WO2010047159A1 - 石炭ガス化炉 - Google Patents
石炭ガス化炉 Download PDFInfo
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- WO2010047159A1 WO2010047159A1 PCT/JP2009/062589 JP2009062589W WO2010047159A1 WO 2010047159 A1 WO2010047159 A1 WO 2010047159A1 JP 2009062589 W JP2009062589 W JP 2009062589W WO 2010047159 A1 WO2010047159 A1 WO 2010047159A1
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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
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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
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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
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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
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
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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
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
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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
- C10J2300/0959—Oxygen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1838—Autothermal gasification by injection of oxygen or 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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1853—Steam reforming, i.e. injection of steam only
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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
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis 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
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Definitions
- the present invention relates to a coal gasification furnace applied to a gasification furnace for combined coal gasification power generation, a chemical coal gasification furnace, and the like.
- coal gasification combined power generation facility Integrated In Coal Gasification Combined Cycle (IGCC)
- IGCC Integrated In Coal Gasification Combined Cycle
- a gasification furnace for power generation an air-blown coal gasification combined power generation gasification furnace that generates fuel gas for a gas turbine from coal
- the generated gas composition CO / H 2 ratio
- the target product synthetic product
- carbon dioxide (CO 2 ) recovery equipment in order to reduce the amount of carbon dioxide discharged into the atmosphere, carbon dioxide (CO 2 ) recovery equipment may be combined.
- a shift reactor is provided to increase the carbon dioxide concentration in the product gas in order to improve the carbon dioxide recovery rate.
- coal gas generated in a coal gasification furnace is cooled by a heat exchanger group, and in this case, water and steam are used for cooling the generated coal gas. Not done.
- Patent Document 1 In addition, some conventional coal gasification systems have a main purpose of cooling the gasification gas and inject water from the gasification furnace outlet.
- Patent Document 2 In example, see Patent Document 2,
- the exit gas of a coal gasifier is high temperature of 1000 degreeC or more.
- quenching medium for quenching water or gas (product gas, inert gas, etc.) Is used.
- water quenching using the quench medium as water is the easiest method, but the thermal efficiency of the plant is low because the furnace temperature is lowered.
- water supplied for quenching does not completely evaporate, it is necessary to treat water (untreated water, black water, black-water) mixed with unburned components.
- the coal gasification gas generated in the coal gasification furnace is enriched with hydrogen, and a shift reactor It is desired to enable downsizing.
- the second stage cooling for cooling the high-temperature coal gasification gas generated in the coal gasification furnace particularly in the case of a gasification furnace for power generation, it solves the problem of black water treatment and is an efficient heat exchanger It is desirable to be able to use.
- the present invention has been made in view of the above circumstances, and an object thereof is to provide a coal gasification furnace that generates hydrogen-rich coal gasification gas and enables downsizing of the shift reactor. There is to do.
- a coal gasification furnace is a coal gasification furnace in which a coal gasification gas is generated by a gasification reaction that proceeds in a furnace charged with a gasification raw material such as coal and a gasifying agent.
- a gasification raw material such as coal and a gasifying agent.
- the coal gasification furnace is a two-stage entrained bed gasification furnace having a combustion chamber and a reduction chamber, and the steam is supplied to the combustion chamber together with the gasification material and the gasifying agent. It is preferable that only the gasification material is charged into the reduction chamber.
- steam is introduced into the combustion chamber together with the gasification material and the gasifying agent, so that the aquatic gasification reaction and shift reaction proceed in the combustion chamber, and only the gasification material is introduced.
- a gasification reaction and an aquatic gasification reaction that are endothermic reactions proceed.
- the coal gasification furnace is a two-stage spouted bed gasification furnace provided with a combustion chamber and a reduction chamber, and the gasification material and the gasifying agent are charged into the combustion chamber, In addition, it is preferable that at least one of the water and the water vapor is introduced into the reduction chamber together with the gasification material.
- the gasification reaction proceeds with the gasification material and the gasifying agent introduced in the combustion chamber, and gasification is performed in the reduction chamber in which water and water vapor are introduced together with the gasification material. Reaction and aquatic gasification reaction proceed.
- the coal gasification gas generated by the gasification reaction is rich in hydrogen with a high proportion of hydrogen components. Further, since the gasification reaction and the aquatic gasification reaction in the reduction chamber are endothermic reactions, a reaction quench is performed to cool the coal gasification gas as the reaction proceeds.
- the input amount of water and steam is in the range of 0.1 to 0.8 (mass basis) with respect to the input amount of the gasification raw material.
- the amount of steam input in this case is a value that ensures a sufficient amount for the reaction within a range in which the furnace temperature does not decrease.
- a gas cooling heat exchanger for cooling the coal gasification gas is provided connected to an outlet of the coal gasification furnace, and passes through the gas cooling heat exchanger together with the coal gasification gas. It is preferable that the residual amount of carbon (C) in the char (unreacted coal) to be set is 30% or more, thereby preventing the char accumulated on the surface of the heat exchanger from being sintered and heat having good thermal efficiency.
- An exchange can be used.
- the water vapor is preferably introduced from a water cooling wall that cools the outer periphery of the gasification furnace and / or a water cooling system that flows through the heat exchanger for gas cooling. It is possible to secure the water vapor for charging by effectively utilizing the equipment (water vapor supply source).
- a gas cooling heat exchanger for cooling the coal gasification gas is provided connected to an outlet of the coal gasification furnace, and passes through the gas cooling heat exchanger together with the coal gasification gas. It is preferable that the residual amount of carbon (C) in the char (unreacted coal) to be set is 30% or more, thereby preventing the char accumulated on the surface of the heat exchanger from being sintered and heat having good thermal efficiency.
- An exchange can be used.
- the coal gasification gas generated by the coal gasification furnace becomes a hydrogen-rich gas having a high hydrogen (H 2 ) ratio in the components, that is, coal at the coal gasification furnace outlet.
- the shift reactor is used particularly in a coal gasification furnace such as a chemical gasification furnace or a carbon dioxide recovery power generation gasification furnace that requires a shift reactor. It can be downsized.
- the carbon (C) residual amount in the char passing through the heat exchanger for gas cooling is set to 30% or more, the problem of black water treatment is solved and heat exchange is performed for the second stage cooling of coal gasification gas.
- the plant thermal efficiency can be improved.
- the dried char can be circulated through the coal gasification furnace and gasified, the carbon conversion rate for obtaining the coal gasification gas from the gasification raw material such as coal can be improved.
- COS carbonyl sulfide
- the coal gasification furnace G shown in FIG. 1 generates coal gasification gas (hereinafter referred to as “coal gas”) by a gasification reaction that proceeds in a furnace charged with a gasification raw material such as coal and a gasifying agent. It is a device to do.
- the illustrated coal gasification furnace G is a two-stage spouted bed gasification furnace including a combustion chamber 10 and a reduction chamber 20.
- the coal gasification furnace G communicates with the upper stage (downstream side in the gas flow direction) of the combustion chamber 10 and has a reduction chamber 20. Is provided.
- combustion chamber 10 and the reduction chamber 20 are collectively referred to as “furnace” or “gasification furnace”.
- the coal gasification furnace G is provided with a heat exchanger 30 that communicates with the downstream side of the reduction chamber 20 and cools the coal gas generated in the gasification furnace.
- the outer peripheral surfaces of the combustion chamber 10, the reduction chamber 20, and the heat exchanger 30 are covered with a water cooling wall W that circulates cooling water to cool it.
- the coal gasification furnace G of the present embodiment is a two-stage entrained bed gasification furnace including the combustion chamber 10 and the reduction chamber 20, and the lower combustion chamber 10 includes a gasification material and a gasifying agent. Steam is introduced and only the gasification material is introduced into the upper reduction chamber 20. That is, in a combustion chamber (combustor) 10 of a two-stage entrained bed gasification furnace, gasification material coal (pulverized coal) and char (unreacted coal) described later are gasified from a plurality of burners 11 provided at appropriate positions. Agent air or oxygen is charged. Furthermore, in this embodiment, water vapor for promptly accelerating the reaction is introduced from the burner 11 into the combustion chamber 10.
- the steam introduced here is premixed with the gasifying agent air or oxygen and introduced into the burner 11. This is because the steam introduced in the premixed state is promoted to be quickly mixed in a high temperature field (furnace temperature is about 1800 ° C.) in the combustion chamber 10. This is because it proceeds quickly.
- a high temperature field furnace temperature is about 1800 ° C.
- steam thrown into the combustion chamber 10 it is not limited to the premixing with the gasifying agent mentioned above, You may throw in water vapor
- coal gas (CO) produced by the gasification reaction is rich in hydrogen with a high proportion of hydrogen in the gas as compared with the case where steam is not added.
- the preferable amount of water vapor to be injected into the combustion chamber 10 is that the proportion of hydrogen (H 2 / CO) in the coal gas (CO) increases when the amount of water vapor is increased.
- H 2 / CO hydrogen
- the product gas generated in the reduction chamber 20 is cooled in the second stage by the heat exchanger 30 connected to the gasification furnace outlet (the outlet of the reduction chamber 20). Since this heat exchanger 30 is configured so that the high-temperature product gas and water exchange heat, the product gas that has absorbed heat drops in temperature and flows to the next process, and the water that has absorbed heat rises in temperature. It becomes water vapor.
- char unreacted coal
- char unreacted coal
- the residual amount of C in the char is 30% or more, the sintering of the char can be prevented. In this case, the value of 30% or more of the C residual amount is a knowledge obtained based on experiments and the like.
- the char described above is recovered by a char recovery device (a cyclone, a high-temperature filter, etc.) (not shown) provided on the downstream side of the heat exchanger 30 and then reintroduced into the combustion chamber 10 as a gasification raw material.
- the char in this case is recovered in a dry state because the problem of black water or the like has been solved. Therefore, since the dried char can be circulated through the coal gasification furnace G and gasified, it is effective in improving the carbon conversion rate for obtaining coal gas from a gasification raw material such as coal.
- the ratio of hydrogen in the product gas is 22.1 (Vol% -dry) when steam is supplied and 16.3 (Vol% -dry) when steam is not supplied. It turns out that it is increasing more. Further, since the gasification reaction and the aquatic gasification reaction in the reduction chamber 20 are endothermic reactions, reaction quenching for cooling the coal gas is performed by the progress of these reactions.
- the high-pressure water vapor source for example, water vapor generated by heating water of the water cooling system flowing through the water cooling wall W or the heat exchanger 30 is introduced, and the pressure is increased to a desired pressure as necessary.
- the existing facilities water cooling wall W such as a water cooling system and the heat exchanger 30
- the coal gasification furnace G are effectively used.
- the method of introducing steam into the high-temperature combustion chamber 10 is suitable when general coal is used as the raw coal. That is, when the temperature in the combustion chamber 10 can be maintained at a high temperature by using general (good quality) raw coal, a large amount of water vapor can be introduced into the high-temperature combustion chamber 10. Moreover, since steam also has an effect as a gasifying agent, the oxygen ratio (oxygen input amount) of air or oxygen input as the gasifying agent can be lowered according to the input amount of water vapor. As a result, the gas turbine The concentration of effective gas components (CO, H 2 ) used as fuel can be increased. In addition, although water vapor
- the illustrated coal gasification furnace G1 is a two-stage entrained bed gasification furnace including the combustion chamber 10 and the reduction chamber 20, as in the above-described embodiment.
- coal (pulverized coal) or char serving as a gasification raw material is charged into the combustion chamber 10 together with a gasifying agent (air or oxygen) from the burner 11A.
- a gasifying agent air or oxygen
- the gasification reaction and the water gasification reaction described above proceed with the coal gas flowing from the combustion chamber 10 and the pulverized coal and water introduced into the reduction chamber 20. Since these reactions are endothermic reactions, a reaction quench is performed to cool the product gas as the reaction proceeds.
- the preferable amount of water input is about 0.1 to 0.8 on a mass basis for the same reason as the above-described embodiment with respect to the coal flow rate of pulverized coal input as the gasification material.
- the gasification reaction by the gasification material and the gasifying agent charged in the combustion chamber 10 proceeds. Further, in the reduction chamber 20, the gasification reaction and the aquatic gasification reaction proceed by introducing the atomized water together with the gasification material. As a result, the hydrogen produced by the aquatic gasification reaction in the reduction chamber 20 turns the coal gasification gas into a hydrogen-rich gas. Further, since the gasification reaction and the aquatic gasification reaction in the reduction chamber 20 are endothermic reactions, a reaction quench is performed to cool the generated gas as the reaction proceeds.
- the coal gasification furnace G1 configured in this manner has very high degree of freedom because there is almost no restriction on the design and arrangement of the nozzle for water injection because water is supplied to the reduction chamber 20 alone.
- high-pressure water that can be boosted by a pump is used as the water, so that a high-pressure steam source is unnecessary.
- water injection into the reduction chamber 20 can be expected for a quenching effect in the reduction chamber 20.
- the coal gasification furnace G1 configured in this manner does not supply steam into the combustion chamber 10, it is easy to maintain the inside of the combustion chamber 10 at a high temperature.
- the coal gasification furnace G1 which introduces atomized water into the reduction chamber 20 is suitable when the coal (pulverized coal) used as the gasification raw material is high ash melting point coal (1500 ° C. or higher). That is, when the high ash melting point coal is the raw coal, the molten ash is stably discharged, so that the combustion chamber 10 is kept at a high temperature without introducing steam, and the quenching effect and reaction progress due to the introduction of steam in the reduction chamber 20. Due to the reaction quenching, the temperature of the hot coal gasification gas can be drastically lowered.
- the illustrated coal gasification furnace G2 is a two-stage entrained bed gasification furnace including the combustion chamber 10 and the reduction chamber 20, as in the above-described embodiment.
- water vapor is supplied from the steam nozzle 23 to the reduction chamber 20 of the coal gasification furnace G2, which is a two-stage entrained bed gasification furnace. Is different.
- the other structure is the same as 2nd Embodiment mentioned above.
- steam is introduced into the reduction chamber 20 of the present embodiment together with the pulverized coal as the gasification raw material.
- the preferable amount of steam input is 0.1 to 0.8 on the mass basis for the same reason as the above-described embodiment with respect to the coal flow rate of the pulverized coal supplied to the combustion chamber 10 and the reduction chamber 20.
- Degree. In the reduction chamber 20, a gasification reaction and a water gasification reaction proceed with the introduction of water vapor. Since all of these reactions are endothermic reactions, reaction quenching is performed to cool the product gas as the reaction proceeds. Further, since hydrogen is generated by the water gasification reaction, hydrogen-rich coal gas is generated.
- the coal gasification furnace G2 configured in this manner does not supply steam to the combustion chamber 10, it becomes easy to maintain the inside of the combustion chamber 10 at a high temperature. For this reason, the coal gasification furnace G2 which introduces water vapor into the reduction chamber 20 is suitable when the coal (pulverized coal) used as the gasification raw material is high ash melting point coal. That is, when the high ash melting point coal (1500 ° C. or higher) is the raw coal, the inside of the combustion chamber 10 is kept at a high temperature in order to stably discharge the molten ash. Due to the reaction quenching, the temperature of the hot coal gasification gas can be drastically lowered.
- the present embodiment in which water vapor is introduced into the reduction chamber 20 is suitable when a low fuel specific coal having a fuel ratio of 1 or less, such as lignite, is used as the raw coal.
- a low fuel specific coal having a fuel ratio of 1 or less such as lignite
- the introduction of steam into the reduction chamber 20 has a cracking effect that promotes the decomposition of gasification by-products originating from volatile components contained in the raw coal.
- the steam introduced into the reduction chamber 20 promotes the decomposition reaction of the volatile components contained in the raw coal introduced into the reduction chamber 20, so that, for example, hydrocarbons, tar (heavy hydrocarbon), ammonia and the like As described above, the generation of by-products originating in the reduction chamber input coal is suppressed.
- the coal gasification furnaces G, G1, and G2 of the present invention in the furnace of the combustion chamber 10 and / or the reduction chamber 20, as a substance for promoting the hydrogen generation reaction that proceeds simultaneously with the gasification reaction, Since at least one of water and water vapor is introduced, the aquatic gasification reaction and / or shift reaction proceeds rapidly to produce hydrogen. As a result, the coal gas generated by the gasification reaction becomes a hydrogen-rich gas with a high proportion of hydrogen components.
- the coal gasification gas generated by the coal gasification furnaces G, G1, and G2 becomes a hydrogen-rich gas having a high hydrogen ratio in the components.
- the shift reactor can be downsized. If the carbon (C) residual amount in the char passing through the heat exchanger 30 for gas cooling is set to 30% or more, the problem of black water treatment is solved and the second stage cooling of the coal gasification gas is achieved. Since a heat exchanger can be used, particularly in the case of a gasifier for carbon dioxide recovery power generation, the plant thermal efficiency can be improved. Furthermore, since the dried char can be circulated through the coal gasification furnaces G, G1, and G2 and gasified, the carbon conversion rate for obtaining the coal gasification gas from the gasification raw material such as coal can be improved.
- the introduction of water vapor into the combustion chamber 10, the introduction of water (water spray) into the reduction chamber 20, and the introduction of water vapor into the reduction chamber 20 are carried out independently, but the present invention is limited to this.
- the combination is possible as appropriate. That is, a combination of water vapor input into the combustion chamber 10 and water spray input into the reduction chamber 20 is performed simultaneously, or a combination of water vapor input into the combustion chamber 10 and water vapor input into the reduction chamber 20 is performed simultaneously. It can be appropriately selected according to various conditions.
- this invention is not limited to embodiment mentioned above, In the range which does not deviate from the summary, it can change suitably.
- G G, G1, G2 Coal gasifier 10 Combustion chamber 20 Reduction chamber 30 Heat exchanger
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Abstract
Description
Coal Gasification Combined Cycle;IGCC)においては、効率のよいガス化炉として、石炭からガスタービンの燃料ガスを生成する空気吹きの石炭ガス化複合発電用ガス化炉(以下、発電用ガス化炉)が開発されている。
一方、化学用ガス化炉では、生成ガスのカロリーが重視される従来の発電用ガス化炉とは異なり、目的とする製品(合成物)に合わせた生成ガス組成(CO/H2比)にする必要がある。このため、化学用ガス化炉においては、CO/H2比を調整するためのシフト反応器が必要となる。
また、従来の石炭ガス化システムにおいては、ガス化ガスの冷却を主目的とし、ガス化炉出口から水を投入するものがある。(たとえば、特許文献2参照)
しかし、クエンチ媒体を水とする水クエンチは最も容易な方法であるが、炉内温度を低下させるためプラントの熱効率は低くなる。さらに、クエンチ用に投入した水が完全に気化しない場合は、未燃分が混入した水(煤水、黒水、Black-water)を処理することが必要となる。
また、石炭ガス化炉で生成された高温の石炭ガス化ガスを冷却する2段目冷却については、特に発電用ガス化炉の場合、黒水処理の問題を解決して効率のよい熱交換器を使用可能とすることが望ましい。
本発明は、上記の事情に鑑みてなされたものであり、その目的とするところは、水素リッチの石炭ガス化ガスを生成してシフト反応器の小型化を可能にした石炭ガス化炉を提供することにある。
本発明の一態様に係る石炭ガス化炉は、石炭等のガス化原料及びガス化剤を投入した炉内で進行するガス化反応により石炭ガス化ガスが生成される石炭ガス化炉において、前記ガス化反応と同時進行する水素生成反応の促進用物質として、前記炉内に水及び水蒸気の少なくとも一方が投入されるものである。
このような二段噴流床ガス化炉は、燃焼室にガス化材料及びガス化剤とともに水蒸気を投入するので、燃焼室内では、水生ガス化反応及びシフト反応が進行し、ガス化材料のみを投入する還元室内では、吸熱反応であるガス化反応及び水生ガス化反応が進行する。この結果、燃焼室内の水生ガス化反応及びシフト反応と、還元室内の水生ガス化反応とにより水素が生成されることになるので、ガス化反応により生成された石炭ガス化ガスは、水素成分の割合が高い水素リッチなガスとなる。また、還元室内のガス化反応及び水生ガス化反応は吸熱反応であるから、反応の進行により石炭ガス化ガスを冷却する反応クエンチが行われる。
この場合の水蒸気は、ガス化剤(空気または酸素)と予混合した状態で燃焼室に投入することが望ましく、これにより、炉内高温場への速やかな混合が促進され、反応の迅速な進行に有効である。
このような二段噴流床ガス化炉は、燃焼室内において、投入されたガス化材料及びガス化剤によりガス化反応が進行し、ガス化材料とともに水や水蒸気を投入する還元室内において、ガス化反応及び水生ガス化反応が進行する。この結果、還元室内の水生ガス化反応により水素が生成されるので、ガス化反応により生成された石炭ガス化ガスは、水素成分の割合が高い水素リッチとなる。また、還元室内のガス化反応及び水生ガス化反応は吸熱反応であるから、反応の進行により石炭ガス化ガスを冷却する反応クエンチが行われる。
また、ガス冷却用熱交換器を通過するチャー中の炭素(C)残留量を30%以上に設定すれば、黒水処理の問題を解消して石炭ガス化ガスの2段目冷却に熱交換器を使用できるので、特に二酸化炭素回収発電用ガス化炉の場合、プラント熱効率を向上させることができる。さらに、乾燥したチャーを石炭ガス化炉に循環させてガス化できるので、石炭等のガス化原料から石炭ガス化ガスを得る炭素転換率も向上させることができる。
<第1の実施形態>
図1に示す石炭ガス化炉Gは、石炭等のガス化原料及びガス化剤を投入した炉内で進行するガス化反応により、石炭ガス化ガス(以下、「石炭ガス」と呼ぶ)を生成する装置である。図示の石炭ガス化炉Gは、燃焼室10及び還元室20を備えた二段噴流床ガス化炉であり、燃焼室10の上段(ガス流れ方向の下流側)に連通して還元室20が設けられている。以下の説明では、燃焼室10及び還元室20を総称して「炉」または「ガス化炉」と呼ぶことにする。
また、石炭ガス化炉Gは、還元室20の下流側に連通して、ガス化炉内で生成した石炭ガスを冷却する熱交換器30が設けられている。
なお、上述した石炭ガス化炉Gは、燃焼室10、還元室20及び熱交換器30の外周面が冷却水を循環させて冷却する水冷壁Wにより覆われている。
すなわち、二段噴流床ガス化炉の燃焼室(コンバスタ)10には、適所に複数設けたバーナ11から、ガス化材料の石炭(微粉炭)及び後述するチャー(未反応石炭)と、ガス化剤の空気もしくは酸素とが投入される。さらに、本実施形態では、反応を迅速に促進させるための水蒸気がバーナ11から燃焼室10に投入される。
なお、燃焼室10へ投入する水蒸気については、上述したガス化剤との予混合に限定されることはなく、水蒸気を単独で投入してもよい。
水性ガス化反応 ; C(固)+H2O
→ H2+CO
シフト反応 ; CO+O2 → H2+CO2
ガス化反応 ; C(固)+CO2
→ 2CO
なお、ヒートロスの割合が小さくなる商用機等においては、水蒸気投入量の増量が可能になるので、石炭ガス中の水素割合を増して水素リッチにしたガスを生成することができる。
この熱交換器30では、生成ガスとともに流入するチャー(未反応石炭)が堆積することにより、チャーの焼結トラブルを発生する場合がある。しかし、チャー中のC残留量を30%以上とすることにより、チャーの焼結防止が可能となる。なお、この場合のC残留量30%以上という値は、実験等に基づいて得られた知見である。
また、還元室20内のガス化反応及び水生ガス化反応は吸熱反応であるから、これらの反応進行により石炭ガスを冷却する反応クエンチが行われる。
また、燃焼室10に水蒸気を投入することにより、石炭ガス化炉Gの副生成物であるアンモニア、硫化カルボニル等の生成量を抑制することができる。すなわち、図5及び図6に示す実験結果によれば、蒸気なしのテスト1と蒸気有のテスト2とを比較した場合、蒸気有のテスト2において生成量が明らかに減少していることが分かる。
なお、上述した実施形態では水蒸気を投入したが、噴霧状の水を投入してもよい。
次に、本発明に係る石炭ガス化炉について、第2の実施形態を図2に示して説明する。なお、上述した実施形態と同様の部分には同じ符号を付し、その詳細な説明は省略する。
図示の石炭ガス化炉G1は、上述した実施形態と同様に、燃焼室10及び還元室20を備えた二段噴流床ガス化炉である。
この実施形態において、燃焼室10には、ガス化原料となる石炭(微粉炭)やチャーがバーナ11Aからガス化剤(空気もしくは酸素)とともに投入される。この結果、燃焼室10内では、投入されたガス化原料及びガス化剤によりガス化反応が進行する。
この結果、還元室20内の水生ガス化反応により生成される水素は、石炭ガス化ガスを水素リッチのガスにする。また、還元室20内のガス化反応及び水生ガス化反応は吸熱反応であるから、反応の進行により生成ガスを冷却する反応クエンチが行われる。
このため、還元室20へ噴霧状の水を投入する石炭ガス化炉G1は、ガス化原料として使用する石炭(微粉炭)が高灰融点炭(1500℃以上)である場合に適している。すなわち、高灰融点炭が原料炭の場合、溶融灰を安定排出するため、水蒸気投入をしないで燃焼室10内を高温に保ち、かつ、還元室20においては、水蒸気投入によるクエンチ効果と反応進行による反応クエンチとにより、高温の石炭ガス化ガスを急激に温度低下させることができる。
次に、本発明に係る石炭ガス化炉について、第3の実施形態を図3に示して説明する。なお、上述した実施形態と同様の部分には同じ符号を付し、その詳細な説明は省略する。
図示の石炭ガス化炉G2は、上述した実施形態と同様に、燃焼室10及び還元室20を備えた二段噴流床ガス化炉である。
この実施形態では、上述した第2の実施形態における還元室20への水投入に代えて、二段噴流床ガス化炉とした石炭ガス化炉G2の還元室20に蒸気ノズル23から水蒸気を投入している点が異なっている。なお、本実施形態の石炭ガス化炉G2において、他の構成は上述した第2の実施形態と同じである。
還元室20では、水蒸気の投入によりガス化反応及び水性ガス化反応が進行する。この反応はいずれも吸熱反応であるから、反応進行により生成ガスを冷却する反応クエンチが行われる。また、水性ガス化反応により水素が生成されるため、水素リッチな石炭ガスが生成される。
また、還元室20へ水蒸気を投入する本実施形態は、たとえば褐炭等のように、燃料比が1以下の低燃料比炭を原料炭とする場合に適している。これは、還元室20への水蒸気投入が、原料炭中に含まれる揮発分を起源とするガス化副生成物の分解を促進するクラッキング効果を有しているためである。
また、還元室20に投入した水蒸気により、還元室20へ投入した原料炭に含まれている揮発分の分解反応が促進されるため、たとえば炭化水素、タール(重質炭化水素)及びアンモニア等のように、還元室投入石炭を起源とする副生成物の発生が抑制される。
また、ガス冷却用の熱交換器30を通過するチャー中の炭素(C)残留量を30%以上に設定すれば、黒水処理の問題を解消して石炭ガス化ガスの2段目冷却に熱交換器を使用できるので、特に二酸化炭素回収発電用ガス化炉の場合、プラント熱効率の向上が可能になる。さらに、乾燥したチャーを石炭ガス化炉G,G1,G2に循環させてガス化できるので、石炭等のガス化原料から石炭ガス化ガスを得る炭素転換率についても向上させることができる。
なお、本発明は上述した実施形態に限定されることはなく、その要旨を逸脱しない範囲内において適宜変更することができる。
10 燃焼室
20 還元室
30 熱交換器
Claims (6)
- 石炭等のガス化原料及びガス化剤を投入した炉内で進行するガス化反応により石炭ガス化ガスが生成される石炭ガス化炉において、
前記ガス化反応と同時進行する水素生成反応の促進用物質として、前記炉内に水及び水蒸気の少なくとも一方が投入される石炭ガス化炉。 - 前記石炭ガス化炉が燃焼室及び還元室を備えた二段噴流床ガス化炉とされ、
前記燃焼室には前記ガス化材料及び前記ガス化剤とともに前記水蒸気が投入され、かつ、前記還元室には前記ガス化材料のみが投入される請求項1に記載の石炭ガス化炉。 - 前記石炭ガス化炉が燃焼室及び還元室を備えた二段噴流床ガス化炉とされ、
前記燃焼室には前記ガス化材料及び前記ガス化剤が投入され、かつ、前記還元室には前記ガス化材料とともに前記水及び前記水蒸気の少なくとも一方が投入される請求項1に記載の石炭ガス化炉。 - 前記水及び水蒸気の投入量は、前記ガス化原料の投入量に対して0.1~0.8(質量基準)である請求項1から3のいずれかに記載の石炭ガス化炉。
- 前記石炭ガス化ガスを冷却するガス冷却用熱交換器が前記石炭ガス化炉の出口に接続して設けられ、前記石炭ガス化ガスとともに前記ガス冷却用熱交換器を通過するチャー(未反応石炭)中の炭素(C)残留量が30%以上に設定されている請求項1から4のいずれかに記載の石炭ガス化炉。
- 前記水蒸気は、前記ガス化炉の外周を冷却する水冷壁及び/または前記ガス冷却用熱交換器を流れる水冷却系統から導入される請求項1から5のいずれかに記載の石炭ガス化炉。
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- 2009-07-10 WO PCT/JP2009/062589 patent/WO2010047159A1/ja active Application Filing
- 2009-07-10 CA CA2730323A patent/CA2730323C/en active Active
- 2009-07-10 CN CN200980127255.1A patent/CN102089406B/zh active Active
- 2009-07-10 US US13/002,109 patent/US20110116979A1/en not_active Abandoned
- 2009-07-10 KR KR1020117000412A patent/KR101318571B1/ko active IP Right Grant
- 2009-07-10 EP EP09821859A patent/EP2338956A4/en not_active Withdrawn
- 2009-07-10 AU AU2009307613A patent/AU2009307613B2/en active Active
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JP5386635B2 (ja) * | 2010-04-16 | 2014-01-15 | 新日鉄住金エンジニアリング株式会社 | 石炭ガス化反応炉の運転方法および石炭ガス化反応炉 |
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Also Published As
Publication number | Publication date |
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AU2009307613B2 (en) | 2015-06-04 |
US20150144843A1 (en) | 2015-05-28 |
KR101318571B1 (ko) | 2013-10-16 |
US9487715B2 (en) | 2016-11-08 |
CA2730323C (en) | 2013-12-24 |
JP4898759B2 (ja) | 2012-03-21 |
US20110116979A1 (en) | 2011-05-19 |
CA2730323A1 (en) | 2010-04-29 |
JP2010100690A (ja) | 2010-05-06 |
EP2338956A4 (en) | 2013-03-13 |
AU2009307613A1 (en) | 2010-04-29 |
CN102089406B (zh) | 2014-10-01 |
CN102089406A (zh) | 2011-06-08 |
ZA201009297B (en) | 2011-10-26 |
KR20110034634A (ko) | 2011-04-05 |
EP2338956A1 (en) | 2011-06-29 |
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