WO2014171393A1 - ガス化ガス生成システム - Google Patents
ガス化ガス生成システム Download PDFInfo
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- WO2014171393A1 WO2014171393A1 PCT/JP2014/060407 JP2014060407W WO2014171393A1 WO 2014171393 A1 WO2014171393 A1 WO 2014171393A1 JP 2014060407 W JP2014060407 W JP 2014060407W WO 2014171393 A1 WO2014171393 A1 WO 2014171393A1
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- gasification
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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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
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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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
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- 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
- C10K3/02—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 catalytic treatment
- C10K3/023—Reducing the tar content
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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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/12—Heating the gasifier
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1853—Steam reforming, i.e. injection of steam only
Definitions
- the present invention relates to a gasification gas generation system that generates gasification gas by gasifying a gasification raw material.
- This application claims priority based on Japanese Patent Application No. 2013-85131 for which it applied to Japan on April 15, 2013, and uses the content here.
- gasified raw materials such as unused fuel such as coal, biomass, and tire chips are gasified to generate gasified gas instead of oil.
- the gasified gas thus generated is used for power generation systems, hydrogen production, synthetic fuel (synthetic petroleum) production, chemical fertilizer (urea) and other chemical products.
- gasification raw materials used as raw materials for gasification gas coal, in particular, has a recoverable period of about 150 years, which is more than three times the extractable period of oil, and reserves are unevenly distributed compared to oil. Therefore, it is expected as a natural resource that can be supplied stably over a long period of time.
- steam gasification that uses steam to gasify coal at about 700 to 900 ° C.
- the temperature can be reduced by setting the temperature low.
- the generated gasification gas often contains much tar as compared with the gasification gas generated by partial oxidation at a high temperature of 2000 ° C.
- the temperature of the gasification gas decreases in the process using the gasification gas generated by steam gasification, the tar contained in the gasification gas condenses, clogging the piping, failure of equipment used in the process, catalyst coverage. Problems such as poisoning occur.
- Patent Document 1 a technique for removing the tar contained in the gasification gas by burning the generated gasification gas with oxygen or air to 1100 ° C. or higher and oxidative reforming is disclosed (for example, Patent Document 1). ).
- the temperature of the oxidation reforming furnace for the oxidation reforming reaction needs to be 1100 ° C. or higher.
- the combustible gas (hydrogen or methane) in the gasification gas must be burned with oxygen or air. Therefore, the combustible gas in the gasified gas is consumed (combusted), and the gasified gas treated in the oxidation reforming furnace may have a reduced ratio of combustible gas per unit volume.
- the inventor of this application oxidizes and removes the tar in the gasification gas by contacting the gasification gas generated in the gasification furnace and the oxidant with the catalyst that promotes the tar reforming.
- Technology to develop In this technique, air at room temperature (about 25 ° C.) is used as an oxidizing agent for oxidizing and reforming tar, for example.
- an object of the present invention is to provide a gasified gas generator that can further suppress the reduction of combustible gas while efficiently removing tar.
- a gasification gas generation system has a gasification furnace that gasifies a gasification raw material to generate gasification gas, and a gasification gas generated in the gasification furnace circulates.
- a flow path a catalyst holding unit that holds a catalyst that promotes reforming of tar in the gasified gas in the flow path, and an oxidant supply unit that supplies an oxidant at 200 ° C to 900 ° C to the catalyst.
- the apparatus further includes a combustion furnace that heats the fluidized medium with the heat generated by burning the fuel, the fluidizing medium heated by the combustion furnace is introduced into the gasification furnace, The gasification raw material is gasified with heat, and the oxidant supply unit exchanges heat between the combustion exhaust gas generated by burning the fuel in the combustion furnace and the oxidant, so that the oxidant is 200 ° C to 900 ° C. You may heat so that it may become.
- the apparatus further includes a combustion furnace that heats the fluidized medium with the heat generated by burning the fuel, the fluidizing medium heated by the combustion furnace is introduced into the gasification furnace,
- the gasification raw material may be gasified by the heat it has, and the oxidant supply unit may supply the combustion exhaust gas of 200 ° C. to 900 ° C. generated by burning the fuel in the combustion furnace as the oxidant to the catalyst.
- steam may be introduced into the gasification furnace, and the gasification furnace may gasify the gasification raw material with steam.
- FIG. 1 is a conceptual diagram for explaining a gasified gas generation system 100 according to the first embodiment.
- the gasification gas generation system 100 includes a gasification gas generation device 110, a combustion exhaust gas treatment device 150, a tar reforming device 200, and a purification device 300.
- the flow of the gasification raw material, gas, water vapor, air, and oxidant is indicated by solid arrows
- the flow of the fluid medium (sand) is indicated by dashed-dotted arrows
- the signal flow is indicated by broken arrows.
- the gasified gas generator 110 includes a combustion furnace 112, a medium separator (cyclone) 114, and a gasifier 116.
- a fluid medium composed of sand such as silica sand having a particle size of about 300 ⁇ m is circulated as a heat medium.
- the fluid medium is first heated to about 1000 ° C. in the combustion furnace 112 and introduced into the medium separator 114 together with the combustion exhaust gas EX1.
- the medium separator 114 the high-temperature fluid medium and the combustion exhaust gas EX ⁇ b> 1 are separated, and the separated high-temperature fluid medium is introduced into the gasification furnace 116.
- the fluidized medium introduced into the gasification furnace 116 is fluidized by a gasifying agent (water vapor) introduced from the bottom surface of the gasification furnace 116, and finally returned to the combustion furnace 112.
- the combustion exhaust gas EX1 separated by the medium separation device 114 is discharged to the combustion exhaust gas treatment device 150 through the exhaust passage 118, processed by the combustion exhaust gas treatment device 150, and then discharged to the outside.
- the gasification furnace 116 is, for example, a bubbling fluidized bed gasification furnace, which uses gasification raw materials such as coal such as lignite, solid raw materials such as petroleum coke, biomass and tire chips, and liquid raw materials such as black liquor. Gasification gas is generated by gasification at 700 ° C to 900 ° C. In the present embodiment, by supplying water vapor to the gasification furnace 116, the gasification raw material is gasified to generate gasified gas (water vapor gasification).
- the gasification furnace 116 has been described by taking a circulating fluidized bed system as an example. However, if the gasification raw material can be gasified, the gasification furnace 116 may be a simple fluidized bed system or a sand having its own weight.
- the moving bed method may be used in which the moving bed is formed by flowing down vertically.
- the gasification gas X1 generated in the gasification furnace 116 contains tar, water vapor, and the like, the gasification gas X1 is sent to the downstream tar reforming device 200 and the purification device 300 and purified.
- the combustion exhaust gas treatment device 150 includes a boiler 152, a denitration device 154, and a desulfurization device 156.
- the boiler 152 recovers the heat of the combustion exhaust gas EX1 by performing heat exchange between the combustion exhaust gas EX1 separated by the medium separation device 114 and water.
- the denitration device 154 removes NOx (nitrogen oxide) from the combustion exhaust gas EX1 cooled by the boiler 152.
- the desulfurization device 156 removes SOx (sulfur oxide) from the combustion exhaust gas EX2 from which NOx has been removed by the denitration device 154.
- SOx sulfur oxide
- the tar reforming apparatus 200 includes a flow passage 210, a catalyst holding unit 220, an oxidant supply unit 230, a temperature measurement unit 240, and an oxidant control unit 250. .
- the flow passage 210 is a flow path through which the gasified gas X1 of about 700 ° C. generated in the gasification furnace 116 flows.
- the catalyst holding unit 220 holds a catalyst that promotes reforming of the tar in the gasification gas X ⁇ b> 1 in the flow passage 210.
- the catalyst is only required to promote tar reforming.
- a catalyst or an ore-based catalyst can be employed.
- the Ni-based catalyst only needs to contain at least Ni as the active species
- the Fe-based catalyst only needs to contain at least Fe as the active species
- the Ru-based catalyst has at least Ru as the active species.
- the Rh-based catalyst only needs to contain at least Rh as the active species
- the Co-based catalyst only needs to contain at least Co as the active species.
- Examples of the active species carrier in these catalysts include aluminum oxide (Al 2 O 3 ), zirconia (ZrO 2 ), cerium oxide (CeO 2 ), silicon oxide (SiO 2 ), magnesium (Mg), magnesium oxide ( MgO), natural ore can be used.
- the ore-based catalyst is an oxide or carbonate of one or more elements selected from the group of Ca (calcium), Mg, Fe, and Si (silicon).
- Ca calcium
- Mg magnesium
- Fe magnesium
- Si silicon
- dolomite olivine
- limonite It is a natural ore such as limestone.
- the oxidant supply unit 230 supplies an oxidant OX (eg, air, oxygen) at 200 ° C. to 900 ° C. to the catalyst in the flow passage 210.
- OX eg, air, oxygen
- the oxidant supply unit 230 supplies air as the oxidant OX to the catalyst by introducing the oxidant OX to the upstream side of the catalyst holding unit 220 in the flow passage 210.
- the oxidant supply unit 230 includes a blower 232, an oxidant supply path 234, and a heat exchanger 236.
- the blower 232 introduces air into the oxidant supply path 234.
- the oxidant supply path 234 is a flow path through which the oxidant OX flows, and connects the blower 232 and the upstream side of the catalyst holding unit 220 in the flow path 210. Therefore, the oxidant OX introduced by the blower 232 is supplied to the catalyst holding unit 220 (upstream of the catalyst holding unit 220 in the flow path 210) through the oxidant supply path 234.
- hydrogen sulfide (H2S) in the gasification gas X1 is adsorbed to the catalyst, but it can be decomposed and the catalyst is covered with sulfur derived from hydrogen sulfide. Poison (adsorption) can be reduced.
- linear unsaturated hydrocarbons eg, ethylene, acetylene, propylene, etc.
- tar are partially oxidized and decomposed into carbon monoxide and carbon dioxide. It is possible to reduce the poisoning (precipitation) of the catalyst by carbon derived from a linear unsaturated hydrocarbon.
- the configuration in which the oxidant supply unit 230 supplies the high-temperature oxidant OX such as 200 ° C. to 900 ° C. has a smaller amount than when the oxidant OX having a relatively low temperature (for example, 25 ° C.) is supplied. With hydrogen, it becomes possible to raise the temperature of the gasification gas X1 itself.
- suction rate of sulfur will be considered, and the preferable temperature of gasification gas X1 will be defined as optimal temperature. Necessary for raising the temperature of the gasification gas X1 to the optimum temperature when the oxidizing gas OX is supplied to burn part of the hydrogen in the gasification gas X1 in order to raise the temperature of the gasification gas X1 to the optimum temperature.
- the amount of hydrogen to be burned is relatively higher (eg, 200 ° C. to 900 ° C.) than oxidant OX supplied at a relatively low temperature (eg, 25 ° C.). Less if you did.
- the configuration in which the oxidant supply unit 230 supplies the high-temperature oxidant OX such as 200 ° C. to 900 ° C. to the catalyst compared to the case where the relatively low-temperature oxidant OX is supplied to the catalyst, combustible gas.
- the temperature of the catalyst can be raised, and the activity of the catalyst can be improved. That is, the tar reforming efficiency by the catalyst (the reaction rate of the tar reforming reaction) can be increased.
- the amount of sulfur adsorbed on the catalyst can be reduced by increasing the temperature of the gasification gas X1. Therefore, it is possible to suppress a decrease in tar reforming efficiency accompanying sulfur adsorption on the catalyst.
- the heat exchanger 236 performs heat exchange between the oxidant OX flowing through the oxidant supply path 234 and the combustion exhaust gas EX1 flowing through the exhaust path 118 (between the medium separation device 114 and the boiler 152), and the combustion exhaust gas EX1
- the oxidant OX is heated with the heat of
- the temperature of the combustion exhaust gas EX1 flowing through the exhaust path 118 is about 800 ° C. to 950 ° C. Therefore, when the heat exchanger 236 heats the oxidant OX with the heat of the combustion exhaust gas EX1, the oxidant OX supplied to the catalyst holding unit 220 can be heated to 200 ° C. to 900 ° C.
- the oxidizing agent OX can be heated without requiring a separate heating source, and the energy consumption for heating the oxidizing agent OX can be reduced.
- the temperature measurement unit 240 measures the temperature of the catalyst.
- the oxidant controller 250 is composed of a semiconductor integrated circuit including a CPU (Central Processing Unit), reads out programs and parameters for operating the CPU itself from the ROM, and cooperates with the RAM as a work area and other electronic circuits. Operates and controls the entire tar reforming apparatus 200.
- the oxidant control unit 250 controls the amount of the oxidant OX supplied by the oxidant supply unit 230 according to the temperature of the catalyst measured by the temperature measurement unit 240.
- the oxidant control unit 250 includes an oxidant supply unit so that the temperature of the catalyst does not fall below the activation temperature (for example, 650 ° C. to 900 ° C.) of the catalyst measured by the temperature measurement unit 240.
- 230 controls the amount of oxidant OX supplied.
- the oxidant control unit 250 performs hysteresis control, and controls the driving amount of the blower 232 to increase the amount of the oxidant OX supplied to the catalyst when the temperature of the catalyst becomes lower than 700 ° C.
- the drive amount of the blower 232 is controlled so as to reduce the amount of the oxidant OX supplied to the catalyst.
- the catalyst can be maintained at an activation temperature or higher, and tar reforming efficiency can be maintained.
- the tar in the gasification gas X1 (tar-containing gas) is reformed by the tar reforming apparatus 200 to become the gasification gas X2.
- FIG. 2 is a diagram for explaining the purification apparatus 300.
- the purification apparatus 300 includes a heat exchanger 310, a first cooler 320, a second cooler 330, a booster 340, a waste water treatment device 350, a desulfurizer 360, and a deammonia. It comprises a device 370 and a desalter 380.
- the desulfurizer 360, the deammonizer 370, and the demineralizer 380 can change the installation order and the presence or absence of installation according to the use of the gasification gas X2 and the kind of gasification raw material.
- the flow of gas is indicated by solid arrows
- the flow of water is indicated by dashed-dotted arrows.
- the heat exchanger 310 performs heat exchange between the gasification gas X2 introduced from the tar reforming apparatus 200 and water vapor, that is, recovers the sensible heat of the gasification gas X2 with water vapor, and the outlet temperature of the gasification gas X2 To 300 ° C to 600 ° C.
- the first cooler 320 further cools the gasification gas X2 having reached 300 ° C. to 600 ° C. by spraying water. Thereby, tar and dust remaining in the gasification gas X2 are condensed and removed from the gasification gas X2.
- the second cooler 330 further cools the gasification gas X2 to 30 ° C. or lower using seawater, brine, or the like, and further condenses and removes remaining tar and dust.
- a mist / dust remover constituted by an electric dust collector or the like may be provided at the subsequent stage of the second cooler 330 to further remove tar and dust.
- the booster 340 includes a blower, a compressor, a turbo pump, a positive displacement pump, and the like, and boosts the gasified gas X2 that has passed through the second cooler 330 to 0.1 MPa to 5 MPa.
- a cooler that cools the gasification gas X2 to 30 ° C. or lower can be provided after the booster 340 to further remove tar and dust.
- the waste water treatment device 350 performs a process of removing tar and dust from waste water containing tar and dust generated by the first cooler 320, the second cooler 330, and the booster 340. Water (treated water) after being treated by the waste water treatment device 350 is reused in the heat exchanger 310, the first cooler 320, and the like.
- the desulfurizer 360 removes sulfur and sulfur compounds remaining in the gasification gas X2.
- the deammonizer 370 removes nitrogen compounds such as ammonia in the gasification gas X2.
- the desalinator 380 removes chlorine and chlorine compounds in the gasification gas X2.
- the gasification gas X2 which is generated by the gasification gas generation system 100 and whose tar is reformed by the tar reforming apparatus 200, is supplied to the heat exchanger 310, the first cooler 320, the second cooler 330, and the pressure increase. Tar and dust are removed in the vessel 340, and sulfur is removed by the desulfurizer 360, ammonia is removed by the deammonizer 370, and chlorine is removed by the demineralizer 380 to be purified gasified gas.
- the reforming of tar is promoted using a catalyst, it is compared with the conventional technique of reforming tar using an oxidation reforming furnace.
- the oxidant supply unit 230 supplies the high-temperature oxidant OX such as 200 ° C. to 900 ° C. to the catalyst, compared with the case where the relatively low-temperature oxidant OX is supplied to the catalyst, Consumption can be reduced, and the reduction of combustible gas in the gasified gas X2 can be further suppressed.
- FIG. 3 is a conceptual diagram for explaining a gasification gas generation system 400 according to the second embodiment.
- the flow of the gasification raw material, gas, water vapor, air, and oxidant is indicated by solid arrows
- the flow of the fluid medium (sand) is indicated by a dashed line arrow
- the signal flow is indicated by a dashed arrow.
- the gasification gas generation system 400 includes a gasification gas generation device 110, a combustion exhaust gas processing device 150, a tar reforming device 410, and a purification device 300.
- the tar reformer 410 includes a flow passage 210, a catalyst holding unit 220, an oxidant supply unit 430, a temperature measurement unit 240, and an oxidant control unit 450.
- gasified gas generation device 110 the flue gas treatment device 150, the flow passage 210, the catalyst holding unit 220, the temperature measurement unit 240, and the purification device 300, which have already been described in the first embodiment, substantially function. Therefore, the redundant description of the oxidant supply unit 430 and the oxidant control unit 450 having different functions will be described in detail.
- the oxidant supply unit 430 supplies the combustion exhaust gas EX1 to the catalyst as an oxidant.
- the combustion exhaust gas EX1 discharged from the combustion furnace 112 (medium separator 114) contains oxygen that functions as an oxidant. Therefore, by supplying the combustion exhaust gas EX1 as an oxidant to the catalyst, the cost required for the oxidant can be reduced.
- the temperature of the combustion exhaust gas EX1 flowing through the exhaust path 118 is about 800 ° C. to 950 ° C. Therefore, by supplying the combustion exhaust gas EX1 as an oxidant to the catalyst, a high-temperature oxidant (combustion exhaust gas EX1) such as 200 ° C. to 900 ° C. can be supplied to the catalyst without requiring a separate heating source, It is possible to reduce energy consumption for heating the oxidizing agent (combustion exhaust gas EX1).
- a high-temperature oxidant such as 200 ° C. to 900 ° C.
- the oxidant supply unit 430 includes an oxidant supply path 432 and a butterfly valve 434.
- the oxidant supply path 432 is branched from the exhaust path 118 and is connected to the upstream side of the catalyst holding unit 220 in the flow path 210 and is a flow path through which the combustion exhaust gas EX1 flows.
- the butterfly valve 434 is provided in an exhaust passage 158 that connects the denitration device 154 and the desulfurization device 156, and the opening degree is controlled by an oxidant control unit 450 described later.
- the oxidant controller 450 is composed of a semiconductor integrated circuit including a CPU (Central Processing Unit), reads out programs and parameters for operating the CPU itself from the ROM, and cooperates with the RAM as a work area and other electronic circuits. Operates and controls the entire tar reformer 410.
- the oxidant control unit 450 controls the amount of the combustion exhaust gas EX1 supplied by the oxidant supply unit 430 according to the temperature of the catalyst measured by the temperature measurement unit 240.
- the oxidant control unit 450 controls the combustion exhaust gas EX1 supplied by the oxidant supply unit 430 so that the temperature of the catalyst does not fall below the activation temperature of the catalyst (for example, 650 ° C. to 900 ° C.). Control the amount.
- the oxidant control unit 450 performs hysteresis control, and controls the opening of the butterfly valve 434 so as to increase the amount of the combustion exhaust gas EX1 supplied to the catalyst when the temperature of the catalyst becomes less than 700 ° C.
- the opening degree of the butterfly valve 434 is controlled so as to reduce the amount of the combustion exhaust gas EX1 supplied to the catalyst.
- the catalyst can be maintained at an activation temperature or higher, and tar reforming efficiency can be maintained.
- the temperature of the gasified gas X1 is increased as compared with the conventional technique in which tar is reformed using an oxidation reforming furnace. Since it is not necessary, tar can be efficiently reformed while reducing the consumption of combustible gas (hydrogen or methane).
- the configuration in which the oxidant supply unit 430 supplies the combustion exhaust gas EX1 to the catalyst as a high-temperature oxidant reduces the consumption of combustible gas as compared with the case of supplying a relatively low-temperature oxidant to the catalyst. It can be reduced, and the reduction of the combustible gas in the gasification gas X2 can be further suppressed.
- the oxidant supply unit 230 heats the oxidant OX with the heat of the combustion exhaust gas EX1 and supplies it to the catalyst has been described as an example.
- the oxidant supply unit 230 only needs to supply a high-temperature oxidant such as 200 ° C. to 900 ° C. to the catalyst.
- the oxidant OX heated by a heater may be supplied to the catalyst.
- the heat exchanger 236 performs heat exchange between the combustion exhaust gas EX1 flowing between the medium separator 114 and the boiler 152 and the oxidant OX as an example. explained.
- the medium in which the heat exchanger 236 performs heat exchange is not limited.
- the heat exchanger 236 since the combustion exhaust gas EX2 flowing between the denitration device 154 and the desulfurization device 156 (exhaust passage 158) is about 200 ° C. to 400 ° C., the heat exchanger 236 includes the denitration device 154 and the desulfurization device 156.
- the oxidant OX may be heated to 200 ° C. to 900 ° C. by exchanging heat between the combustion exhaust gas EX2 flowing between them and the oxidant OX.
- the butterfly valve 434 is provided in the exhaust passage 158 that connects the denitration device 154 and the desulfurization device 156 has been described. It may be provided in the exhaust passage.
- the oxidant control units 250 and 450 are supplied to the oxidant supply units 230 and 430 based on the catalyst temperature measured by the temperature measurement unit 240, or the combustion exhaust gas EX1. ) Is adjusted.
- the oxidant supply unit 230 depends on the flow rate of the gasification gas X1 flowing through the flow passage 210. The amount of oxidant supplied to 430 may be adjusted.
- the case of reforming tar in the gasification gas X1 generated in the gasification furnace 116 that performs steam gasification has been described as an example.
- the agent is not limited, and may be nitrogen, for example.
- the present invention further suppresses the reduction of combustible gas while efficiently removing tar in a gasification gas generation system that generates gasification gas by gasifying a gasification raw material.
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Abstract
Description
本願は、2013年4月15日に日本に出願された特願2013-85131号に基づき優先権を主張し、その内容をここに援用する。
図1は、第1の実施形態にかかるガス化ガス生成システム100を説明するための概念図である。図1に示すように、ガス化ガス生成システム100は、ガス化ガス生成装置110と、燃焼排ガス処理装置150と、タール改質装置200と、精製装置300とを含んで構成される。なお、図1中、ガス化原料、ガス、水蒸気、空気、酸化剤の流れを実線の矢印で、流動媒体(砂)の流れを一点鎖線の矢印で、信号の流れを破線の矢印で示す。
ガス化ガス生成装置110は、燃焼炉112と、媒体分離装置(サイクロン)114と、ガス化炉116とを含んで構成される。ガス化ガス生成装置110では、全体として、粒径が300μm程度の硅砂(珪砂)等の砂で構成される流動媒体を熱媒体として循環させている。具体的に説明すると、まず、流動媒体は、燃焼炉112で1000℃程度に加熱され、燃焼排ガスEX1とともに媒体分離装置114に導入される。媒体分離装置114においては、高温の流動媒体と燃焼排ガスEX1とが分離され、この分離された高温の流動媒体が、ガス化炉116に導入される。そして、ガス化炉116に導入された流動媒体は、ガス化炉116の底面から導入されるガス化剤(水蒸気)によって流動層化された後、最終的に、燃焼炉112に戻される。
燃焼排ガス処理装置150は、ボイラ152と、脱硝装置154と、脱硫装置156とを含んで構成される。ボイラ152は、媒体分離装置114で分離された燃焼排ガスEX1と水とで熱交換を行うことで、燃焼排ガスEX1が有する熱を回収する。脱硝装置154は、ボイラ152によって冷却された燃焼排ガスEX1からNOx(窒素酸化物)を除去する。脱硫装置156は、脱硝装置154によってNOxが除去された燃焼排ガスEX2からSOx(硫黄酸化物)を除去する。こうして、NOxおよびSOxが除去された燃焼排ガスEX3は、外部に排出される。
図1に示すように、タール改質装置200は、流通路210と、触媒保持部220と、酸化剤供給部230と、温度測定部240と、酸化剤制御部250とを含んで構成される。
図2は、精製装置300を説明するための図である。図2に示すように、精製装置300は、熱交換器310と、第1冷却器320と、第2冷却器330と、昇圧器340と、排水処理器350と、脱硫器360と、脱アンモニア器370と、脱塩器380とを含んで構成される。なお、脱硫器360、脱アンモニア器370、脱塩器380はガス化ガスX2の用途およびガス化原料の種類に応じて、設置順序および設置有無を変更することができる。なお、図2中、ガスの流れを実線の矢印で、水の流れを一点鎖線の矢印で示す。
上述した第1の実施形態では、媒体分離装置114から排出された燃焼排ガスEX1が有する熱によって、200℃~900℃の酸化剤OXを生成し、触媒に供給する場合を例に挙げて説明した。本実施形態では、他の方法で200℃~900℃の酸化剤を触媒に供給するガス化ガス生成システム400について説明する。
図3は、第2の実施形態にかかるガス化ガス生成システム400を説明するための概念図である。図3中、ガス化原料、ガス、水蒸気、空気、酸化剤の流れを実線の矢印で、流動媒体(砂)の流れを一点鎖線の矢印で、信号の流れを破線の矢印で示す。図3に示すように、ガス化ガス生成システム400は、ガス化ガス生成装置110と、燃焼排ガス処理装置150と、タール改質装置410と、精製装置300とを含んで構成される。また、タール改質装置410は、流通路210と、触媒保持部220と、酸化剤供給部430と、温度測定部240と、酸化剤制御部450とを含んで構成される。
112 燃焼炉
116 ガス化炉
210 流通路
220 触媒保持部
230、430 酸化剤供給部
240 温度測定部
250、450 酸化剤制御部
Claims (6)
- ガス化原料をガス化させてガス化ガスを生成するガス化炉と、前記ガス化炉において生成されたガス化ガスが流通する流通路と、前記ガス化ガス中のタールの改質を促進する触媒を前記流通路内に保持する触媒保持部と、
前記触媒に200℃~900℃の酸化剤を供給する酸化剤供給部と、を備えるガス化ガス生成システム。 - 燃料を燃焼させることで生じた熱で、流動媒体を加熱する燃焼炉をさらに備え、前記ガス化炉には、前記燃焼炉によって加熱された流動媒体が導入され、前記ガス化炉は、前記流動媒体が有する熱で前記ガス化原料をガス化させ、
前記酸化剤供給部は、前記燃焼炉において燃料を燃焼させることで生じた燃焼排ガスと、前記酸化剤とを熱交換することで、前記酸化剤が200℃~900℃となるように加熱する請求項1に記載のガス化ガス生成システム。 - 燃料を燃焼させることで生じた熱で、流動媒体を加熱する燃焼炉をさらに備え、前記ガス化炉には、前記燃焼炉によって加熱された流動媒体が導入され、前記ガス化炉は、前記流動媒体が有する熱で前記ガス化原料をガス化させ、
前記酸化剤供給部は、前記燃焼炉において燃料を燃焼させることで生じた200℃~900℃の燃焼排ガスを酸化剤として前記触媒に供給する請求項1に記載のガス化ガス生成システム。 - 前記触媒の温度を測定する温度測定部と、
測定された前記触媒の温度に応じて、前記酸化剤供給部が供給する酸化剤の量を制御する酸化剤制御部と、をさらに備える請求項1から3のいずれか1項に記載のガス化ガス生成システム。 - 前記ガス化炉には、水蒸気が導入され、前記ガス化炉は、前記水蒸気で前記ガス化原料をガス化させる請求項1から3のいずれか1項に記載のガス化ガス生成システム。
- 前記ガス化炉には、水蒸気が導入され、前記ガス化炉は、前記水蒸気で前記ガス化原料をガス化させる請求項4に記載のガス化ガス生成システム。
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