CN107794219B - Bioreactor for fermenting gaseous substrate - Google Patents
Bioreactor for fermenting gaseous substrate Download PDFInfo
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- CN107794219B CN107794219B CN201610780231.8A CN201610780231A CN107794219B CN 107794219 B CN107794219 B CN 107794219B CN 201610780231 A CN201610780231 A CN 201610780231A CN 107794219 B CN107794219 B CN 107794219B
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- 239000000758 substrate Substances 0.000 title claims abstract description 21
- 239000012528 membrane Substances 0.000 claims abstract description 230
- 238000000855 fermentation Methods 0.000 claims abstract description 187
- 230000004151 fermentation Effects 0.000 claims abstract description 182
- 238000000034 method Methods 0.000 claims abstract description 22
- 230000005764 inhibitory process Effects 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 31
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- 239000000047 product Substances 0.000 claims description 26
- 238000007789 sealing Methods 0.000 claims description 15
- 244000005700 microbiome Species 0.000 claims description 14
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 12
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 claims description 11
- 239000002207 metabolite Substances 0.000 claims description 11
- 238000001914 filtration Methods 0.000 claims description 10
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 claims description 9
- 238000003860 storage Methods 0.000 claims description 9
- 230000010261 cell growth Effects 0.000 claims description 8
- 238000000108 ultra-filtration Methods 0.000 claims description 8
- 238000001471 micro-filtration Methods 0.000 claims description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 6
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- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 claims description 6
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- YQUVCSBJEUQKSH-UHFFFAOYSA-N protochatechuic acid Natural products OC(=O)C1=CC=C(O)C(O)=C1 YQUVCSBJEUQKSH-UHFFFAOYSA-N 0.000 claims description 3
- 229940107700 pyruvic acid Drugs 0.000 claims description 3
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 claims description 3
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- 229940005605 valeric acid Drugs 0.000 claims description 3
- WKOLLVMJNQIZCI-UHFFFAOYSA-N vanillic acid Chemical compound COC1=CC(C(O)=O)=CC=C1O WKOLLVMJNQIZCI-UHFFFAOYSA-N 0.000 claims description 3
- TUUBOHWZSQXCSW-UHFFFAOYSA-N vanillic acid Natural products COC1=CC(O)=CC(C(O)=O)=C1 TUUBOHWZSQXCSW-UHFFFAOYSA-N 0.000 claims description 3
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- FERIUCNNQQJTOY-UHFFFAOYSA-M Butyrate Chemical compound CCCC([O-])=O FERIUCNNQQJTOY-UHFFFAOYSA-M 0.000 claims 1
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 241000193459 Moorella thermoacetica Species 0.000 description 3
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 3
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- 241001223493 Acetoanaerobium noterae Species 0.000 description 2
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 2
- 241001464894 Blautia producta Species 0.000 description 2
- 241000620137 Carboxydothermus hydrogenoformans Species 0.000 description 2
- 241000186566 Clostridium ljungdahlii Species 0.000 description 2
- 241000252867 Cupriavidus metallidurans Species 0.000 description 2
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- 241000178985 Moorella Species 0.000 description 2
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- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 2
- AMQJEAYHLZJPGS-UHFFFAOYSA-N N-Pentanol Chemical compound CCCCCO AMQJEAYHLZJPGS-UHFFFAOYSA-N 0.000 description 2
- 241000205156 Pyrococcus furiosus Species 0.000 description 2
- 241000204649 Thermoanaerobacter kivui Species 0.000 description 2
- 241000605118 Thiobacillus Species 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 2
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 2
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 2
- 229940044197 ammonium sulfate Drugs 0.000 description 2
- 235000011130 ammonium sulphate Nutrition 0.000 description 2
- 229940041514 candida albicans extract Drugs 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- ZPWVASYFFYYZEW-UHFFFAOYSA-L dipotassium hydrogen phosphate Chemical compound [K+].[K+].OP([O-])([O-])=O ZPWVASYFFYYZEW-UHFFFAOYSA-L 0.000 description 2
- 229910000396 dipotassium phosphate Inorganic materials 0.000 description 2
- 235000019797 dipotassium phosphate Nutrition 0.000 description 2
- CCIVGXIOQKPBKL-UHFFFAOYSA-M ethanesulfonate Chemical compound CCS([O-])(=O)=O CCIVGXIOQKPBKL-UHFFFAOYSA-M 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- WRUGWIBCXHJTDG-UHFFFAOYSA-L magnesium sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Mg+2].[O-]S([O-])(=O)=O WRUGWIBCXHJTDG-UHFFFAOYSA-L 0.000 description 2
- 229940061634 magnesium sulfate heptahydrate Drugs 0.000 description 2
- 238000005374 membrane filtration Methods 0.000 description 2
- 230000002503 metabolic effect Effects 0.000 description 2
- 230000000813 microbial effect Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910000402 monopotassium phosphate Inorganic materials 0.000 description 2
- 235000019796 monopotassium phosphate Nutrition 0.000 description 2
- 229960005181 morphine Drugs 0.000 description 2
- 235000005985 organic acids Nutrition 0.000 description 2
- GNSKLFRGEWLPPA-UHFFFAOYSA-M potassium dihydrogen phosphate Chemical compound [K+].OP(O)([O-])=O GNSKLFRGEWLPPA-UHFFFAOYSA-M 0.000 description 2
- 235000013619 trace mineral Nutrition 0.000 description 2
- 239000011573 trace mineral Substances 0.000 description 2
- 239000012138 yeast extract Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
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Classifications
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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
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/04—Filters; Permeable or porous membranes or plates, e.g. dialysis
-
- 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
- C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
- C12M27/02—Stirrer or mobile mixing elements
-
- 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
- C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
- C12M27/18—Flow directing inserts
-
- 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
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/24—Recirculation of gas
-
- 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
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
-
- 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
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/26—Means for regulation, monitoring, measurement or control, e.g. flow regulation of pH
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Wood Science & Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
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- Engineering & Computer Science (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Health & Medical Sciences (AREA)
- Biochemistry (AREA)
- Microbiology (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Biotechnology (AREA)
- Sustainable Development (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
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Abstract
The present invention relates to a bioreactor for the fermentation of gaseous substrates. Specifically, the bioreactor of the present invention comprises (1) a fermenter; and (2) a membrane module disposed within the fermentor; wherein the membrane component comprises a membrane and a connecting pipe fitting positioned at one end of the membrane and used for communicating the membrane with an external pipeline; wherein the other end of the membrane is a blind end. The invention also includes a fermentation apparatus of the bioreactor, and a method of fermentation using the bioreactor and the fermentation apparatus. The invention can efficiently generate fermentation products from the closed synthetic gas fermentation system and continuously separate the fermentation products, thereby preventing the inhibition of the products.
Description
Technical Field
The present invention is in the field of biotechnology equipment and microbiology. More particularly, the present invention relates to a bioreactor for fermentation of synthesis gas.
Background
In the conventional batch culture fermentation process, the specific growth rate of cells gradually decreases as the metabolites accumulate due to the inhibition of the cells by the metabolites. Thus, the fermentation is performed to a certain extent to stop the propagation of the cells.
In the field, in the fermentation process, under the condition of not influencing the activity of the thalli, the target product or metabolic byproducts inhibiting the thalli from growing are separated in situ, so that the thalli grow to a very high concentration rapidly, the continuous fermentation process is kept, and the yield of the target product is improved.
Disclosure of Invention
The invention provides a synthesis gas fermentation bioreactor with high-efficiency fermentation and product separation, and a component thereof, in particular to a membrane component.
Specifically, the membrane module of the present invention comprises:
A membrane; and
A connection pipe member located at one end of the membrane for communicating the membrane with an external pipeline;
Wherein the other end of the membrane is a blind end.
In one or more embodiments, the membrane is an organic membrane, a ceramic membrane, or a metal membrane.
In one or more embodiments, the membrane is tubular, plate-like or roll-like in structure.
In one or more embodiments, the membrane is an ultrafiltration membrane or a microfiltration membrane.
In one or more embodiments, the membrane is a hollow fiber ultrafiltration membrane or a microfiltration membrane.
In one or more embodiments, the blind end is formed by sealing the other end of the membrane using a stationary seal head.
In one or more embodiments, the membrane module includes more than 2, such as 2 to 20, membranes connected in parallel, each membrane having a blind end at one end and a connecting tube at the other end for connecting the membranes to an external line.
In one or more embodiments, in the membrane module containing more than 2, for example, 2 to 20, membranes connected in parallel, each membrane is fixed in a symmetrical position via a fixing member.
The bioreactor of the present invention comprises:
(1) A fermentation tank; and
(2) A membrane module disposed within the fermenter;
wherein the membrane module comprises:
A membrane; and
A connection pipe member located at one end of the membrane for communicating the membrane with an external pipeline;
Wherein the other end of the membrane is a blind end.
In one or more embodiments, the membrane is an organic membrane, a ceramic membrane, or a metal membrane.
In one or more embodiments, the membrane is tubular, plate-like or roll-like in structure.
In one or more embodiments, the membrane is an ultrafiltration membrane or a microfiltration membrane.
In one or more embodiments, the membrane is a hollow fiber ultrafiltration membrane or a microfiltration membrane.
In one or more embodiments, the blind end is formed by sealing the other end of the membrane using a stationary seal head.
In one or more embodiments, the membrane module includes more than 2, such as 2 to 20, membranes connected in parallel, each membrane having a blind end at one end and a connecting tube at the other end for connecting the membranes to an external line.
In one or more embodiments, in the membrane module containing more than 2, for example, 2 to 20, membranes connected in parallel, each membrane is fixed in a symmetrical position via a fixing member.
In one or more embodiments, the membrane is removably secured with the connecting tube.
In one or more embodiments, the bioreactor further comprises a bubble generator disposed within the fermentor.
In one or more embodiments, the bubble generator is located at the bottom of the fermenter, in a number of 1 to 8.
In one or more embodiments, the bubble generator is a porous venturi, an in-line mixer, or a vortex bubble generator.
In one or more embodiments, the bioreactor further comprises a draft tube disposed within the fermenter.
In one or more embodiments, the membrane module is located within a draft tube disposed within a fermenter.
In one or more embodiments, the guide shell has a securing grid therein for securing the membrane assembly.
In one or more embodiments, the membrane assembly is removably secured to the guide cylinder, or a member of the membrane assembly for securing a membrane is integrally formed with the guide cylinder.
In one or more embodiments, the membrane assembly is disposed in a lower middle portion of the draft tube.
In one or more embodiments, the wall of the guide cylinder has a through hole to allow a pipe connecting the membrane module with external equipment to pass through.
In one or more embodiments, the fermenter wall has a through hole to allow a pipe connecting the membrane module with external equipment to pass through.
In one or more embodiments, the piping connecting the membrane module and the external device is connected to the external device via the fermenter cover.
In one or more embodiments, a three-way valve is provided on a portion of the pipeline fermentation tank that is external to the pipeline fermentation tank.
In one or more embodiments, the bubble generator is disposed inside the draft tube.
In one or more embodiments, the fermenter is a stirred or airlift fermenter.
In one or more embodiments, the fermenter further comprises a seed liquid inlet, a gas outlet, a pH adjustor inlet, and a medium inlet.
In one or more embodiments, the bioreactor comprises: the fermentation tank, a bubble generator, a membrane component and a guide cylinder are arranged in the fermentation tank; wherein the number of the bubble generators is 1-8 and the bubble generators are positioned at the bottom of the fermentation tank; the membrane component is provided with more than 2 membranes, for example, 2-20 membranes, which are uniformly distributed in the guide cylinder, the bottom of the membrane is a blind end, and the upper part of the membrane is provided with a connecting pipe fitting for communicating with an external pipeline.
The present invention also provides a fermentation apparatus comprising:
(1) A bioreactor as described herein; and
(2) And a gas supply device.
In one or more embodiments, the gas supply includes a gas buffer tank, a gas compressor, and a gas cooler.
In one or more embodiments, the apparatus further comprises a seed tank in communication with the gas cooler and the bioreactor for providing seed liquid to the bioreactor.
In one or more embodiments, the gas cooler provides gas to the seed tank and provides gas to the fermentor via the bioreactor bottom and via the membrane module.
In one or more embodiments, the apparatus further comprises a circulation fan for circulating gas from the seed tank and the bioreactor into the seed tank or the bioreactor.
In one or more embodiments, the apparatus further comprises a pH adjustment tank for providing the culture broth of the bioreactor with reagents for adjusting its pH.
In one or more embodiments, the apparatus further comprises a make-up tank for adding fermentation broth to the bioreactor.
In one or more embodiments, the apparatus further comprises a metering pump for metering the seed solution, pH adjustor or the culture medium into the bioreactor.
In one or more embodiments, the apparatus further comprises a product reservoir connected to the membrane module via the three-way valve.
The invention also provides a fermentation process comprising the step of fermenting a microorganism using the bioreactor or fermentation device of the invention.
In one or more embodiments, coke oven gas is used as a fermentation substrate.
In one or more embodiments, during fermentation using the bioreactor or fermentation device of the present invention, coke oven gas as a fermentation substrate is passed through the membrane module and cellular metabolites that have an inhibitory effect on cell growth are filtered out through the membrane module.
In one or more embodiments, the cellular metabolites that inhibit cell growth include: formic acid, acetic acid, propionic acid, butyric acid, isobutyric acid, succinic acid, lactic acid, pyruvic acid, malic acid, citric acid, benzoic acid, vanillic acid, caproic acid, valeric acid, or a combination of two or more thereof.
In one or more embodiments, when the concentration of the cell metabolites that have an inhibitory effect on cell growth within the fermenter reaches 1% or more, the introduction of coke oven gas via the membrane module is stopped, and the cell metabolites that have an inhibitory effect on cell growth are filtered out by the membrane module.
In one or more embodiments, the pressure within the fermentor is in the range of 0-2 MPa.
In one or more embodiments, the fermenter outlet gas is circulated with a circulation ratio of 2 to 10.
In one or more embodiments, the liquid-out and aeration modes are alternately switched for the membrane module.
In one or more embodiments, the fermenting microorganism is selected from the group consisting of: clostridium (e.g., clostridium ljungdahlii), moorella (e.g., moorella thermoacetica), fireball (e.g., pyrococcus furiosus), eubacterium (e.g., eubacterium limosum), thiobacillus (e.g., desulfobacterium autotrophicum), carbothermus (e.g., carboxydothermus hydrogenoformans), acetogenic (e.g., acetogenium kivui), acetobacter (e.g., acetobacterium woodii), anaerobically acetogenic (e.g., acetoanaerobium noterae), butyric acid (e.g., butyribaceteriummethylotrophicum), streptococcus (e.g., peptostreptococcus productus), and lautersia (e.g., ralstonia eutropha).
In one or more embodiments, the pH of the fermentation broth is from 6.0 to 8.0.
In one or more embodiments, the fermentation temperature is 25-75 ℃.
Other aspects of the invention will be apparent to those skilled in the art in view of the disclosure herein.
Drawings
FIG. 1 is a block diagram of a syngas bioreactor 10, comprising: 11, a fermentation tank body; 21, a membrane module; 31, a guide cylinder; 41, an air inlet pipe; 51, a membrane connection tube; 61, fixing the grille; 71, a bubble generator.
FIG. 2 is a block diagram of a single membrane module, comprising: 210, a membrane; 61, fixing the grille; 51, a membrane connection tube; 220, a connector; 230, fixing the end socket.
FIG. 3 is a process flow diagram of an integrated fermentation process in which anaerobic microorganisms perform fermentation and product separation in a bioreactor using syngas as a fermentation substrate. The device comprises: 1, a gas buffer tank; 2, a gas compressor; 3, a gas cooler; 4, a circulating fan; 5, a seed tank; 6, a pH adjusting tank; 7, supplementing a material tank; 8, a product storage tank; 9, metering pump; 10, a bioreactor.
Detailed Description
The invention aims to improve the microbial fermentation efficiency of gaseous substrate fermentation, in particular coke oven gas substrates containing CO, H 2 and CO 2, and to realize separation of products in the fermentation process. The invention can efficiently generate fermentation products from the closed synthetic gas fermentation system and continuously separate the fermentation products, thereby preventing the inhibition of the products.
The objects of the various aspects herein are achieved by employing the bioreactor and fermentation apparatus provided herein.
The bioreactor of the present invention comprises:
(1) A fermentation tank; and
(2) A membrane module disposed within the fermenter;
wherein the membrane module comprises:
A membrane; and
A connection pipe member located at one end of the membrane for communicating the membrane with an external pipeline;
Wherein the other end of the membrane is a blind end.
In certain embodiments, the bioreactor of the present invention is a fermenter.
A fermenter suitable for use in accordance with the invention can have a conventional fermenter body and can be modified accordingly to the requirements of the invention. For example, the fermenter can have a tank body of a conventional stirred or airlift fermenter. Typically, the fermentor comprises a tank body, a lid, and corresponding outlets and inlets, such as a gas inlet, a gas outlet, a fermentation broth (culture medium) inlet, a seed liquid inlet, a pH modifier inlet, etc.
The membrane module is typically located in the lower middle of the fermenter. The membranes in the membrane module may be various membranes commonly used in the art to separate fermentation products, including but not limited to organic, ceramic or metal membranes, which may be tubular, plate-like or roll-like in structure. The membrane may also be an ultrafiltration membrane or a microfiltration membrane. In certain embodiments, the membrane is a hollow fiber ultrafiltration membrane or microfiltration membrane. In certain embodiments, the average pore size of the membrane is in the range of 4 to 100nm, for example in the range of 30 to 70 nm. The diameter of the membrane may be in the range of2 to 10cm, for example 2 to 7cm. The height of the membrane may be 1/6 to 2/3, for example 1/6 to 1/3, of the height of the fermenter. Typically, the membrane module should be below the liquid level of the fermentation broth. The diameter and height of the membranes, etc. may be determined according to the number of membranes in the membrane module, the volume of the fermenter, etc.
In the invention, one end of the membrane is a blind end, and a fixed seal head can be used for sealing. The other end of the membrane is fixed with a connecting pipe fitting for communicating the membrane with an external pipeline. The connecting tube may have any suitable configuration and may be removably connected to the membrane. For example, the connecting tube may have a base for securing (e.g., tightening) the membrane, and a tube extending from the base.
Fig. 2 shows an example of a membrane module of the present invention, comprising a membrane 210, a connecting tube 220 and a stationary seal head 230.
The membrane module may comprise more than 2 membranes, for example 2 to 20 (e.g. 2 to 15, 2 to 10, 2 to 8) membranes connected in parallel, each membrane having a blind end at one end and a connecting tube at the other end for connecting the membrane to an external pipeline. The number of membranes can be determined according to the capacity of the fermenter. In such membrane modules, the membranes may be secured together, preferably in symmetrical positions, by means of fasteners. For example, the fasteners may connect the fixing heads in series, or connect the bases of the connecting tubes in series. Herein, the symmetrical positions mean that the linear distances of the films are equal to each other. For example, in the case of using 3 films, the 3 films are located at three vertexes of an equilateral triangle, respectively, as viewed in cross section. Typically, the membrane in the membrane module of the present invention has no structure such as a housing outside the membrane.
The connecting tube of the membrane can be communicated with an external pipeline. The external piping generally refers to piping structures other than the membrane modules. The tank body or the tank cover may have a through hole therein to allow an external pipe to communicate with an external device through the tank body of the fermenter or through the tank cover of the fermenter. Alternatively, the connecting pipe may be designed long enough to pass through the tank or the tank cover and then be connected to an external pipeline.
A guide cylinder can be arranged in the fermentation tank. The two ends of the guide cylinder are provided with openings, and can be placed at the bottom of the fermentation tank. At this time, the membrane module is generally located within the guide cylinder and is generally located at the middle lower portion of the guide cylinder. A grid can be arranged on the inner wall of the guide cylinder and used for fixing the membrane component. Typically, the thickness of the wall of the guide cylinder does not exceed 1cm. The outer diameter of the guide cylinder is 1/3 to 2/3 of the inner diameter of the fermentation tank. The height of the draft tube should not exceed the height of the fermenter, typically between 2/3 and 3/4 of the height of the fermenter. Typically, the height of the draft tube should also be below the level of the broth. In certain embodiments, the membrane assembly is removable from the guide shell; in other embodiments, the means for securing the membrane in the membrane assembly is integrally formed with the guide shell. Herein, the means for fixing the membrane is other components of the membrane assembly than the membrane, including, but not limited to, the fixing head described above, a fixing member connecting the fixing head or the base of the connecting tube in series, and the like.
In the case of a pipe passing through the tank, a through hole may be provided in the guide cylinder, allowing an external pipe or connecting tube to pass through the through hole and through the tank.
Typically, through holes in the draft tube, the tank body, and the tank cover are tightly coupled to the tubing to prevent fermentation broth from passing through the through holes. In certain embodiments, a connecting tube may be disposed in the through hole of the guide cylinder, the can body or the can lid, and the connecting tube is in sealing connection with the guide cylinder, the can body or the can lid via a sealing member, or is integrally formed with the guide cylinder, the can body or the can lid. In these embodiments, the connecting tube on the membrane module may be directly in sealing connection with the connecting tube on the guide cylinder or may be in sealing connection with the connecting tube on the guide cylinder via a separate connecting tube. Likewise, the connecting pipe fitting of the guide cylinder and the connecting pipe fitting of the tank body can be directly connected in a sealing way, and also can be connected in a sealing way through independent connecting pipe fittings. The pipelines outside the tank body or the tank cover can be connected in a sealing way through the connecting pipe fittings on the tank body or the tank cover. The manner of sealing the connection is well known in the art, for example using a screw seal as is conventional in the art.
The fermentation tank can be also provided with a bubble generator. The bubble generators are usually located at the bottom of the fermenter, and the number is 1 to 8. The bubble generator may be a variety of bubble generators known in the art including, but not limited to, a porous venturi, an in-line mixer, or a vortex bubble generator. In the case of a draft tube, the bubble generator is typically disposed within the draft tube. The gas in the bubble generator is coke oven gas used in the invention.
In certain embodiments, a three-way valve is provided on the line outside the fermentor in communication with the membrane. Typically, the number of three-way valves is the same as the number of membranes. The flow and switching of fluid within each membrane is controlled by a respective three-way valve. The pipelines extending from the three-way valves can be gathered into one pipeline which is communicated with other external equipment. The three-way valve is used for controlling the communication between the membrane and the air supply device and between the membrane and the product storage tank.
Fig. 1 shows a specific embodiment of a bioreactor 10 according to the invention. The bioreactor 10 comprises a fermenter pot 11, a membrane module 21, a guide cylinder 31, an air inlet pipe 41, a membrane connecting pipe 51, a fixed grid 61 and a bubble generator 71.
In certain embodiments, the bioreactor of the present invention comprises: the fermentation tank, a bubble generator, a membrane component and a guide cylinder are arranged in the fermentation tank; the number of the bubble generators is 1-8, and the bubble generators are positioned at the bottom of the fermentation tank and inside the guide cylinder; the membrane component is provided with more than 2 membranes, for example, 2-20 membranes, which are uniformly distributed in the guide cylinder, the bottom of the membrane is a blind end, and the upper part of the membrane is provided with a connecting pipe fitting for communicating with an external pipeline.
In a preferred embodiment, the guide cylinder and the tank body are provided with through holes which allow the pipeline connecting the membrane assembly and the external equipment to pass through in a sealing manner. In other preferred embodiments, connecting pipes are provided in the through holes on the guide cylinder and the tank, which are connected to the guide cylinder, the tank or the tank cover in a sealing manner via a sealing element or are formed integrally with the guide cylinder, the tank or the tank cover. In a preferred embodiment, the membrane module is removable from the cartridge. In other preferred embodiments, the means for securing the membrane is integrally formed with the guide shell. In a preferred embodiment, a three-way valve is provided on the piping outside the fermentor in communication with the membranes for controlling the flow and switching of fluid within each membrane.
The fermentation apparatus of the present invention comprises a bioreactor as described herein and a gas supply. In certain embodiments, the gas supply includes a gas buffer tank, a gas compressor, and a gas cooler. In certain embodiments, the apparatus further comprises a seed tank for providing a seed liquid. A metering pump can be connected between the seed liquid and the fermentation tank, and the seed liquid is added into the fermentation tank after being metered by the metering pump. The gas supply device may supply gas to the seed tank and the fermenter. In certain embodiments, the gas provides the gas to the seed tank via a gas cooler. Likewise, the gas cooler supplies gas to the fermenter from the bottom of the fermenter of the bioreactor and/or to the membrane module via the three-way valve, thereby achieving gas supply to the fermenter.
The fermentation apparatus of the present invention may further comprise a circulation fan for circulating the gas in the seed tank and the fermentation tank of the bioreactor. In particular, the gas in the seed tank as well as the gas in the fermenter may be circulated back to the seed tank and fermenter via a circulation fan. The circulated gas may be returned to the fermenter via the same line after mixing with the gas from the gas cooler.
The fermentation apparatus of the present invention may further comprise a pH adjustment tank for supplying a reagent for adjusting the pH of the culture liquid of the bioreactor; and a feed tank for adding fermentation broth to the bioreactor. Fermentation broth in the primary bioreactor of the fermentation may also be provided by the feed tank. Both the pH adjusting tank and the replenishing tank can be connected with the fermentation tank via metering pumps.
The fermentation apparatus of the present invention may further comprise a product reservoir connected to the membrane module via the three-way valve.
FIG. 3 shows a specific embodiment of the fermentation apparatus of the present invention. The set of fermentation equipment comprises a gas buffer tank 1, a gas compressor 2, a gas cooler 3, a circulating fan 4, a seed tank 5, a pH adjusting tank 6, a material supplementing tank 7, a product storage tank 8, a metering pump 9 and a bioreactor 10.
The purified coke oven gas and carbon dioxide are mixed in a proper proportion, enter a gas buffer tank 1, are compressed to a proper pressure by a gas compressor 2, enter a gas cooler 3, are cooled to a proper temperature, and are respectively provided for a seed tank and a fermentation tank to serve as a fermentation substrate of seed liquid in the seed tank 5 and a fermentation substrate of microorganisms in the fermentation tank. Gas may be provided to the fermentor of bioreactor 10 through the bottom of bioreactor 10 and into the membrane module via a three-way valve. The seed liquid in the seed tank 5 is supplied to the fermentation tank after being metered by the metering pump 9, and the gas generated by fermentation in the seed tank is circulated by the circulating fan, mixed with the gas supplied by the gas cooler 3 and supplied to the seed tank 5 and the bioreactor 10 again. After fermentation for a certain period of time under suitable conditions, the gas in the bioreactor 10 is discharged from the top of the fermenter, circulated via a circulation fan, mixed with the gas supplied from the gas cooler 3 and/or the gas discharged from the seed tank 5, and supplied again to the seed tank 5 and the bioreactor 10. When necessary, a suitable pH regulator can be provided into the fermentation tank through the pH regulating tank to regulate the pH of the fermentation liquid; likewise, fermentation broth may be replenished to the fermentor via a replenishing tank. In the fermentation process, all the membrane components can be connected to a gas pipeline by switching the three-way valve for supplying gas to the fermentation tank. As the fermentation progresses gradually, part of the membranes in the membrane module can be switched to a liquid outlet mode, namely, a three-way valve is adjusted to stop supplying gas to the membranes, so that the membranes are communicated with a product storage tank 8, filtration power is generated through the pressure difference between the inside and the outside of the fermentation tank, cross flow scouring is generated on the membrane module by the gas-liquid circulation flow in the fermentation tank, and the membranes continuously filter out fermentation products such as ammonium acetate solution. During the continuous fermentation process, back flushing of the membrane module is required. Every interval of several hours (for example, 4-6 hours), the liquid outlet mode and the ventilation mode are alternately switched for each membrane in the membrane assembly, namely, the membrane assembly is backwashed by coal gas, so that filter cakes attached to the membrane surface in the filtration process are broken and fall off, and the membrane flux is recovered.
It is to be understood that the materials and dimensions of the various components involved in the bioreactor and fermentation apparatus of the present invention may be those conventional in the art. For example, the height and width of the draft tube may be designed according to the depth and width of the body of the fermenter. The guide cylinder can be made of metal or ceramic. Each pipeline can be made of plastic, metal or ceramic. In addition, other devices in the fermentation apparatus of the present invention, such as a gas buffer tank, a gas compressor, a circulating fan, a seed tank, a pH adjusting tank, a make-up tank, a product storage tank, a metering pump, a three-way valve, and connecting lines therebetween, may be those conventionally used in the art.
Accordingly, the present invention also provides a fermentation process comprising the step of fermenting a microorganism using the bioreactor or fermentation device of the present invention.
The fermentation method is anaerobic fermentation, and uses coke oven gas as a fermentation substrate. Coke oven gas conventional in the art can be used as a fermentation substrate. In certain embodiments, the cleaned coke oven gas may contain, in volume percent (v/v), 20 to 30% CH 4, 55 to 65% H 2, 1 to 5% CO 2, 2 to 6% CO, and 7 to 10% other components (e.g., N 2). In certain embodiments, the cleaned coke oven gas may contain 22-26% CH 4, 58-63% H 2, 2-4% CO 2, 3-5% CO, 8-10% other components (e.g., N 2) by volume percent.
The purified coke oven gas is supplemented with CO 2 to allow for thorough mixing of the gas in, for example, the gas tank of the present invention. Generally, the CO 2 is fed in such an amount that the molar ratio of H 2 to CO 2 in the gas obtained is between 1.0 and 5.0:1, for example, in the range of 1.5 to 4.5:1, or in the range of 1.5 to 4.0:1, or in the range of 1.5 to 3.5:1, or in the range of 1.5 to 3.0:1, or in the range of 2.0 to 3.5:1, or in the range of 2.0 to 3.0: 1.
In certain preferred embodiments, the coke oven gas used in the fermentation of the present invention contains, in volume percent, 16 to 23% CH 4, 44 to 51% H 2, 18 to 30% CO 2, 2.5 to 4.0% CO, 4.5 to 6.5% N 2, and the balance impurities (including O 2). More preferably, the coke oven gas used for fermentation contains, in volume percent, 18 to 20% CH 4, 45 to 49% H 2, 20 to 27% CO 2, 2.8 to 3.6% CO, 5.0 to 6.0% N 2, and the balance impurities (including O 2).
After sufficient mixing, the gas is compressed (e.g., in the gas compressor 2 of the present invention) to a pressure of 0.1 to 2.0MPa, for example, 0.1 to 1.0MPa, 0.1 to 0.5MPa, 0.3 to 2.0MPa, 0.5 to 2.0MPa, 1.0 to 1.5 MPa. Then the temperature of the gas is controlled to be between 30 and 50 ℃ or between 35 and 45 ℃. This control can be performed in the gas cooler 3 of the present invention.
And then, introducing the gas into the fermentation tank through the bottom of the fermentation tank and the membrane component, and fermenting the gas serving as a fermentation substrate.
Microorganisms suitable for use in the fermentation of the present invention may be selected from: clostridium (e.g., clostridium ljungdahlii), moorella (e.g., moorella thermoacetica), fireball (e.g., pyrococcus furiosus), eubacterium (e.g., eubacterium limosum), thiobacillus (e.g., desulfobacterium autotrophicum), carbothermus (e.g., carboxydothermus hydrogenoformans), acetogenic (e.g., acetogenium kivui), acetobacter (e.g., acetobacterium woodii), anaerobically acetogenic (e.g., acetoanaerobium noterae), butyric acid (e.g., butyribaceteriummethylotrophicum), streptococcus (e.g., peptostreptococcus productus), and lautersia (e.g., ralstonia eutropha).
The fermentation medium suitable for the growth and fermentation of the anaerobic microorganism may be selected according to the specific anaerobic microorganism used. For example, in general, the medium has the main components: monopotassium phosphate, dipotassium phosphate, ammonium sulfate, magnesium sulfate heptahydrate, yeast extract, morphine ethane sulfonic acid, and trace element solution ATCC 1754PETC. The amounts of the respective main components in the medium are conventional in the art, and the contents of the respective components in the medium can be appropriately adjusted by those skilled in the art according to the contents of the medium, fermentation conditions, etc. known in the art.
Typically, the pressure within the fermenter is in the range of 0 to 2MPa, for example 0.1 to 2MPa or 0.1 to 1MPa; the pH of the fermentation broth is 6.0-8.0, e.g., 6.0-7.0; the fermentation temperature is 25 to 75℃such as 45 to 60 ℃.
The fermentation of the present invention may be a continuous fermentation. Therefore, in the fermentation process, coke oven gas is continuously introduced as a substrate for microbial fermentation, so that anaerobic microorganisms continuously grow. In general, the amount of coke oven gas introduced during fermentation may be such that the working pressure of the anaerobic fermentation tank is in the range of 0.1 to 2.0MPa, for example 0.1 to 2.0MPa, 0.1 to 0.5MPa, 0.3 to 2.0MPa, 0.5 to 2.0MPa, 1.0 to 1.5 MPa.
When the total concentration of the organic acid and/or alcohol in the anaerobic fermentation tank is measured to be more than 1% (for example, more than 2%, more than 3%, more than 5%, different selections can be made according to different anaerobic microorganisms), the membranes of part of the membrane modules are switched into a liquid outlet mode through the three-way valve, and the filtration power is generated through the pressure difference between the inside and the outside of the fermentation tank, so that the membranes continuously filter out fermentation products such as ammonium acetate solution. While the fermentation tank continuously discharges, part of the gas at the outlet of the fermentation tank is circulated, and the circulation ratio can be 2-10, for example, 2-8, 2-6, 2-5, 3-10, 3-8, 3-6, 5-10 and 6-8 are different. In certain embodiments, the fermentation is performed with high fermenter pressure and high recycle ratio. In other embodiments, the fermentation is performed with low fermenter pressure and high recycle ratio.
When the fermentation tank continuously discharges, fresh anaerobic microorganisms and culture medium can be continuously supplemented (for example, through the seed tank 5 and the supplementing tank 7) according to actual conditions, and the volume of the fermentation liquid is controlled to be unchanged. If desired, a suitable pH adjustor such as ammonia may also be added through the pH adjusting tank to adjust the pH of the fermentation broth in the fermentation tank to within a suitable range. The volume of fermentation broth, pH, and total concentration of organic acids and/or alcohols in the fermentation broth can be monitored by conventional methods.
During the continuous fermentation process, back flushing of the membrane module is required. Every interval of several hours (for example, 4-6 hours), the liquid outlet mode and the ventilation mode are alternately switched for each membrane in the membrane assembly, namely, the membrane assembly is backwashed by coal gas, so that filter cakes attached to the membrane surface in the filtration process are broken and fall off, and the membrane flux is recovered.
Thus, during fermentation using the bioreactor or fermentation device of the present invention, coke oven gas as a fermentation substrate may be fed through the membrane module, and cell metabolites having an inhibitory effect on cell growth may be filtered out through the membrane module.
As used herein, an organic acid or alcohol is one or more organic acids or alcohols produced by the reaction of CO, CO 2, and H 2 in coke oven gas with anaerobic microorganisms, including formic acid, acetic acid, propionic acid, butyric acid, isobutyric acid, succinic acid, lactic acid, pyruvic acid, malic acid, citric acid, benzoic acid, vanillic acid, caproic acid, valeric acid, methanol, ethanol, propylene glycol, butanol, pentanol, or a combination of two or more thereof.
The invention has the advantages that the micro-nano bubble generating device, the gaseous substrate fermentation tank and the membrane separation system are integrated into a set of synthesis gas fermentation reactor, and the pressure and the flowing state of fermentation liquid are utilized to realize efficient fermentation and product separation and prevent product inhibition.
The invention will be illustrated by way of specific examples. It is to be understood that these examples are illustrative only and are not limiting of the invention. Unless otherwise indicated, all numbers expressing quantities of ingredients, such as operating pressure ranges, temperature ranges, pH ranges, gas compositions, and the like, used in the specification, claims, and embodiments are not to be understood as being absolute precise values, which are within the limits of tolerance of known techniques as understood by those of ordinary skill in the art.
Examples
This example uses Mulberry Moorella thermoacetica, ATCC 49707.
The culture medium comprises the following components: monopotassium phosphate, dipotassium phosphate, ammonium sulfate, magnesium sulfate heptahydrate, yeast extract, morphine ethane sulfonic acid, trace element solution ATCC 1754PETC.
The bioreactor fermentation tank for fermentation adopts a 2m 3 airlift anaerobic fermentation tank, a guide cylinder is arranged in the fermentation tank, 4 vortex bubble generators are arranged at the bottom of the fermentation tank, 6 metal ultrafiltration membrane components are uniformly distributed in the guide cylinder, the average pore diameter is 50nm, the bottom is a blind end, the blind end is fixed on the guide cylinder of the fermentation tank through a grid, the upper parts are respectively connected with a pipeline, and the blind end is communicated with a product storage tank and a gas pipeline through respective three-way valves, as shown in figures 1 and 2.
The fermentation gas substrate adopts purified coke oven gas, and the main components of the gas are shown in table 1:
TABLE 1 Main Components of gas (%, v/v)
| CO | H2 | CO2 | CH4 | Others (N 2, etc) | Totals to |
| 4％ | 60％ | 2.5％ | 24％ | 9.5％ | 100％ |
The coke oven gas was supplemented with a gas of carbon source CO 2, thoroughly mixed in a gas tank so that the molar ratio of H 2 to CO 2 was about 2.5, and then the mixture was pressurized to 0.3MPa with a gas temperature of 55 ℃. 10Nm 3/h of gas substrate is introduced into an airlift fermentation tank inoculated with Mulberry bacteria, the pressure of the fermentation tank is kept at 0.3MPa, the temperature is 55 ℃, the pH is 6.4, and the gas at the outlet of the fermentation tank is circulated, wherein the circulation ratio is 2. Meanwhile, 6 membrane modules are also communicated with a gas pipeline, and gas is blown into the fermentation tank.
In the gas introducing process, the number of fermentation thalli is continuously increased, metabolic acetic acid products are produced simultaneously, the pH value is maintained to be 6.4 by supplementing ammonia water, after the fermentation is carried out for 72 hours, 5 of 6 membrane modules are switched to a liquid outlet mode after the concentration of ammonium acetate reaches 5.5wt%, a three-way valve is adjusted to a discharging storage tank, filtering power is produced through the internal and external pressure difference of the fermentation tank, cross flow scouring is produced on the membrane modules by gas-liquid circulation flow in the fermentation tank, the ammonium acetate solution is filtered out continuously by the membrane modules, and the liquid outlet rate is about 100L/h.
During the continuous fermentation process, back flushing of the membrane module is required. And (3) switching liquid outlet and ventilation modes of 6 membrane modules alternately every 4 hours, namely back flushing the membrane modules by coal gas, and recovering the membrane flux by breaking and falling filter cakes attached to the membrane surfaces in the filtering process. Through experiments, the flux of the membrane component subjected to gas back flushing can be recovered to more than 80% of the initial flux in long-time continuous fermentation.
The bioreactor of the invention realizes in-situ fermentation product separation through continuous operation, and the stable discharge concentration is about 5.5wt% of ammonium acetate feed liquid, and anaerobic fermentation strains are not in the filtrate feed liquid. The reactor reduces pumps and complex pipelines of an external membrane filtration system, is easy to sterilize integrally, and reduces the risk of infection of mixed bacteria.
Claims (13)
1. A fermentation method, characterized in that fermentation equipment is used for fermentation, wherein the fermentation equipment comprises a gas buffer tank, a gas compressor, a gas cooler, a circulating fan, a seed tank, a pH adjusting tank, a feeding tank, a product storage tank, a metering pump and a bioreactor; the bioreactor comprises a fermentation tank, a membrane component, a bubble generator and a guide cylinder, wherein the guide cylinder is positioned in the fermentation tank, the membrane component is positioned in the guide cylinder, the membrane component comprises a membrane, a connecting pipe fitting and a fixed end socket, and the membrane is a hollow fiber ultrafiltration membrane or a microfiltration membrane; the average pore diameter of the membrane is in the range of 4-100 nm; the diameter of the membrane is in the range of 2-10 cm; the height of the membrane is 1/6-2/3 of the height of the fermentation tank; the membrane component is below the liquid level of the fermentation liquid; one end of the membrane is a blind end, and the fixed end socket is used for sealing; the other end of the membrane is fixedly provided with a connecting pipe fitting for communicating the membrane with an external pipeline; the connecting pipe fitting is detachably connected with the membrane; the membrane component comprises 2-20 membranes which are connected in parallel and are uniformly distributed in the guide cylinder; fixing each film at symmetrical positions by a fixing piece; the bubble generator is arranged in the fermentation tank and is positioned at the bottom of the fermentation tank; the fermentation method comprises the following steps:
The purified coke oven gas and carbon dioxide are mixed in a proper proportion, then enter a gas buffer tank, are compressed to a proper pressure by a gas compressor, then enter a gas cooler to be cooled to a proper temperature, and are respectively provided for a seed tank and a fermentation tank to be used as a fermentation substrate of seed liquid in the seed tank and a fermentation substrate of microorganisms in the fermentation tank; gas is supplied to the fermenter of the bioreactor through the bottom of the bioreactor and into the membrane module via the three-way valve; the seed liquid in the seed tank is provided for the fermentation tank after being metered by a metering pump, and the gas generated by fermentation in the seed tank is circulated by a circulating fan, is mixed with the gas provided by the gas cooler and is provided for the seed tank and the bioreactor again; after fermenting for a certain time under proper conditions, the gas in the bioreactor is discharged from the top of the fermentation tank, circulated by a circulating fan, mixed with the gas provided by the gas cooler and/or the gas discharged from the seed tank and provided for the seed tank and the bioreactor again; providing a suitable pH adjustor to the fermentation tank through the pH adjustment tank to adjust the pH of the fermentation broth, if desired; supplementing fermentation liquor to the fermentation tank through a material supplementing tank; in the fermentation process, all the membrane components are connected to a gas pipeline by switching a three-way valve and are used for providing gas for a fermentation tank; along with the gradual progress of fermentation, part of the membranes in the membrane assembly are switched into a liquid outlet mode, a three-way valve is regulated, gas supply to the membranes is stopped, the membranes are communicated with a product storage tank, filtration power is generated through the pressure difference between the inside and the outside of the fermentation tank, cross flow scouring is generated on the membrane assembly by the gas-liquid circulation flow in the fermentation tank, and the membranes continuously filter out fermentation products; in the continuous fermentation process, back flushing of the membrane assembly is required; every 4-6 hours, each membrane in the membrane assembly is alternately switched into a liquid outlet mode and a ventilation mode, and the membrane assembly is backwashed by coal gas, so that filter cakes attached to the membrane surface in the filtering process are broken and fall off, and the membrane flux is recovered.
2. The method according to claim 1, wherein the purified coke oven gas contains, in volume percent (v/v), 20 to 30% CH 4, 55 to 65% H 2, 1 to 5% CO 2, 2 to 6% CO,7 to 10% other components; the other components include N 2.
3. The method according to claim 2, wherein the purified coke oven gas contains 22 to 26% by volume of CH 4, 58 to 63% by volume of H 2, 2 to 4% by volume of CO 2, 3 to 5% by volume of CO, and 8 to 10% by volume of other components.
4. A method according to claim 3, characterized in that CO 2,CO2 is fed to the cleaned coke oven gas in such a quantity that the molar ratio of H 2 to CO 2 in the gas obtained is between 1.0 and 5.0: 1.
5. The method of claim 4, wherein CO 2 is fed in such an amount that the molar ratio of H 2 to CO 2 in the resulting gas is between 1.5 and 4.5: 1.
6. The method of claim 4, wherein CO 2 is fed in such an amount that the molar ratio of H 2 to CO 2 in the resulting gas is between 1.5 and 4.0: 1.
7. The method of claim 4, wherein CO 2 is fed in such an amount that the molar ratio of H 2 to CO 2 in the resulting gas is between 1.5 and 3.5: 1.
8. The method of claim 4, wherein CO 2 is fed in such an amount that the molar ratio of H 2 to CO 2 in the resulting gas is between 1.5 and 3.0: 1.
9. The method of claim 4, wherein CO 2 is fed in such an amount that the molar ratio of H 2 to CO 2 in the resulting gas is in the range of 2.0 to 3.5: 1.
10. The method of claim 4, wherein CO 2 is fed in such an amount that the molar ratio of H 2 to CO 2 in the resulting gas is between 2.0 and 3.0: 1.
11. The method according to claim 2, characterized in that the coke oven gas used for fermentation contains, in volume percent, 16-23% CH 4, 44-51% H 2, 18-30% CO 2, 2.5-4.0% CO, 4.5-6.5% N 2 and the balance impurities.
12. The method according to claim 11, wherein the coke oven gas used for the fermentation contains, in volume percent, 18 to 20% CH 4, 45 to 49% H 2, 20 to 27% CO 2, 2.8 to 3.6% CO, 5.0 to 6.0% N 2 and the balance impurities.
13. The method of claim 2, wherein the method has one or more of the following features:
(1) Introducing coke oven gas serving as a fermentation substrate through the membrane component, and filtering out cell metabolites with an inhibition effect on cell growth through the membrane component; when the concentration of the cell metabolite with the inhibition effect on the cell growth in the fermentation tank reaches 1% or more, stopping the feeding of the coke oven gas through the membrane component, and filtering out the cell metabolite with the inhibition effect on the cell growth by the membrane component; wherein the cellular metabolites that inhibit cell growth include: formic acid, acetic acid, propionic acid, butyric acid, isobutyric acid, succinic acid, lactic acid, pyruvic acid, malic acid, citric acid, benzoic acid, vanillic acid, caproic acid, valeric acid, or a combination of two or more thereof;
(2) The fermentation is continuous fermentation;
(3) The pressure in the fermentation tank is in the range of 0-2 MPa;
(4) The gas at the outlet of the fermentation tank is circulated, and the circulation ratio is 2-10;
(5) The fermenting microorganism is selected from the group consisting of: clostridium, murella, fireball, eubacterium, desulphurized bacillus, carbothermus, acetobacter, anaerobism acetobacter, butyrate, streptococcus and laus;
(6) The pH value of the fermentation culture solution is 6.0-8.0; and
(7) The fermentation temperature is 25-75 ℃.
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