WO2012114821A1 - 燃焼装置 - Google Patents

燃焼装置 Download PDF

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Publication number
WO2012114821A1
WO2012114821A1 PCT/JP2012/051674 JP2012051674W WO2012114821A1 WO 2012114821 A1 WO2012114821 A1 WO 2012114821A1 JP 2012051674 W JP2012051674 W JP 2012051674W WO 2012114821 A1 WO2012114821 A1 WO 2012114821A1
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Prior art keywords
fuel
pressure
temperature
lpg
gas
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PCT/JP2012/051674
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English (en)
French (fr)
Japanese (ja)
Inventor
横濱　克彦
哲也 木津
斎臣 吉田
弘実 石井
潤 葛西
慎也 ▲濱▼▲崎▼
健太 羽有
Original Assignee
三菱重工業株式会社
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Application filed by 三菱重工業株式会社 filed Critical 三菱重工業株式会社
Priority to AU2012221495A priority Critical patent/AU2012221495B2/en
Priority to CN201280003046.8A priority patent/CN103119367B/zh
Publication of WO2012114821A1 publication Critical patent/WO2012114821A1/ja

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K5/00—Feeding or distributing other fuel to combustion apparatus
    • F23K5/02—Liquid fuel
    • F23K5/14—Details thereof
    • F23K5/142—Fuel pumps
    • 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
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K5/00—Feeding or distributing other fuel to combustion apparatus
    • F23K5/02—Liquid fuel
    • F23K5/04—Feeding or distributing systems using pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K5/00—Feeding or distributing other fuel to combustion apparatus
    • F23K5/02—Liquid fuel
    • F23K5/14—Details thereof
    • F23K5/20—Preheating devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K5/00—Feeding or distributing other fuel to combustion apparatus
    • F23K5/02—Liquid fuel
    • F23K5/14—Details thereof
    • F23K5/22—Vaporising devices
    • 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
    • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • 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
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • 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
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0989—Hydrocarbons as additives to gasifying agents to improve caloric properties
    • 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
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • 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
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
    • 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
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/1653—Conversion of synthesis gas to energy integrated in a gasification combined cycle [IGCC]
    • 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
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C10J2300/1675—Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
    • 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
    • C10J2300/1678—Integration of gasification processes with another plant or parts within the plant with air separation
    • 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]
    • 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 combustion apparatus used in a high-pressure reactor such as a gasification furnace or a gas turbine.
  • the coal gasification combined cycle power generation facility is a power generation facility aiming at higher efficiency and higher environmental performance than conventional coal-fired power by gasifying coal and combining it with combined cycle power generation.
  • This coal gasification combined cycle power generation facility has a great merit that it can use coal with abundant resources, and it is known that the merit can be further increased by expanding the applicable coal types.
  • coal gasification combined power generation facilities generally have a coal supply device, a coal gasification furnace, a char recovery device, a gas turbine facility, a steam turbine facility, an exhaust heat recovery boiler, and a gas purification device. Therefore, coal (pulverized coal) is supplied to the coal gasifier by the coal feeder, and air is taken in. The coal gas is combusted and gasified in the coal gasifier, and the produced gas (combustible gas). Is generated. And this product gas is gas refined after the unburned part (char) of coal is removed by the char recovery device, and it is burned by being supplied to the gas turbine equipment to produce high temperature and high pressure combustion gas. And drive the turbine.
  • the exhaust gas after driving the turbine recovers thermal energy by the exhaust heat recovery boiler, generates steam and supplies it to the steam turbine equipment, and drives the turbine. As a result, power generation is performed.
  • the exhaust gas from which the thermal energy has been recovered is released into the atmosphere through a chimney after harmful substances are removed by the gas purification device.
  • the coal gasification furnace in the coal gasification combined power generation facility described above combusts and gasifies pulverized coal, char, compressed air (oxygen) or water vapor as a gasifying agent, and converts carbon dioxide into A combustible gas having a main component is generated, and a gasification reaction takes place using the combustible gas as a gasifying agent.
  • the coal gasification furnace has a starter burner and a combustion burner as combustion devices. At the time of start-up, auxiliary fuel (for example, kerosene, light oil) is burned using the starter burner. After that, the pulverized coal is burned using a combustion burner for combustion and gasification.
  • Patent Document 1 As such a coal gasification furnace, for example, there is one described in Patent Document 1 below, and as an auxiliary fuel supply device, for example, there is one described in Patent Document 2 below.
  • JP 2009-179790 A Japanese Patent Laid-Open No. 06-011099
  • This invention solves the subject mentioned above, and aims at providing the combustion apparatus which enables stable fuel flow control.
  • a combustion apparatus of the present invention includes a fuel tank that stores fuel, a fuel supply line that supplies the fuel in the fuel tank to a high-pressure reactor, and fuel that is provided in the fuel supply line.
  • a booster that boosts pressure
  • a heating device that is provided in the fuel supply line and heats the fuel after boosting
  • a fuel flow rate regulator that is provided in the fuel supply line and adjusts the flow rate of the boosted and heated fuel
  • a control device for setting the flow rate for setting the flow rate.
  • the fuel when there is a request for operation of the high-pressure reactor, the fuel is boosted beyond the critical pressure and heated above the critical temperature, and its flow rate is adjusted before being supplied to the high-pressure reactor. Because there is no need to control the fuel pressure near the critical pressure and temperature, the fuel has almost no deviation between the actual fuel density and the ideal fuel density with respect to pressure change and temperature change. A stable fuel flow rate can be controlled by the adjusting device.
  • the control device when the control device has requested the high pressure reactor to pressurize the fuel to exceed the critical pressure, the control device exceeds the critical temperature after boosting the fuel to exceed the critical pressure.
  • the fuel is heated, and thereafter, the temperature of the fuel is increased or decreased in a region away from the critical temperature by a predetermined temperature.
  • the fuel is heated above the critical temperature after being boosted above the critical pressure, and then the fuel temperature is increased or decreased in a region away from the critical temperature by a predetermined temperature according to the operation requirements of the high-pressure reactor. Therefore, stable fuel flow rate control can be performed.
  • a pressure sensor for detecting the pressure of the fuel boosted by the booster and a temperature sensor for detecting the temperature of the fuel heated by the heating unit are provided, and the control unit includes the pressure sensor
  • a target temperature of fuel supplied to the pressure reactor is set based on a detection result of the sensor, and the heating device is controlled based on the detection result of the temperature sensor so that the temperature of the fuel becomes a target temperature. It is said.
  • control device controls the heating device so that the temperature of the fuel becomes a target temperature set based on the pressure of the fuel after the pressure increase, the temperature of the fuel can be controlled with high accuracy.
  • the fuel is a fuel that becomes a liquid in a storage device such as a tank, and the control device boosts the fuel in a liquid state to exceed the critical pressure and then uses the heating device to It is characterized by being fed to the high-pressure reactor in a state where the density is stabilized by heating beyond the temperature.
  • the fuel is pressurized in excess of the critical pressure in a liquid state, and then heated to exceed the critical temperature to stabilize the density. In this state, the fuel is supplied to the high-pressure reactor, and the flow control is performed. Stabilization can be enabled.
  • the fuel is boosted above the critical pressure by the booster according to the operation demand of the high-pressure reactor and heated above the critical temperature by the heating device, and then the high-pressure reaction is performed by the fuel flow rate regulator. Since the flow rate of the fuel supplied to the furnace is set, stable fuel flow rate control can be achieved.
  • FIG. 1 is a schematic configuration diagram showing a combustion apparatus according to an embodiment of the present invention.
  • FIG. 2 is a graph showing the state of LPG in the relationship between fuel temperature and fuel pressure.
  • FIG. 3 is a graph showing the relationship between fuel pressure and fuel density.
  • FIG. 4 is a graph showing the relationship between fuel temperature and fuel density.
  • FIG. 5 is a schematic configuration diagram of a coal gasification combined power generation facility to which the combustion apparatus of the present embodiment is applied.
  • FIG. 1 is a schematic configuration diagram showing a combustion apparatus according to an embodiment of the present invention
  • FIG. 2 is a graph showing a state of LPG in the relationship between fuel temperature and fuel pressure
  • FIG. 3 is a graph showing fuel pressure and fuel density.
  • FIG. 4 is a graph showing the relationship between the fuel temperature and the fuel density
  • FIG. 5 is a schematic configuration diagram of the coal gasification combined power generation facility to which the combustion apparatus of this embodiment is applied.
  • the coal gasification combined power generation facility (IGCC: Integrated Coal Gasification Combined Cycle) of the present embodiment adopts an air combustion method in which coal gas is generated in a gasification furnace using air as an oxidizer, and is purified by a gas purification device. Coal gas is supplied as fuel gas to gas turbine equipment to generate electricity. That is, the combined coal gasification combined power generation facility of this embodiment is a power generation facility of an air combustion system (air blowing).
  • the coal gasification combined power generation facility of the present embodiment includes a coal supply device 11, a coal gasification furnace 12, a char recovery device 13, a gas purification device 14, a gas turbine facility 15, a steam turbine facility 16, A generator 17, a waste heat recovery boiler (HRSG) 18, and a gas purification device 19 are included.
  • the coal feeder 11 includes a fluidized bed drying device 21 and a coal pulverizer (mill) 22.
  • the fluidized bed drying apparatus 21 heats the coal by supplying a drying gas to the input coal and removes moisture contained therein.
  • the coal pulverizer 22 pulverizes the coal dried by the fluidized bed dryer 21 into fine particles to produce pulverized coal.
  • the drying gas used in the fluidized bed drying device 21 the gas turbine equipment 15, the exhaust heat recovery boiler 18, or a part of the exhaust gas released into the atmosphere may be used.
  • a cyclone is provided on the downstream side of the coal pulverizer 22 to separate a gas component such as a drying gas and pulverized coal (particle component), and the pulverized coal of the particle component is dropped by gravity and collected in a hopper. On the other hand, the gas component may be exhausted.
  • a gas component such as a drying gas and pulverized coal (particle component)
  • the pulverized coal of the particle component is dropped by gravity and collected in a hopper.
  • the gas component may be exhausted.
  • the coal gasification furnace 12 is connected to a coal supply line 31 from a coal supply device 11 and can supply pulverized coal treated by the coal supply device 11. Further, the char gas recovery furnace 12 is connected to a char return line 32 from the char recovery device 13, and char (unburned coal) recovered by the char recovery device 13 is returned and can be recycled. Yes.
  • the coal gasification furnace 12 is connected to the compressed air supply line 33 from the gas turbine equipment 15 (compressor 61), and can supply compressed air compressed by the gas turbine equipment 15.
  • the air separation device 34 separates and generates nitrogen and oxygen from air in the atmosphere.
  • the first nitrogen supply line 35 is connected to the coal supply line 31 and the second nitrogen supply line 36 is a char return line 32.
  • the oxygen supply line 37 is connected to the compressed air supply line 33. In this case, nitrogen is used as a carrier gas for coal and char, and oxygen is used as an oxidant.
  • the coal gasifier 12 is connected to a fuel line 39 from a fuel tank 38, and can supply LPG (liquefied petroleum gas, LPG) as auxiliary fuel stored in the fuel tank 38. It has become.
  • LPG liquefied petroleum gas
  • the coal gasification furnace 12 is, for example, a spouted bed type gasification furnace, which combusts and gasifies coal, char, air (oxygen) supplied therein, or water vapor as a gasifying agent, and produces carbon dioxide.
  • a combustible gas (product gas, coal gas) containing carbon as a main component is generated, and a gasification reaction takes place using this combustible gas as a gasifying agent.
  • the coal gasification furnace 12 is not limited to a spouted bed gasification furnace, and may be a fluidized bed gasification furnace or a fixed bed gasification furnace.
  • the coal gasification furnace 12 is provided with a combustible gas generation line 40 toward the char recovery device 13 so that the combustible gas containing char can be discharged.
  • the combustible gas may be cooled to a predetermined temperature and then supplied to the char recovery device 13.
  • the char collection device 13 includes a first cyclone 41, a second cyclone 42, a hopper 43, a bin 44 and hoppers 45a and 45b configured as an unburned portion storage unit.
  • the second cyclone 42 separates the fine char contained in the combustible gas from which the coarse char is separated by the first cyclone 41, and the second cyclone discharges the combustible gas from which the fine char is separated at the upper part.
  • a gas discharge line 48 is connected, and a second char discharge line 49 for discharging fine char separated from the combustible gas is connected to the lower part.
  • the hopper 43 is provided in the second char discharge line 49, and temporarily deposits (stores) the fine char separated from the combustible gas by the second cyclone 42.
  • a first pressure equalizing line 50 is provided between the first gas discharge line 46 and the bin 44 to equalize the pressures of both.
  • the bin 44 is connected to the downstream ends of the first char discharge line 47 and the second char discharge line 49, and the coarse char and fine char separated from the combustible gas by the first cyclone 41 and the second cyclone 42. Is to be stored.
  • the hoppers 45a and 45b are connected to the bin 44 via the switching lines 51a and 51b.
  • the switching lines 51a and 51b are provided with the first switching valves 52a and 52b on the upstream side of the hoppers 45a and 45b, and on the downstream side.
  • the second switching valves 53a and 53b are mounted on.
  • the hoppers 45a and 45b are alternately used to enable continuous operation.
  • the switching lines 51 a and 51 b merge at the downstream side of the hoppers 45 a and 45 b and are connected to the char return line 32.
  • the bin 44 is disposed upstream of the two switching lines 51a and 51b (two hoppers 45a and 45b), and the bin 44 for temporarily storing the char is not provided.
  • a configuration in which the bin 44 is not disposed may be employed.
  • the gas purification device 14 performs gas purification by removing impurities such as sulfur compounds and nitrogen compounds from the combustible gas from which the char has been separated by the char recovery device 13.
  • the gas purifier 14 purifies the combustible gas to produce fuel gas, and supplies it to the gas turbine equipment 15.
  • the gas turbine equipment 15 includes a compressor 61, a combustor 62, and a turbine 63, and the compressor 61 and the turbine 63 are connected by a rotating shaft 64.
  • the combustor 62 has a compressed air supply line 65 connected to the compressor 61, a fuel gas supply line 66 connected to the gas purification device 14, and a combustion gas supply line 67 connected to the turbine 63.
  • the gas turbine equipment 15 is provided with a compressed air supply line 33 extending from the compressor 61 to the coal gasification furnace 12, and a booster 68 is provided in the middle.
  • the generator 17 can be driven.
  • the steam turbine facility 16 has a turbine 69 connected to the rotating shaft 64 in the gas turbine facility 15, and the generator 17 is connected to the base end portion of the rotating shaft 64.
  • the exhaust heat recovery boiler 18 is provided in the exhaust gas line 70 from the gas turbine facility 15 (the turbine 63), and generates steam by performing heat exchange between air and high-temperature exhaust gas. Therefore, the exhaust heat recovery boiler 18 is provided with a steam supply line 71 between the steam turbine equipment 16 and the turbine 69 of the steam turbine equipment 16, a steam recovery line 72 is provided, and a condenser 73 is provided in the steam recovery line 72. Yes. Therefore, in the steam turbine equipment 15, the turbine 69 is driven by the steam supplied from the exhaust heat recovery boiler 18, and the generator 17 can be driven by rotating the rotating shaft 64.
  • the gas purification device 19 removes harmful substances from the exhaust gas whose heat has been recovered by the exhaust heat recovery boiler 18, and the purified exhaust gas is discharged from the chimney 74 to the atmosphere.
  • the coal is dried by the fluidized bed drying device 21 in the coal feeding device 11 and pulverized by the coal pulverizer 22 to produce pulverized coal.
  • the pulverized coal is supplied to the coal gasifier 12 through the coal supply line 31 by nitrogen supplied from the air separation device 34.
  • the char recovered by the char recovery device 13 to be described later is supplied to the coal gasification furnace 12 through the char return line 32 by nitrogen supplied from the air separation device 34.
  • the compressed air extracted from the gas turbine equipment 15 to be described later is boosted by the booster 68 and then supplied to the coal gasification furnace 12 through the compressed air supply line 33 together with the oxygen supplied from the air separation device 34.
  • the coal gasification furnace 12 is supplied with the LPG in the fuel tank 38 through the fuel line 39 and is ignited by an ignition torch (not shown) so that the LPG burns and the temperature is raised. Then, when the inside of the coal gasifier 12 is heated to a predetermined temperature, as described above, the pulverized coal is supplied to the coal gasifier 12 through the coal supply line 31 so that the pulverized coal burns. To do.
  • the supplied pulverized coal and char are combusted by compressed air (oxygen), and the pulverized coal and char are gasified, thereby combustible gas (coal gas) containing carbon dioxide as a main component. ) Can be generated.
  • This combustible gas is discharged from the coal gasifier 12 through the gas generation line 40 and sent to the char recovery device 13.
  • the combustible gas is first supplied to the first cyclone 41 so that the coarse char contained in the gas is separated from the combustible gas.
  • the combustible gas from which the coarse char is separated is discharged to the first gas discharge line 46, while the coarse char separated from the combustible gas is discharged to the bin 44 through the first char discharge line 47.
  • the combustible gas from which the coarse char is separated by the first cyclone 41 and discharged to the first gas discharge line 46 is then supplied to the second cyclone 42, where the combustible gas is changed to this gas.
  • the contained fine char is separated.
  • the combustible gas from which the fine char is separated is discharged to the second gas discharge line 48, while the fine char separated from the combustible gas is deposited on the hopper 43 and passes through the second char discharge line 49 to the bin 44.
  • the bin 44 stabilizes the flow. be able to.
  • the char stored in the bin 44 alternately uses the switching line 51a and the hopper 45a, and the switching line 51b and the hopper 45b by alternately opening and closing the switching valves 52a and 53a and the switching valves 52b and 53b. I have to.
  • the char of the bin 44 is stored in the hopper 45a by the switching line 51a.
  • the switching valves 52a and 53a are closed and the switching valves 52b and 53b are opened, whereby the char of the bin 44 is stored in the hopper 45b through the switching line 51b.
  • the char storage operation can be performed continuously, and the char recovery device 13 can be continuously operated.
  • the char stored in the hoppers 45a and 45b is returned to the coal gasification furnace 12 through the char return line 32 and recycled.
  • the combustible gas from which the char has been separated by the char recovery device 13 is gas purified by removing impurities such as sulfur compounds and nitrogen compounds by the gas purification device 14 to produce fuel gas.
  • the gas turbine equipment 15 when the compressor 61 generates compressed air and supplies the compressed air to the combustor 62, the combustor 62 is supplied from the compressed air supplied from the compressor 61 and the gas purification device 14. The fuel gas is mixed and burned to generate combustion gas, and the turbine 63 is driven by this combustion gas, so that the generator 17 can be driven via the rotating shaft 64 to generate power.
  • the exhaust gas discharged from the turbine 63 in the gas turbine equipment 15 generates steam by exchanging heat with air in the exhaust heat recovery boiler 18, and supplies the generated steam to the steam turbine equipment 16. .
  • the turbine 69 is driven by the steam supplied from the exhaust heat recovery boiler 18, so that the generator 17 can be driven via the rotating shaft 64 to generate power.
  • the exhaust gas discharged from the exhaust heat recovery boiler 18 is removed of harmful substances by the gas purification device 19, and the purified exhaust gas is discharged from the chimney 74 to the atmosphere.
  • the combustion apparatus of the present embodiment is configured such that the auxiliary fuel is set to high pressure and high temperature, and is conveyed to a coal gasification furnace 12 used as a high pressure reactor for combustion.
  • the auxiliary fuel used here is a fuel that becomes liquid in the storage facility, that is, LPG mainly composed of propane used as liquefied petroleum gas.
  • the fuel tank 38 can store the LPG as a liquid at room temperature.
  • a fuel line 39 as a fuel supply line has a base end portion connected to the fuel tank 38 and a tip end portion connected to the start burner 101 of the coal gasification furnace 12. (Oxygen) can be supplied.
  • the pump 102 as a booster device is disposed in the vicinity of the fuel tank 38 in the fuel line 39, and can suck LPG from the fuel tank 38 to increase the pressure exceeding a predetermined pressure.
  • An evaporator (heat exchanger) 103 serving as a heating device is disposed downstream of the pump 102 in the fuel line 39, and includes a high-pressure LPG after pressure increase flowing through the fuel line 39 and a heating medium (for example, superheated steam). This LPG can be heated by performing heat exchange between them.
  • the flow rate adjusting valve 104 as a fuel flow rate adjusting device is disposed downstream of the evaporator 103 in the fuel line 39, and can adjust the flow rate of the LPG stabilized in density at high temperature and pressure flowing through the fuel line 39.
  • the control device 105 can control the pump 102, the evaporator 103, and the flow rate adjustment valve 104. That is, the control device 105 can adjust the amount of pressure increase of the LPG by adjusting the rotation speed of the pump 102. Further, the control device 105 can adjust the heating temperature by adjusting the temperature and flow rate of the superheated steam in the evaporator 103. In addition, the control device 105 can adjust the supply amount of LPG supplied to the activation burner 101 through the fuel line 39 by adjusting the opening degree of the flow rate adjustment valve 104.
  • the fuel line 39 is provided with a pressure sensor 106 that detects the pressure of the LPG boosted by the pump 102 on the downstream side of the pump 102.
  • the fuel line 39 is provided with a temperature sensor 107 that detects the temperature of the LPG heated by the evaporator 103 on the downstream side of the flow rate adjustment valve 104 and on the upstream side of the activation burner.
  • the fuel line 39 is provided with a flow rate sensor 108 that detects the supply amount of LPG supplied to the activation burner on the downstream side of the flow rate adjustment valve 104.
  • Each sensor 106, 107, 108 outputs a detection result to the control device 105.
  • the control device 105 adjusts the pump 102, the evaporator 103, and the flow rate adjustment valve 104 based on the detection results of the sensors 106, 107, and 108.
  • the control device 105 controls the pump 102 to increase the LPG exceeding the critical pressure and control the evaporator 103 in accordance with the operation request of the coal gasification furnace 12. Then, the fuel is heated beyond the critical temperature, and then the flow rate of the fuel supplied to the coal gasification furnace 12 is set by controlling the flow rate adjustment valve 104.
  • the control device 105 increases the LPG above the critical pressure and then heats the LPG beyond the critical temperature. Thereafter, the temperature of the LPG is increased or decreased in a region away from the critical temperature by a predetermined temperature.
  • control device 105 sets the target temperature of the LPG supplied to the coal gasification furnace 12 based on the detection result of the pressure sensor 106, and the LPG temperature becomes the target temperature based on the detection result of the temperature sensor 107.
  • the evaporator 103 is controlled.
  • FIG. 2 is a graph showing the LPG state in the relationship between the fuel temperature and the fuel pressure.
  • the left side of the solid line is maintained in the liquid state and the right side is maintained in the gas state.
  • the LPG is first heated beyond the critical pressure without being heated in a liquid state, and then the liquid LPG is heated above the critical temperature at a high pressure to stabilize the density.
  • LPG is supplied to the coal gasifier 12 by the start burner 101, and the temperature of the LPG is adjusted according to the operating state of the coal gasifier 12. Further, the supply amount of LPG is adjusted according to the operating state of the coal gasification furnace 12.
  • FIG. 3 is a graph showing the fuel density that changes as the fuel pressure increases.
  • the fuel density increases, and when it exceeds the critical pressure, it fluctuates greatly and is greatly displaced relative to the pressure of the ideal gas. Will occur.
  • the pressure is increased while the LPG is heated to a predetermined temperature (about 150 ° C.), the fuel density rises almost uniformly and does not fluctuate greatly even if the critical pressure is exceeded. It will be almost the same.
  • FIG. 4 is a graph showing the fuel density that changes as the fuel temperature rises.
  • a predetermined pressure for example, 4 MPa
  • the fuel density tends to increase more than the ideal gas as the temperature decreases in the low temperature region.
  • the fuel density decreases with increasing temperature and tends to approximate an ideal gas.
  • LPG cannot be said to be stable yet when the fuel temperature is close to the critical temperature, and is almost stabilized in the region where the fuel temperature exceeds 50 ° C. from the critical temperature.
  • it is desirable to apply a stable region where the fuel temperature is 200 ° C. or lower than the critical temperature.
  • the flow rate is desirably controlled in this state. As a result, there is little error in the LPG flow rate measurement, and adjustment control of the LPG flow rate supplied to the coal gasification furnace 12 can be performed with high accuracy.
  • the fuel tank 38 that stores LPG the fuel line 39 that supplies the LPG in the fuel tank 38 to the coal gasification furnace 12, and the LPG provided in the fuel line 39.
  • a pump 102 for boosting the pressure an evaporator 103 for heating the boosted LPG, a flow rate adjusting valve 104 for adjusting the flow rate of the boosted and heated fuel provided in the fuel line 39, coal
  • the LPG is pressurized to exceed the critical pressure by the pump 102 and heated to exceed the critical temperature by the evaporator 103, and then supplied to the coal gasification furnace 12 by the flow rate adjustment valve 104.
  • a control device 105 for setting the flow rate of.
  • the LPG when there is a request for operation of the coal gasifier 12, the LPG is boosted to exceed the critical pressure and heated to exceed the critical temperature, and its flow rate is adjusted before being supplied to the coal gasifier 12. Therefore, since it is not necessary to control the flow rate of LPG in the vicinity of the critical pressure and critical temperature of the fuel, LPG is a deviation between the actual LPG density and the ideal density with respect to pressure change and temperature change. Therefore, the LPG flow rate can be stably controlled by the flow rate adjustment valve 104.
  • the controller 105 when the control apparatus 105 has requested the coal gasification furnace 12 to increase the LPG exceeding the critical pressure, the controller 105 increases the LPG after exceeding the critical pressure. After the temperature is exceeded, the LPG temperature is increased or decreased in a region away from the critical temperature by a predetermined temperature. Accordingly, the LPG is heated to exceed the critical temperature after being increased to exceed the critical pressure, and then the LPG temperature is increased or decreased in a region away from the critical temperature by a predetermined temperature according to the operation request of the coal gasification furnace 12. Therefore, stable LPG flow rate control can be performed.
  • a pressure sensor 106 that detects the pressure of the LPG boosted by the pump 102 and a temperature sensor 107 that detects the temperature of the LPG heated by the evaporator 103 are provided.
  • the control device 105 controls the evaporator 103 so that the temperature of the LPG becomes a target temperature set based on the pressure of the LPG after the pressure increase, so that the temperature control of the LPG can be performed with high accuracy. .
  • the control apparatus 105 increases the pressure of the propane to exceed the critical pressure in a liquid state, and then heats the propane to exceed the critical temperature and supplies it to the coal gasifier 12. Yes. Therefore, propane is supplied to the coal gasification furnace 12 in a state in which the density is stabilized by being heated above the critical temperature after being pressurized above the critical pressure in a liquid state. Flow rate control can be performed.
  • the booster is the pump 102.
  • the heating device is the evaporator 103.
  • an electric heater may be used.
  • propane is used as the fuel, for example, LPG or LNG may be used. That is, the fuel may be any fuel that exceeds the critical pressure in the pressurization stage.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Feeding And Controlling Fuel (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
PCT/JP2012/051674 2011-02-21 2012-01-26 燃焼装置 WO2012114821A1 (ja)

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS63135492A (ja) * 1986-11-27 1988-06-07 Babcock Hitachi Kk 石炭ガス化炉用バ−ナ装置
JP2002161283A (ja) * 2000-11-27 2002-06-04 Babcock Hitachi Kk 石炭ガス化装置の起動方法
JP2009179790A (ja) * 2008-01-29 2009-08-13 Mitsubishi Heavy Ind Ltd 石炭ガス化炉の起動方法および起動装置

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JP3097583B2 (ja) * 1996-02-14 2000-10-10 トヨタ自動車株式会社 内燃機関の燃料供給方法及び装置
JPH10141170A (ja) * 1996-11-14 1998-05-26 Toyota Motor Corp 高温高圧噴射用インジェクタ
JP2003262330A (ja) * 2002-03-08 2003-09-19 Nippon Control Kogyo Co Ltd 石油燃焼器用バーナの燃料流量制御装置
JP4078956B2 (ja) * 2002-11-12 2008-04-23 トヨタ自動車株式会社 燃料供給装置
JP2004197655A (ja) * 2002-12-18 2004-07-15 Toyota Motor Corp 燃料供給装置
JP2007085175A (ja) * 2005-09-20 2007-04-05 Hitachi Ltd 車両の燃料性状判定装置
US7655215B2 (en) * 2006-03-06 2010-02-02 Bioconversion Technology Llc Method and apparatus for producing synthesis gas from waste materials

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS63135492A (ja) * 1986-11-27 1988-06-07 Babcock Hitachi Kk 石炭ガス化炉用バ−ナ装置
JP2002161283A (ja) * 2000-11-27 2002-06-04 Babcock Hitachi Kk 石炭ガス化装置の起動方法
JP2009179790A (ja) * 2008-01-29 2009-08-13 Mitsubishi Heavy Ind Ltd 石炭ガス化炉の起動方法および起動装置

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AU2012221495B2 (en) 2014-09-25
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JP5615199B2 (ja) 2014-10-29
AU2012221495A1 (en) 2013-04-18
CN103119367B (zh) 2015-07-01

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