WO2019230861A1 - 揮発性の化学品の製造方法および発酵装置 - Google Patents
揮発性の化学品の製造方法および発酵装置 Download PDFInfo
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- WO2019230861A1 WO2019230861A1 PCT/JP2019/021450 JP2019021450W WO2019230861A1 WO 2019230861 A1 WO2019230861 A1 WO 2019230861A1 JP 2019021450 W JP2019021450 W JP 2019021450W WO 2019230861 A1 WO2019230861 A1 WO 2019230861A1
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- KUHYFIGWEQUAER-UHFFFAOYSA-N CCCC1C2(CC(C)CC2)C1CC Chemical compound CCCC1C2(CC(C)CC2)C1CC KUHYFIGWEQUAER-UHFFFAOYSA-N 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M33/00—Means for introduction, transport, positioning, extraction, harvesting, peeling or sampling of biological material in or from the apparatus
- C12M33/14—Means for introduction, transport, positioning, extraction, harvesting, peeling or sampling of biological material in or from the apparatus with filters, sieves or membranes
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/12—Bioreactors or fermenters specially adapted for specific uses for producing fuels or solvents
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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
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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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- 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
- C12P7/16—Butanols
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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
- C12P7/24—Preparation of oxygen-containing organic compounds containing a carbonyl group
- C12P7/26—Ketones
- C12P7/28—Acetone-containing products
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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
- C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
- C12P7/54—Acetic acid
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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 manufacturing method and a manufacturing apparatus for reducing loss of volatile chemicals.
- a method of manufacturing various chemicals using microorganisms such as yeast and bacteria using organic compounds in biomass as fermentation raw materials has been put into practical use.
- the target chemical may be extracted from the culture solution or the culture solution may be concentrated. In such a case, the culture solution is once collected in a storage tank or the like.
- the volatile chemical product evaporates from the culture solution, so that the culture tank or storage tank in which fermentation is performed is filled with a gas containing the chemical product. If the culture solution is transferred to a storage tank filled with a gas containing chemicals, the pressure in the tank will increase, which is dangerous. For this reason, a vent that releases the gas to the outside of the tank is installed. However, if the gas is released to the outside of the tank, the chemical contained in the gas will also be released to the outside of the tank. Loss.
- Patent Document 1 when ethanol is produced by a fermentation method, the gas in the culture tank is sucked and the inside of the culture tank is maintained at a reduced pressure, so that the ethanol concentration in the culture solution is reduced and the fermentation rate is set. A method of maintaining is described.
- the reverse flow condenser is also called Cold trap, and the reverse flow condenser installed in the culture tank or storage tank is provided with a pipe through which coolant flows around or inside the line connecting the gas phase inside the tank and the outside of the tank.
- the pressure in the tank can be prevented from increasing, and loss of volatile chemicals can be prevented. If the reverse flow condenser is installed not only in the culture tank but also in the storage tank, it is considered that the loss of volatile chemicals is further suppressed.
- Patent Document 2 prevents loss of volatile chemicals by culturing while supplying a gas containing methanol in a process for producing methanol.
- the present inventors have examined the installation of a reverse flow condenser in the storage tank. As a result, even if the reverse flow condenser is installed in the storage tank, the loss of volatile chemicals is reduced. We found a new problem that could not be suppressed sufficiently. In other words, it is difficult to condense all volatile substances even if a backflow condenser is installed, and only a condensable amount can be recovered at least at the temperature of the cooling water, and the rest is discharged as a gas. Moreover, even if the heat transfer area of the backflow condenser is not sufficient, part of it flows out as a loss.
- the reverse flow condenser is installed not only in the culture tank but also in the storage tank, the culture solution is further diluted. Further, in the method of Patent Document 1, it is possible to prevent loss of volatile chemicals, but energy for reducing the pressure in the culture tank is necessary, and the more the apparatus becomes larger, the more necessary it is. Increased energy will also increase. Moreover, the density
- An object of the present invention is to provide an apparatus and a method for easily preventing loss of volatile chemicals from a storage tank without using a backflow condenser in the storage tank.
- the present invention is as follows (1) to (9).
- a culture tank for culturing microorganisms capable of producing volatile chemicals a storage tank for storing a solution containing chemicals obtained by culturing the microorganisms, and a culture solution cultured in the culture tank
- the separation membrane module that separates the microorganisms in the culture solution the culture solution delivery line that sends the culture solution to the separation membrane module, and the filtrate of the separation membrane module that stores the filtrate.
- the filtrate obtained by passing the culture solution through the separation membrane module is sent to the storage tank as a solution containing the volatile chemical, and the culture solution is obtained by passing the culture solution through the separation membrane module.
- the volatile chemical is ethanol, methanol, 1-propanol, 2-propanol, 1-butanol, 2-methyl-1-propanol, 2-butanol, 2-methyl-2-propanol, acetone, or The method for producing a volatile chemical according to any one of (1) to (6), which is acetic acid.
- a culture tank for culturing microorganisms capable of producing volatile chemicals a storage tank for storing a solution containing chemicals obtained by culturing the microorganisms, and a culture solution cultured in the culture tanks
- An apparatus for producing volatile chemicals including a liquid feed line for feeding the liquid to the storage tank, and a vent pipe for connecting the gas phase portions in the culture tank and the storage tank.
- the separation membrane module for separating the microorganisms in the culture solution, the culture solution feeding line for feeding the culture solution to the separation membrane module, the filtrate of the separation membrane module,
- the volatile chemistry according to (8) including a filtrate pipe for sending a solution containing a chemical product to the storage tank, and an unfiltrate pipe for returning the unfiltered liquid of the separation membrane module to the culture tank.
- the gas generated in the storage tank is not discharged to the outside and moves to the fermenter via the aeration pipe, so that loss of volatile chemicals in the fermenter and the storage tank can be easily reduced. be able to.
- FIG. 1 is a schematic diagram for explaining a culture apparatus including an aeration pipe used in Example 1.
- FIG. 1 is a schematic diagram for demonstrating the culture apparatus which does not contain the aeration piping used by the comparative example 1.
- FIG. 1 is a schematic diagram for explaining a culture apparatus including an aeration pipe used in Example 1.
- FIG. 4 is a schematic diagram for explaining a continuous culture apparatus including an aeration pipe used in Example 2.
- FIG. It is a schematic diagram for demonstrating the continuous culture apparatus which does not contain the aeration piping used in the comparative example 3.
- the present invention relates to a culture tank for cultivating a microorganism having the ability to produce a volatile chemical, a storage tank for storing a solution containing the chemical obtained by culturing the microorganism, and a culture cultured in the culture tank.
- a technical feature is that the gas phase portions in the storage tank and the culture tank are connected to each other by an aeration pipe. If the liquid of each tank does not mix, the connection location of an aeration piping can connect any part of a culture tank and a storage tank.
- the shape of the ventilation pipe is not particularly limited as long as it is tubular.
- the material of the ventilation pipe is preferably a metal from the viewpoint of durability, but a resin can also be used.
- the inner diameter of the ventilation pipe is not particularly limited as long as the gas pipe can be easily moved.
- the gas in the storage tank and the gas in the culture tank move in both directions so that the pressure is equal, or the culture in the storage tank It is possible to move in both directions so that the concentration of volatile chemicals in the gas phase in the tank is uniform, and loss of volatile chemicals can be suppressed. Specifically, the concentration of the volatile chemicals in the solution containing the volatile chemicals stored in the storage tank can be maintained at a higher concentration than when not connected by the ventilation pipe.
- the connection by the aeration pipe may be a permanent connection as a culture apparatus configuration, or may be a temporary connection.
- the culture tank in which the culture solution is held may be in culture or may be in a state where culture has been completed.
- the solution containing volatile chemicals corresponds to a culture solution retained in a culture tank or a solution obtained by removing cells from the culture solution.
- Microorganism culture methods can be roughly classified into (1) batch culture method (Batch culture method), fed-batch culture method (Fed-Batch culture method), and (2) continuous culture method.
- the batch culture method and fed-batch culture method of (1) have the advantage that the equipment is simple, the culture is completed in a short time, and the influence of contamination with bacteria is small. However, as the time passes, the concentration of the fermented product in the culture solution increases, and the productivity and yield decrease due to an increase in osmotic pressure and the inhibition of fermentation by the product itself.
- the continuous culture method aims to avoid accumulation of fermented products at a high concentration in the culture tank by continuously supplying and discharging raw materials and fermentation broth, and by doing so, It is possible to maintain a high yield and productivity of chemicals over a long period of time.
- volatile chemicals can be obtained by any one of (1) batch culture method (Batch culture method), fed-batch culture method (Fed-Batch culture method), and (2) continuous culture method. Even when manufactured, it can be expected to reduce the loss of volatile chemicals, but (2) continuous culture is preferred.
- the method of the present invention is a method in which the gas phase portions in the culture tank and the storage tank are connected to each other by an aeration pipe, and the solution containing the volatile chemical is held in the storage tank while being cultured in the culture tank.
- a specific example of the culture time is preferably 100 hours or more, more preferably 150 hours or more, and further preferably 200 hours or more.
- the culture method in the culture tank is (1) a batch culture method (Batch culture method) or a fed-batch culture method
- the culture is performed according to these culture methods in the culture tank.
- the culture solution is sent to the storage tank via a liquid supply line, and the culture solution is stored in the storage tank as a solution containing volatile chemicals. At this time, a part of the culture solution may be left in the culture tank, or a new culture may be started in the culture tank.
- the culture solution is fed through the solution feeding line, it is preferable that the gas phase portions in the culture vessel and the storage vessel are connected to each other by an aeration pipe.
- the culture method in the culture tank is (2) a continuous culture method, a multistage culture method or a membrane-based culture method is preferably applied, but a membrane-based culture method is more preferably applied.
- the membrane-based culture method is a continuous culture method as exemplified in, for example, WO 2007/097260.
- a separation membrane module that separates at least microorganisms in the culture solution into the liquid feeding line
- a culture solution feeding line for sending the culture solution to the separation membrane module
- a filtrate pipe for sending the filtrate of the separation membrane module to the storage tank
- an unfiltered solution of the separation membrane module for the culture vessel After placing the non-filtrate piping to reflux, culture in the culture tank and continuous membrane filtration of the culture solution by the method described in WO 2007/097260, and the obtained filtrate is converted into a volatile chemical product. It can implement by storing in the said storage tank as a solution containing.
- the connection between the gas phase portions in the culture vessel and the storage vessel by the ventilation pipe is It is preferable that the culture apparatus has a permanent connection.
- the separation membrane either an inorganic membrane or an organic membrane can be used as long as microorganisms can be filtered from the culture solution.
- a porous ceramic membrane, a porous glass membrane, a porous organic polymer membrane, A metal fiber knitted fabric, a nonwoven fabric, etc. can be used.
- a porous organic polymer film or a ceramic film is particularly preferable.
- the separation membrane if the separation membrane can be treated for 20 minutes at 2 atm of saturated water vapor at 121 ° C., the separation membrane module can be sterilized. Therefore, the separation membrane preferably has heat resistance.
- a separation membrane it is preferable that it is a separation membrane which contains a porous resin layer as a functional layer from the point of dirt resistance, for example.
- 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. Or either.
- the preferred average thickness of the porous substrate is 50 ⁇ m to 3000 ⁇ m.
- the porous substrate is made of an organic material and / or an inorganic material, and among these, an organic fiber is preferable.
- Preferred organic fibers used for the porous substrate are cellulose fibers, cellulose triacetate fibers, polyester fibers, polypropylene fibers, polyethylene fibers, and the like, and these woven fabrics and nonwoven fabrics are preferably used.
- a nonwoven fabric that is relatively easy to control density, easy to manufacture, and inexpensive is preferable.
- An organic polymer film can be preferably 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 culture cannot pass, but clogging occurs due to secretions of microorganisms used in culture 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 ⁇ m to 5 ⁇ m. More preferably, when the average pore diameter of the separation membrane is 0.01 ⁇ m to 1 ⁇ m, both a high exclusion rate without causing leakage of microorganisms and high water permeability can be achieved, and the water permeability can be maintained for a long time. be able to.
- the average pore diameter of the separation membrane is not too large compared to the size of the microorganism in order to prevent the leakage of the microorganism, that is, the occurrence of the problem that the rejection rate is lowered.
- the average pore diameter is preferably 0.01 ⁇ m or more and 0.4 ⁇ m or less, more preferably 0.01 ⁇ m or more and 0.2 ⁇ m or less.
- 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 with a scanning electron microscope at a magnification of 10,000 times, 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 culture solution 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 permeability 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 as long as it is within a range where microorganisms and other solid substances attached to the membrane can be peeled off, but is preferably 0.1 ⁇ m or less. When the surface roughness is 0.1 ⁇ m or less, microorganisms and other solid substances attached to the film 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, in the filtration of microorganisms, the shearing force generated on the membrane surface can be reduced, the destruction of microorganisms is suppressed, and the clogging of the separation membrane is also suppressed.
- the surface roughness of the separation membrane is preferably as small as possible.
- the membrane surface roughness of the separation membrane is a value measured under the following conditions using the following atomic force microscope (AFM).
- Apparatus Atomic force microscope apparatus (“Nanoscope (registered trademark) IIIa” manufactured by Digital Instruments) Measurement conditions
- 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.
- 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 ⁇ m 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.
- the transmembrane pressure difference at the time of filtration is not particularly limited as long as the culture solution can be filtered. However, if the transmembrane pressure difference is too high, the structure of the separation membrane is destroyed, and the transmembrane pressure difference is low. If the pressure is too high, filtration is not sufficiently performed, and therefore, a transmembrane pressure difference in the range of 0.1 kPa to 150 kPa is preferable, more preferably in the range of 0.1 kPa to 50 kPa, and most preferably in the range of 0.1 kPa to 20 kPa. is there.
- the temperature in the storage tank it is preferable to control the temperature in the storage tank to be lower than that in the culture tank regardless of the culture method. If the temperature in the storage tank is controlled lower than in the culture tank, the concentration of volatile chemicals in the gas phase of the storage tank will be lower than in the gas phase of the culture tank. Volatile chemicals move by diffusion through the vent pipe. Therefore, it is preferable that the temperature of the storage tank for storing the solution containing the volatile chemical is lower.
- the temperature in the culture tank refers to the liquid temperature of the culture solution
- the temperature in the storage tank refers to the liquid temperature in the storage tank.
- the volatile chemical produced by the method of the present invention is not particularly limited as long as it has a vapor pressure at room temperature and pressure, but is preferably a substance mainly present as a liquid at room temperature and pressure.
- a substance having a vapor pressure of 1 kPa to 101 kPa at 30 ° C. is preferable.
- Specific examples of substances having a vapor pressure of 1 kPa to 101 kPa at 30 ° C. include ethanol, methanol, 1-propanol, 2-propanol, 1-butanol, 2-methyl-1-propanol, 2-butanol, and 2-methyl.
- the microorganism used in the present invention is not particularly limited as long as it is a microorganism having the ability to produce volatile chemicals.
- specific examples of such microorganisms include yeasts such as baker's yeast often used in the fermentation industry, bacteria such as Escherichia coli and coryneform bacteria, filamentous fungi, actinomycetes, and the like. It may be isolated from the natural environment, or may be partially modified by mutation or genetic recombination.
- FIG. 1 shows an embodiment of the culture apparatus of the present invention when the culture method in the culture tank is (1) a batch culture method (Batch culture method) or a fed-batch culture method (Fed-Batch culture method).
- the culture apparatus of FIG. 1 includes a culture tank 1 for culturing microorganisms having the ability to produce volatile chemicals, a storage tank 2 for storing the culture solution after culture, and the culture solution from the culture tank 1 to the storage tank 2.
- a liquid supply line 3 for supplying liquid and an aeration pipe 5 for connecting gas phase portions in the culture tank and the storage tank are included.
- the liquid feed line 3 includes a pump 4 as a liquid feed means
- the culture tank 1 includes a raw material supply line 7 and a microorganism supply line 8 in addition to the above. It is not essential and may not be included.
- the culture tank 1 preferably includes a vent 6 for safety.
- a stirrer, a gas supply device, a pH sensor, a pH control device, a temperature controller, a liquid level sensor, and the like may be further included.
- the culture solution in the culture vessel 1 is held in the culture vessel after completion of fermentation, or is sent to the storage tank 2 via the liquid supply line 3. Since the culture tank 1 and the storage tank 2 are connected by the ventilation pipe 5, the gas in the culture tank 1 and the storage tank 2 can move in both directions via the ventilation pipe 5.
- the aeration pipe 5 is connected even when the culture solution is sent from the culture tank 1 to the storage tank 2, the liquid level in the culture tank 1 decreases and the liquid level in the storage tank 2 increases. To do.
- the gas in the storage tank 2 moves to the culture tank 1 side through the aeration pipe 5. That is, by providing the aeration pipe 5, it is possible to prevent the outflow of gas from the culture tank 1 and the storage tank 2 to the outside of the tank and the inflow of gas from the outside of the tank.
- FIG. 2 shows an embodiment of the culture apparatus of the present invention when the culture method in the culture tank is a multistage continuous culture method among (2) continuous culture methods.
- Multi-stage continuous culture is a culture method in which a plurality of culture tanks are connected, and the culture tanks are connected in series or in parallel.
- FIG. 2 is an example in which culture vessels are connected in three stages in series.
- the culture apparatus of FIG. 2 includes culture tanks 1, 1a, 1b for culturing microorganisms capable of producing volatile chemicals, multistage liquid feed lines 11, 11a connecting the respective culture tanks, and culture tank 1b.
- a liquid feed line 3 for feeding the culture solution to the storage tank 2 a storage tank 2 for storing the culture solution after the culture, and an aeration pipe 5 for connecting the gas phase portions in the culture tank 1 and the storage tank 2 are included.
- the culture solution in the culture tanks 1 and 1a is sent to the culture tanks 1a and 1b through the multistage liquid supply lines 11 and 11a, respectively.
- FIG. 2 includes pumps 4, 4a and 4b as liquid feeding means for the liquid feeding line 3 and the multistage liquid feeding lines 11 and 11a, but these are not essential devices and are not included in the device. May be.
- the aeration pipe 5 is connected also when the culture solution is sent between each culture tank and the storage tank 2, the liquid level in each culture tank and the storage tank 2 is increased or decreased. Since the gas in the culture tank 1 and the storage tank 2 can move through the aeration pipe 5 along with the upper and lower sides of the culture tank, the culture tank and the storage tank can be provided by providing the aeration pipe even in the culture method of multistage continuous culture. The outflow of gas from the tank and the inflow of gas from outside the tank can be prevented.
- the culture tanks 1, 1a, 1b preferably contain a vent 6 for safety.
- a stirrer, a gas supply device, a pH sensor / control device, a temperature controller, a liquid level sensor, and the like may be included as necessary in addition to these devices.
- gas phase portions in the culture tank 1, 1 a, 1 b, and storage tank 2 may be connected to each other by an aeration pipe.
- FIG. 3 shows one mode of the main culture device when the culture method in the culture tank is (2) continuous culture using a separation membrane module among continuous culture methods.
- continuous culture using a separation membrane module volatile compounds are cultured in a culture tank, and the resulting culture is filtered into microorganisms and filtrate through the separation membrane module, and the filtrate is collected in a storage tank and unfiltered. The liquid is retained or refluxed to the culture tank, and the fermentation raw material is added to the culture tank.
- the culture apparatus shown in FIG. 3 includes a culture tank 1 for culturing microorganisms capable of producing volatile chemicals and a separation membrane module 12 for filtering the culture solution.
- the culture tank 1 and the separation membrane module 12 are connected by a culture solution feed line 15 and a non-filtrate pipe 13 (circulation line).
- the secondary side (filtration side) of the separation membrane module 12 and the storage tank 2 are connected by a filtrate pipe 14.
- a vent pipe 5 for connecting the gas phase portions in the storage tank 2 and the culture tank 1 is connected.
- the raw material supply line 7 for adding fermentation raw materials to the culture tank is connected to the culture tank 1.
- the microorganism supply line 8 is included in the culture tank 1 of FIG. 3, these are not essential devices and may not be included.
- the culture tank 1 preferably includes a vent 6 for safety.
- a stirrer, a gas supply device, a pH sensor, a pH control device, a temperature controller, a liquid level sensor, and the like may be included.
- the culture solution supply line 15 in FIG. 3 includes the pump 4 for supplying the culture solution, but this is not an essential device and may not be included. Also, although not an essential device, a pump may be included in the non-filtrate piping 13 as necessary.
- the secondary-side filtrate pipe 14 may include a pump and a control valve in order to adjust the filtration rate.
- the filtrate filtered from the culture solution by the separation membrane module 12 is sent to the storage tank 2 through the filtrate pipe 14.
- the filtrate is stored in the storage tank 2 for a certain period of time, and is sent to a subsequent process such as distillation as necessary.
- the shape of the separation membrane module 12 is not particularly limited as long as the culture solution feeding line 15 and the non-filtrate piping 13 can be connected to the primary side, and the filtrate piping 14 can be connected to the secondary side.
- the liquid level in the culture tank rises due to the addition of the fermentation medium to the culture tank 1, there is no room to sufficiently receive the gas moved from the storage tank.
- the loss of volatile chemicals can be further reduced by collecting only the culture liquid by collecting the culture liquid from the lower part of the storage tank.
- Example 1 The test was performed using the culture apparatus shown in FIG. Schizo Saccharomyces pombe NBRC1628 strain was inoculated into a test tube containing 5 ml of SD medium and cultured overnight with shaking (pre-culture). The obtained culture solution was inoculated into a 45 ml Erlenmeyer flask containing the molasses prepared in Reference Example 3, and cultured with shaking at 30 ° C. and 120 rpm for 8 hours (preculture).
- 35 mL of 50 mL of the pre-culture solution is collected and inoculated into a culture tank into which 700 mL of waste molasses prepared in Reference Example 3 has been added, and stirred at 300 rpm with a stirrer, no aeration, and no neutralization for the first time. Ethanol fermentation was performed. In addition, since carbon dioxide was generated during ethanol fermentation, the culture tank 1 was equipped with a backflow condenser 16. The end of the fermentation was judged by the consumption of all the sugar contained in the medium by the method of Reference Example 2. The culture broth was sent and held via the liquid feed line 3 to the storage tank 2 connected to the culture tank 1 and the aeration pipe 5, and the culture liquid was stored in the storage tank.
- a second ethanol fermentation was performed.
- the second ethanol fermentation was carried out under the same conditions as in the first, and the culture solution after the fermentation was held in the culture tank as it was.
- the ethanol concentration in the storage tank from the time when the second ethanol fermentation was started to 320 hours was measured over time by the method of Reference Example 1. The result is shown in FIG.
- Comparative Example 1 The test was performed using the apparatus of FIG. In the apparatus of FIG. 5, the vent pipe 5 of the apparatus of FIG. 4 is removed, and the storage tank 2 is provided with a vent 6. All other conditions and operations were performed in the same manner as in Example 1. The result is shown in FIG. In Comparative Example 1, the ethanol concentration in the storage tank decreased with time.
- Example 2 (Comparative Example 2) The test was performed using the apparatus of FIG.
- the apparatus shown in FIG. 6 includes a reverse flow condenser instead of the vent 6 in the storage tank of the apparatus shown in FIG. All other conditions and operations were performed in the same manner as in Example 1. The result is shown in FIG.
- Comparative Example 2 the decrease in ethanol concentration in the storage tank was improved by installing a reverse flow condenser in the storage tank as compared with Comparative Example 1, but the ethanol in the storage tank with the passage of time as in Comparative Example 1. It was found that the concentration was lowered and the improvement effect was lower than the result of Example 1.
- Example 2 The test was performed using the culture apparatus shown in FIG. Since carbon dioxide was generated during the ethanol fermentation, the culture tank 1 was equipped with a back-flow condenser 16. The waste molasses prepared in Reference Example 3 was used as a raw material, and yeast was cultured and inoculated in the same manner as in Example 1. The culture medium circulation pump was operated immediately after inoculation, and the liquid between the separation membrane module and the culture tank was used. Circulation was performed for 24 hours. Thereafter, extraction of the filtrate from the separation membrane module was started. After the start of filtration, ethanol was continuously fermented for 600 hours under the following continuous fermentation conditions while controlling the addition of fermentation raw materials so that the amount of the culture solution in the continuous fermentation apparatus was 700 mL.
- the filtrate was sent to the storage tank 2 connected to the culture tank 1 and the aeration pipe 5 via the liquid feed line 15 and the filtrate pipe 14 and held.
- the change in ethanol concentration in the storage tank after 200 hours from the start of inoculation where continuous culture becomes a steady state was measured over time by the method of Reference Example 1.
- the average value of the ethanol concentration between 200 hours and 600 hours after the start of the culture was 64.1 g / l.
- Example 3 (Comparative Example 3) The test was performed using the apparatus of FIG. In the apparatus of FIG. 8, the vent 6 is provided in the storage tank 2 instead of the ventilation pipe 5 in the apparatus of FIG. All other conditions are the same as in Example 2.
- the average value of ethanol concentration between 200 hours and 600 hours was 57.0 g / l.
- Example 4 The test was performed using the apparatus of FIG.
- the apparatus of FIG. 9 includes a backflow condenser 16 in the storage tank 2 instead of the ventilation pipe 5 of FIG. All other conditions and operations were performed in the same manner as in Example 2.
- the average value of ethanol concentration between 200 hours and 600 hours was 60.7 g / l.
- Comparative Example 4 the reduction of ethanol concentration in the storage tank was improved by installing a backflow condenser in the storage tank as compared with Comparative Example 3, but the average value of ethanol concentration was compared with the result of Example 2. The result was low.
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Abstract
Description
(1)揮発性の化学品を製造する能力を有する微生物を培養する培養槽、前記微生物を培養して得られた化学品を含む溶液を貯蔵する貯蔵槽および前記培養槽で培養された培養液を前記貯蔵槽へ送液する送液ラインを含む培養装置を用いて、前記貯蔵槽に前記溶液を保持しながら前記培養槽にて前記微生物を培養する揮発性の化学品の製造方法であって、前記貯蔵槽内と前記培養槽内の気相部分同士が通気配管で接続されている方法。
(2)前記送液ラインが、前記培養液中の微生物を分離する分離膜モジュール、前記培養液を前記分離膜モジュールへ送液する培養液送液ライン、前記分離膜モジュールのろ液を前記貯蔵槽へ送液するろ液配管、および前記分離膜モジュールの未ろ過液を前記培養槽へ還流する未ろ過液配管を含み、前記培養槽から前記貯蔵槽へ前記培養液を送液する際に、前記培養液を前記分離膜モジュールに通じて得たろ液を前記揮発性の化学品を含む溶液として前記貯蔵槽に送液し、かつ、前記培養液を前記分離膜モジュールに通じて得た未ろ過液を前記培養槽に還流する、(1)に記載の揮発性の化学品の製造方法。
(3)前記分離膜の平均細孔径が0.01μm以上5μm未満である、(2)に記載の揮発性の化学品の製造方法。
(4)前記分離膜の膜間差圧が0.1kPaから150kPaである、(2)または(3)に記載の揮発性の化学品の製造方法。
(5)前記培養槽内の液温>前記貯蔵槽内の液温である、(1)から(4)のいずれか一項に記載の揮発性の化学品の製造方法。
(6)前記揮発性の化学品の蒸気圧が30℃で1kPa以上101kPa以下である、(1)から(5)のいずれか一項に記載の揮発性の化学品の製造方法。
(7)前記揮発性の化学品が、エタノール、メタノール、1-プロパノール、2-プロパノール、1-ブタノール、2-メチル-1-プロパノール、2-ブタノール、2-メチル-2-プロパノール、アセトン、または酢酸である、(1)から(6)のいずれか一項に記載の揮発性の化学品の製造方法。
(8)揮発性の化学品を製造する能力を有する微生物を培養する培養槽、前記微生物を培養して得られた化学品を含む溶液を貯蔵する貯蔵槽、前記培養槽で培養された培養液を前記貯蔵槽へ送液する送液ライン、および前記培養槽内と前記貯蔵槽内の気相部分同士を接続する通気配管を含む、揮発性の化学品の製造装置。
(9)前記送液ラインが、前記培養液中の微生物を分離する分離膜モジュール、前記培養液を前記分離膜モジュールへ送液する培養液送液ライン、前記分離膜モジュールのろ液を、前記化学品を含む溶液として前記貯蔵槽へ送液するろ液配管、および前記分離膜モジュールの未ろ過液を前記培養槽へ還流する未ろ過液配管を含む、(8)に記載の揮発性の化学品の製造装置。
装置 原子間力顕微鏡装置(Digital Instruments(株)製“Nanoscope(登録商標) IIIa”)
測定条件
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。
エタノール濃度は、下記に示すガスクロマトグラフの条件で、標品との比較により測定した。
機器:SHIMADZU GAS CHROMATOGRAPH GC-2010(SHIMADZU)
カラム:TC-BOND Q 0.25mm*30ミリ
移動相:ヘリウム
検出方法:FID
流速:40cm/s
温度:250℃。
糖の濃度は、下記に示すHPLC条件で、標品との比較により定量した。
機器:SHIMADZU HPLC システム(Shimadzu)
カラム:HILICpak VG-50 4E(Shodex)
移動相:アセトニトリル:水=3:1
検出方法:RI検出器
流速 移動相:0.6mL/min
温度:40℃。
発酵原料には、廃糖蜜と水を1:3の重量比で混合し、発酵原料として用いた。廃糖蜜に含まれる糖を参考例2に示す方法により分析した結果を表1に示す。
図4に示す培養装置を用いて試験を行った。シゾサッカロマイセス・ポンベNBRC1628株を5mlのSD培地を投入した試験管に植菌し一晩振とう培養した(前々培養)。得られた培養液を、45mlの参考例3で調製した廃糖蜜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(前培養)。前培養液50mLのうち35mLを分取して、700mLの参考例3で調製した廃糖蜜を投入した培養槽に植菌し、撹拌機によって300rpmで撹拌、無通気、無中和で1回目のエタノールの発酵を行った。なお、エタノール発酵の際には二酸化炭素が発生するため、培養槽1には逆流コンデンサー16を備え付けた。発酵の終了は、参考例2の方法によって、培地中に含まれていた糖がすべて消費されている事により判断した。培養液は培養槽1と通気配管5で接続された貯蔵槽2へ送液ライン3を介して送液して保持し、貯蔵槽には培養液が貯蔵されている状態とした。続いて2回目のエタノール発酵を行った。2回目のエタノール発酵は、1回目と同様の条件で行い、発酵終了後の培養液はそのまま培養槽に保持した。2回目のエタノール発酵開始した時点から320時間までの貯蔵槽中のエタノール濃度を参考例1の方法により、経時的に測定した。その結果を図10に示す。
図5の装置を用いて試験を行った。図5の装置は、図4の装置の通気配管5を取り外し、貯蔵槽2にベント6を備えた。他の条件・操作は全て実施例1と同様に行った。その結果を図10に示す。比較例1では、時間の経過と共に貯蔵槽のエタノール濃度が低下した。
図6の装置を用いて試験を行った。図6の装置は、図5の装置のうち貯蔵槽にベント6の代わりに逆流コンデンサーを備えている。他の条件・操作は全て実施例1と同様に行った。その結果を図10に示す。
図7に示す培養装置を用いて試験を行った。エタノール発酵の際に二酸化炭素が発生するため、培養槽1には逆流コンデンサー16を備え付けた。原料としては参考例3で調製した廃糖蜜を利用し、実施例1と同様に酵母を培養、植菌し、植菌後直ちに培養液循環ポンプを稼動させ、分離膜モジュールと培養槽間の液循環を24時間おこなった。その後、分離膜モジュールからろ液の抜き出しを開始した。ろ過開始後は、連続発酵装置の培養液量を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エタノールの連続発酵を600時間行った。ろ液は培養槽1と通気配管5で接続された貯蔵槽2へ送液ライン15とろ液配管14を介して送液して保持した。連続培養が定常状態となる、植菌開始から200時間後以降の貯蔵槽中エタノール濃度変化を参考例1の方法により経時的に測定した。培養開始後200時間から600時間の間のエタノール濃度の平均値は64.1g/lであった。
上記連続発酵装置1を用いた連続発酵条件は、以下の通りとした。
発酵用微生物:シゾサッカロマイセス・ポンベNBRC1628株
発酵微生物植菌量:10v/v%(培養液体積[ml]/体積[ml])
発酵条件:
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濾過膜
分離膜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
濾過フラックス設定値(発酵原料速度も同じ):0.1(m3/m2/日)
滅菌:分離膜エレメントおよび発酵槽は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。
図8の装置を用いて試験を行った。図8の装置では、図7の装置のうち通気配管5の代わりに貯蔵槽2にベント6を備えている。他の条件は全て実施例2と同様である。200時間から600時間の間のエタノール濃度の平均値は57.0g/lであった。
図9の装置を用いて試験を行った。図9の装置は、図8の装置のうち、図7の通気配管5の代わりに貯蔵槽2に逆流コンデンサー16を備えている。他の条件・操作は全て実施例2と同様に行った。200時間から600時間の間のエタノール濃度の平均値は60.7g/lであった。
2 貯蔵槽
3、3a、3b 送液ライン
4、4a、4b ポンプ
5 通気配管
6 ベント
7 原料供給ライン
8 微生物供給ライン
9 原料供給ライン用ポンプ
10 微生物供給ラインポンプ
11、11a 多段用送液ライン
12 分離膜モジュール
13 未ろ過液配管
14 ろ液配管
15 培養液送液ライン
16 逆流コンデンサー
Claims (9)
- 揮発性の化学品を製造する能力を有する微生物を培養する培養槽、前記微生物を培養して得られた化学品を含む溶液を貯蔵する貯蔵槽および前記培養槽で培養された培養液を前記貯蔵槽へ送液する送液ラインを含む培養装置を用いて、前記貯蔵槽に前記溶液を保持しながら前記培養槽にて前記微生物を培養する揮発性の化学品の製造方法であって、前記貯蔵槽内と前記培養槽内の気相部分同士が通気配管で接続されている方法。
- 前記送液ラインが、前記培養液中の微生物を分離する分離膜モジュール、前記培養液を前記分離膜モジュールへ送液する培養液送液ライン、前記分離膜モジュールのろ液を前記貯蔵槽へ送液するろ液配管、および前記分離膜モジュールの未ろ過液を前記培養槽へ還流する未ろ過液配管を含み、前記培養槽から前記貯蔵槽へ前記培養液を送液する際に、前記培養液を前記分離膜モジュールに通じて得たろ液を前記揮発性の化学品を含む溶液として前記貯蔵槽に送液し、かつ、前記培養液を前記分離膜モジュールに通じて得た未ろ過液を前記培養槽に還流する、請求項1に記載の揮発性の化学品の製造方法。
- 前記分離膜の平均細孔径が0.01μm以上5μm未満である、請求項2に記載の揮発性の化学品の製造方法。
- 前記分離膜の膜間差圧が0.1kPaから150kPaである、請求項2または3に記載の揮発性の化学品の製造方法。
- 前記培養槽内の液温>前記貯蔵槽内の液温である、請求項1から4のいずれか一項に記載の揮発性の化学品の製造方法。
- 前記揮発性の化学品の蒸気圧が30℃で1kPa以上101kPa以下である、請求項1から5のいずれか一項に記載の揮発性の化学品の製造方法。
- 前記揮発性の化学品が、エタノール、メタノール、1-プロパノール、2-プロパノール、1-ブタノール、2-メチル-1-プロパノール、2-ブタノール、2-メチル-2-プロパノール、アセトン、または酢酸である、請求項1から6のいずれか一項に記載の揮発性の化学品の製造方法。
- 揮発性の化学品を製造する能力を有する微生物を培養する培養槽、前記微生物を培養して得られた化学品を含む溶液を貯蔵する貯蔵槽、前記培養槽で培養された培養液を前記貯蔵槽へ送液する送液ライン、および前記培養槽内と前記貯蔵槽内の気相部分同士を接続する通気配管を含む、揮発性の化学品の製造装置。
- 前記送液ラインが、前記培養液中の微生物を分離する分離膜モジュール、前記培養液を前記分離膜モジュールへ送液する培養液送液ライン、前記分離膜モジュールのろ液を、前記揮発性の化学品を含む溶液として前記貯蔵槽へ送液するろ液配管、および前記分離膜モジュールの未ろ過液を前記培養槽へ還流する未ろ過液配管を含む、請求項8に記載の揮発性の化学品の製造装置。
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BR112020022287-9A BR112020022287A2 (pt) | 2018-05-31 | 2019-05-30 | método para a produção de uma substância química volátil e aparelho para produzir uma substância química volátil |
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JP2005013048A (ja) | 2003-06-24 | 2005-01-20 | Osaka Gas Co Ltd | メタン資化菌を用いたメタノールの製造方法及び装置 |
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 |
JP2010246512A (ja) | 2009-04-20 | 2010-11-04 | Bio Trust Kk | 減圧発酵システム |
JP2011530304A (ja) * | 2008-08-14 | 2011-12-22 | スタトイル・アーエスアー | アルコールの製造方法 |
US20110318800A1 (en) * | 2009-12-28 | 2011-12-29 | Chevron U.S.A. Inc. | Integrated mechanical vapor recompression (mvr) and membrane vapor permeation process for ethanol recovery (ethanol dehydration) from fermentation broth |
JP2013059274A (ja) * | 2011-09-12 | 2013-04-04 | Honda Motor Co Ltd | バイオマスの糖化前処理におけるアンモニア処理方法 |
WO2017175833A1 (ja) * | 2016-04-06 | 2017-10-12 | 中越パルプ工業株式会社 | バイオマス資源からエタノールを製造する装置及びバイオマス資源からエタノールを生産する方法 |
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2019
- 2019-05-30 US US17/057,826 patent/US20210301243A1/en not_active Abandoned
- 2019-05-30 CN CN201980028646.1A patent/CN112041452A/zh not_active Withdrawn
- 2019-05-30 JP JP2019530849A patent/JPWO2019230861A1/ja active Pending
- 2019-05-30 WO PCT/JP2019/021450 patent/WO2019230861A1/ja unknown
- 2019-05-30 BR BR112020022287-9A patent/BR112020022287A2/pt not_active Application Discontinuation
- 2019-05-30 EP EP19812370.5A patent/EP3805398A1/en not_active Withdrawn
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JP2005013048A (ja) | 2003-06-24 | 2005-01-20 | Osaka Gas Co Ltd | メタン資化菌を用いたメタノールの製造方法及び装置 |
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 |
JP2011530304A (ja) * | 2008-08-14 | 2011-12-22 | スタトイル・アーエスアー | アルコールの製造方法 |
JP2010246512A (ja) | 2009-04-20 | 2010-11-04 | Bio Trust Kk | 減圧発酵システム |
US20110318800A1 (en) * | 2009-12-28 | 2011-12-29 | Chevron U.S.A. Inc. | Integrated mechanical vapor recompression (mvr) and membrane vapor permeation process for ethanol recovery (ethanol dehydration) from fermentation broth |
JP2013059274A (ja) * | 2011-09-12 | 2013-04-04 | Honda Motor Co Ltd | バイオマスの糖化前処理におけるアンモニア処理方法 |
WO2017175833A1 (ja) * | 2016-04-06 | 2017-10-12 | 中越パルプ工業株式会社 | バイオマス資源からエタノールを製造する装置及びバイオマス資源からエタノールを生産する方法 |
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Publication number | Publication date |
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CN112041452A (zh) | 2020-12-04 |
JPWO2019230861A1 (ja) | 2021-04-22 |
EP3805398A1 (en) | 2021-04-14 |
BR112020022287A2 (pt) | 2021-03-23 |
US20210301243A1 (en) | 2021-09-30 |
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