WO2021221165A1 - Dispositif de gazéification de biomasse - Google Patents

Dispositif de gazéification de biomasse Download PDF

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Publication number
WO2021221165A1
WO2021221165A1 PCT/JP2021/017236 JP2021017236W WO2021221165A1 WO 2021221165 A1 WO2021221165 A1 WO 2021221165A1 JP 2021017236 W JP2021017236 W JP 2021017236W WO 2021221165 A1 WO2021221165 A1 WO 2021221165A1
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WIPO (PCT)
Prior art keywords
heat
pyrolyzer
biomass
housing
medium
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PCT/JP2021/017236
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English (en)
Japanese (ja)
Inventor
直城 堂脇
恒 上内
Original Assignee
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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Application filed by 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 filed Critical 株式会社ジャパンブルーエナジー
Priority to US17/922,347 priority Critical patent/US20230174877A1/en
Priority to JP2022518154A priority patent/JPWO2021221165A1/ja
Publication of WO2021221165A1 publication Critical patent/WO2021221165A1/fr

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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
    • 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
    • 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
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1246—Heating the gasifier by external or indirect heating
    • 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
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
    • 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

Definitions

  • the present invention relates to a biomass gasification device using a heat-supporting medium.
  • 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 spherical ceramic balls which are heat-supporting media housed in the preheater and the pyrolyzer, hardly move and may stay.
  • the present invention has been made in view of these points, and provides a biomass gasification device capable of smoothly moving a heat-carrying medium housed in a temporary holding portion such as a preheater or a pyrolyzer. do.
  • the biomass gasifier according to the present invention A biomass gasifier equipped with a temporary holding section for temporarily accommodating and discharging a heat-carrying medium.
  • the temporary holding part is With the housing
  • the partition wall provided in the housing and A discharge portion provided below the partition wall for discharging the heat-carrying medium, and a discharge portion.
  • a gap may be provided between the partition wall and the inner wall of the side portion of the housing for passing the heat-carrying medium, and the tube portion for passing the heat-carrying medium through the inner wall of the side portion of the housing. May be provided.
  • the temporary holding portion is a preheater that preheats the heat-supporting simple substance.
  • the discharge part is a preheater discharge part, and is The heat-supporting medium discharged from the preheater discharge unit may be supplied to the pyrolyzer.
  • the temporary holding unit is a thermal cracker that receives a supply of a heat-supporting medium preheated by a preheater and executes thermal decomposition of biomass by the heat of the heat-supporting medium.
  • the discharge part is a pyrolyzer discharge part, and is The heat-carrying medium discharged from the pyrolyzer discharge unit may be supplied to the preheater via the circulation unit.
  • the front surface of the partition wall is positioned so that the central region is higher than the peripheral region, and an inclined surface may be provided between the central region and the peripheral region.
  • the back surface of the partition wall is positioned at a position where the central region is lower than the peripheral region, and an inclined surface may be provided between the central region and the peripheral region.
  • a plurality of fixing members for fixing the main body to the housing are provided between the main body of the partition and the inner side wall of the housing, and the gap between the fixing members is heat-supported. It may be a gap for the medium to pass through.
  • the main body of the partition has a disk shape.
  • the main body may be fixed to the housing by a fixing member provided between the inner side wall of the housing or a fixing member provided on the back surface of the main body.
  • the housing has an upper tank and a lower tank provided below the upper tank.
  • the cross section of the lower end of the upper tank is smaller than the cross section of the upper end of the lower tank.
  • a partition wall is provided below the lower end of the upper tank. A gap may be formed between the partition wall and the lower tank.
  • a gap for passing the heat-supporting medium is provided between the partition wall and the inner wall of the side portion of the housing, or a tube portion for passing the heat-supporting medium through the inner wall of the side portion of the front housing.
  • the heat-carrying medium housed in the temporary holding portion such as a preheater or a pyrolyzer can be smoothly moved.
  • FIG. 1 is a schematic view showing one form of a biomass gasification device.
  • FIG. 2 is a diagram showing the movement (before movement) of the heat-carrying medium in the pyrolyzer in the biomass gasifier of the present embodiment.
  • FIG. 3 is a diagram showing the movement (after movement) of the heat-carrying medium in the pyrolyzer in the biomass gasifier of the reference example.
  • FIG. 4 is a diagram showing the movement (before movement) of the heat-carrying medium in the pyrolyzer in the biomass gasifier of the present embodiment.
  • FIG. 5 is a diagram showing the movement (after movement) of the heat-carrying medium in the pyrolyzer 20 in the biomass gasification device of the present embodiment.
  • FIG. 6 is a diagram showing an example of a partition wall installed in the lower tank in the biomass gasification device of the present embodiment.
  • FIG. 7 is a diagram showing one aspect of the preheater in the biomass gasification device of the present embodiment.
  • FIG. 8 is a diagram showing one aspect of a pyrolyzer in the biomass gasification device of the present embodiment.
  • FIG. 9 is a diagram showing another aspect of the preheater in the biomass gasifier of the present embodiment.
  • FIG. 10 is a diagram showing another aspect of the pyrolyzer in the biomass gasifier of the present embodiment.
  • FIG. 11 is a schematic view showing another form of the biomass gasifier.
  • FIG. 12 is a plan view showing a mode in which a plurality of fixing members are provided between the main body of the partition wall and the inner side wall of the housing.
  • 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 control device 100 (see FIG. 11) that performs various controls.
  • 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 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.
  • the biomass gasifier of the present embodiment has temporary holding units 10 and 20 for accommodating the heat-supporting medium 30 to be supplied and discharging the heat-supporting medium 30.
  • the temporary holding portions 10 and 20 are provided in the housings 111 and 121 and the housings 111 and 121, and are provided below the partition walls 115 and 125 having a front surface and the partition walls 115 and 125 to generate heat. It has discharge sections 119 and 129 for discharging the carrier medium 30.
  • a gap G may be provided between the partition walls 115 and 125 and the side inner walls of the housings 111 and 121 for the heat-supporting medium 30 to pass through (see FIGS. 7 and 8).
  • the temporary holding portion means the preheater 10 and the pyrolyzer 20.
  • partition walls 115 and 125 may be provided inside the housings 111 and 121 of the preheater 10 and the pyrolyzer 20 respectively.
  • the preheater 10 is provided in the preheating housing 111, the preheating housing 111, and has a front surface, and is below the preheating partition 115 and the preheating partition 115. It may have a preheater discharge unit 119 for discharging the heat-carrying medium 30.
  • the heat-carrying medium 30 discharged from the preheater discharge unit 119 is supplied from the top surface of the pyrolyzer 20 to the inside of the pyrolyzer 20 provided below.
  • a gap G is provided between the inner wall of the side portion of the preheating housing 111 and the preheating partition wall 115, and the heat-carrying medium 30 falls downward through the gap G.
  • the pyrolyzer 20 is provided in the pyrolysis housing 121 and the pyrolysis housing 121 and has a front surface, and is more than the pyrolysis partition 125 and the pyrolysis partition 125. It may have a pyrolyzer discharge unit 129, which is provided below and discharges the heat-bearing medium 30.
  • a gap G is provided between the inner wall of the side portion of the pyrolysis housing 121 and the pyrolysis partition wall 125, and the heat-carrying medium 30 falls downward through the gap G.
  • the heat-carrying medium 30 discharged from the pyrolyzer discharge unit 29 is returned to the preheater 10 provided above via the discharge treatment unit 240 and the circulation unit 290 (see FIG. 1).
  • pipe portions 131 and 141 for passing the heat-carrying medium 30 may be provided on the inner wall of the side portions of the housings 111 and 121.
  • a preheating tube portion 131 for passing the heat-carrying medium 30 is provided on the inner wall of the side portion of the preheating housing 111, and by passing through the preheating tube portion 131, The heat-carrying medium 30 may be supplied from above to the pyrolyzer 20 provided below.
  • a thermal decomposition tube portion 141 for passing the heat carrying medium 30 is provided on the inner wall of the side portion of the thermal decomposition housing 121, and the heat is generated by passing through the thermal decomposition tube portion 141.
  • the carrying medium 30 may be discharged from above with respect to the discharge processing unit 240 provided below.
  • the partition walls 115 and 125 may be provided inside the housings 111 and 121.
  • the pyrolyzer 20 and / or the preheater 10 is a moving floor having upper tanks 111a, 121a and bottom cone-shaped lower tanks 111b, 121b, and the heat-carrying medium 30 in the upper tanks 111a, 121a is once the upper tank.
  • It may have a structure in which the lower tanks 111b and 121b are discharged from the bottom of the tank to the outside.
  • the pyrolyzer 20 located below the preheater 10 in the biomass gasifier is provided with an inlet 127 for the heat-bearing medium 30 (see FIG. 1) at the top (upper part), preferably at the top, for thermal decomposition.
  • a discharge port for the heat-bearing medium 30 (this discharge port constitutes the pyrolyzer discharge section 129) is provided below (lower), preferably at the bottom, of the vessel 20.
  • a so-called two-stage valve system is provided above the introduction port 127 of the heat-carrying medium 30 and below the pyrolyzer discharge unit 129, for example, having a total of two valves, one above and one below the pipe. May be good.
  • a first valve 50 may be 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, even if the control device 100 controls so that the first opening / closing portion is opened while the second opening / closing portion is closed and the second opening / closing portion is opened while the first opening / closing portion is closed. good.
  • 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 upper and lower first damper valves 51a and the second damper valve 51b are closed, and first, the upper first damper valve 51a is opened to drop the heat carrier into the pipe, and between the second damper valve 51b and the first damper valve 51a. Is filled with a heat carrier.
  • the heat carrier filled between the first damper valve 51a and the second damper valve 51b is introduced into the pyrolyzer 20 or the pyrolyzer 20 is introduced. Extract from.
  • the heat carrier is introduced into the pyrolyzer 20 substantially continuously and is withdrawn from the pyrolyzer 20 substantially continuously.
  • the introduction / extraction method is an example, and the method is not limited to this method.
  • 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, and the soot contained in the biomass gas falls downward through the filter F and does not pass through the filter F. 30 is circulated by a circulation unit 290 composed of an elevator type, an escalator type, etc., and is charged into the preheater 10.
  • the preheater 10 is preferably provided on the upper part of the pyrolyzer 20, where all the heat-bearing media 30 are heated to a predetermined temperature, and the heat-bearing medium 30 heated to the temperature is brought into the pyrolyzer. Can be supplied to 20.
  • the pyrolyzer 20 and / or the preheater 10 is a moving floor having upper tanks 111a, 121a and bottom cone-shaped lower tanks 111b, 121b, and the heat-carrying medium 30 in the upper tanks 111a, 121a is once the upper tank 111a.
  • 121a after being laterally discharged to the outside of the upper tanks 111a, 121a, descend along the tank walls of the lower tanks 111b, 121b, move to the lower tanks 111b, 121b, and further, the lower tanks 111b, 121b. It may have a structure in which the lower tanks 111b and 121b are discharged from the bottom to the outside.
  • the pyrolyzer 20 was designed as a volume for gasifying a predetermined amount of biomass, which was found in conventional moving beds, but only a small volume in the central part where the heat medium moves is gasified.
  • the problem that it cannot be used and a predetermined amount cannot be gasified and the problem that the preheated heat-bearing medium 30 in the preheater 10 does not move smoothly to the pyrolyzer 20 can be solved, and the volume can be effectively used evenly. , Efficient thermal decomposition of biomass can be achieved.
  • FIG. 3 shows a mode in which the partition wall used in the present embodiment is not provided. According to this mode, the heat-carrying medium 30 colored in black is bent so as to protrude downward, and heat is generated near the center. Although the carrier medium 30 is easy to fall, it was confirmed that the heat carrier medium 30 is hard to fall at the peripheral portion and a difference is formed in the circulated heat carrier medium 30.
  • the partition walls 115 and 125 are provided inside the housings 111 and 121, as shown in FIGS. 2, 4 and 5, the heat-carrying medium 30 colored in black is lowered while maintaining a horizontal state. The heat-carrying medium 30 could be moved downward without bias.
  • the shapes of the upper tanks 111a and 121a are not particularly limited as long as the heat-carrying medium 30 can be moved to the lower part, but are preferably cylindrical or square.
  • the shape of the floors of the lower tanks 111b and 121b is not particularly limited as long as the heat-supporting medium 30 can be discharged from the bottom of the lower tanks 111b and 121b, but an inverted conical shape and an inverted conical trapezoid are preferable.
  • the cross section of the lower end of the upper tanks 111a, 121a may be smaller than the cross section of the upper end of the lower tanks 111b, 121b.
  • the diameter of the lower end portions of the upper tanks 111a and 121a may be smaller than the diameter of the upper end portions of the lower tanks 111b and 121b.
  • the upper surface of the upper end portion of the lower tanks 111b, 121b and the lower surface of the lower end portion of the upper tanks 111a, 121a are continuously provided, and the uppermost portion of the lower tanks 111b, 121b is the maximum of the lower tanks 111b, 121b.
  • a top may be provided extending from the outer position to the lower ends of the upper tanks 111a, 121a.
  • upper outer tanks 111c and 121c and upper tanks 111a and 121a are provided in the outer peripheral tanks 111c and 121c, and the outer peripheral tanks 111c and 111c are provided.
  • the region below the upper tanks 111a and 121a of 121c may form the lower tanks 111b and 121b.
  • upper partition walls 115 and 125 extending in the in-plane direction and lower partition walls 115 and 125 extending in the vertical direction are provided in the lower tanks 111b and 121b. There is. In some cases, the effect of smoothly flowing the heat-carrying medium 30 can be expected by providing the partition walls 115 and 125 extending in the vertical direction.
  • the partition walls 115 and 125 may be provided below the lower ends of the upper tanks 111a and 121a, and the lower tanks 111b and 121b may be provided outside the peripheral edges of the partition walls 115 and 125.
  • the opening 23 is formed between the lower ends of the upper tanks 111a and 121a and the partition walls 115 and 125 in the vertical direction (see FIGS. 4 and 5). Further, a gap G is formed between the partition walls 115 and 125 and the lower tanks 111b and 121b in the in-plane direction.
  • the heat-carrying medium 30 once spreads out of the peripheral edge of the upper tanks 111a and 121a through the opening 23, and goes out of the peripheral edge in the in-plane direction of the upper tanks 111a and 121a through the gap G. It will move to the lower tanks 111b and 121b.
  • the partition walls 115 and 125 may be installed in the central portion of the lower tanks 111b and 121b.
  • the centers of the upper tanks 111a, 121a, the lower tanks 111b, 121b, and the partition walls 115, 125 in the in-plane direction may be aligned. According to such an aspect, it is advantageous in that the heat-carrying medium 30 can be uniformly flowed in the in-plane direction.
  • the shapes of the partition walls 115 and 125 are not particularly limited as long as they achieve the above object, but when the lower tanks 111b and 121b have an inverted conical shape or an inverted conical trapezoidal shape, the upper tanks 111a and 121a and the lower portions It is preferable that the partition walls 115 and 125 are installed under the partition walls 115 and 125 with the tanks 111b and 121b and are selected from the group consisting of a conical shape, an inverted conical shape and a coma shape.
  • the front surface (upper surface in the present embodiment) of the partition walls 115 and 125 is positioned at a higher position in the central region than the peripheral region, and an inclined surface is provided between the central region and the peripheral region. You may become like this.
  • conical see FIG. 6A
  • prefix conical bulkheads 115, 125 with vertices pointing upwards may be provided, according to this embodiment, to the lower tanks 111b, 121b of the heat carrier 30. Good discharge (see FIG. 6A).
  • the back surfaces of the partition walls 115 and 125 are positioned so that the central region is positioned lower than the peripheral region, and an inclined surface is provided between the central region and the peripheral region. May become.
  • septa 115, 125 having a conical shape with the apex facing downward (see FIG. 6B) or a prefix conical shape may be provided. According to this aspect, since the central portions of the partition walls 115 and 125 are thickened, the resistance to bending stress by the heat-supporting medium 30 becomes better (see FIG. 6B).
  • FIGS. 6A and 6B may be combined, and as an example, the coma-shaped partition walls 115 and 125 as shown in FIG. 6C may be adopted.
  • This aspect can comprise the performance of both the aspect shown in FIG. 6A and the aspect shown in FIG. 6B (see FIG. 6C).
  • the lower tanks 111b and 121b are pyramidal, they are pyramid-shaped or inverted pyramid-shaped bulkheads 115 and 125 installed under the partition walls 115 and 125 between the upper tanks 111a and 121a and the lower tanks 111b and 121b. Is preferable.
  • the heat-carrying medium 30 moves in the lower tanks 111b and 121b in the flow indicated by the arrows in FIGS. 6A to 6C, and the lower tanks 111b and 121b It is discharged to the outside.
  • the fixing member 130 of the above may be provided.
  • the gap between the fixing members 130 may be a gap G for the heat-carrying medium to pass through.
  • the main bodies 115a and 125a of the partition walls 115 and 125 may have a disk shape (see FIG. 12).
  • the main bodies 115a and 125a may be fixed to the housings 111 and 121 by a fixing member 130 provided between the main bodies 115a and 125a and the inner side walls of the housings 111 and 121. Further, as shown in FIGS. 7 and 8, the fixing members 130 provided on the back surfaces of the main bodies 115a and 125a may be fixed to the housings 111 and 121.
  • the embodiment of the present embodiment may be incorporated into a 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 pyrolyzer 20 and / or the preheater 10 is a moving floor having upper tanks 111a, 121a and bottom cone-shaped lower tanks 111b, 121b, and the heat-supporting medium 30 in the upper tanks 111a, 121a is once the upper tank 111a.
  • 121a is discharged laterally from the lower part to the outside of the upper tanks 111a and 121a, then descends along the tank wall of the lower tanks 111b and 121b to move to the lower tanks 111b and 121b, and further to the lower tanks 111b and 121b. It is possible to provide a biomass gasification device having a structure in which the bottom tanks 111b and 121b are discharged to the outside.
  • 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 pyrolyzer 20 and / or the preheater 10 is a moving floor having upper tanks 111a, 121a and bottom cone-shaped lower tanks 111b, 121b, and the heat-supporting medium 30 in the upper tanks 111a, 121a is once the upper tank 111a.
  • 121a is discharged laterally from the lower part to the outside of the upper tanks 111a and 121a, then descends along the tank wall of the lower tanks 111b and 121b to move to the lower tanks 111b and 121b, and further to the lower tanks 111b and 121b. It is possible to provide a biomass gasification device having a structure in which the bottom tanks 111b and 121b are discharged to the outside.
  • 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 the heat in the presence of steam, and the preheated heat-supporting medium 30 is charged into the pyrolyzer 20 to bring the heat-supporting medium 30 into the pyrolyzer 20.
  • Pyrolysis of the biomass is carried out by the heat possessed, and then the pyrolysis gas generated by the pyrolysis of the biomass is introduced into the pyrolysis gas reformer 40 to carry out 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.
  • the heat-supporting medium 30 is contained in the upper tanks 111a, 121a in the pyrolyzer 20 having the upper tanks 111a, 121a and the bottom cone-shaped lower tanks 111b, 121b. After being discharged laterally from the lower part to the outside of the upper tanks 111a and 121a, it descends along the tank wall of the lower tanks 111b and 121b, moves to the lower tanks 111b and 121b, and further from the bottom of the lower tanks 111b and 121b. A method for gasifying biomass, which is discharged to the outside of the lower tanks 111b and 121b, is provided.
  • the heat-supporting medium 30, that is, the heat carrier, is preheated in the preheater 10 before being introduced into the pyrolyzer 20.
  • 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 a 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 remaining after being gasified are discharged from the bottom of the pyrolyzer 20 while still adhering to the heat-bearing medium 30.
  • the pyrolyzer 20 and / or the preheater 10 is a moving floor having upper tanks 111a and 121a and bottom cone-shaped lower tanks 111b and 121b.
  • the heat-supporting medium 30 introduced from the preheater 10 into the pyrolyzer 20 first enters the upper tanks 111a and 121a of the pyrolyzer 20.
  • the heat-carrying medium 30 is once discharged laterally from the opening 23 at the bottom of the upper tanks 111a and 121a to the outside of the upper tanks 111a and 121a.
  • the heat-supporting medium 30 introduced into the lower tanks 111b and 121b descends along the tank wall of the lower tanks 111b and 121b, moves to the lower part of the lower tanks 111b and 121b, and further moves from the bottom of the lower tanks 111b and 121b to the lower tank. It is discharged to the outside of 111b and 121b.
  • the lower tanks 111b and 121b are provided with partition walls 115 and 125 installed in the central portion and which promote the movement of the heat-carrying medium 30 to the bottom of the lower tanks 111b and 121b.
  • the partition walls 115 and 125 prevent the heat-carrying medium 30 from moving along the heat-carrying medium 30 and staying inside the lower tanks 111b and 121b, thereby promoting the movement to the bottom of the lower tanks 111b and 121b. do.
  • the heat-supporting medium layer is formed in the pyrolyzer 20 and the thickness of the layer is formed.
  • the temperature can be controlled to an appropriate value, and the temperature of the pyrolyzer 20 can be controlled to the above-mentioned predetermined temperature.
  • the heat-bearing medium 30 is introduced only into the thermal cracker 20, and the heat is used to thermally decompose the biomass, while steam and oxygen or air are introduced into the thermal decomposition gas reformer 40.
  • the internal temperatures of the pyrolyzer 20 and the pyrolysis gas reformer 40 can be controlled individually. As a result, the reforming reaction in the pyrolysis gas reformer 40 can be carried out at an appropriate temperature, and the thermal decomposition of biomass in the pyrolysis device 20 can be carried out at an appropriate temperature.
  • the residence time of biomass in the pyrolyzer 20 is preferably 5 to 60 minutes, more preferably 10 to 40 minutes, and even more preferably 15 to 35 minutes. If it is less than the above lower limit (5 minutes), heat is not uniformly transferred to the biomass and uniform pyrolysis is not performed, so that the amount of pyrolysis gas generated is reduced. On the other hand, even if the above upper limit (60 minutes) is exceeded, no significant increase in the effect is observed, and on the contrary, the equipment cost increases.
  • the residence time of biomass in the pyrolyzer 20 can be appropriately adjusted from the moving speed of the heat-carrying medium 30 and the amount of biomass supplied.
  • the residence time in each container that is, the residence time for biomass pyrolysis in the pyrolysis device 20, and the tar in the pyrolysis gas. It was impossible to individually control the residence time for decomposition of the pyrolysis and the residence time required for the reformation reaction between the pyrolysis gas and steam in the pyrolysis gas reformer 40.
  • heating only the thermal decomposition device 20 with the heat-bearing medium 30, and separately introducing steam and oxygen or air into the thermal decomposition gas reformer 40 heating is performed by partial oxidation of the thermal decomposition gas. Since the residence time in each of the thermal decomposition device 20 and the thermal decomposition gas reformer 40 can be controlled independently, the temperature inside each of the thermal decomposition device 20 and the thermal decomposition gas reformer 40 can be controlled independently. Can be controlled.
  • the heat-supporting medium 30 that has passed through the thermal decomposition device 20 contains the thermal decomposition residue (char) of the biomass, and a small amount of tar and soot and dust that have adhered to the heat-supporting medium 30 and remain without being pyrolyzed. Together, it is discharged from the bottom of the pyrolyzer 20.
  • the treatment of the discharged material including the discharged heat-supporting medium 30 is carried out by a conventionally known method such as separating the char in the discharge processing unit.
  • the heat-supporting medium 30 treated in this manner is returned to the preheater 10 again and supplied to the pyrolyzer 20.
  • 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.
  • biomass raw material used in the examples and the gasifier used for the thermal decomposition and gas reforming of the biomass raw material are as follows.
  • 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, for air or oxygen and steam, instead of the above-mentioned air or oxygen introduction pipe (261) and steam injection port 242, the air or oxygen introduction pipe 262 and steam injection provided in the heat decomposition gas introduction pipe 200 are provided. It can be introduced from the port 243, or can be introduced from all the air or oxygen introduction pipes 261,262 and the 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. Heat 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 rise. While continuing the circulation of the heat-supporting medium 30, 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 was the same as the supply amount, and was 200 kg / 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 can be 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 is 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 reformed gas can be obtained, and by realizing the stable continuous supply of the heat-carrying medium 30 in the gasifier, the pressure fluctuation of the pyrolyzer 20 is suppressed, and the separation ability in gas separation is lowered. It is possible to solve the problem and provide a gas with stable quality.
  • the heat-bearing medium 30 is once laterally discharged from the lower part of the cylindrical body to the outside of the upper tanks 111a and 121a in the pyrolyzer 20 and / or the preheater 10. , It descends along the tank wall of the lower tanks 111b, 121b, moves to the lower tanks 111b, 121b, and further discharges from the bottom of the lower tanks 111b, 121b to the outside of the lower tanks 111b, 121b. In, the heat-bearing medium 30 drops uniformly in the width direction, the volume can be effectively used evenly, and efficient thermal decomposition of biomass can be achieved.
  • the biomass gasifier of the present embodiment can generate a reformed gas containing a large amount of valuable gas such as hydrogen from biomass, preferably biomass having a relatively high ash content, and is contained in the biomass. not only can prevent clogging and corrosion of the piping caused by the volatilization of diphosphorus pentoxide and potassium (potassium) contained in the ash, resulting suppressing the occurrence of N 2 O, and the generation amount of tar and dust It is expected that it will be widely used as a gasifier for biomass, especially biomass with a relatively high ash content, because it can be reduced.
  • Preheater temporary hold
  • Pyrolyzer temporary hold
  • Heat-supporting medium 40 Pyrolysis gas reformer 111
  • Preheating housing 121 Pyrolysis housing (housing) 111a, 121a Upper tank 111b, 121b Lower tank 115,125 Partition wall 119,129 Discharge section 131,141 Pipe section

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Abstract

L'invention concerne un dispositif de gazéification de biomasse équipé d'une unité de stockage temporaire (10, 20) dans laquelle un milieu caloporteur (30) est stocké temporairement et à partir de laquelle le milieu caloporteur (30) est déchargé. L'unité de stockage temporaire comprend un logement (111, 121) et une unité de décharge (119, 129) pour décharger le milieu caloporteur. Dans le logement (111, 121), une paroi de séparation (115, 125) est disposée pour former un espace dans lequel le milieu caloporteur peut passer entre la paroi de séparation (115, 125) et une paroi interne de partie latérale du logement (111, 121) ou, en variante, une partie tubulaire (131, 141) à travers laquelle le milieu caloporteur peut passer est disposée au niveau d'une paroi interne de partie latérale du logement (111, 121).
PCT/JP2021/017236 2020-04-30 2021-04-30 Dispositif de gazéification de biomasse WO2021221165A1 (fr)

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS56500256A (fr) * 1978-03-02 1981-03-05
US20120073198A1 (en) * 2009-05-28 2012-03-29 Prerak Goel Process for generating energy from organic materials and/or biomass
WO2013172301A1 (fr) * 2012-05-18 2013-11-21 株式会社ジャパンブルーエナジー Dispositif gazéifieur de biomasse
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 (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS56500256A (fr) * 1978-03-02 1981-03-05
US20120073198A1 (en) * 2009-05-28 2012-03-29 Prerak Goel Process for generating energy from organic materials and/or biomass
WO2013172301A1 (fr) * 2012-05-18 2013-11-21 株式会社ジャパンブルーエナジー Dispositif gazéifieur de biomasse
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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