WO2009096062A1 - バイオマスの水熱分解装置及び方法 - Google Patents
バイオマスの水熱分解装置及び方法 Download PDFInfo
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- WO2009096062A1 WO2009096062A1 PCT/JP2008/067040 JP2008067040W WO2009096062A1 WO 2009096062 A1 WO2009096062 A1 WO 2009096062A1 JP 2008067040 W JP2008067040 W JP 2008067040W WO 2009096062 A1 WO2009096062 A1 WO 2009096062A1
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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
- C12P7/08—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
- C12P7/10—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate substrate containing cellulosic material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/0215—Solid material in other stationary receptacles
- B01D11/0223—Moving bed of solid material
- B01D11/0226—Moving bed of solid material with the general transport direction of the solids parallel to the rotation axis of the conveyor, e.g. worm
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/0288—Applications, solvents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
- C08B37/00—Preparation of polysaccharides not provided for in groups C08B1/00 - C08B35/00; Derivatives thereof
- C08B37/0006—Homoglycans, i.e. polysaccharides having a main chain consisting of one single sugar, e.g. colominic acid
- C08B37/0057—Homoglycans, i.e. polysaccharides having a main chain consisting of one single sugar, e.g. colominic acid beta-D-Xylans, i.e. xylosaccharide, e.g. arabinoxylan, arabinofuronan, pentosans; (beta-1,3)(beta-1,4)-D-Xylans, e.g. rhodymenans; Hemicellulose; Derivatives thereof
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08H—DERIVATIVES OF NATURAL MACROMOLECULAR COMPOUNDS
- C08H6/00—Macromolecular compounds derived from lignin, e.g. tannins, humic acids
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08H—DERIVATIVES OF NATURAL MACROMOLECULAR COMPOUNDS
- C08H8/00—Macromolecular compounds derived from lignocellulosic materials
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
- C10G1/047—Hot water or cold water extraction processes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L5/00—Solid fuels
- C10L5/40—Solid fuels essentially based on materials of non-mineral origin
- C10L5/44—Solid fuels essentially based on materials of non-mineral origin on vegetable substances
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L9/00—Treating solid fuels to improve their combustion
- C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
- C10L9/086—Hydrothermal carbonization
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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
- 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
- C12M45/00—Means for pre-treatment of biological substances
- C12M45/02—Means for pre-treatment of biological substances by mechanical forces; Stirring; Trituration; Comminuting
-
- 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
- C12M45/00—Means for pre-treatment of biological substances
- C12M45/20—Heating; Cooling
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D2011/002—Counter-current extraction
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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
-
- 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
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Definitions
- the present invention is a biomass hydrothermal decomposition apparatus and method capable of efficiently hydrothermally decomposing biomass raw materials, and efficiently producing organic raw materials such as alcohols, petroleum substitutes or amino acids using the same.
- the present invention relates to an organic raw material manufacturing system using a biomass raw material.
- Patent Document 1 Korean Patent Document 1
- chemical industrial raw material production for example, lactic acid fermentation etc.
- the biomass refers to the accumulation of organisms incorporated into the material circulation system of the earth biosphere or organic substances derived from the organisms (see JIS K 3600 1258).
- sugarcane, corn, and the like that are currently used as alcohol raw materials are originally provided for food, but making these edible resources a long-term, stable industrial use resource is an effective food product. From the viewpoint of life cycle, it is not preferable.
- Cellulose resources vary from 38 to 50% for cellulose, 23 to 32% for hemicellulose components, and 15 to 22% for lignin components that do not become fermentation raw materials.
- the raw materials are assumed to be fixed, and there is no disclosure of production system technology considering the versatility of raw materials.
- the resulting sugar solution is a 6-carbon sugar solution from cellulose and a 5-carbon sugar solution from the hemicellulose component.
- a suitable yeast is required for alcohol fermentation, and both a 6-carbon solution and a 5-carbon solution are mixed.
- the present invention performs a biomass hydrothermal decomposition apparatus and method capable of separating a cellulose-based component from a biomass raw material, an efficient sugar solution using the same, and the sugar
- An object of the present invention is to provide an organic raw material production system using a biomass raw material capable of efficiently producing various organic raw materials (for example, alcohols, petroleum substitutes, amino acids, etc.) based on the liquid.
- the first invention of the present invention for solving the above-described problem is that a biomass feed device that feeds biomass material from normal pressure to pressurized pressure, and a supplied biomass material are screwed into the inside of the device body from either one.
- pressurized hot water is supplied into the main body from the end side different from the biomass raw material supply location, hydrothermal decomposition is performed while the biomass raw material and the pressurized hot water are opposed to each other, and pressurized.
- a hydrothermal decomposition apparatus in which a lignin component and a hemicellulose component are transferred into hot water, and the lignin component and the hemicellulose component are separated from the biomass raw material.
- a biomass hydrothermal decomposition apparatus comprising a biomass extraction apparatus for extracting under pressure.
- the second invention is the biomass hydrothermal decomposition apparatus according to the first invention, wherein a scraper for preventing the hot water discharge liquid from being blocked is provided in the conveying screw.
- a third aspect of the invention is the biomass hydrothermal decomposition apparatus according to the first or second aspect, wherein the reaction temperature of the hydrothermal decomposition apparatus is 180 to 240 ° C. and is in a state of pressurized hot water. It is in.
- the weight ratio of the biomass raw material to be supplied and the pressurized hot water is 1: 1 to 1:10. Located in the pyrolysis unit.
- the pressurized hot water is supplied into the main body from the end side different from the location, and the biomass raw material and the pressurized hot water are hydrothermally decomposed while facing each other, the lignin component and the hemicellulose component in the pressurized hot water
- 6th invention is the pre-processing apparatus which pre-processes a biomass raw material, the hydrothermal decomposition apparatus in any one of 1st thru
- a first enzyme decomposing apparatus that is enzymatically decomposed into a sugar solution containing six carbon sugars, and a sugar solution obtained by the first enzyme decomposing apparatus, and then alcohols, petroleum substitutes or amino acids by fermentation treatment It is in the manufacturing system of the organic raw material using the biomass raw material characterized by comprising the fermentation apparatus which manufactures any one of the kind.
- a second enzyme decomposing apparatus for enzymatically decomposing the hemicellulose component in the hot water discharge liquid into a sugar liquid containing pentose, and the second enzymatic decomposition
- a fermentation apparatus for producing any one of alcohols, petroleum substitutes or amino acids by fermentation treatment using the sugar solution obtained in the apparatus, In the manufacturing system.
- a hydrothermal decomposition apparatus in which a biomass raw material conveyed by a screw means and pressurized hot water are brought into contact with each other, cellulose (which becomes a hexose solution by enzymatic saccharification) is obtained as a target component.
- cellulose which becomes a hexose solution by enzymatic saccharification
- a biomass solid content mainly composed of cellulose can be obtained.
- the components that are easily solubilized in hot water are discharged out of the reaction system in sequence by facing each other, and a temperature gradient is generated from the biomass charging section to the hot water charging section, thereby suppressing the excessive decomposition of the hemicellulose component.
- the pentose component can be efficiently recovered.
- FIG. 1 is a schematic diagram of a hydrothermal decomposition apparatus according to a first embodiment.
- FIG. 2 is a schematic diagram of another hydrothermal decomposition apparatus according to the first embodiment.
- FIG. 3 is a schematic diagram of another hydrothermal decomposition apparatus according to the first embodiment.
- FIG. 4 is a schematic diagram of another hydrothermal decomposition apparatus according to the first embodiment.
- FIG. 5 is a schematic diagram of an alcohol production system according to the second embodiment.
- FIG. 6 is a schematic diagram of an alcohol production system according to the third embodiment.
- FIG. 1 is a conceptual diagram illustrating a biomass hydrothermal decomposition apparatus according to a first embodiment.
- the biomass hydrothermal decomposition apparatus 41A includes a biomass supply device 31 that supplies the biomass raw material 11 from normal pressure to pressurized pressure, and a supplied biomass raw material (in this embodiment, For example, the straw 11 is gradually conveyed from the lower end side to the inside of the inclined apparatus main body (hereinafter referred to as “apparatus main body”) 42 by the conveying screw 43, and the upper end side is different from the supply location of the biomass raw material 11.
- apparatus main body inclined apparatus main body
- the pressurized hot water 15 is supplied to the inside of the apparatus main body 42, hydrothermally decomposed while the biomass raw material 11 and the pressurized hot water 15 are brought into contact with each other, and the lignin component and the hemicellulose component are transferred into the pressurized hot water 15.
- the hydrothermal decomposition apparatus 41A obtained by separating the lignin component and the hemicellulose component from the biomass raw material 11 and the biomass solids from the upper end side of the apparatus main body 42 7 is for and a biomass discharger 51 to withdraw the atmospheric pressure from the pressure.
- the biomass raw material 11 is supplied from the lower end side, but the present invention is not limited to this, and conversely, the biomass raw material 11 may be supplied from the upper end side.
- the pressurized hot water 15 is supplied from the lower end side.
- the biomass supply device 31 that supplies from the normal pressure to the pressurization include pump means such as a piston pump or a slurry pump.
- the hydrothermal decomposition apparatus 41A is an inclined apparatus as shown in FIG. 1, but the present invention is not limited to this, and the vertical water as shown in FIG. It is good also as the thermal decomposition apparatus 41B. Moreover, it is good also as a horizontal-type hydrothermal decomposition reaction apparatus.
- the inclined type or the vertical type is preferable because the gas generated in the hydrothermal decomposition reaction, the gas brought into the raw material, and the like can quickly escape from above. Moreover, since a decomposition product is extracted with the pressurized hot water 15, the concentration of the extract increases from the upper side to the lower side from the point of extraction efficiency, which is preferable.
- a scraper 43a that prevents the discharge hole 16a of the hot water discharge liquid 16 from being blocked may be provided in the conveying screw 43.
- the biomass supplied to the hydrothermal decomposition apparatus 41 is not particularly limited, and refers to the accumulation of organisms incorporated into the material circulation system of the earth biosphere or organic matter derived from organisms (JIS). K 3600 1258), however, in the present invention, it is particularly preferable to use woody lignocellulosic resources such as hardwood, herbaceous, agricultural waste, food waste and the like.
- the biomass raw material 11 is not particularly limited in particle size, but is preferably pulverized to 5 mm or less.
- the pretreatment device may be pretreated using, for example, a pulverizer. Moreover, you may make it wash
- the biomass raw material 11 is, for example, rice husk or the like, it can be supplied to the hydrothermal decomposition apparatus 41A as it is without being pulverized.
- the reaction temperature in the hydrothermal decomposition apparatus 41A is preferably in the range of 180 to 240 ° C. More preferably, the temperature is 200 to 230 ° C. This is because at a low temperature of less than 180 ° C., the hydrothermal decomposition rate is low, a long decomposition time is required, leading to an increase in the size of the apparatus, which is not preferable. On the other hand, when the temperature exceeds 240 ° C., the decomposition rate becomes excessive, and the cellulose component increases from the solid to the liquid side, and the excessive decomposition of the hemicellulose saccharide is promoted, which is not preferable.
- the hemicellulose component dissolves from about 140 ° C., the cellulose from about 230 ° C., and the lignin component from about 140 ° C., but the cellulose remains on the solid side, and the hemicellulose component and the lignin component have a sufficient decomposition rate. It should be in the range of 180 ° C to 240 ° C.
- reaction pressure is preferably set to a pressure higher by 0.1 to 0.5 MPa than the saturated vapor pressure of water at each temperature at which the inside of the main body is in a pressurized hot water state.
- the reaction time is preferably 20 minutes or less and 3 to 10 minutes. This is because if the reaction is carried out too long, the proportion of the overdecomposed product increases, which is not preferable.
- the flow of the pressurized hot water 15 and the biomass raw material 11 in the main body of the hydrothermal decomposition apparatus is contacted by a so-called counter flow in which the biomass raw material 11 and the pressurized hot water 15 are opposed to each other. It is preferable to stir and flow.
- the solid content of the biomass raw material 11 is supplied from the left side in the figure, while the pressurized hot water 15 is supplied from the right side in the figure, and the pressurized hot water 15 (The hot water and the liquid in which the decomposition products are dissolved) move while oozing between the solid raw material 11 and the counter flow between the solid particles.
- the solid-liquid ratio of the solid to the liquid is preferably as the liquid content is small because the amount of steam for heating for the recovered water and hydrothermal decomposition can be reduced.
- the weight ratio of the biomass material to be supplied and the pressurized hot water varies depending on the apparatus configuration, but is preferably 1: 1 to 1:10, and more preferably 1: 1 to 1: 5, for example.
- the biomass raw material 11 and water are mixed in advance and supplied to the apparatus main body, a considerably large amount of water is added to the solid in order to provide the fluidity of the slurry. (10 to 20 times by weight) must be added, but the biomass raw material 11 that is the raw material and the pressurized hot water 15 that removes the lignin component and hemicellulose component in the biomass are separated into a hydrothermal decomposition apparatus 41A. Therefore, the weight ratio of the liquid to the solid can be reduced, which contributes to improvement of the economic efficiency of the apparatus.
- pressurized nitrogen (N 2 ) is supplied to the inside.
- the temperature increase of the biomass raw material 11 in the hydrothermal decomposition apparatus can be performed by direct heat exchange by bringing it into contact with the pressurized hot water 15 in the apparatus main body 42. In addition, you may make it heat using water vapor
- the biomass supply apparatus 31 employs a screw-type extrusion mechanism 32 having a material seal mechanism by the biomass itself, and supplies the solid biomass raw material 11 from under normal pressure to under pressure. That is, by using the extrusion mechanism 32 including the screw feeder 32a and the hydraulic cylinder 32b, the biomass raw material 11 supplied to the inside is compressed to form the biomass plug 33, and the biomass plug 33 itself is used in the hydrothermal decomposition apparatus. A material seal that cuts off pressure is used. The biomass is gradually pushed out by the screw feeder 32a and gradually cut out from the tip of the hydraulic cylinder 32b, and the biomass raw material 11 is reliably supplied into the apparatus main body 42.
- the biomass extraction device 51 has the same configuration as the biomass supply device 31 and is configured as an extrusion mechanism composed of a screw feeder 52a and a hydraulic cylinder 52b, so that the biomass solids 17 reacted in the hydrothermal decomposition device 17 can be obtained. Is compressed to form a biomass plug 53, and the biomass plug 53 itself performs a material seal that cuts off the pressure in the hydrothermal decomposition apparatus. And the biomass solid content 17 which transferred the lignin component and the hemicellulose component to the hot water discharge liquid 16 can be discharged from under pressure to normal pressure. At this time, water remaining from the biomass plug 53 is dehydrated. Since the dehydrated liquid 54 contains a pressurized hot water soluble component (lignin component and hemicellulose component), the dehydrated liquid 54 is sent to the hot water discharge liquid 16 and separately processed together with the hot water discharge liquid 16.
- the dehydrated liquid 54 contains a pressurized hot water soluble component (lignin component and hemicellulose component)
- either one or both of the volatile enzyme saccharification inhibiting component and the ethanol fermentation inhibiting component which are reduced in molecular weight can be removed.
- the biomass raw material and the pressurized hot water are brought into contact with each other so that the components that are easily solubilized in the hot water are sequentially discharged, and the temperature gradient from the biomass charging section to the hot water charging section is increased. Therefore, the excessive decomposition of the hemicellulose component is suppressed, and as a result, the pentose component can be efficiently recovered. Furthermore, heat recovery can be achieved by making the opposite contact, which is preferable in terms of system efficiency.
- the surplus water removal line is provided so that the surplus water 34 contained in biomass may be removed in the part to which the biomass raw material 11 of the apparatus main body 42 is supplied. .
- This surplus water 34 may be used to make the biomass material 11 wet.
- FIG. 5 is a conceptual diagram which shows the manufacturing system of the organic raw material using the biomass raw material which concerns on an Example.
- the alcohol production system 10-1 using the biomass raw material according to the present embodiment pressurizes the pretreated apparatus 12 for pulverizing the biomass raw material 11, for example, and the pretreated biomass pulverized material 13
- Hydrothermal decomposition as shown in FIG. 1 is performed by hydrothermal decomposition while facing the hot water 15, transferring the lignin component and hemicellulose component into the pressurized hot water 15, and separating the lignin component and hemicellulose component from the biomass solid.
- the hydrothermal decomposition apparatus 41A as shown in FIG. 1 by adopting a counter flow, the lignin component and the hemicellulose component are transferred into the pressurized hot water 15 on the liquid side, and the biomass on the solid side Cellulose remains in the solid content 17, and the first sugar solution (6-carbon sugar) 20-1 is obtained by the first enzymatic decomposition apparatus 19-1 for enzymatic saccharification.
- a fermentation process according to hexose (fermentation according to the final product: in this embodiment, the ethanol 23 is obtained by fermentation using the first alcohol fermentation apparatus 21-1) can be constructed.
- ethanol as an alcohol was exemplified as what is obtained by fermentation treatment.
- the present invention is not limited to this, and petroleum substitutes or foods and feeds that are raw materials for chemical products other than alcohols.
- Amino acids as raw materials can be obtained by a fermentation apparatus.
- a chemical product based on a sugar solution for example, LPG, automatic fuel, jet fuel for aircraft, kerosene, diesel oil, various heavy oils, fuel gas, naphtha, naphtha decomposition product ethylene glycol, ethanolamine
- examples include alcohol ethoxylate, vinyl chloride polymer, alkylaluminum, PVA, vinyl acetate emulsion, polystyrene, polyethylene, polypropylene, polycarbonate, MMA resin, nylon, and polyester. Therefore, the sugar solution derived from biomass can be efficiently used as a substitute for a chemical product derived from crude oil, which is a depleted fuel, and as a raw material for producing the substitute.
- FIG. 6 is a conceptual diagram showing an organic raw material alcohol production system using a biomass raw material according to the present embodiment.
- the alcohol production system 10-2 using the biomass raw material according to this embodiment is configured to discharge hot water discharged from the hydrothermal decomposition apparatus 41A in the alcohol production system 10-1 shown in FIG.
- a second enzyme decomposing apparatus 19-2 is provided for enzymatically decomposing the hemicellulose component transferred into the liquid 16 into a second sugar liquid 20-2 containing pentose.
- the enzyme decomposing apparatus, the alcohol fermentation apparatus, and the refining apparatus are separately provided in two units (the first enzyme decomposing apparatus 19-1, the second enzyme decomposing apparatus 19-2, the first alcohol fermenting apparatus 21-1, and the first decomposing apparatus). 2 alcohol fermentation apparatus 21-2, first purification apparatus 25-1, and second purification apparatus 25-2). Then, an ethanol degradation process, an alcohol fermentation process and a purification process corresponding to the first sugar liquid (hexose sugar) 20-1 and the second sugar liquid (pentose sugar) 20-2 are performed, and ethanol 23 Like to get.
- ethanol 23 can be produced by fermentation using the second sugar solution (pentose) 20-2 obtained by the second enzymatic decomposition apparatus 19-2.
- the hot water discharge liquid is not necessarily processed in a separate system.
- the subsequent steps of the enzymatic decomposition apparatus are shared, the processes after the alcohol fermentation apparatus are shared, or the purification apparatus is shared. Changes can be made as appropriate.
- cellulose remains in the solid biomass solids 17 and the first enzymatic decomposition apparatus 19-1 for enzymatic saccharification changes the first.
- 1 sugar liquid (6-carbon sugar) 20-1 is obtained, and in the pressurized hot water 15 on the liquid side, the hemicellulose component soluble in the pressurized hot water is separated as the hot water discharge liquid 16, which is separately enzymatically saccharified.
- the second sugar solution (5-carbon sugar) 20-2 is obtained by the second enzymatic decomposition device 19-2, both can be efficiently separated and saccharified.
- the fermentation Fermentation according to the final product: example: ethanol fermentation
- process according to hexose and pentose can be constructed.
- the side reaction component that becomes an inhibitor in the enzymatic saccharification reaction to obtain hexose and the lignin component that is soluble in pressurized hot water are used as the pressurized hot water 15. Therefore, the biomass solid content 17 mainly composed of cellulose is obtained, and the saccharification reaction yield of hexose in the subsequent saccharification reaction is improved.
- the hemicellulose component contained in the separated hot water discharge liquid 16 is then saccharified in the second enzymatic decomposition apparatus 19-2 to obtain a sugar liquid containing pentose.
- yeast suitable for each of hexose and pentose ethanol can be obtained efficiently and individually by fermentation.
- the side reaction product causes the enzyme saccharification inhibition and the sugar yield is reduced.
- the cellulose-based component and the hemicellulose component from the biomass material are used. Is converted into pressurized hot water to separate the two, and an efficient sugar solution (6-carbon sugar solution, 5-carbon sugar solution) suitable for each is manufactured, and various organic raw materials are used based on the sugar solution. It is possible to provide an organic raw material production system and method using a biomass raw material that can efficiently produce (for example, alcohols, petroleum substitutes, amino acids, etc.).
- a cellulose-based component is separated from a biomass raw material by a hydrothermal decomposition apparatus to efficiently produce a sugar solution, and various organic (for example, Alcohols, petroleum substitutes, amino acids, etc.) can be efficiently produced.
- various organic for example, Alcohols, petroleum substitutes, amino acids, etc.
Abstract
Description
また、糖を出発原料として、化学工業原料生産(例えば乳酸発酵等)も考えられる。
ここで、バイオマスとは、地球生物圏の物質循環系に組み込まれた生物体又は生物体から派生する有機物の集積をいう(JIS K 3600 1258参照)。
12 前処理装置
13 バイオマス粉砕物
15 加圧熱水
16 熱水排出液
17 バイオマス固形分
18 酵素
19 酵素分解装置
19-1 第1の酵素分解装置
19-2 第2の酵素分解装置
20-1 第1の糖液(6炭糖)
20-2 第2の糖液(5炭糖)
23 エタノール
41A~41D 水熱分解装置
図1は、実施例1に係るバイオマスの水熱分解装置を示す概念図である。
図1に示すように、本実施例に係るバイオマスの水熱分解装置41Aは、バイオマス原料11を常圧下から加圧下に供給するバイオマス供給装置31と、供給されたバイオマス原料(本実施例では、例えば麦わら等)11を、下端部側から傾斜型装置本体(以下「装置本体」という)42の内部に搬送スクリュー43により徐々に搬送すると共に、前記バイオマス原料11の供給箇所とは異なる上端部側から加圧熱水15を装置本体42内部に供給し、バイオマス原料11と加圧熱水15とを対向接触させつつ水熱分解し、加圧熱水15中にリグニン成分及びヘミセルロース成分を移行し、バイオマス原料11中からリグニン成分及びヘミセルロース成分を分離してなる水熱分解装置41Aと、装置本体42の上端部側からバイオマス固形分17を加圧下から常圧下に抜出すバイオマス抜出装置51とを具備するものである。
前記常圧下から加圧下に供給するバイオマス供給装置31としては、例えばピストンポンプ又はスラリーポンプ等のポンプ手段を挙げることができる。
K 3600 1258参照)が、本発明では特に木質系の例えば広葉樹、草本系等のリグノセルロース資源や農業系廃棄物、食品廃棄物等を用いるのが好ましい。
本実施例では、バイオマスの供給前において、前処理装置として、例えば粉砕装置を用いて前処理するようにしてもよい。また、洗浄装置により洗浄するようにしてもよい。
なお、バイオマス原料11として、例えば籾殻等の場合には、粉砕処理することなく、そのまま水熱分解装置41Aに供給することができるものとなる。
これは、180℃未満の低温では、水熱分解速度が小さく、長い分解時間が必要となり、装置の大型化につながり、好ましくないからである。一方240℃を超える温度では、分解速度が過大となり、セルロース成分が固体から液体側へ移行を増大すると共に、ヘミセルロース系糖類の過分解が促進され、好ましくないからである。
また、ヘミセルロース成分は約140℃付近から、セルロースは約230℃付近から、リグニン成分は140℃付近から溶解するが、セルロースを固形分側に残し、且つヘミセルロース成分及びリグニン成分が十分な分解速度を持つ180℃~240℃の範囲とするのがよい。
また、反応時間は20分以下、3分~10分とするのが好ましい。これはあまり長く反応を行うと過分解物の割合が増大し、好ましくないからである。
ここで、供給するバイオマス原料と加圧熱水との重量比は、装置構成により適宜異なるが、例えば1:1~1:10、より好ましくは1:1~1:5とするのが好ましい。
すなわち、スクリューフィーダー32aと油圧シリンダー32bとからなる押出機構32とすることで、内部に供給されたバイオマス原料11が圧縮され、バイオマスプラグ33を形成し、このバイオマスプラグ33自身で水熱分解装置内圧力を遮断するマテリアルシールを行うようにしている。スクリューフィーダー32aにより徐々に押されて、油圧シリンダー32bの先端部分から徐々にバイオマスが切り出され、装置本体42内部に確実にバイオマス原料11を供給することとなる。
この脱水液54は、加圧熱水可溶分(リグニン成分及びヘミセルロース成分)を含むものであるので、熱水排出液16に送られ、熱水排出液16と共に別途処理される。
さらに、対向接触させることで、熱回収ができシステム効率から好ましいものとなる。
また、理想的なカウンターフローの実現が可能となる。
図5に示すように、本実施例に係るバイオマス原料を用いたアルコールの製造システム10-1は、バイオマス原料11を例えば粉砕処理する前処理装置12と、前処理したバイオマス粉砕物13を加圧熱水15と対向接触させつつ水熱分解し、加圧熱水15中にリグニン成分及びヘミセルロース成分を移行し、バイオマス固体中からリグニン成分及びヘミセルロース成分を分離してなる図1に示す水熱分解装置41Aと、前記水熱分解装置41Aから排出されるバイオマス固形分17中のセルロースを酵素処理して6炭糖を含む糖液に酵素(セルラーゼ)18-1で酵素分解する第1の酵素分解装置19-1と、第1の酵素分解装置19-1で得られた第1の糖液(6炭糖)20-1を用いて、発酵処理によりアルコール類(本実施の形態ではエタノール)を製造する第1のアルコール発酵装置21-1と、第1のアルコール発酵液22-1を精製して目的生成物のエタノール23と残渣24-1とに分離処理する第1の精製装置25-1とを具備するものである。
そして、6炭糖に応じた発酵(最終製品に応じた発酵:本実施例では第1のアルコール発酵装置21-1を用いてエタノール23を発酵により求める)プロセスを構築することができる。
図6は、本実施例に係るバイオマス原料を用いた有機原料のアルコール製造システムを示す概念図である。
図6に示すように、本実施例に係るバイオマス原料を用いたアルコールの製造システム10-2は、図5に示すアルコール製造システム10-1において、水熱分解装置41Aから排出される熱水排出液16中に移行されたヘミセルロース成分を酵素処理して5炭糖を含む第2の糖液20-2に酵素分解する第2の酵素分解装置19-2を設けてなるものである。
なお、酵素分解装置、アルコール発酵装置、精製装置は、それぞれ別途2機(第1の酵素分解装置19-1、第2の酵素分解装置19-2、第1のアルコール発酵装置21-1、第2のアルコール発酵装置21-2、第1の精製装置25-1、第2の精製装置25-2)設置している。そして、第1の糖液(6炭糖)20-1、第2の糖液(5炭糖)20-2に応じた酵素分解工程、アルコール発酵工程及び精製工程を行うようにして、エタノール23を得るようにしている。
そして、6炭糖、5炭糖の各々に適した酵母等を用いることでエタノールを効率的に個別に発酵により求めることができるものとなる。
Claims (7)
- バイオマス原料を常圧下から加圧下に供給するバイオマス供給装置と、
供給されたバイオマス原料を、いずれか一方から装置本体の内部にスクリュー手段により搬送すると共に、前記バイオマス原料の供給箇所とは異なる端部側から加圧熱水を本体内部に供給し、バイオマス原料と加圧熱水とを対向接触させつつ水熱分解し、加圧熱水中にリグニン成分及びヘミセルロース成分を移行し、前記バイオマス原料中からリグニン成分及びヘミセルロース成分を分離してなる水熱分解装置と、
前記装置本体の上端部側からバイオマス固形分を加圧下から常圧下に抜出すバイオマス抜出装置とを具備することを特徴とするバイオマスの水熱分解装置。 - 請求項1において、
前記搬送スクリューに熱水排出液の抜出し孔の閉塞を防止するスクレーパーを設けたことを特徴とするバイオマスの水熱分解装置。 - 請求項1又は2において、
前記水熱分解装置の反応温度が180~240℃であると共に、加圧熱水の状態であることを特徴とするバイオマスの水熱分解装置。 - 請求項1乃至3のいずれか一つにおいて、
供給するバイオマス原料と加圧熱水との重量比は、1:1~1:10であることを特徴とするバイオマスの水熱分解装置。 - バイオマス原料を常圧下から加圧下に供給するバイオマス供給工程と、
供給されたバイオマス原料を、いずれか一方から装置本体の内部にスクリュー手段により搬送すると共に、前記バイオマス原料の供給箇所とは異なる端部側から加圧熱水を本体内部に供給し、前記バイオマス原料と加圧熱水とを対向接触させつつ水熱分解し、前記加圧熱水中にリグニン成分及びヘミセルロース成分を移行し、前記バイオマス原料中からリグニン成分及びヘミセルロース成分を分離してなる水熱分解工程と、
前記装置本体の上端部側からバイオマス固形分を加圧下から常圧下に抜出すバイオマス抜出工程とを具備することを特徴とするバイオマスの水熱分解方法。 - バイオマス原料を前処理する前処理装置と、
請求項1乃至4のいずれか一つの水熱分解装置と、
前記水熱分解装置から排出される前記バイオマス固形分中のセルロースを酵素処理して6炭糖を含む糖液に酵素分解する第1の酵素分解装置と、
該第1の酵素分解装置で得られた糖液を用いて、発酵処理によりアルコール類、石油代替品類又はアミノ酸類のいずれか一つを製造する発酵装置とを具備することを特徴とするバイオマス原料を用いた有機原料の製造システム。 - 請求項6において、
熱水排出液中のヘミセルロース成分を酵素処理して5炭糖を含む糖液に酵素分解する第2の酵素分解装置と、
該第2の酵素分解装置で得られた糖液を用いて、発酵処理によりアルコール類、石油代替品類又はアミノ酸類のいずれか一つを製造する発酵装置とを具備することを特徴とするバイオマス原料を用いた有機原料の製造システム。
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