WO2021221164A1 - Dispositif de gazéification de biomasse - Google Patents

Dispositif de gazéification de biomasse Download PDF

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Publication number
WO2021221164A1
WO2021221164A1 PCT/JP2021/017235 JP2021017235W WO2021221164A1 WO 2021221164 A1 WO2021221164 A1 WO 2021221164A1 JP 2021017235 W JP2021017235 W JP 2021017235W WO 2021221164 A1 WO2021221164 A1 WO 2021221164A1
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valve
pyrolysis gas
oxygen
heat
temperature
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PCT/JP2021/017235
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English (en)
Japanese (ja)
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直城 堂脇
恒 上内
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株式会社ジャパンブルーエナジー
株式会社Ｊｂｅｃエンジニアリング
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Publication of WO2021221164A1 publication Critical patent/WO2021221164A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • C10B49/18—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form according to the "moving bed" type
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/12—Continuous processes using solid heat-carriers
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/005—Reducing the tar content by partial oxidation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/006—Reducing the tar content by steam reforming
    • 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
    • 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
    • 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
    • C10J2300/0923—Sludge, e.g. from water treatment plant
    • 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
    • C10J2300/0976—Water as steam
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion
    • 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
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • 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
    • C10J2300/1853—Steam reforming, i.e. injection of steam only
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing

Definitions

  • the present invention relates to a biomass gasifier having a preheater, a pyrolyzer and a pyrolyzed gas reformer.
  • sewage sludge having an ash content of 20% by weight is dried and then pyrolyzed in an air-blown fluidized layer pyrolysis furnace at 500 to 800 ° C. to pyrolyze the pyrolysis gas.
  • a method of generating turbine power by burning with air at a high temperature of 1000 to 1,250 ° C and generating steam with the heat Japanese Patent Laid-Open No. 2002-322902
  • high ash biomass as a raw material is circulated by air blowing.
  • Pyrolysis is carried out in a flow heating furnace at a temperature of 450 to 850 ° C., and char, which is a thermal decomposition residue, is recovered by a cyclone, while pyrolysis gas containing tar is reformed at 1000 to 1200 ° C. in the presence of oxygen.
  • Method Japanese Unexamined Patent Publication No. 2004-517405
  • the char is pyrolyzed by the same method to separate the char, and then the char is granulated and supplied into the circulating flow reforming furnace.
  • a method of producing a granulated sintered body by sintering at a temperature of 900 to 1000 ° C. (Japanese Patent No. 4155507) or the like is disclosed.
  • a heat-carrying medium for carrying heat a preheater for heating the heat-carrying medium, a reformer for steam reforming of the heat-decomposed gas, and a heat-decomposing wood biomass raw material.
  • the preheater, the reformer, and the heat decomposer 20 are provided with a heat decomposer, a separator for separating the heat-bearing medium and the char, and a hot air furnace that burns the char to generate hot air.
  • Devices arranged vertically in order from the top are known (Japanese Patent Laid-Open No. 2011-144329).
  • the heat-decomposed coke obtained by separating the mixture consisting of the heat-decomposed coke and the heat-bearing medium is burned in a combustion device, and the heat-bearing medium is heated in the heating zone by utilizing the apparent heat generated thereby.
  • An embodiment of producing a product gas having a high calorific value from an organic substance and a substance mixture Japanese Patent No. 4264525) is known.
  • a pyrolysis gas introduction tube for introducing the pyrolysis gas from the pyrolysis device to the pyrolysis gas reformer is formed on the pyrolysis device side on the upper surface of the preheated heat-bearing medium layer formed in the pyrolysis device.
  • a gasification method Japanese Patent Laid-Open No. 2019-65160 installed on the side surface of a lower pyrolyzer is known.
  • the thermometer In the oxygen supply method of the conventional pyrolysis gas reformer, when the biogas temperature is raised from 600 ° C. to 1000 ° C. at the reformer outlet, it takes time for the thermometer to detect the predetermined temperature. Even though sufficient oxygen gas has already been supplied to reach the specified 1000 ° C, as a result of the temperature not being detected, more oxygen gas will be supplied, and by the time the temperature is detected, There was a problem that the temperature became 1000 ° C or higher. On the other hand, when the temperature exceeds 1000 ° C., the automatic valve starts to close and the oxygen gas supply amount starts to decrease.
  • the temperature drop is not easily detected, the amount of oxygen gas is further reduced even though the amount of oxygen gas is sufficiently reduced to 1000 ° C or less, and by the time the temperature is detected, the temperature drops significantly. There was a problem. As described above, since the temperature fluctuates greatly, the hydrogen concentration fluctuates greatly due to the influence of the reforming reaction, and there is a problem that hydrogen cannot be stably collected.
  • the biomass gasifier according to the present invention A preheater that preheats the heat-bearing medium, and a pyrolyzer that receives the heat-supporting medium preheated by the preheater and performs thermal decomposition of biomass by the heat of the heat-supporting medium.
  • a pyrolysis gas reformer that at least partially burns the pyrolysis gas generated by pyrolysis with air or oxygen.
  • a supply unit that supplies air or oxygen to the pyrolysis gas reformer, With A first valve for the supply unit to continuously supply air or oxygen to the pyrolysis gas reformer, and a second valve for intermittently supplying air or oxygen to the pyrolysis gas reformer. May have.
  • the first valve is a manual valve.
  • the second valve may be an on / off valve.
  • the biomass gasifier according to the present invention By continuously supplying air or oxygen through the first valve, the temperature inside the pyrolysis gas reformer is adjusted to a predetermined temperature range, and then continuously through the first valve. Even if it is provided with a control device that controls the temperature inside the pyrolysis gas reformer to reach the target temperature by intermittently supplying air or oxygen through the second valve while supplying air or oxygen. good.
  • the predetermined temperature range is 800 to 900 degrees.
  • the target temperature may be 980 to 1030 degrees.
  • the opening degree of the first valve may be constant.
  • the temperature inside the pyrolysis gas reformer may be controlled to be the target temperature.
  • the diameter of the first supply pipe provided with the first valve and the diameter of the second supply pipe provided with the second valve may be substantially the same.
  • the supply unit has a first valve for continuously supplying air or oxygen to the pyrolysis gas reformer and a second valve for intermittently supplying air or oxygen to the pyrolysis gas reformer.
  • FIG. 1 is a schematic view showing one form of a biomass gasification device.
  • FIG. 2 is a diagram showing an oxygen supply method of a pyrolysis gas reformer in the biomass gasification device of the present embodiment.
  • FIG. 3A is a diagram showing the temperature of the pyrolysis gas in the oxygen supply method of the pyrolysis gas reformer over time in the reference example.
  • FIG. 3B is a diagram showing the temperature of the pyrolysis gas in the oxygen supply method of the pyrolysis gas reformer in the present embodiment over time.
  • FIG. 4 is a diagram showing an oxygen supply control device of the pyrolysis gas reformer in the biomass gasification device of the present invention.
  • FIG. 5 is a schematic view showing a mode in which oxygen is supplied to the pyrolysis gas reformer using only the automatic valve.
  • the biomass gasifier of the present embodiment receives heat from the preheater 10 that preheats the heat-bearing medium 30 and the heat-supporting medium 30 that has been preheated by the preheater 10.
  • a thermal decomposition device (biomass thermal decomposition device) 20 that executes thermal decomposition of biomass by the heat of the supporting medium 30 and a thermal decomposition gas generated by the thermal decomposition are partially burned by air or oxygen to execute steam reforming. It has a thermal decomposition gas reformer 40 and a supply mechanism provided between the preheater 10 and the thermal cracker 20 for supplying the heat-bearing medium 30 from the preheater 10 to the thermal cracker. There is.
  • the heat-supporting medium 30 (also referred to as "heat carrier”) is a plurality of granules and / or lumps, preferably made of one or more materials selected from the group consisting of metals and ceramics.
  • the metal is preferably selected from the group consisting of iron, stainless steel, nickel alloy steel, and titanium alloy steel, and more preferably stainless steel.
  • the ceramic is selected from the group consisting of alumina, silica, silicon carbide, tungsten carbide, zirconia and silicon nitride, and more preferably alumina.
  • the shape of the heat-supporting medium 30 is preferably spherical (ball), but it does not necessarily have to be a true sphere, and it may be a spherical object having an elliptical or oval cross-sectional shape.
  • the diameter (maximum diameter) of the spherical object is preferably 3 to 25 mm, more preferably 8 to 15 mm. Exceeding the above upper limit (25 mm) may impair the fluidity inside the pyrolyzer 20, that is, the free fall property, which causes the spherical object to stand still inside the pyrolyzer 20 and cause blockage. May become.
  • the spheroids themselves may stick to the spheroids due to tar and soot and dust adhering to the spheroids in the pyrolyzer 20, which may cause blockage.
  • the diameter of the spherical object is less than 3 mm, the spherical object adheres to the inner wall of the pyrolyzer 20 and grows due to the influence of tar and dust adhering to the spherical object, and in the worst case, the pyrolyzer There is a concern that 20 will be blocked.
  • the spherical object to which tar is attached is extracted from the valve at the bottom of the pyrolyzer 20
  • the spherical object having a thickness of less than 3 mm is light, and since the tar is attached, it does not fall naturally and sticks to the inside of the valve. May promote obstruction.
  • the biomass of this embodiment means a so-called biomass resource.
  • the biomass resource refers to plant-based biomass, for example, agricultural products such as thinned wood, sludge waste, pruned branches, forest land residue, unused trees, etc., which are discarded from agriculture, and vegetable residues and fruit tree residues, which are discarded from agriculture.
  • plant-based biomass for example, agricultural products such as thinned wood, sludge waste, pruned branches, forest land residue, unused trees, etc., which are discarded from agriculture, and vegetable residues and fruit tree residues, which are discarded from agriculture.
  • biological biomass for example, biological waste such as livestock excrement and sewage sludge
  • the apparatus of this embodiment is preferably suitable for gasification of plant-based biomass and biological-based biomass.
  • high ash biomass having an ash content of preferably 5.0% by mass or more, more preferably 10.0 to 30.0% by mass, and further preferably 15.0 to 20.0% by mass on a drying basis.
  • high ash biomass having an ash content of preferably 5.0% by mass or more, more preferably 10.0 to 30.0% by mass, and further preferably 15.0 to 20.0% by mass on a drying basis.
  • it is suitable for gasification of sewage sludge and livestock excrement.
  • the heat-supporting medium 30 preheated by the preheater 10 is supplied from the preheater 10 to the pyrolyzer 20 via a valve described later by free fall.
  • the heat-supporting medium 30 causes thermal decomposition of the biomass supplied into the pyrolyzer 20 by its own heat.
  • the heat-supporting medium 30 in the pyrolyzer 20 is discharged from the pyrolyzer 20 by free fall via a valve, and is preferably recirculated to the preheater 10.
  • a first valve 50 is provided between the preheater 10 and the pyrolyzer 20.
  • the first valve 50 may have an adjusting portion, a first opening / closing portion provided below the adjusting portion, and a second opening / closing portion provided below the first opening / closing portion. Then, the supply control device 100 controls so that the first opening / closing part is opened while the second opening / closing part is closed and the second opening / closing part is opened while the first opening / closing part is closed. You may.
  • Each of the first opening / closing part and the second opening / closing part may be a damper valve.
  • first opening / closing portion is the first damper valve 51a and the second opening / closing portion is the second damper valve 51b will be described. Further, the embodiment in which the adjusting portion of the first valve 50 is the swing valve 52 will be described.
  • the pyrolysis gas generated by thermally decomposing the biomass in the pyrolysis device 20 is introduced into the pyrolysis gas reformer 40 through the pyrolysis gas introduction pipe 200.
  • the pyrolysis gas introduced into the pyrolysis gas reformer 40 is partially oxidized by air or oxygen, whereby the inside of the pyrolysis gas reformer 40 is heated.
  • the pyrolysis gas and steam can be changed to reform the pyrolysis gas into a hydrogen-rich gas.
  • the pyrolysis gas reformer 40 is provided with a supply unit that supplies air or oxygen to the pyrolysis gas reformer 40.
  • the supply pipes 141 and 142 of the supply unit are provided with a first valve for continuously supplying air or oxygen to the pyrolysis gas reformer and intermittently supplying air or oxygen to the pyrolysis gas reformer.
  • a second valve is provided (see FIGS. 2 and 4). While the gas is reformed by the pyrolysis gas reformer 40, the first valve may be in the open state so that the opening degree thereof is not changed. On the other hand, the second valve may be opened and closed repeatedly.
  • the opening and closing of the second valve may be performed according to a predetermined sequence stored in a storage unit (not shown), or may be controlled by receiving a detection result in the detector 44 that detects the reformed gas temperature.
  • the state of the second valve may be changed between the open state and the closed state.
  • the first valve may be a manual valve 41 that supplies a predetermined amount of oxygen determined by the opening degree and capacity to the pyrolysis gas reformer 40.
  • the second valve may be an on / off valve 42 that supplies oxygen to the pyrolysis gas reformer 40 on / off.
  • a mode in which the first valve is the manual valve 41 and the second valve is the on / off valve 42 will be described.
  • the manual valve 41 which is the first valve
  • the on / off valve 42 which is the second valve
  • Oxygen is supplied into the pyrolysis gas reformer 40 via each of the first supply pipe 141 and the second supply pipe 142.
  • the diameters of the first supply pipe 141 and the second supply pipe 142 may be substantially the same. In the present embodiment, “substantially the same” means that the difference is within 5% based on the larger size.
  • the diameter R1 of the first supply pipe 141 is the second supply pipe.
  • the diameter of 142 is R2 or more, R1 ⁇ 0.95 ⁇ R2 ⁇ R1 ⁇ 1.05.
  • each of the diameter R1 of the first supply pipe 141 and the diameter R2 of the second supply pipe 142 may be 5 to 15 mm.
  • oxygen or air is selected from the group consisting of the pyrolysis gas reformer 40 and its vicinity, and the pyrolysis gas introduction pipe 200 between the pyrolysis device 20 and the pyrolysis gas reformer 40. It is introduced from the oxygen or air supply port provided at the above positions.
  • the upper limit of the vapor phase temperature in the pyrolysis gas reformer 40 is preferably 1050 ° C, more preferably 1030 ° C, still more preferably 1000 ° C, and the lower limit is preferably 850 ° C, more preferably 880 ° C, further. It is preferably 900 ° C. Below the above lower limit (850 ° C.), the reforming reaction may not proceed. It can also be a factor in generating N 2 O. On the other hand, even if the above upper limit (1050 ° C.) is exceeded, a significant increase in the effect cannot be expected, and the amount of heat required for heating increases, leading to an increase in cost.
  • the gas phase temperature in the pyrolysis gas reformer 40 is 850 ° C. or higher, which is the above-mentioned preferable lower limit value, the reforming of carbon monoxide by steam becomes remarkable, and when the vapor phase temperature is 880 ° C. or higher, which is the more preferable lower limit value, steam reforming is performed. Reformation of methane becomes remarkable. Therefore, in order to efficiently reform both carbon monoxide and methane, it is more preferable that the vapor phase temperature in the pyrolysis gas reformer 40 is 880 ° C. or higher.
  • a more preferable upper limit of the gas phase temperature in the pyrolysis gas reformer 40 is 1050 ° C., and the pyrolysis gas can be sufficiently reformed below the temperature, but 1030 ° C. or lower in order to reduce the amount of fuel used. Is more preferable.
  • the gas phase temperature of the pyrolysis gas reformer 40 is the heat generated comprehensively from the temperature generated by mixing the pyrolysis gas array steam and air or oxygen introduced into the pyrolysis gas reformer 40. It refers to the gas phase temperature inside the decomposition gas reformer 40.
  • the gas phase temperature of the pyrolysis gas reformer 40 can be appropriately controlled by the amount of air or oxygen supplied.
  • the supply of oxygen gas is divided into two, and a constant amount of oxygen gas is constantly supplied from the manual valve 41 to set the temperature of the reforming gas to a predetermined temperature.
  • the temperature can be raised in the range, preferably 800 ° C. to 900 ° C., and the temperature of the reformed gas can be controlled in the vicinity of 1000 ° C., which is the target temperature, by supplying oxygen gas from the on / off valve 42.
  • the manual valve 41 refers to a valve in which the opening is fixed after adjustment by changing the opening, and the valve may be an automatic valve, a manual valve, or a remote controlled valve, and the valve can be directly changed on site. It may be a thing.
  • the on-off valve 42 refers to a valve such as a solenoid valve, an electric valve, an air valve, etc., which has only two positions of fully open / fully closed valve opening.
  • the temperature of the reformed gas is raised to a predetermined temperature, preferably about 800 ° C. to 900 ° C. by supplying oxygen gas from the manual valve 41, the difference from the target temperature is reduced in advance, and it is necessary to reach the target temperature. Reduce time.
  • a predetermined temperature preferably about 800 ° C. to 900 ° C.
  • the temperature exceeding the target temperature of 1050 ° C. can be suppressed as much as possible.
  • the on / off valve 42 closes and the temperature drops beyond the target temperature of 1000 ° C., the temperature does not drop below the maintained temperature because the automatic valve constantly supplies oxygen gas. By doing so, the temperature of the reforming gas can be controlled to be close to the target predetermined temperature of 1000 ° C.
  • the predetermined temperature range of 900 ° C. or lower is preferably 800 ° C. to 900 ° C., more preferably 850 ° C. to 880 ° C.
  • the on / off valve 42 can reach the target temperature near 1000 ° C. (see FIG. 3B).
  • the temperature is controlled as shown in FIG. 3A, and the temperature fluctuates in a wide range of 800 to 1080 ° C. Things can happen.
  • the temperature of the reformed gas can be raised to the target temperature by supplying oxygen gas from the on / off valve 42.
  • the target temperature is preferably 850 ° C to 1050 ° C, more preferably 880 ° C to 1030 ° C, and even more preferably 900 ° C to 1000 ° C.
  • the predetermined temperature range can be fed back and adjusted.
  • the temperature of the reformed gas in the pyrolysis gas reformer 40 is brought closer to the target temperature, the reforming reaction is stabilized, and the hydrogen concentration is stabilized, so that stable hydrogen can be supplied.
  • the biomass gasification device of the present embodiment may be provided with a control device 43 for making adjustments in the pyrolysis gas reformer 40 (see FIG. 4).
  • the control device 43 continuously supplies air or oxygen through the manual valve 41, which is an example of the first valve, to bring the temperature inside the pyrolysis gas reformer 40 in a predetermined temperature range (for example, 800 to 900 ° C.). Yes, if more limited, it is adjusted to 850 to 880 ° C.), and then, while continuously supplying air or oxygen through the manual valve 41 which is the first valve, it is an example of the second valve.
  • the temperature inside the pyrolysis gas reformer becomes a target temperature (for example, 980 to 1030 ° C, typically 1000 ° C). It may be controlled to.
  • the opening degree of the manual valve 41 may not be changed and may be constant.
  • the temperature inside the pyrolysis gas reformer 40 may be controlled by the control device 100 so as to be the target temperature.
  • the detector 45, the switch and the regulator that receive the temperature measured by the detector 44 that detects the reformed gas temperature in the pyrolysis gas reformer 40 or detect the temperature based on the data from the detector 44.
  • the control unit 48 for instructing the operation of the above and the calculation unit 49 for executing the calculation for feedback control may be provided.
  • An on / off valve switch 46 that controls the opening / closing of the on / off valve 42 and an automatic valve adjuster 47 that adjusts the opening / closing degree of the manual valve 41 may be provided in response to a command from the control unit 48 (see FIG. 4). Based on the actual temperature reached by the adjustment by the manual valve 41 and the on / off valve 42, the predetermined temperature range may be fed back and adjusted.
  • the on / off valve switch 46 and the automatic valve adjuster may be used.
  • a command is sent from the control unit 48 to 47.
  • the opening / closing degree of the manual valve 41 may be automatically adjusted by the automatic valve adjuster 47 by directly using the detection result of the detector 44, or the opening / closing degree of the on / off valve 42 is automatically adjusted. It may be (see FIG. 2).
  • the second valve 90 may be provided between the pyrolyzer 20 and the waste treatment device 240.
  • the second valve 90 may have a pair of damper valves 91a and 91b which are an example of an opening / closing part and a swing valve 92 which is an example of an adjusting part. Similar to the first valve 50, in the second valve 90, the swing valve 92, the first damper valve 91a, and the second damper valve 91b may be arranged in order from the top.
  • the waste treatment device 240 is provided with a filter F (see FIG.
  • the aspect of the supply control device 100 in the biomass gasification device of the present embodiment may be incorporated into the conventional biomass gasification device.
  • the pyrolyzer 20 has a biomass supply port and a non-oxidizing gas supply port and / or a steam blow port.
  • the pyrolysis gas reformer 40 has a steam inlet and a reformed gas outlet.
  • a pyrolysis gas introduction pipe 200 provided between the pyrolysis device 20 and the pyrolysis gas reformer 40, which introduces the pyrolysis gas generated in the pyrolysis device 20 into the pyrolysis gas reformer 40.
  • Each of the thermal decomposition device 20 and the thermal decomposition gas reformer 40 further includes an inlet and an outlet for a preheated heat-bearing medium, and the heat of the heat-bearing medium causes thermal decomposition of biomass and thermal decomposition of biomass.
  • the pyrolysis device 20 and the pyrolysis gas reformer 40 are provided in parallel with respect to the flow of the heat-bearing medium, and the pyrolysis gas introduction pipe 200 is provided with the pyrolysis device 20 and the pyrolysis gas reformer.
  • the pyrolysis gas introduction pipe 200 is provided and is provided substantially horizontally with respect to the direction of gravity.
  • the pyrolysis gas reformer 40 includes a manual valve 41 that constantly supplies a predetermined amount of oxygen to the pyrolysis gas reformer 40, and an on / off valve 42 that supplies oxygen to the pyrolysis gas reformer 40 on and off.
  • a biomass gasifier can be provided.
  • the pyrolyzer 20 has a biomass supply port and a non-oxidizing gas supply port and / or a steam blow port.
  • the pyrolysis gas reformer 40 has a steam inlet and a reformed gas outlet.
  • a pyrolysis gas introduction pipe 200 provided between the pyrolysis device 20 and the pyrolysis gas reformer 40 is provided, and the pyrolysis gas generated in the pyrolysis device 20 is transferred to the pyrolysis gas reformer 40.
  • the pyrolyzer 20 further includes an inlet and an outlet for a heat-supporting medium that has been preheated, and uses the heat of the heat-supporting medium to carry out thermal decomposition of biomass.
  • the pyrolysis gas reformer 40 executes steam reforming of the pyrolysis gas generated by the thermal decomposition of biomass.
  • the pyrolysis gas reformer 40 further includes an air or oxygen inlet, and performs steam reforming by partially burning the pyrolysis gas generated by the thermal decomposition of biomass with the air or oxygen.
  • the pyrolysis gas introduction pipe 200 is provided on the side surface of the pyrolyzer 20 below the upper surface of the heat-carrying medium layer formed in the pyrolyzer 20.
  • the pyrolysis gas reformer 40 includes a manual valve 41 that constantly supplies a predetermined amount of oxygen to the pyrolysis gas reformer 40, and an on / off valve 42 that supplies oxygen to the pyrolysis gas reformer 40 on and off.
  • a biomass gasifier can be provided. Since the pyrolyzer 20 and the pyrolyzed gas reformer 40 are separated from each other with respect to the flow of the heat-carrying medium, their respective temperatures can be controlled separately.
  • the pyrolyzer 20 that heats the biomass in a non-oxidizing gas atmosphere or a mixed gas atmosphere of a non-oxidizing gas and steam, and the gas generated in the pyrolyzing device 20.
  • a pyrolysis gas reformer 40 that reforms in the presence of steam, and a preheated heat-bearing medium is put into the pyrolyzer 20 and the heat of the heat-supporting medium is used.
  • the pyrolysis of the biomass is then carried out, and then the pyrolysis gas generated by the pyrolysis of the biomass is introduced into the pyrolysis gas reformer 40 to carry out the steam reforming of the pyrolysis gas.
  • a pyrolysis gas introduction tube provided on the side surface of the pyrolysis device 20 below the upper surface of the heat-supporting medium layer, in which the pyrolysis gas generated by the thermal decomposition of the biomass is formed in the pyrolysis device 20.
  • the pyrolysis gas reformer 40 is introduced into the pyrolysis gas reformer 40, and then the introduced pyrolysis gas is partially introduced into the pyrolysis gas reformer 40 by air or oxygen separately introduced into the pyrolysis gas reformer 40.
  • the method of gasifying biomass which is pyrolyzed and reformed by steam introduced at the same time as the above air or oxygen.
  • a manual valve 41 provided in the pyrolysis gas reformer 40 that constantly supplies a predetermined amount of oxygen to the pyrolysis gas reformer 40 raises the temperature of the reformed gas to a predetermined temperature range, and in addition, the pyrolysis gas.
  • a method for gasifying biomass is provided in which the temperature of the reformed gas is raised to a target temperature by an on-off valve 42 that supplies oxygen to the reformer 40 on and off.
  • the heat-supporting medium 30 is preferably heated to 650 to 800 ° C, more preferably 700 to 750 ° C.
  • the biomass for example, high ash biomass
  • the amount of pyrolyzed gas generated decreases.
  • it exceeds the above upper limit (800 ° C.) it causes volatilization of phosphorus and potassium (potassium), and causes blockage and corrosion of pipes by diphosphorus pentoxide and potassium (potassium).
  • it is not expected that the effect will be significantly increased only by giving extra heat, and on the contrary, it will only lead to high cost. It also causes a decrease in the thermal efficiency of the equipment.
  • the heat-supporting medium 30 heated to the predetermined temperature in the preheater 10 is then introduced into the pyrolyzer 20.
  • the heat-carrying medium 30 is separately contacted with the biomass supplied to the pyrolyzer 20 from the biomass supply port 220.
  • the biomass is heated and thermally decomposed to generate a thermal decomposition gas.
  • the generated pyrolysis gas passes through the pyrolysis gas introduction pipe 200 and is introduced into the pyrolysis gas reformer 40. At this time, tar, soot, etc.
  • the tar, soot, and the like that have been heated and gasified and remain are discharged from the bottom of the pyrolyzer 20 while still adhering to the heat-bearing medium 30.
  • the pyrolysis gas generated by thermally decomposing the biomass in the pyrolysis device 20 is introduced into the pyrolysis gas reformer 40 through the pyrolysis gas introduction pipe 200.
  • the pyrolysis gas introduced into the pyrolysis gas reformer 40 is partially oxidized by air or oxygen, whereby the inside of the pyrolysis gas reformer 40 is heated.
  • the pyrolysis gas reacts with steam, and the pyrolysis gas can be reformed into a hydrogen-rich gas.
  • the pyrolysis gas introduced into the pyrolysis gas reformer 40 is partially oxidized by the air or oxygen supplied from the above air or oxygen inlet. And steam reforming is performed by the heat generated by it.
  • the pyrolysis gas reformer 40 usually does not have a heating device, for example, a heating device that supplies heat from the outside and / or inside of the pyrolysis gas reformer by steam or an electric heater.
  • the supply of oxygen gas is divided into two, and a constant amount of oxygen gas is constantly supplied from the manual valve 41 to keep the temperature of the reformed gas in a predetermined temperature range, preferably 800.
  • the temperature can be raised from ° C. to 900 ° C., and the temperature of the reformed gas can be controlled to be close to the target temperature of 1000 ° C. by supplying oxygen gas from the on / off valve 42.
  • the temperature of the reformed gas is raised to a predetermined temperature, preferably about 800 ° C. to 900 ° C. by supplying oxygen gas from the manual valve 41, the difference from the target temperature is reduced in advance, and it is necessary to reach the target temperature. Reduce time.
  • a predetermined temperature preferably about 800 ° C. to 900 ° C.
  • the on / off valve 42 closes and the temperature drops when the target temperature exceeds 1000 ° C., the temperature does not drop below the maintained temperature because the manual valve 41 constantly supplies oxygen gas. By doing so, the temperature of the reforming gas can be controlled to be close to the target predetermined temperature of 1000 ° C.
  • sewage sludge As a biomass raw material, sewage sludge was granulated and used. The maximum size of the sewage sludge after granulation was about 6 to 15 mm. The properties of the sewage sludge are shown in Table 1. Table 2 shows the composition of the ash obtained by burning the sewage sludge.
  • silicon dioxide, aluminum oxide, ferric oxide, magnesium oxide, calcium oxide, sodium oxide, potassium oxide, diphosphorus pentoxide and manganese oxide were measured in accordance with JIS M8815.
  • Mercury, chromium, cadmium, copper oxide, lead oxide, zinc oxide and nickel were measured in accordance with JIS Z 7302-5: 2002.
  • the gasifier basically includes a pyrolyzer 20, a pyrolyzed gas reformer 40, and a preheater 10 (see FIG. 1), and includes the pyrolyzer 20 and the pyrolyzed gas reformer 40. Is connected by a pyrolysis gas introduction pipe 200 that introduces the pyrolysis gas generated in the pyrolysis device 20 into the pyrolysis gas reformer 40.
  • one preheater 10 is provided above the thermal decomposition device 20, and the preheater 10 preheats the heat-bearing medium 30 supplied to the thermal decomposition device 20, and the heated heat.
  • the carrying medium 30 is supplied to the thermal decomposer 20, supplies heat necessary for thermal decomposition of biomass, is extracted from the bottom thereof, and is returned to the preheater 10 again.
  • the pyrolysis gas generated in the pyrolysis device 20 is introduced into the pyrolysis gas reformer 40 through the pyrolysis gas introduction pipe 200.
  • air or oxygen is separately introduced into the pyrolysis gas reformer 40 from the air or oxygen introduction pipes 261,262, whereby the pyrolysis gas is partially burned, and at the same time, steam is generated. It is introduced from the steam inlet 242, the pyrolysis gas is reformed by steam, and the reformed gas obtained thereby is taken out from the reformed gas discharge port 230. Further, instead of the above-mentioned air or oxygen introduction pipe 261 and steam injection port 242, the air or oxygen and steam are provided in the heat decomposition gas introduction pipe 200, and the air or oxygen introduction pipe 262 and the steam injection port 243 are provided. It can be introduced from, or it can be introduced from all air or oxygen introduction pipes 261,262 and steam inlets 242 and 243.
  • the inner diameter of the straight body portion of the pyrolyzer 20 is about 550 mm, the height is about 1100 mm, and the internal volume is about 260 liters.
  • the inner diameter of the straight body portion of the pyrolysis gas reformer 40 is about 600 mm, the height is about 1200 mm, and the internal volume is about 340 liters.
  • the pyrolysis gas introduction pipe 200 is provided on the side of the pyrolyzer 20 on the side of the pyrolyzer 20 below the upper surface of the heat-bearing medium layer formed in the pyrolyzer 20. On the pyrolysis gas reformer 40 side, it is provided on the side surface near the bottom surface of the pyrolysis gas reformer 40. Further, the pyrolysis gas introduction pipe 200 is provided substantially horizontally with respect to the direction of gravity.
  • a pipe having a length of about 1000 mm and an inner diameter of about 80 mm is used, the inside thereof is covered with a heat insulating material, and the protruding portion is also formed of the heat insulating material.
  • a substantially spherical alumina ball having a diameter (maximum diameter) of 10 to 12 mm is used.
  • the heat-supporting medium 30 is pre-filled in the pyrolyzer 20 and the preheater 10 to a height of about 70% of each container, and then the heat-supporting medium 30 is charged in the preheater 10 at a temperature of about 700 ° C. Heated to. Next, the heat-supporting medium 30 is introduced from the top of the pyrolyzer 20 at an amount of 200 kilograms / hour, and an appropriate amount is extracted from the bottom of the pyrolyzer 20 to start circulation of the heat-supporting medium 30.
  • the gas phase temperature inside the pyrolyzer 20 and the temperature of the container itself gradually increased. While continuing such circulation of the heat-supporting medium 30, at the same time, the temperature of the heat-supporting medium 30 inside the preheater 10 is gradually raised to 800 ° C. After the heat-bearing medium 30 reaches the temperature, the circulation is further continued to gradually raise the gas phase temperature inside the pyrolyzer 20 from the time when the gas phase temperature of the pyrolyzer 20 exceeds 550 ° C.
  • the biomass raw material, nitrogen gas and steam are introduced into the pyrolyzer 20 from the biomass supply port 220, the non-oxidizing gas supply port 250 and the steam inlet 241 respectively, and the temperature of the pyrolyzer 20 becomes 600 ° C. To control.
  • the heat-supporting medium 30 is deposited in layers in the pyrolyzer 20, and the accumulated amount is about 60% by volume of the internal volume of the pyrolyzer 20.
  • the amount of the heat-carrying medium 30 extracted from the pyrolyzer 20 is the same as the supply amount, and is 200 kilograms / hour in the pyrolyzer 20.
  • the temperature of the heat-supporting medium 30 at the time of extraction is 650 ° C. However.
  • the amount of the heat-carrying medium 30 extracted from the pyrolyzer 20 can be appropriately controlled according to the temperature condition.
  • the amount of sewage sludge as a biomass raw material is gradually increased from the biomass supply port 220 to the pyrolyzer 20 using a quantitative feeder, and finally about 22 kg / hour (drying standard). ) Is introduced continuously.
  • the temperature of the pyrolyzer 20 gradually decreases with the introduction of the biomass raw material, but at the same time, by introducing nitrogen gas and superheated steam into the pyrolyzer 20 while adjusting the supply amount thereof, the pyrolyzer 20 is introduced.
  • the temperature of 20 is maintained at 600 ° C. Further, the pressure in the pyrolyzer 20 is maintained at 101.3 kPa.
  • nitrogen gas is finally introduced at a fixed amount of 1000 liters / hour from the non-oxidizing gas supply port 250 provided in the upper part of the pyrolyzer 20.
  • superheated steam 160 ° C., 0.6 MPa
  • the residence time of the biomass raw material in the pyrolyzer 20 is about 1 hour.
  • the gas generated by the thermal decomposition in the pyrolyzer 20 is obtained at 15 kilograms / hour.
  • char and ash are discharged from the pyrolysis residue (char) outlet 210 at a total of 6.5 kg / hour.
  • the pyrolysis gas obtained in the pyrolysis device 20 subsequently passes through the pyrolysis gas introduction pipe 200 from the lower side surface of the pyrolysis device 20 and is introduced into the pyrolysis gas reformer 40.
  • the temperature inside the pyrolysis gas reformer 40 becomes unstable, but the superheated steam introduced from the steam inlet 242 provided at the bottom of the pyrolysis gas reformer 40
  • the pyrolysis gas is partially combusted and the temperature inside the pyrolysis gas reformer 40 is adjusted to 1000 ° C. do.
  • the pyrolysis gas reformer 40 is held at a pressure of 101.3 kPa.
  • the superheated steam from the steam inlet 242 provided at the bottom of the pyrolysis gas reformer 40 was finally introduced at a fixed amount of 3.7 kg / hour.
  • Oxygen from the air or oxygen inlet 261 is finally introduced at a fixed amount of 2.3 m 3-normal / hour.
  • this amount of oxygen is appropriately increased or decreased depending on the degree of temperature rise inside the pyrolysis gas reformer 40.
  • the pyrolyzer 20 is held at a temperature of 600 ° C. and a pressure of 101.3 kPa, and the pyrolyzed gas reformer 40 is held at a temperature of 950 ° C. and a pressure of 101.3 kPa.
  • the reformed gas having a temperature of 1000 ° C. is obtained from the reformed gas outlet 230 at an amount of 31 kg / hour.
  • the obtained reformed gas is collected in a rubber bag, and the gas composition is measured by gas chromatography. Table 3 shows the composition of the obtained reformed gas.
  • the operation can be carried out continuously for 3 days. During the operation period, good continuous operation can be maintained without troubles, especially troubles caused by tar. Further, during the operation period, the heat-supporting medium 30 does not become blocked by tar or the like in the pyrolysis gas introduction pipe 200, and the pyrolysis gas from the pyrolysis device 20 to the pyrolysis gas reformer 40 does not occur. Smooth introduction is maintained.
  • the amount of tar in the reformed gas taken out from the outlet of the pyrolysis gas reformer 40 is about 10 mg / m 3- normal.
  • the pressure fluctuation of the pyrolyzer 20 is suppressed, and the problem of deterioration of the separability in gas separation is a problem. It is possible to solve the problem and provide a gas with stable quality.
  • the biomass gasifier of the present embodiment includes a preheater, a pyrolysis device 20, and a pyrolysis gas reformer 40, and further, the pyrolysis gas reformer 40 is always placed in the pyrolysis gas reformer 40.
  • a manual valve 41 that supplies a fixed amount of oxygen
  • an on-off valve 42 that supplies oxygen on and off to the pyrolysis gas reformer 40
  • Stable hydrogen can be supplied by approaching the temperature, stabilizing the reforming reaction, and stabilizing the hydrogen concentration.

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  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • Physics & Mathematics (AREA)
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  • Water Supply & Treatment (AREA)
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  • Treatment Of Sludge (AREA)

Abstract

Dispositif de gazéification de biomasse qui comprend : un préchauffeur (10) qui préchauffe un milieu caloporteur (30) ; un pyrolyseur (20) qui est alimenté par le milieu caloporteur (30) préchauffé par le préchauffeur (10) et pyrolyse de la biomasse avec la chaleur du milieu caloporteur (30) ; un reformeur de gaz de pyrolyse (40) qui, au moyen d'air ou d'oxygène, brûle au moins partiellement un gaz de pyrolyse généré par la pyrolyse ; et une unité d'alimentation qui fournit de l'air ou de l'oxygène au reformeur de gaz de pyrolyse (40). L'unité d'alimentation comprend une première vanne d'alimentation en air ou oxygène en continu au reformeur de gaz de pyrolyse (40), et une seconde vanne d'alimentation en air ou oxygène par intermittence au reformeur de gaz de pyrolyse (40).
PCT/JP2021/017235 2020-04-30 2021-04-30 Dispositif de gazéification de biomasse WO2021221164A1 (fr)

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2004307682A (ja) * 2003-04-08 2004-11-04 Nippon Steel Corp 可燃性廃棄物のガス化方法および装置
WO2019065851A1 (fr) * 2017-09-29 2019-04-04 株式会社ジャパンブルーエナジー Dispositif de gazéification de biomasse
WO2020008622A1 (fr) * 2018-07-06 2020-01-09 株式会社 翼エンジニアリングサービス Procédé de production hydrogène utilisant la biomasse comme matière première

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2004307682A (ja) * 2003-04-08 2004-11-04 Nippon Steel Corp 可燃性廃棄物のガス化方法および装置
WO2019065851A1 (fr) * 2017-09-29 2019-04-04 株式会社ジャパンブルーエナジー Dispositif de gazéification de biomasse
WO2020008622A1 (fr) * 2018-07-06 2020-01-09 株式会社 翼エンジニアリングサービス Procédé de production hydrogène utilisant la biomasse comme matière première

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