WO2004016718A1 - バイオマスの改質方法、改質バイオマス、バイオマス水スラリーとその製造方法、改質バイオマスガスおよびバイオマスのガス化方法 - Google Patents
バイオマスの改質方法、改質バイオマス、バイオマス水スラリーとその製造方法、改質バイオマスガスおよびバイオマスのガス化方法 Download PDFInfo
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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
- C10L1/00—Liquid carbonaceous fuels
- C10L1/32—Liquid carbonaceous fuels consisting of coal-oil suspensions or aqueous emulsions or oil emulsions
- C10L1/326—Coal-water suspensions
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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
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/08—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by treating with water
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
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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
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
- C10J2300/092—Wood, cellulose
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
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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
- C10L2250/00—Structural features of fuel components or fuel compositions, either in solid, liquid or gaseous state
- C10L2250/06—Particle, bubble or droplet size
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/04—Gasification
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/24—Mixing, stirring of fuel components
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/28—Cutting, disintegrating, shredding or grinding
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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
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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
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Definitions
- Biomass reforming method modified biomass, biomass water slurry and its production method, modified biomass gas and biomass gasification method
- the present invention relates to a method for reforming cellulosic biomass, a method for slurrying cellulosic biomass, and a method for gasifying modified biomass.
- a slurry made of powdered solid fuel such as coal and added with water and additives is known as CWM (Coal Water Mixture) and is attracting attention as a new fuel.
- Slurry fuel is required to be 1,50 OmPa.s or less (rotary viscometer, 25 ° C, shear rate 100 [lZ sec], the same applies hereinafter) due to its handling properties and the like. .
- rotary viscometer 25 ° C, shear rate 100 [lZ sec], the same applies hereinafter
- a calorific value of 16.5 MJ / kg (4, OO OkcalZkg) or more is required.
- Biomass such as wood, is a non-fossil renewable energy that is considered to have zero carbon dioxide emissions and has extremely low ash and sulfur content, which can reduce the cost of building combustion facilities.
- Thinning materials, wood processing, wood chips, street tree pruning materials, bagasse, rice straw, waste paper, etc. are discarded without much use, and they are being disposed of at a fee.
- Organic resources can be used effectively.
- the unused organic resources are solids of various shapes, and if they can be liquefied or slurried as in coal, the range of use is expected to greatly expand.
- a cellulose-based biomass which originally has an oxygen Z carbon atom ratio of 0.5 or more, is reformed so that the oxygen Z carbon atom ratio is reduced to 0.38 or less.
- Calorific value of the solid component of the solid reactant is 25.1M J / kg (6, OOO kca
- the biomass reforming method of the present invention comprises reforming a cellulose-based biomass having an oxygen-carbon atom ratio of 0.5 or more in the presence of water at a pressure equal to or higher than the saturated steam pressure, and reducing the oxygen-Z carbon atom ratio. And a separation step of separating the reformed reaction product obtained in the reforming step into a solid component and a liquid component.
- the modified biomass of the present invention is obtained by the above-mentioned reforming method. From the modified biomass of the present invention, a biomass water slurry having a high solid content and a sufficient calorific value as an alternative fuel for heavy oil or coal can be easily obtained.
- the modified biomass can be used as it is as a solid fuel similar to coal, and can also be used as a soil adsorbent
- the method for producing a biomass water slurry of the present invention comprises: a reforming step of performing a reforming treatment on a cellulosic biomass raw material in the presence of water at a pressure equal to or higher than a saturated steam pressure; and a reforming reaction product obtained in the reforming step.
- the pulverizing step and the kneading step may be performed simultaneously, or may be performed sequentially in the order described above.
- cellulosic biomass which has not been effectively used in the past, is used as a raw material, has a high solid content, has a sufficient calorific value as a heavy oil or coal alternative fuel, Even if stored for a long period of time, the slurry does not lose its properties, and a slurry having a viscosity that can be transported through a pipe can be stably obtained.
- the biomass water slurry of the present invention is a modified biomass obtained by reforming a cellulosic biomass raw material in the presence of water at a pressure higher than the saturated steam pressure and further pulverizing the raw material to an average particle size of 30 ⁇ m or less. 0 mass. /. It contains above.
- the biomass water slurry of the present invention has a high solid content, has a sufficient amount of heat as an alternative fuel to heavy oil and coal, and has a viscosity that enables pipe transportation. Even if this slurry is stored for a long period of time, the solid content and the liquid in the slurry do not separate and can be stored stably.
- the biomass water slurry of the present invention and the method for producing the same can be used for wood-based materials such as thinned wood, sawdust, chips, scrap wood, street tree pruned wood, wood-based building waste, bark, driftwood, etc., which have not been effectively used in the past.
- Biomass Biomass from grasses such as rice straw, straw, bagasse; bamboo, bamboo grass, burdock, etc .; Biomass from cellulose products such as waste paper can be used as a raw material. Therefore, resources can be used effectively, and non-fossil renewable energy, which is regarded as zero carbon dioxide emission, can be obtained, which is one of the effective measures against environmental problems such as increase of carbon dioxide gas. Extremely low ash and sulfur content Therefore, the construction cost of the combustion equipment can be reduced.
- the gasification method of the modified biomass according to the present invention is characterized in that the modified biomass is gasified in the presence of a gasifying agent containing 25 to 40% of oxygen required for complete combustion and a required amount of steam. Gasification is performed at a gasification temperature of 800 to 130 ° C and a gasification pressure of 0.1 to 1 OMPa or more.
- the reformed biomass gas of the present invention is a gas obtained by the gasification method and mainly containing hydrogen and carbon monoxide.
- oxygen and steam are used as gasifying agents, and gasification is performed by partial oxidation, with the supply amount of oxygen being about 1/4 to 1Z2.5 of the amount required for complete combustion.
- the gasification method of this invention compared with the case where raw biomass is directly gasified, the oxygen supply amount at the time of direct oxidation can be reduced, and cold gas efficiency can be improved. Furthermore, the concentration of the active components H 2 and C ⁇ in the obtained gasification product can be increased.
- Examples of the cellulosic biomass raw material that can be used in the present invention include wood-based biomass such as thinned wood, sawdust, chips, scrap wood, etc., pruning materials for street trees, waste wood, bark, driftwood, etc .; rice straw, straw And biomass from grasses such as bagasse; bamboo, bamboo grass, burdock; biomass from cellulose products such as waste paper. Furthermore, sludge, livestock, agricultural waste, and municipal waste can also be used as long as they contain cellulose as a raw material. Among cellulosic biomass, woody biomass is particularly preferred.
- the cellulosic biomass raw material is preferably crushed in advance to, for example, 5 Omm or less. It is more preferably 5 mm or less, and further preferably 1 mm or less.
- the method of crushing and introducing into the reforming step after crushing, it can be further slurryed with an aqueous medium such as water and introduced into the reforming step.
- an aqueous medium such as water
- there is no limitation on the means of introducing the biomass raw material into the reforming process and it is possible to directly introduce the raw material into the reforming process without slurrying.
- the reforming step is for reducing the oxygen content of the cellulosic biomass raw material and improving the calorific value as a fuel, and in the presence of water at a pressure equal to or higher than the saturated steam pressure for a predetermined time.
- the reforming process is performed by keeping the temperature within a predetermined temperature range.
- the processing temperature in the reforming step is not limited, it is preferably from 250 to 380C, more preferably from 270 to 350C.
- the treatment pressure is not limited, but is preferably 0.5 to 5 MPa higher than the saturated vapor pressure of water, more preferably 1 to 3 MPa higher.
- the treatment time is not limited, it is preferably 5 minutes to 120 minutes, and more preferably 10 minutes to 60 minutes.
- the processing time is related to the processing temperature. The higher the processing temperature, the shorter the processing time, and the lower the processing temperature, the longer the processing time.
- the reforming step may be a batch process using an autoclave or the like, or may be a continuous reaction apparatus including one or two or more reaction zones. In the reforming step, in order to maintain the above-mentioned temperature range, it is necessary that the apparatus be maintained in pressurized hot water, and that a pressure-reducing system be used for cooling and returning to normal pressure.
- the reforming reaction product obtained in the reforming step is separated into a solid component and a liquid component in the separation step.
- a drying treatment may be performed as necessary.
- the solid component is dehydrated so as to have a solid content concentration of 50% by mass or more, preferably 70% by mass or more.
- the separated liquid component may be reused as water used in the reforming step. Separation of the solid component and the liquid component in the separation process is performed by using a device such as a leaf filter, a filter press, a squeezing machine, a centrifugal filter, a centrifugal separator, etc., which is usually used for separation. Is also good. Separation may be performed at a high temperature as long as it can be handled, or at room temperature. If the dehydration rate is insufficient, dry to the required solid content concentration by heating and drying.
- the solid component from which the liquid component has been removed in the separation step and which has been dehydrated to a predetermined solid content concentration is then pulverized by a pulverizing means so that the average particle size becomes 3 ⁇ or less.
- Ball mills, rod minoles, hammer mills, disk grinding mills, fluids An energy mill or the like, or a combination of two or more of these can be used.
- the pulverization may be either dry pulverization or wet pulverization, but wet pulverization is desirable from the viewpoint of energy efficiency.
- the average particle size of the pulverized solid component obtained in the above separation step must be 30 ⁇ or less, but 20 ⁇ or less. Is preferably 15 ⁇ or less, more preferably 15 ⁇ or less.
- the average particle size refers to a value obtained by measurement with a microtrack (FSA type, manufactured by Nikkiso Co., Ltd.).
- a pulverized product having an average particle diameter of 3 ⁇ or less When a pulverized product having an average particle diameter of 3 ⁇ or less is obtained by the first-stage pulverization treatment, it may be sent to the kneading step as it is. If the average particle size does not become 3 ⁇ or less by one-stage pulverization, the particles may be further pulverized so that the average particle size becomes 3 ⁇ or less. Re-grinding may be carried out by a closed system in which sieving is performed at a constant particle size, particles under the sieve are sent to a kneading process, and coarse particles on the sieve are crushed.
- an additive and, if necessary, water are added to the pulverized solid component and kneaded to obtain a biomass water slurry.
- an additive an anionic, cationic, nonionic surfactant or the like is used alone or in combination. Additives are appropriately selected according to the properties of the ground solid.
- anionic surfactants include alkyl sulfates, higher alcohol sulfates, nonionic ether sulfates, olefin sulfates, polyoxyethylene alkynole (alkylphenol) sulfates, esterolenates, and alkylaryl sulfonates.
- Basic acid ester sulfonates, alkylbenzenesulfonates, alkylnaphthalenesulfonates, dialkylsulfosuccinates, alkylphosphate esters, and acylsarcosinates can be used.
- an alkylamine salt As the cationic surfactant, an alkylamine salt, a quaternary amine salt, an alkylpyridinium sulfate and the like can be used.
- Nonionic surfactants include polyoxyalkyl ethers, polyoxyethylene olenoquinolenophenol ethers, oxyethylene / oxypropylene block polymers, polyoxyethylene alkylamines, sorbitan fatty acid esters, polyoxyethylene sorbitan fatty acid esters, and alkyltrimethyl.
- Ammonii Muchloride, alkyldimethylbenzylammonium chloride, polyoxyethylene fatty acid ester, aliphatic alcohol polyoxyethylene ether, polyhydric alcohol fatty acid ester, fatty acid ethanolamide and the like are used.
- Alkyl betaine and the like are used as the amphoteric surfactant.
- the net addition amount of the additive is preferably 1.0% by mass or less, more preferably 0.1% by mass or less, based on the milled solid component.
- the additive When water is added together with the additive, the additive may be added to water so that the additive has a predetermined concentration, and the resulting mixture may be kneaded with a solid component.
- water, a solid component, and an additive may be mixed and kneaded at the same time.
- the kneader any type can be used, but a type having strong stirring power is more preferable.
- the solid content may be pulverized in the pulverizing step, and the pulverized solid material may be put into the kneading step.
- the pulverizing step and the kneading step may be performed simultaneously by one fi. I'm sorry.
- the solid content concentration is preferably 50% by mass or more. Preferably, it is 55% by mass or more, more preferably 60% by mass or more.
- the biomass water slurry should have a low viscosity, that is, 1,500 OmPa-s or less, and 1,000 mPa-s or less in order to enable pipe transportation. More preferably, there is.
- a modified powdered biomass having a higher solid content than the desired biomass water slurry is used, and the additive-containing water or the additive and water are gradually mixed while kneading the modified ground biomass. It is preferable to add the water little by little and stop the addition of water when the viscosity sharply decreases, since the modified biomass will not be excessively diluted with water.
- the biomass water slurry obtained as described above has a high solid content, has a sufficient amount of heat as an alternative fuel to heavy oil or coal, and has a viscosity that allows pipe transport. In addition, even if this slurry is stored for a long time, it can be stored stably without the separation of the solid content and the liquid in the slurry occurring to a degree that causes operational problems.
- This biomass water slurry is a woody biomass that has not been effectively used in the past, such as thinned wood, sawdust, chips, scrap wood, and other wood-processing wood chips, street tree pruning materials, wood-based building waste, bark, driftwood, and the like; rice.
- the biomass water slurry has extremely low ash and sulfur contents, and therefore, the construction cost of fuel production facilities can be reduced.
- any of the above-mentioned biomass raw materials having an oxygen / carbon atom ratio of 0.5 or more is used.
- cedar has an oxygen-Z carbon atom ratio of 0.620
- pine has 0.632
- acacia has 0.644
- bamboo has 0.693
- burdock has 0.949.
- the oxygen / carbon atomic ratio is a value obtained by mass spectrometry of a dried object, and although there is some variation, it is almost constant depending on the type of plant. By the way, coal varies depending on its type, but it ranges from 0.1 to 0.3.
- the cellulosic biomass raw material to be subjected to the reforming step is preferably crushed in advance in the same manner as described above, for example, to have a size of 50 mm or less, more preferably 5 mm or less, and further preferably 1 mra or less.
- the oxygen / carbon atomic ratio of the cellulosic biomass raw material is reduced to increase the calorific value as a fuel.
- the amount of water added to the cellulosic biomass feedstock depends on the amount of water originally contained in the cellulosic biomass feedstock. It is preferably added so as to be about 1 to 20 times by base), more preferably about 1 to 15 times.
- the processing temperature in the reforming step is preferably from 250 to 380 ° C, more preferably from 270 to 350 ° C.
- the operating pressure is preferably 0.5-5 MPa higher than the saturated vapor pressure of water, more preferably 1-3 MPa higher.
- the processing time in the reforming step is not particularly limited, but is preferably 5 minutes to 120 minutes, and more preferably 10 minutes to 60 minutes. If the processing temperature is high, the processing time can be short, and if the processing temperature is low, the processing time can be longer.
- the reforming step may be a batch process using an autoclave or the like, or may be a continuous reaction apparatus including one or more reaction zones. In the reforming step, it is necessary to maintain the above temperature range, and to maintain conditions of pressurized hot water in the apparatus, and to provide a pressure reduction system for cooling and returning to normal pressure.
- the reforming reaction product obtained in the reforming step is separated into a solid component and a liquid component in the separation step.
- the separation step of the present invention not only separates the solid component from the liquid component, but also includes drying such as heating and drying that is performed as necessary when the water content is high.
- a solid component is obtained as a cake of modified biomass.
- the cake preferably has a solid content of 50% by mass or more, more preferably 60% by mass or more.
- the liquid component separated in the separation step may be returned as water used in the reforming step.
- Separation of the solid component and the liquid component in the separation process is performed by using a device such as a leaf filter, a filter press, a squeezing machine, a centrifugal filter, a centrifugal separator, etc., which is usually used for separation. Is also good. This separation may be performed at a high temperature or at room temperature as long as it can be handled.
- the conditions such as the reforming temperature, pressure, and time are set so that the oxygen-Z carbon atom ratio of the obtained reforming reactant is 0.38 or less, preferably 0.3 or less. It is selected and implemented as appropriate.
- the lower limit of the oxygen-Z carbon atom ratio is about 0.1 in consideration of the energy efficiency given in the reforming step.
- the oxygen / carbon atomic ratio in biomass can be described as compared to charcoal production obtained by carbonizing wood.In charcoal, wood is steamed at 400 to 100 ° C at high temperatures. Pyrolyzed, carbon content 9 mass. / 0 or more, and the oxygen content is almost 0, but in the present invention, mild pyrolysis is performed in the presence of water at a lower temperature and higher pressure than the steaming, and partially deoxygenated. The oxygen Z carbon atom ratio is reduced to 0.38 or less by the treatment.
- the recovered weight of charcoal is about 10 to 25%, but the recovered weight of the reformed reaction product of the present invention is 40% or more, and the fuel recovery rate is high.
- the solid component of the reformed reaction product obtained in the separation step after the reforming treatment so that the oxygen / carbon atom ratio is 0.38 or less has a calorific value per unit weight of 27 MjZkg or more.
- such solid components have a high quality of heat generation per unit weight of 16.5 MjZkg or more (4, OOO kcal Zkg or more) even in the state of slurry in water as described later. It becomes fuel. That is, in this reforming method, the reformed product can be easily crushed, has good affinity for water, and can produce a modified biomass that can be a high-density water slurry fuel.
- This reformed biomass may directly burn solids other than slurry fuel, or may be mixed with existing fuels such as coal and burned in a boiler to be used as a high calorific value fuel.
- the volatile content in the modified biomass is preferably at least 50% by mass.
- the volatile content is a value measured according to JI SM8812, and the difference between the moisture and the water loss is determined by heating the sample at 900 ° C for 7 minutes without contact with air. It is the value subtracted. The higher the volatile content, the better the flammability.
- This modified biomass has a high solids concentration and can be transported by pipes, for example, by adding an additive thereto, and further adding water as needed, and then pulverizing or kneading, or pulverizing and kneading. It is possible to obtain a slurry having a viscosity as low as possible.
- the concentration of the solid content is, for example, 50% by mass or more, preferably 55% by mass or more, and more preferably 60% by mass or more.
- the above-mentioned anionic, cationic or nonionic surfactants are used alone or in combination, and are appropriately selected according to the properties of the obtained pulverized solid.
- the net component amount of the additive is preferably 1.0% by mass or less, more preferably 0.1% by mass or less based on the solid component.
- the mixture of water and the additive may be kneaded with the solid component as described above, or the water, the solid component, and the additive may be mixed and kneaded at the same time. Further, additives may be added at the time of pulverization.
- the average particle diameter thereof is 30 ⁇ m or less, more preferably 20 ⁇ or less, and 15 ⁇ or less. It is more preferred that:
- This average particle size refers to a value obtained by measurement with a Microtrac (FSA type, manufactured by Nikkiso Co., Ltd.).
- a ball mill As a pulverizing means, a ball mill, a rod mill, a hammer mill, a disk mill, a fluid energy mill, or a combination of two or more of these can be used.
- the pulverization may be either dry pulverization or wet pulverization, but wet pulverization is desirable from the viewpoint of energy efficiency.
- the pulverization may be performed in one stage or in multiple stages. In the case of multiple stages, it may be a closed system in which the pulverized material obtained in the first stage of milling is sieved with a fixed particle size and the coarse particles on the sieve are reground. By kneading the milled modified biomass, a biomass water slurry can be obtained. As the kneader, various types can be applied, but a type having strong stirring power is more preferable.
- the solid content may be pulverized in the pulverizing step, and the pulverized solid may be put into the kneading step, or the pulverizing step and the kneading step may be performed simultaneously.
- the slurry may be formed only in the pulverizing step or only in the kneading step.
- a modified ground biomass having a solid concentration higher than a desired solid concentration is used as a biomass water slurry, and the modified ground biomass is gradually kneaded with the additive-containing water or water. It is preferable to add the additive and water little by little and stop adding the water when the viscosity suddenly decreases, since the reformed biomass will not be excessively diluted with water.
- the biomass water slurry obtained as described above has a high solid content, has a sufficient calorific value as an alternative fuel to heavy oil and coal, and has a viscosity that allows pipe transport.
- the modified biomass is modified so that the oxygen-carbon atomic ratio is 0.38 or less at a pressure higher than the saturated steam pressure, it does not contain harmful bacteria and is made porous. Therefore, when mixed in soil, it becomes a breeding place for useful soil bacteria and adsorbs harmful components in soil, so it is also useful as a soil conditioner and can also be used as an adsorbent .
- Wood-based biomass such as thinned wood, sawdust, chips, scrap wood, and other wood-processed wood chips, street pruned wood, wood-based building waste, bark, driftwood, etc .; Biomass from grasses such as straw, bagasse, etc .; Biomass from cellulosic products such as waste paper is used as a raw material, so it is also an effective use of resources and is a non-fossil natural energy that is considered to have zero carbon dioxide emissions. It is one of the effective measures against environmental problems such as increase of acid gas. Also, since the ash and sulfur content are extremely low, the construction cost of fuel facilities can be reduced.
- oxygen and steam are used as gasifying agents.
- the amount of oxygen should be about 1/4 to 1 Z2.5 of the amount required to completely burn the reformed biomass.
- the amount of oxygen required for gasification is related to the gasification temperature. Oxygen can be replaced by air. In this method, gasification can be achieved with a small amount of oxygen at a set gasification temperature as compared with the case where raw biomass is gasified.
- the gasification temperature is not limited as long as gasification occurs, but it is possible to set the gasification temperature to 800 to 130 ° C to suppress the generation of tar and soot. . Preferably it is 800 to 1200 ° C.
- the gasification pressure is not particularly limited, it can be set to 0 :! to 1 OMPa. Considering the treatment of the gas generated in the latter stage, it is preferable to gasify at a high pressure of 0.5 to 10 MPa.
- the modified biomass used for gasification may be dried, hydrated, or slurried with water.
- a mixture of modified biomass powder or slurry and coal powder may be used.
- Modified biomass is easier to pulverize than raw biomass and can be supplied to a gasification reactor at a high pressure, so that it is a preferable raw material for obtaining a high-pressure gasification product.
- the amount of oxygen supply can be reduced and cold gas efficiency can be improved as compared with the case where raw biomass is directly oxidized. Furthermore, the concentration of the active components H 2 and CO in the obtained gasification product can be increased.
- the use of the modified biomass can reliably reduce the size of the crushed particles, the direct gasification by the partial oxidation reaction can be efficiently performed, and the gasification reaction can be easily processed at a high pressure.
- gasification of biomass such as wood is usually possible at a low temperature of about 800 ° C, but if the gasification rate is reduced due to tar or carbon deposition or operational troubles occur, It is said. (Reference: Biomass Handbook, edited by The Institute of Energy, 2002, p-95)
- the gasification method of the present invention has no tar-carbon deposition, and thus has the above-mentioned reduction in efficiency and operation. There is no problem of trouble. '
- the solid content of the slurry obtained after kneading was 66% by mass, and the viscosity of the slurry was 830 mPa ⁇ s. This slurry was still in a slurry state after being stored at room temperature for 2 months. This slurry had the same fuel properties as the biomass water slurry of Experimental Example 1.
- the solid content of the slurry obtained after kneading was 68.5% by mass, and the viscosity of the slurry was 990 mPa's. This slurry remained in a slurry state after being stored at room temperature for 2 months.
- Example 4 Use 430 g of cedar dried and crushed to a particle size of 1 mm or less, and 3,600 g of water.Set the reforming temperature and pressure to 270 ° C and 14 MPa. A slurry was obtained in the same manner as in Experimental Example 1 except that the reforming treatment was performed. The average particle size of the fine powder after pulverization with a ball mill was 11.3 ⁇ m.
- the solid content of the slurry obtained after kneading was 67% by mass, and the viscosity of the slurry was 770 mPa ⁇ s. This slurry was in a slurry state even after being stored at room temperature for 2 months. This slurry also had the same fuel properties as the biomass water slurry of Experimental Example 1.
- the filtrate 3, 20 obtained by filtration of the modified slurry of Experimental Examples 2 and 3 was used instead of water.
- a slurry was obtained in the same manner as in Experimental Example 1, except that 0 g was used, the reforming treatment was performed at a set temperature and a set pressure of 330 MPa and 18 MPa for the reforming treatment.
- Bolmi The average particle size of the fine powder after F crushing was 11 ⁇ .
- the solid content of the slurry obtained after the kneading was 70% by mass, and the viscosity of the slurry was 1, 10 OmPa-s. This slurry remained in a slurry state after being stored at room temperature for 2 months.
- the solid content concentration of the slurry obtained after kneading was 70% by mass, and the viscosity of the slurry was 940 mPa ⁇ s. This slurry was in a slurry state even after being stored at room temperature for 2 months.
- the elemental composition of the dry powder was determined by Yanako Co. CHN coder one oxygen / carbon atom ratio at 0.25 8, in higher heating value (calorific value in combustion, heat of condensation of the H 2 0 was also generated
- the calorific value (including calorific value) was 29.9 MJ / kg (7.150 kcal / kg), and the volatile content was 60% by mass.
- the oxygen-Z carbon atom ratio of the raw material cedar was 0.620, the higher calorific value was 20.
- OM J / kg (4,780 kcalZkg) and the volatile content was 85% by mass.
- the raw material was reformed in the same manner as in Experimental Example 10, except that the pressure at the pump was 9 MPa and the temperature of the reforming section was 270 ° C. After filtration and drying, a black powder was obtained.
- the resulting black powder had an oxygen-Z carbon atom ratio of 0.262, a higher calorific value of 29.8 MJ / kg (7.120 kcal / kg), and a volatile content of 60% by mass.
- the raw material was reformed in the same manner as in Experimental Example 10, except that the pressure in the pump was 7 MPa and the temperature of the reforming section was 250 ° C, followed by filtration and drying. Thus, a black powder was obtained.
- the resulting black powder had an oxygen-Z carbon atom ratio of 0.376, a higher calorific value of 27.OMJ / kg (6,450 kcalZkg), and a volatile content of 68% by mass.
- the raw material was reformed in the same manner as in Experimental Example 10 except that the residence time in the reforming section was set to 5 minutes, followed by filtration and drying to obtain a black powder.
- the resulting black powder had an oxygen-Z carbon atom ratio of 0.260, a higher calorific value of 29.7 Mj / kg (7,100 kca 1 / kg), and a volatile content of 74% by mass.
- the raw materials were reformed in the same manner as in Experimental Example 10, except that the pressure in the pump was 5 MPa and the temperature of the reforming section was 230 ° C, followed by filtration and drying. This gave a dark brown powder.
- the resulting powder had an oxygen / carbon atomic ratio of 0.496, a higher calorific value of 23.9 MJ / kg (5,700 kca 1 / kg), and a volatile content of 74% by mass.
- the raw materials were reformed in the same manner as in Experimental Example 10, except that the pressure in the pump was 3 MPa and the temperature of the reforming section was 200 ° C, followed by filtration and drying. As a result, a brown powder was obtained.
- the resulting brown powder had an oxygen-Z carbon atom ratio of 0.615, a high calorific value of 20.lMj / kg (4,800 kcal Zkg), and a volatile content of 84% by mass.
- Dry black powder (oxygen / carbon atomic ratio: 0.258, high calorific value: 29.9 MjZkg) obtained by the reforming process of Experimental Example 10 was supplied at 1,466 kg / hr, and acid was added.
- the amount of oxygen required to bring the gasification reactor temperature to 1,100 ° C and the gas composition at that time were determined by simulation calculations.
- the required oxygen amount is 28.1 kg—mo 1 hr
- the amount of (C 0 + HJ in the produced gas is 130.2 kg—mo 1 Zhr, which is (CO + H 2 )
- the gas concentration was 84.1%
- the cold gas efficiency was 84.9% .
- the simulation results show that the generated gas composition can be calculated using the following equations (1) and (2). In the reverse reaction equation, it is determined to be thermodynamically balanced.
- Dry cedar (oxygen-Z carbon atom ratio: 0.620, high calorific value: 20. OMj / kg) was supplied at 2,340 kg / hr, and the gasification reactor temperature was reduced by oxygen blowing. The amount of oxygen required to reach 1,100 ° C and the gas composition at that time were determined by simulation calculations.
- cellulosic biomass which has not been effectively used in the past, has a high solid content, has a sufficient calorific value as a fuel alternative to heavy oil or coal, and has a slurry characteristic even when stored for a long time. And a slurry having a viscosity that enables pipe transport can be obtained stably.
Abstract
Description
Claims
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US10/523,749 US7465844B2 (en) | 2002-08-12 | 2003-04-25 | Method of upgrading biomass, upgraded biomass, biomass water slurry and method of producing same, upgraded biomass gas, and method of gasifying biomass |
AU2003235820A AU2003235820B2 (en) | 2002-08-12 | 2003-04-25 | Method of modifying biomass, modified biomass, aqueous biomass slurry and method of producing the same, modified biomass gas and method of gasifying biomass |
US12/264,169 US8049049B2 (en) | 2001-10-25 | 2008-11-03 | Method of upgrading biomass, upgraded biomass, biomass water slurry and method of producing same, upgraded biomass gas, and method of gasifying biomass |
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US8049049B2 (en) | 2011-11-01 |
MY143323A (en) | 2011-04-15 |
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JP2005179379A (ja) | 2005-07-07 |
US20070068077A2 (en) | 2007-03-29 |
AU2003235820B2 (en) | 2009-01-22 |
US20060112638A1 (en) | 2006-06-01 |
AU2003235820A1 (en) | 2004-03-03 |
JP4334857B2 (ja) | 2009-09-30 |
US7465844B2 (en) | 2008-12-16 |
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