US20110116979A1 - Coal gasifier - Google Patents

Coal gasifier Download PDF

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Publication number
US20110116979A1
US20110116979A1 US13/002,109 US200913002109A US2011116979A1 US 20110116979 A1 US20110116979 A1 US 20110116979A1 US 200913002109 A US200913002109 A US 200913002109A US 2011116979 A1 US2011116979 A1 US 2011116979A1
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Prior art keywords
coal
fed
steam
gas
gasifier
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Inventor
Takashi Yamamoto
Katsuhiko Yokohama
Yoshinori Koyama
Katsuhiro Ota
Hiromi Ishii
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Mitsubishi Power Ltd
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Mitsubishi Heavy Industries Ltd
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Assigned to MITSUBISHI HEAVY INDUSTRIES, LTD. reassignment MITSUBISHI HEAVY INDUSTRIES, LTD. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: ISHII, HIROMI, KOYAMA, YOSHINORI, OTA, KATSUHIRO, YAMAMOTO, TAKASHI, YOKOHAMA, KATSUHIKO
Publication of US20110116979A1 publication Critical patent/US20110116979A1/en
Assigned to MITSUBISHI HITACHI POWER SYSTEMS, LTD. reassignment MITSUBISHI HITACHI POWER SYSTEMS, LTD. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MITSUBISHI HEAVY INDUSTRIES, LTD.
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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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1838—Autothermal gasification by injection of oxygen or steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1853—Steam reforming, i.e. injection of steam 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
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • 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
    • 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 gasifier applied to, for example, an integrated coal gasification combined cycle gasifier or a coal gasifier for chemical uses.
  • gasifiers for chemical uses unlike known gasifiers for power generation, which place value on calories of syngas, it is necessary to adapt the composition (CO/H 2 ratio) of syngas to that of an intended product (compound). Therefore, gasifiers for chemical uses need a shift reactor for adjusting the CO/H 2 ratio.
  • gasifiers for power generation in order to reduce the amount of carbon dioxide to be discharged into the atmosphere, equipment for recovering carbon dioxide (CO 2 ) may be combined with the furnaces.
  • a shift reactor is provided to increase the concentration of carbon dioxide in syngas for improving the recovery rate of carbon dioxide.
  • the coal gas generated by the coal gasifier is cooled by heat exchangers. In this case, no water or steam for cooling the generated coal gas is fed (for example, see Patent Literature 1).
  • water is fed from the outlet of a gasifier mainly in order to cool the gasified gas (for example, see Patent Literature 2).
  • the shift reactor can be reduced in volume by increasing the hydrogen (H 2 ) concentration at the outlet of the coal gasifier as much as possible.
  • the outlet gas of the coal gasifier has a high temperature of 1000° C. or more. Accordingly, when gas is purified for to be used as a chemical raw material or fuel gas, cooling by a heat exchanger or quenching feeding is necessary.
  • the quenching medium for the quenching feeding water or gas (such as the syngas or inert gas) is used.
  • water quenching using water as the quenching medium is the simplest method, it decreases the temperature inside the furnace, resulting in a reduction in thermal efficiency of the plant. Furthermore, if the water fed for quenching is not completely evaporated, treatment of water mixed with unburnt components (soot water, black water) is necessary.
  • coal gasifiers such as the gasifier for chemical uses and the carbon-dioxide-recovery power-generation gasifier
  • the present invention has been made in view of the above circumstances, and an object thereof is to provide a coal gasifier allowing a reduction in size of the shift reactor by generating hydrogen-rich gasified coal gas.
  • the present invention employs the following solutions for solving the above-mentioned problems.
  • the coal gasifier according to an aspect of the present invention is a coal gasifier generating gasified coal gas by a gasification reaction that proceeds in a furnace fed with a gasifiable raw material, such as coal, and a gasifying agent, wherein at least one of water and steam is fed to the furnace as a material accelerating a hydrogen-generating reaction proceeding simultaneously together with the gasification reaction.
  • a gasifiable raw material such as coal
  • a gasifying agent wherein at least one of water and steam is fed to the furnace as a material accelerating a hydrogen-generating reaction proceeding simultaneously together with the gasification reaction.
  • the gasified coal gas generated by the gasification reaction is hydrogen-rich gas having a high hydrogen component ratio (H 2 ratio).
  • the coal gasifier is a two-stage entrained-bed gasifier having a combustion chamber and a reduction chamber, wherein the combustion chamber is preferably fed with the steam together with the gasifiable material and the gasifying agent, and the reduction chamber is preferably fed with the gasifiable material only.
  • the steam in this case is desirably fed to the combustion chamber in the state where the steam is premixed with a gasifying agent (air or oxygen).
  • a gasifying agent air or oxygen
  • the coal gasifier is a two-stage entrained-bed gasifier having a combustion chamber and a reduction chamber, and the combustion chamber is preferably fed with the gasifiable material and the gasifying agent, and the reduction chamber is preferably fed with at least one of the water or the steam together with the gasifiable material.
  • a gasification reaction proceeds in the combustion chamber due to a gasifiable material and a gasifying agent fed therein, and a gasification reaction and an water gas reaction proceed in the reduction chamber to which water and/or steam is fed together with a gasifiable material.
  • the gasified coal gas generated by the gasification reaction has a high hydrogen component ratio, that is, is hydrogen rich.
  • reaction quenching which cools the gasified coal gas is performed as the reactions proceed.
  • the amount of the water or the steam to be fed is preferably in the range of 0.1 to 0.8 (mass basis) relative to the amount of the gasifiable raw material to be fed.
  • the amount of steam to be fed in this case is a value that ensures an amount sufficient for the reaction within a range not to decrease the temperature inside the furnace.
  • a gas-cooling heat exchanger for cooling the gasified coal gas is preferably provided so as to be connected to the outlet of the coal gasifier and is preferably set so that the amount of carbon (C) remaining in char (unreacted coal) passing through the gas-cooling heat exchanger together with the gasified coal gas is 30% or more.
  • the steam is preferably introduced from a water cooling wall cooling the periphery of the gasifier and/or a water cooling system flowing in the gas-cooling heat exchanger.
  • the gas-cooling heat exchanger cooling the gasified coal gas is preferably provided to be connected to the outlet of the coal gasifier and is preferably set so that the amount of carbon (C) remaining in char (unreacted coal) passing through the gas-cooling heat exchanger together with the gasified coal gas is 30% or more.
  • the gasified coal gas generated by the coal gasifier is hydrogen-rich gas having a high hydrogen (H 2 ) component fraction, that is, since the concentration of hydrogen in the gasified coal gas at the outlet of the coal gasifier can be increased, in particular, in coal gasifiers such as gasifiers for chemical uses and carbon-dioxide-recovery power-generation gasifiers, which need shift reactors, the shift reactors can be reduced in size.
  • the thermal efficiency of the plant can be improved. Furthermore, since gasification can be performed by circulating the dried char in the coal gasifier, the carbon conversion ratio at which gasified coal gas is obtained from a gasifiable raw material such as coal can be also increased.
  • FIG. 1 is a configuration diagram showing a first embodiment of a coal gasifier according to the present invention.
  • FIG. 2 is a configuration diagram showing a second embodiment of a coal gasifier according to the present invention.
  • FIG. 3 is a configuration diagram showing a third embodiment of a coal gasifier according to the present invention.
  • FIG. 4 is experimental data showing that the ratio of hydrogen contained in the gasified coal gas is increased by feeding steam.
  • FIG. 5 is experimental data showing that carbonyl sulfide (COS) is decreased by feeding steam.
  • FIG. 6 is experimental data showing that the amount of generated ammonia (NH 3 ) is reduced by feeding steam.
  • FIG. 7 is a graph showing that the hydrogen ratio is increased by feeding steam.
  • the coal gasifier G shown in FIG. 1 is an apparatus for generating gasified coal gas (hereinafter, referred to as “coal gas”) by a gasification reaction proceeding in a furnace to which a gasifiable raw material, such as coal, and a gasifying agent are fed.
  • the coal gasifier G shown in the drawing is a two-stage entrained-bed gasifier having a combustion chamber 10 and a reduction chamber 20 , and the reduction chamber 20 is disposed so as communicate with the upper stage (downstream side in the gas flow direction) of the combustion chamber 10 .
  • the combustion chamber 10 and the reduction chamber 20 are collectively referred to as “furnace” or “gasifier” in the following description.
  • the coal gasifier G includes a heat exchanger 30 communicating with the downstream side of the reduction chamber 20 and cooling the coal gas generated in the gasifier.
  • 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 circulating cooling water for cooling.
  • the coal gasifier G of the Embodiment is a two-stage entrained-bed gasifier having a combustion chamber 10 and a reduction chamber 20 , and the combustion chamber 10 of the lower stage is fed with steam together with a gasifiable material and a gasifying agent, and the reduction chamber 20 of the upper stage is fed with only the gasifiable material.
  • the combustion chamber (combustor) 10 of the two-stage entrained-bed gasifier is fed with coal (pulverized coal) and char (unreacted coal), described below, serving as gasifiable materials, and air or oxygen, serving as a gasifying agent, from a plurality of burners 11 disposed at appropriate positions. Furthermore, in this Embodiment, steam for promoting a rapid reaction is fed to the combustion chamber 10 from the burners 11 .
  • the steam fed here is desirably premixed with air or oxygen serving as the gasifying agent and is then fed to the burners 11 . This is because, since steam fed in the premixed state promotes rapid mixing in a high-temperature portion (furnace core temperature: about 1800° C.) in the combustion chamber 10 , as a result, the reaction in the combustion chamber 10 proceeds rapidly.
  • the steam to be fed to the combustion chamber 10 is not limited to that premixed with the gasifying agent described above, and steam alone may be fed.
  • coal gas (CO) generated by the gasification reaction had a high ratio of hydrogen in the gas, that is, is hydrogen-rich, compared with the case where steam is not fed.
  • An appropriate amount of steam to be fed to the combustion chamber 10 is about 0.1 to 0.8, on a mass basis, relative to the flow rate of pulverized coal to be fed as the gasifiable material, since, for example, as shown in FIG. 7 , the hydrogen ratio (H 2 /CO) in coal gas (CO) is increased with the amount of steam to be fed.
  • An increase in the amount of steam to be fed decreases the temperature of the combustion chamber 10 and deteriorates combustion properties and slug-discharging properties.
  • a simulation was performed to confirm that the coal gasifier 10 can be operated without causing any trouble by regulating the upper limit of the amount of steam to be fed to about 0.8 (mass basis).
  • the appropriate amount of steam to be fed to the combustion chamber 10 is based on the simulation result. That is, the amount of steam to be fed is desirably optimized by considering the trade-off between ensuring a sufficient amount of steam to be fed for accelerating the reaction, and inhibiting a decrease in temperature inside the combustion chamber 10 .
  • the reduction chamber (reductor) 20 only coal (pulverized coal) serving as a gasifiable material is fed from the burners 21 .
  • the above-mentioned gasification reaction and water gas reaction proceed due to products such as coal gas, hydrogen and carbon dioxide flowing in from the combustion chamber 10 , and the coal additionally fed. Since both these reactions are endothermic reactions, reaction quenching which cools the syngases (gasified coal gas) containing coal gas and hydrogen as main components is performed as the reactions proceed.
  • the syngas generated in the reduction chamber 20 is subjected to second-stage gas cooling by a heat exchanger 30 connected to the outlet of the gasifier (outlet of the reduction chamber 20 ). Since this heat exchanger 30 is configured so as to perform heat exchange between the high-temperature syngas and water, the heat-absorbed syngas is decreased in temperature and flows out to the next step, and the heat-absorbing water is increased in temperature and is converted into steam.
  • the fed steam is completely vaporized by maintaining a high temperature inside the furnace, the problem of treating, for example, soot water and black water in which char is mixed is also solved. Therefore, it becomes possible to use a heat exchanger with a high heat exchange efficiency for the second stage cooling of the coal gas.
  • the cooling of the syngas by such a heat exchanger 30 is effective in improving the thermal efficiency of the plant, in particular, for example, in the carbon-dioxide-recovery power-generation gasifier.
  • the above-mentioned char is recovered by a char-recovering device (for example, a cyclone or high-temperature filter, not shown) disposed on the downstream side of the heat exchanger 30 and is then re-fed to the combustion chamber 10 as a gasifiable raw material.
  • a char-recovering device for example, a cyclone or high-temperature filter, not shown
  • the char is recovered in a dried state. Therefore, gasification can be performed by circulating the dried char in the coal gasifier G, which is also effective for improving the carbon conversion ratio at which coal gas is obtained from a gasifiable material such as coal.
  • reaction quenching which cools the coal gas is performed as the reactions proceed.
  • the amounts of by-products, such as ammonia and carbonyl sulfide, produced by the coal gasifier G can be restricted by feeding steam to the combustion chamber 10 . That is, according to the experimental results shown in FIGS. 5 and 6 , it is confirmed by comparing test 1 where steam is not fed and test 2 where steam is fed that the amount of by-products is obviously lower in test 2 where steam is fed.
  • a high-pressure steam source is necessary. Accordingly, for example, the steam generated by heating the water in water cooling systems, that is, the water flowing in the water cooling wall W or the heat exchanger 30 , is introduced to the high-pressure steam source, and the pressure is increased to a desired level as required. That is, though a pressure-raising device for producing high-pressure steam may be necessary in some cases, a sufficient amount of steam for feeding can be obtained by effectively utilizing existing facilities (the water cooling wall W and the heat exchanger 30 of the water cooling system) of the coal gasifier G as the steam supply.
  • the system where steam is thus-fed to the high-temperature combustion chamber 10 is suitable for a case where common coal is used as raw material coal. That is, when the temperature inside the combustion chamber 10 can be maintained high by using common (good-quality) raw material coal, a large amount of steam can be fed into the high-temperature combustion chamber 10 .
  • steam also has an effect as a gasifying agent, the oxygen ratio of air or oxygen (oxygen feeding rate) to be fed as the gasifying agent can be reduced according to the amount of steam to be fed.
  • the concentrations of active gas components (CO, H 2 ) being used as gas turbine fuel can be increased.
  • water may be fed in the form of a spray.
  • the coal gasifier G 1 shown in the drawing is, as in the above-described embodiment, a two-stage entrained-bed gasifier having a combustion chamber 10 and a reduction chamber 20 .
  • the combustion chamber 10 is fed with coal (pulverized coal) and char serving as gasifiable raw materials from burners 11 A together with a gasifying agent (air or oxygen).
  • a gasification reaction proceeds in the combustion chamber 10 due to the gasifiable materials and the gasifying agent that have been fed.
  • the reduction chamber 20 is fed with water in a sprayed form from spray nozzles 22 together with coal (pulverized coal) serving as a gasifiable raw material from burners 21 .
  • coal pulverized coal
  • the above-mentioned gasification reaction and water gas reaction proceed in the reduction chamber 20 due to the coal gas flowing in from the combustion chamber 10 and the pulverized coal and water fed into the reduction chamber 20 . Since both these reactions are endothermic reactions, reaction quenching which cools the syngas is performed as the reactions proceed.
  • an appropriate amount of water to be fed is about 0.1 to 0.8, on a mass basis, relative to the flow rate of pulverized coal to be fed as the gasifiable material, for the same reasons as those in the above-described embodiment.
  • the gasification reaction proceeds due to the gasifiable materials and the gasifying agent fed into the combustion chamber 10 . Furthermore, in the reduction chamber 20 , the gasification reaction and the water gas reaction proceed by being fed with water in a sprayed form together with the gasifiable material.
  • the hydrogen generated by the water gas reaction in the reduction chamber 20 makes the gasified coal gas a hydrogen-rich gas.
  • reaction quenching which cools the syngas is performed as the reactions proceed.
  • the nozzles for feeding water have almost no restriction in design and configuration and have a considerably high degree of freedom. Furthermore, since water in this case is fed as high-pressure water whose pressure can be increased by a pump, a high-pressure steam supply is unnecessary. Furthermore, the feeding of water to the reduction chamber 20 can be expected to exhibit a quenching effect on the inside of the reduction chamber 20 .
  • the coal gasifier G 1 feeding water in a sprayed form to the reduction chamber 20 is suitable for the case where the coal (pulverized coal) used as a gasifiable raw material is coal having a high ash melting point (1500° C. or more). That is, when the raw material coal is a coal having a high ash melting point, the temperature inside the combustion chamber 10 can be maintained high by not feeding steam for stably discharging melted ash, and, in the reduction chamber 20 , the temperature of the gasified coal having a high gas temperature can be sharply decreased by the quenching effect due to feeding of steam and reaction quenching as the reaction proceeds.
  • the coal (pulverized coal) used as a gasifiable raw material is coal having a high ash melting point (1500° C. or more). That is, when the raw material coal is a coal having a high ash melting point, the temperature inside the combustion chamber 10 can be maintained high by not feeding steam for stably discharging melted ash, and, in the reduction chamber 20 , the
  • the coal gasifier G 2 shown in the drawing is a two-stage entrained-bed gasifier having a combustion chamber 10 and a reduction chamber 20 , as in the above-described embodiments.
  • This embodiment is different in that, instead of feeding water to the reduction chamber 20 in the above-described second embodiment, steam is fed from steam nozzles 23 to the reduction chamber 20 of the coal gasifier G 2 , which is the two-stage entrained-bed gasifier. Note that remaining configuration of the coal gasifier G 2 of this embodiment is the same as that of the second embodiment.
  • the reduction chamber 20 of this embodiment is fed with steam together with pulverized coal serving as a gasifiable raw material.
  • an appropriate amount of steam to be fed is about 0.1 to 0.8, on a mass basis, relative to the flow rate of coal to be fed as pulverized coal to the combustion chamber 10 and the reduction chamber 20 , because of the same reasons as those in the above-described embodiments.
  • the gasification reaction and the water gas reaction proceed due to the feeding of steam. These reactions are both endothermic reactions, reaction quenching which cools the syngas is performed as the reactions proceed. In addition, since hydrogen is generated by the water gas reaction, hydrogen-rich coal gas is generated.
  • the coal gasifier G 2 feeding steam to the reduction chamber 20 is suitable for the case where coal (pulverized coal) having a high ash melting point is used as the gasifiable raw material. That is, when the raw material coal is a coal having a high ash melting point (1500° C. or more), the temperature inside the combustion chamber 10 can be maintained high for stably discharging the melting ash, and, in the reduction chamber 20 , the temperature of the high-temperature gasified coal gas can be sharply decreased by the quenching effect due to feeding of steam and reaction quenching as the reaction proceeds.
  • the embodiment in which steam is fed to the reduction chamber 20 is suitable for the case where coal having a low fuel rate of one or less, such as lignite, is used. This is because feeding of steam to the reduction chamber 20 has a cracking effect that accelerates decomposition of gasified by-products originating from volatile substances contained in the raw material coal.
  • coal gasifiers G, G 1 , and G 2 of the present invention since at least one of water and steam is fed into the furnace of the combustion chamber 10 and/or the reduction chamber 20 as a material accelerating a hydrogen-generating reaction that proceeds simultaneously with the gasification reaction, the water gas reaction and/or the shift reaction rapidly proceed to generate hydrogen. As a result, the coal gas generated by the gasification reaction is made a hydrogen-rich gas having a high hydrogen component fraction.
  • the gasified coal gas generated by the coal gasifiers G, G 1 , or G 2 is hydrogen-rich gas having a high hydrogen component fraction, in particular, in coal gasifiers, such as gasifiers for chemical uses and carbon-dioxide-recovery power-generation gasifiers, which need shift reactors, the shift reactors can be reduced in size.
  • the problem of black water treatment can be solved to enable use of a heat exchanger in the second-stage cooling of the gasified coal gas by setting the amount of carbon (C) remaining in char passing through the gas-cooling heat exchanger 30 to 30% or more: in particular, in the case of a carbon-dioxide-recovery power-generation gasifier, the thermal efficiency of the plant can be improved. Furthermore, since gasification can be performed by circulating the dried char in the coal gasifier G, G 1 , or G 2 , the carbon conversion ratio at which gasified coal gas is obtained from a gasifiable raw material such as coal can be also increased.
  • feeding of steam to the combustion chamber 10 , feeding of water (water spray) to the reduction chamber 20 , and feeding of steam to the reduction chamber 20 are performed alone, but the present invention is not limited thereto, and various combinations are possible. That is, for example, feeding of steam to the combustion chamber 10 and feeding of water spray to the reduction chamber 20 may be combined and simultaneously performed, or feeding of steam to the combustion chamber 10 and feeding of steam to the reduction chamber 20 may be combined and simultaneously performed. Accordingly, they can be selected according to various conditions.

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  • Chemical Kinetics & Catalysis (AREA)
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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110005395A1 (en) * 2009-07-10 2011-01-13 Southern Company Carbon Dioxide Absorber And Regeneration Assemblies Useful For Power Plant Flue Gas
US20120167585A1 (en) * 2009-09-18 2012-07-05 Wormser Energy Solutions, Inc. Integrated gasification combined cycle plant with char preparation system
US8877136B1 (en) 2012-09-05 2014-11-04 Andrei Razumau Method of producing synthesis gas from coal
US20180230008A1 (en) * 2015-04-30 2018-08-16 CCP Technology GmbH Apparatus and method for producing a synthesis gas
CN108774549A (zh) * 2018-08-29 2018-11-09 中国石油化工股份有限公司 气流床粉煤加氢气化炉、加氢气化系统及加氢气化方法
US10358613B2 (en) * 2015-11-13 2019-07-23 Hyunyong KIM Industrial high-temperature reformer and reforming method
CN110498395A (zh) * 2019-08-08 2019-11-26 中石化宁波工程有限公司 一种用于水煤浆多水气比工况的一氧化碳全部变换工艺

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102884162B (zh) * 2010-04-16 2015-02-25 新日铁住金工程技术株式会社 煤气化反应炉的运转方法及煤气化反应炉
JP5583062B2 (ja) * 2011-03-17 2014-09-03 三菱重工業株式会社 炭化水素原料ガス化炉
EP3423550B1 (en) * 2016-03-04 2021-04-21 Lummus Technology LLC Two-stage gasifier and gasification process with feedstock flexibility
CN105670692A (zh) * 2016-03-30 2016-06-15 浙江工业大学 一种污泥高温水蒸气气化制备富氢燃气的系统
JP6865149B2 (ja) * 2017-11-30 2021-04-28 三菱パワー株式会社 石炭ガス化設備の閉塞防止装置及び閉塞防止方法
CN112831352B (zh) 2021-01-09 2021-09-07 中国华能集团清洁能源技术研究院有限公司 一种高效气化炉及其工作方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3664100A (en) * 1970-06-30 1972-05-23 Sperry Rand Corp Axial combine with rotor and concave convertible to support different threshing elements
US3988123A (en) * 1975-08-15 1976-10-26 The United States Of America As Represented By The United States Energy Research And Development Administration Gasification of carbonaceous solids
US4158552A (en) * 1977-08-29 1979-06-19 Combustion Engineering, Inc. Entrained flow coal gasifier
US4168956A (en) * 1977-08-18 1979-09-25 Combustion Engineering, Inc. Method of operating a coal gasifier
US4343627A (en) * 1980-11-28 1982-08-10 Combustion Engineering, Inc. Method of operating a two-stage coal gasifier
US4872866A (en) * 1987-09-11 1989-10-10 Davis Richard C Medical lavage apparatus

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3864100A (en) 1973-01-02 1975-02-04 Combustion Eng Method and apparatus for gasification of pulverized coal
CA1118600A (en) * 1979-02-21 1982-02-23 Dennis Hebden Two-stage coal gasification process and apparatus
JPH0649874B2 (ja) * 1982-08-25 1994-06-29 株式会社日立製作所 石炭の噴流層ガス化方法
JPH0765484B2 (ja) 1985-04-09 1995-07-19 三菱重工業株式会社 石炭ガス化複合発電装置
US4872886A (en) * 1985-11-29 1989-10-10 The Dow Chemical Company Two-stage coal gasification process
JP2622333B2 (ja) * 1992-10-22 1997-06-18 三菱重工業株式会社 噴流床石炭ガス化炉
JPH06330058A (ja) * 1993-05-26 1994-11-29 Mitsubishi Heavy Ind Ltd 噴流床石炭ガス化炉
JP3546313B2 (ja) * 1994-09-21 2004-07-28 バブコック日立株式会社 噴流層石炭ガス化炉
KR20000015802A (ko) * 1996-05-20 2000-03-15 가나이 쓰도무 석탄 가스화 장치, 석탄 가스화 방법 및 석탄 가스화 복합 발전시스템
JP3976888B2 (ja) 1998-04-15 2007-09-19 新日本製鐵株式会社 石炭の気流床ガス化方法および装置
JP4072612B2 (ja) * 2000-12-27 2008-04-09 独立行政法人産業技術総合研究所 バイオマスを利用した石炭の加圧噴流床ガス化方法
JP2005171148A (ja) * 2003-12-12 2005-06-30 Mitsubishi Heavy Ind Ltd 石炭ガス化炉及びその運転方法
US20090320368A1 (en) * 2006-03-31 2009-12-31 Castaldi Marco J Methods and Systems for Gasifying a Process Stream
CN101432400B (zh) 2006-05-01 2012-11-14 国际壳牌研究有限公司 气化反应器及其应用
JP2008150463A (ja) * 2006-12-15 2008-07-03 Mitsubishi Heavy Ind Ltd 二段噴流床ガス化炉及びその運転制御方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3664100A (en) * 1970-06-30 1972-05-23 Sperry Rand Corp Axial combine with rotor and concave convertible to support different threshing elements
US3988123A (en) * 1975-08-15 1976-10-26 The United States Of America As Represented By The United States Energy Research And Development Administration Gasification of carbonaceous solids
US4168956A (en) * 1977-08-18 1979-09-25 Combustion Engineering, Inc. Method of operating a coal gasifier
US4158552A (en) * 1977-08-29 1979-06-19 Combustion Engineering, Inc. Entrained flow coal gasifier
US4343627A (en) * 1980-11-28 1982-08-10 Combustion Engineering, Inc. Method of operating a two-stage coal gasifier
US4872866A (en) * 1987-09-11 1989-10-10 Davis Richard C Medical lavage apparatus

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110005395A1 (en) * 2009-07-10 2011-01-13 Southern Company Carbon Dioxide Absorber And Regeneration Assemblies Useful For Power Plant Flue Gas
US8303696B2 (en) * 2009-07-10 2012-11-06 Southern Company Carbon dioxide absorber and regeneration assemblies useful for power plant flue gas
US20120167585A1 (en) * 2009-09-18 2012-07-05 Wormser Energy Solutions, Inc. Integrated gasification combined cycle plant with char preparation system
US9873840B2 (en) * 2009-09-18 2018-01-23 Wormser Energy Solutions, Inc. Integrated gasification combined cycle plant with char preparation system
US8877136B1 (en) 2012-09-05 2014-11-04 Andrei Razumau Method of producing synthesis gas from coal
US20180230008A1 (en) * 2015-04-30 2018-08-16 CCP Technology GmbH Apparatus and method for producing a synthesis gas
US10906806B2 (en) * 2015-04-30 2021-02-02 Caphenia Gmbh Apparatus and method for producing a synthesis gas
US10358613B2 (en) * 2015-11-13 2019-07-23 Hyunyong KIM Industrial high-temperature reformer and reforming method
CN108774549A (zh) * 2018-08-29 2018-11-09 中国石油化工股份有限公司 气流床粉煤加氢气化炉、加氢气化系统及加氢气化方法
CN110498395A (zh) * 2019-08-08 2019-11-26 中石化宁波工程有限公司 一种用于水煤浆多水气比工况的一氧化碳全部变换工艺

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CA2730323C (en) 2013-12-24
JP4898759B2 (ja) 2012-03-21
CA2730323A1 (en) 2010-04-29
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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
WO2010047159A1 (ja) 2010-04-29
KR20110034634A (ko) 2011-04-05
EP2338956A1 (en) 2011-06-29

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