzymes, antibiotics, and recombinant proteins. These chemicals are recovered from the filtrate by known methods (membrane separation, concentration, distillation, crystallization, extraction, etc.).
- the present invention is not limited to the above-described chemical production method, and may be a culture method for the purpose of growing microorganisms by the above-described method.
- culture using a microorganism as a production target can be mentioned.
- Example 1 Separation membrane-based continuous fermentation using Schizo Saccharomyces pombe NBRC1628 strain Ethanol-producing yeast Schizosaccharomyces pombe NBRC1628 strain as a culture microorganism, and a kenmorasses-containing material shown in Table 2 as a culture medium, Utilized continuous culture was performed.
- the separation membrane element the form of a hollow fiber described in JP2010-22321 was adopted.
- Schizo Saccharomyces pombe NBRC1628 strain was inoculated into a test tube containing 5 ml of the raw material shown in Table 2 and cultured overnight with shaking (pre-culture).
- the obtained culture broth was inoculated into a fresh 45 ml Erlenmeyer flask charged with the raw materials shown in Table 2, and cultured with shaking at 30 ° C. and 120 rpm for 8 hours (pre-culture).
- 35 mL of 50 mL of the culture broth was collected in advance and inoculated into a continuous fermentation apparatus charged with 700 mL of the cane molasses-containing raw material shown in Table 2, and the fermentation reaction tank was stirred at 300 rpm with the attached stirrer. Time culture was performed (pre-culture).
- the fermented liquid circulation pump was operated immediately after inoculation, and the liquid was circulated between the separation membrane module and the fermenter.
- the filtration pump was operated to start extracting the fermentation broth from the separation membrane module. After the start of filtration, continuous cultivation was performed for about 300 hours under the following continuous fermentation conditions while controlling the addition of fermentation raw materials so that the amount of fermentation liquid in the continuous fermentation apparatus was 700 mL. The transition of transmembrane pressure difference and filtration rate during continuous culture is shown in FIG.
- Fermentation reactor capacity 2 (L) Separation membrane: Polyvinylidene fluoride filtration membrane separation element Effective filtration area: 218 (cm 2 ) Temperature adjustment: 30 (° C) Aeration rate of fermentation reaction tank: Stirring speed of non-aeration fermentation reaction tank: 300 (rpm) pH adjustment: Unadjusted filtration flux set value: 0.1 (m 3 / m 2 / day) Sterilization: The culture tank containing the separation membrane element is autoclaved at 121 ° C. for 20 min.
- FIG. 3 shows changes in transmembrane pressure difference and filtration flux during a 600 hour continuous filtration test. As shown in FIG. 3, the transmembrane pressure difference was almost constant, no membrane clogging occurred, and the filtration flux was stably maintained at a constant value.
- Example 2 Separation membrane-based continuous fermentation using Schizosaccharomyces japonicus NBRC1609 strain
- Continuous culture was performed in the same manner as in Example 1 except that Schizosaccharomyces japonicus NBRC1609 strain was used as the culture microorganism. It was.
- the transition of transmembrane pressure difference and filtration flux during continuous culture is shown in FIG. As shown in FIG. 4, during the continuous culture for about 300 hours, the transmembrane pressure difference was almost constant, the membrane was not clogged, and the filtration flux was stably maintained at a constant value.
- FIG. 5 shows changes in transmembrane pressure difference and filtration rate during continuous culture.
- membrane clogging may or may not occur depending on the combination of fermentation raw materials and yeast used.
- Example 3 Measurement result of average particle size in culture supernatant Supernatant was obtained by centrifuging each culture solution of Example 1, Example 2, Comparative Example 1, and Reference Example 3 and the raw material containing Kane molasses. The average particle size of the supernatant was measured. Specifically, Schizosaccharomyces pombe NBRC1628 strain, NBRC1609 strain or Saccharomyces cerevisiae NBRC2260 strain was inoculated into a test tube containing 5 mL of the raw material containing Kane molasses of Reference Example 2 and cultured at 30 ° C. and 120 rpm for 72 hours. did.
- Each yeast culture solution and the cane molasses-containing raw material of Reference Example 3 were centrifuged at 1000 ⁇ G for 10 minutes, and 3 mL of each supernatant was collected. 30 ⁇ L of the collected supernatant was diluted with 970 ⁇ L of pH 5 citrate buffer, each diluted solution was placed in a 1 mL capacity disposable cell, and the average particle size was measured by dynamic light scattering.
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Abstract
Description
(1)微生物を、ケーンモラセスを主成分として含む発酵原料で培養し、培養液を分離膜で濾過して微生物が分離された化学品を含む濾過液を回収し、さらに微生物を含む未濾過液を培養液に保持または還流し、かつ発酵原料を培養液に追加して連続発酵する化学品の製造方法において、前記培養液の遠心上清中に平均粒子径が100nm以上の粒子を含有せしめる微生物を培養する、化学品の製造方法。
(2)前記粒子の平均粒子径が300nm以上である、(1)に記載の化学品の製造方法。
(3)前記発酵原料がケーンモラセスおよびセルロース含有バイオマス由来糖液の混合物を含む、(1)または(2)に記載の化学品の製造方法。
(4)前記微生物がシゾサッカロマイセス(Schizosaccharomyces)属に属する酵母である、(1)~(3)のいずれかに記載の化学品の製造方法。
(5)微生物を、ケーンモラセスを主成分として含む発酵原料で培養し、培養液を分離膜で濾過して微生物を含む未濾過液を培養液に保持または還流し、かつ発酵原料を培養液に追加して連続培養する微生物の培養方法において、前記培養液の遠心上清中に平均粒子径100nm以上の粒子を含有せしめる微生物を培養する、微生物の培養方法。
・装置 原子間力顕微鏡装置(Digital Instruments(株)製“Nanoscope IIIa”)
・条件 探針 SiNカンチレバー(Digital Instruments(株)製)
走査モード コンタクトモード(気中測定)
水中タッピングモード(水中測定)
走査範囲 10μm、25μm四方(気中測定)
5μm、10μm四方(水中測定)
走査解像度 512×512
・試料調製 測定に際し膜サンプルは、常温でエタノールに15分浸漬後、RO水中に24時間浸漬し洗浄した後、風乾し用いた。RO水とは、濾過膜の一種である逆浸透膜(RO膜)を用いて濾過し、イオンや塩類などの不純物を排除した水を指す。RO膜の孔の大きさは、概ね2nm以下である。
原料中の糖類、エタノール濃度は、下記に示すHPLC条件で、標品との比較により定量した。
カラム:Shodex SH1011(昭和電工株式会社製)
移動相:5mM 硫酸(流速0.6mL/分)
反応液:なし
検出方法:RI(示差屈折率)
温度:65℃。
バガスを水熱処理して得られる固形分(C6画分)および水を混合し、固形分仕込濃度10%とした混合液に糖化酵素を20mg/g-乾燥バガスを添加して48時間糖化反応を行った。なお、糖化反応は50℃で行い、pH制御は行わなかった。48時間後に最終的に表1に示す割合になるようにケーンモラセスを添加した後に、フィルタープレスによって糖化残渣と糖化液の固液分離を行い、その後、精密濾過膜、限外濾過膜を通じて、ケーンモラセス含有原料を得た。参考例1に示す方法によるケーンモラセス含有原料の分析結果を表2に示す。
培養微生物としてエタノール生産酵母シゾサッカロマイセス・ポンベNBRC1628株、培地として表2に示すケーンモラセス含有原料を用い、分離膜を利用した連続培養を行なった。分離膜エレメントとしては特開2010-22321に記載の中空糸の形態を採用した。シゾサッカロマイセス・ポンベNBRC1628株を5mlの表2に示す原料を投入した試験管に植菌し一晩振とう培養した(前々々培養)。得られた培養液を、新鮮な45mlの表2に示す原料を投入した三角フラスコに植菌し、30℃、120rpmで8時間振とう培養した(前々培養)。前々培養液50mLのうち35mLを分取して、700mLの表2に示すケーンモラセス含有原料を投入した連続発酵装置に植菌し、発酵反応槽を付属の撹拌機によって300rpmで撹拌し、24時間培養を行った(前培養)。なお、植菌後直ちに発酵液循環ポンプを稼動させ、分離膜モジュールと発酵槽間の液循環をおこなった。前培養終了後、ろ過ポンプを稼動させて分離膜モジュールより発酵液の抜き出しを開始した。ろ過開始後は、連続発酵装置の発酵液量を700mLになるよう発酵原料添加制御を行いながら以下の連続発酵条件で約300時間の連続培養を行った。連続培養中の膜間差圧およびろ過速度の推移を図1に示す。
発酵反応槽容量:2(L)
使用分離膜:ポリフッ化ビニリデン製ろ過膜
膜分離エレメント有効濾過面積:218(cm2)
温度調整:30(℃)
発酵反応槽通気量:無通気
発酵反応槽撹拌速度:300(rpm)
pH調整:無調整
ろ過フラックス設定値:0.1(m3/m2/日)
滅菌:分離膜エレメントを含む培養槽は121℃、20minのオートクレーブにより高圧蒸気滅菌
平均細孔径:0.1μm
平均細孔径の標準偏差:0.035μm
膜表面粗さ:0.06μm
純水透過係数:50×10-9m3/m2/s/pa。
培養微生物としてエタノール生産酵母のサッカロマイセス・セレビセNBRC2260株を用いた以外は実施例1と同様の方法にて連続培養を行った。連続培養中の膜間差圧およびろ過フラックスの推移を図2に示す。図2に示したように、300時間の連続培養中、100時間を経過した後から膜間差圧の急激な上昇が起こり、膜閉塞が起こったためろ過フラックスも設定値より低下していくことがわかった。また、連続培養終了時点のエタノール濃度は65g/Lであった。
次に、表2に示すケーンモラセス含有原料のみを用いた連続ろ過試験を行った。ろ過中の温度、攪拌速度、pH等の条件は実施例1に記載した方法と同様の方法で行った。600時間の連続ろ過試験中の膜間差圧およびろ過フラックスの推移を図3に示す。図3に示したように膜間差圧はほぼ一定であり、膜閉塞も起こらずろ過フラックスも安定して一定値で推移した。
培養微生物としてシゾサッカロマイセス・ジャポニカスNBRC1609株を用いた以外は実施例1と同様の方法にて連続培養を行った。連続培養中の膜間差圧およびろ過フラックスの推移を図4に示す。図4に示したように、約300時間の連続培養中、膜間差圧はほぼ一定であり、膜閉塞も起こらずろ過フラックスも安定して一定値で推移した。
培養微生物としてエタノール生産酵母のサッカロマイセス・セレビセNBRC2260株を用い、発酵原料として表3に示すケーンモラセス非含有原料を用いて実施例1と同様の方法で連続培養を行った。ただし設定ろ過フラックスは0.2(m3/m2/日)で実施した。連続培養中の膜間差圧およびろ過速度の推移を図5に示す。
実施例1、実施例2、比較例1、参考例3のそれぞれの培養液および、ケーンモラセス含有原料を遠心分離し、得られた上清の平均粒子径測定を実施した。具体的には、参考例2のケーンモラセス含有原料を5mL加えた試験管に、シゾサッカロマイセス・ポンベNBRC1628株、NBRC1609株またはサッカロマイセス・セレビセNBRC2260株を植菌し、30℃、120rpmで72時間培養した。各酵母培養液および参考例3のケーンモラセス含有原料を1000×Gで10分間遠心して、それぞれの上清3mLを回収した。回収した上清30μLをpH5のクエン酸緩衝液970μLに加えて希釈し、希釈した各溶液を1mL容量のディスポセルに入れ、動的光散乱により平均粒子径を測定した。
・光源のピンホールサイズ:100μm
・測定波長:660nm
・測定角度:165°
・測定積算回数:70回
・溶媒屈折率:1.3313
・溶媒粘度:0.8852cp。
粒子径の解析には、大塚電子株式会社のゼータ電位・粒子測定システムELS-Z2を用い、25℃の条件で、大気中で測定を行った。動的光散乱によって得られた散乱強度の揺らぎからキュムラント解析によって自己相関関数を求め、散乱強度に対する粒度分布へ変換した。粒度分布のヒストグラム解析範囲は最小値を1nm、最大値を5000nmとした。得られた平均粒子径を表4に示す。
Claims (5)
- 微生物を、ケーンモラセスを主成分として含む発酵原料で培養し、培養液を分離膜で濾過して微生物が分離された化学品を含む濾過液を回収し、さらに微生物を含む未濾過液を培養液に保持または還流し、かつ発酵原料を培養液に追加して連続発酵する化学品の製造方法において、前記培養液の遠心上清中に平均粒子径が100nm以上の粒子を含有せしめる微生物を培養する、化学品の製造方法。
- 前記粒子の平均粒子径が300nm以上である、請求項1に記載の化学品の製造方法。
- 前記発酵原料がケーンモラセスおよびセルロース含有バイオマス由来糖液の混合物を含む、請求項1または2に記載の化学品の製造方法。
- 前記微生物がシゾサッカロマイセス(Schizosaccharomyces)属に属する酵母である、請求項1~3のいずれかに記載の化学品の製造方法。
- 微生物を、ケーンモラセスを主成分として含む発酵原料で培養し、培養液を分離膜で濾過して微生物を含む未濾過液を培養液に保持または還流し、かつ発酵原料を培養液に追加して連続培養する微生物の培養方法において、前記培養液の遠心上清中に平均粒子径100nm以上の粒子を含有せしめる微生物を培養する、微生物の培養方法。
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Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2019054469A1 (ja) * | 2017-09-15 | 2019-03-21 | 東レ株式会社 | エタノールの製造方法およびエタノール発酵液 |
WO2021117849A1 (ja) * | 2019-12-13 | 2021-06-17 | 東レ株式会社 | 膜濾過性を改善する連続発酵による化学品の製造方法 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2007097260A1 (ja) * | 2006-02-24 | 2007-08-30 | Toray Industries, Inc. | 化学品の製造方法、および、連続発酵装置 |
WO2011135588A2 (en) * | 2010-04-29 | 2011-11-03 | Shree Renuka Sugars Limited | A continuous process for the preparation of alcohol |
WO2012118171A1 (ja) * | 2011-03-03 | 2012-09-07 | 東レ株式会社 | 糖液の製造方法 |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5372939A (en) * | 1991-03-21 | 1994-12-13 | The United States Of America As Represented By The United States Department Of Energy | Combined enzyme mediated fermentation of cellulous and xylose to ethanol by Schizosaccharoyces pombe, cellulase, β-glucosidase, and xylose isomerase |
JP5082496B2 (ja) * | 2006-02-24 | 2012-11-28 | 東レ株式会社 | 連続発酵による化学品の製造方法および連続発酵装置 |
WO2009100102A2 (en) * | 2008-02-04 | 2009-08-13 | Danisco Us Inc., Genencor Division | Ts23 alpha-amylase variants with altered properties |
WO2014156998A1 (ja) * | 2013-03-28 | 2014-10-02 | 旭硝子株式会社 | 化成品の製造方法および製造装置 |
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Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2007097260A1 (ja) * | 2006-02-24 | 2007-08-30 | Toray Industries, Inc. | 化学品の製造方法、および、連続発酵装置 |
WO2011135588A2 (en) * | 2010-04-29 | 2011-11-03 | Shree Renuka Sugars Limited | A continuous process for the preparation of alcohol |
WO2012118171A1 (ja) * | 2011-03-03 | 2012-09-07 | 東レ株式会社 | 糖液の製造方法 |
Non-Patent Citations (3)
Title |
---|
BAKHIET SHAMI E. A. ET AL.: "Production of Bio-ethanol from Molasses by Schizosaccharomyces Species", ANNUAL RESEARCH & REVIEW IN BIOLOGY, vol. 7, no. 1, 13 April 2015 (2015-04-13), pages 45 - 53, XP055601580, DOI: 10.9734/ARRB/2015/15918 * |
DALE M C ET AL.: "Ethanol from Concentrated Sucrose and Molasses Solutions Using S. Pombe in an Immobilized Cell Reactor-Separator", AICHE SYMPOSIUM SERIES, vol. 90, no. 300, 1994, pages 56 - 62 * |
SAITHONG PRAMUAN ET AL.: "Prevention of bacterial contamination using acetate-tolerant Schizosaccharomyces pombe during bioethanol production from molasses", JOURNAL OF BIOSCIENCE AND BIOENGINEERING, vol. 108, no. 3, 2009, pages 216 - 219, XP026436941 * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2019054469A1 (ja) * | 2017-09-15 | 2019-03-21 | 東レ株式会社 | エタノールの製造方法およびエタノール発酵液 |
WO2021117849A1 (ja) * | 2019-12-13 | 2021-06-17 | 東レ株式会社 | 膜濾過性を改善する連続発酵による化学品の製造方法 |
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