WO1997044412A1 - Appareil de gazeification du charbon, procede de gazeification et centrale integree de production d'energie a gazeification de charbon a cycle combine - Google Patents

Appareil de gazeification du charbon, procede de gazeification et centrale integree de production d'energie a gazeification de charbon a cycle combine Download PDF

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Publication number
WO1997044412A1
WO1997044412A1 PCT/JP1997/001668 JP9701668W WO9744412A1 WO 1997044412 A1 WO1997044412 A1 WO 1997044412A1 JP 9701668 W JP9701668 W JP 9701668W WO 9744412 A1 WO9744412 A1 WO 9744412A1
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WIPO (PCT)
Prior art keywords
coal
heat recovery
section
gasification
heat
Prior art date
Application number
PCT/JP1997/001668
Other languages
English (en)
Japanese (ja)
Inventor
Atsushi Morihara
Syntaro Koyama
Yoshio Naganuma
Shinji Tanaka
Sadao Takahashi
Takanori Kudou
Eiji Kida
Yoshiki Noguchi
Original Assignee
Hitachi, Ltd.
Babcock-Hitachi Kabushiki Kaisha
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
Application filed by Hitachi, Ltd., Babcock-Hitachi Kabushiki Kaisha filed Critical Hitachi, Ltd.
Priority to AU27900/97A priority Critical patent/AU730980B2/en
Priority to JP54199397A priority patent/JP4150937B2/ja
Publication of WO1997044412A1 publication Critical patent/WO1997044412A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/466—Entrained flow 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
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/10—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle with exhaust fluid of one cycle heating the fluid in another cycle
    • 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
    • C10J2300/0959—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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • 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]
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • the present invention relates to an integrated coal gasification combined cycle system that supplies fuel gasified using a coal gasifier to a gas turbine to generate power, and mainly relates to a coal gasifier and a coal gasification method.
  • coal in coal gasification, coal is not directly burned, but is converted into flammable gas by a gasification reaction using an oxidizing agent, and is directly supplied to power generation equipment such as gas turbines and fuel cells to be converted into electric energy. It is a method to do.
  • the heat generated in this process is supplied to a steam turbine, which converts it into electrical energy.
  • This method is more efficient because the gas turbine and fuel cell are driven directly by coal gas, compared to the conventional method of generating electricity by generating steam by directly burning coal.
  • power can be generated by using a steam turbine, which can further improve efficiency.
  • the power generation system based on coal gasification is expected as a next-generation high-efficiency power generation system.
  • Coal gasification technology is a technology that generates flammable gas composed of hydrogen, carbon monoxide, methane, carbon dioxide, steam, etc. by bringing coal into contact with oxidizing agents such as oxygen and steam at high temperature. It is.
  • the gas-bed type is a device in which coal is pulverized into fine particles of about 10 microns to improve the contact efficiency with gas. Since the reaction is fast, the temperature in the gasification furnace of the apparatus becomes high and the reaction is completed quickly.
  • a gas-bed gasifier is a coal gasifier with high efficiency and excellent environmental friendliness.
  • the generated gas is also hot.
  • the generated gas contains unreacted carbon remaining after the coal has not completed the reaction, ash contained in the coal, corrosive hydrogen sulfide, and ammonia. If the temperature is higher than 150 ° C, This measure is necessary because the ash in the coal also becomes molten (the molten ash is called slag) and adheres to various equipment.
  • a heat exchanger is provided directly connected to a gasification furnace (however, it is not provided in the same vessel).
  • the heat exchanger was not installed so as to block the gas flow, but was arranged so as to surround the gas flow. are doing. That is, a heat exchanger is installed in parallel with the gas flow. A heat exchanger is placed at a high density where the slag cools and solidifies to block the gas flow.
  • the heat exchanger In the method in which the heat exchanger is arranged so as to surround the gas flow, heat can be recovered without greatly disturbing the gas flow. In particular, even if suspended matter such as slag exists in the generated gas, there is little obstacle due to it. However, since the gas flow is arranged so as to surround the gas flow, the amount of heat transfer per volume of the heat exchange part of the heat exchanger becomes small, and there is a problem that the heat exchanger itself becomes large. Increasing the size of the heat exchanger will increase the cost of the entire system.
  • Japanese Patent Application Laid-Open No. 7-97579 discloses a method of providing a convection heat transfer surface for the purpose of recovering heat not only by radiation but also by heat transfer.
  • the heat transfer tubes can be packed in a large amount, so that the apparatus can be downsized, which is advantageous.
  • the slag in the gas flow adheres to the convection heat transfer surface, which may cause a blockage of the gas flow path or a local high temperature state.
  • the subsequent equipment in the above includes a dust removal device, a desulfurization device, and the like.
  • An object of the present invention is to provide a coal gasification apparatus and a coal gasification method capable of recovering heat obtained by a gasification reaction of coal at a low cost with a reduced burden on subsequent equipment.
  • the gist of the present invention that achieves the above object is as follows.
  • the heat recovery section is directly connected to a stage subsequent to the gasification reaction section, and is provided with power, radiation, and radiation. And a heat transfer tube that transfers heat by convection.
  • the heat transfer tube is provided substantially orthogonal to the gas flow, and the heat recovery unit and the gasification reaction unit are provided in one vessel.
  • the gasification reaction section is in a coal gasifier having an upper reaction area and a lower reaction area.
  • a heat recovery section provided directly after the gasification reaction section is provided with a first heat recovery section, and a surface of a first heat recovery section provided downstream of the first heat recovery section.
  • a coal gasifier consisting of a second heat recovery unit with a low temperature surface is there.
  • the first heat recovery section cools the generated gas temperature from about 140 CTC to about 90 CTC
  • the second heat recovery section converts the 900 ° C gas to about 400 ° C. It is to cool down.
  • coal gasifier having a carbon supply means between the gasification reaction section and the heat recovery section, which adjusts the ratio of carbon and ash in the produced gas by supplying carbon.
  • the heat recovery unit is provided directly after the gasification reaction unit, and is composed of a heat transfer tube that transfers heat by radiation and convection.
  • the heat transfer tube is provided substantially orthogonal to the gas flow.
  • the reaction section has an upper reaction area and a lower reaction area.
  • the upper reaction area is supplied with an amount of oxidizing agent at a temperature at which the ash contained in the coal does not melt, and the lower reaction area has an upper and lower reaction area.
  • Oxidizer is supplied by subtracting the oxidizer supplied to the upper part from the oxidizer required to convert all supplied coal to carbon monoxide and hydrogen, and the radiation provided directly to the reaction section And a coal gasification method in which heat of reaction is recovered by a heat recovery unit that transfers heat by convection.
  • the coal and the oxidizing agent are reacted in the gasification reaction section configured so that the cross-sectional area of the upper end and the lower end is reduced, and the ash content is melted and discharged from the lower end of the gasification reaction section.
  • Combustible gas generated from the upper end This is a coal gasification method in which cooling is performed by a heat recovery unit directly connected to the gasification system.
  • An oxidizing agent is supplied to the lower part of the gasification reaction unit in such a way that the ash of the supplied coal can be melted.
  • the upper part of the gasification reaction section is supplied with an oxidizing agent in an amount such that the ash content in the coal does not melt, and further, carbon is supplied from carbon supply means provided between the gasification reaction section and the heat recovery section.
  • This is a coal gasification method that controls the amount of carbon supplied so that ash does not adhere to the heat recovery section by supplying it.
  • FIG. 1 is a schematic diagram showing a state of a gasification reaction of a gasifier of the present invention.
  • FIG. 2 is a graph showing the relationship between the ratio of carbon and ash in the ash of a coal gasifier and the adhesion of the ash depending on the temperature.
  • FIG. 3 is a schematic longitudinal sectional view of the coal gasifier of Example 1.
  • FIG. 4 is a schematic cross-sectional view of the coal gasifier of the first embodiment.
  • FIG. 5 is a configuration diagram of an integrated coal gasification combined cycle system using the coal gasifier of the first embodiment.
  • FIG. 6 is a graph comparing the operating temperatures of the coal gasifier of the present embodiment and the conventional example.
  • FIG. 7 is a graph comparing the size of the coal gasifier of the present embodiment with that of the conventional example.
  • FIG. 8 is a schematic vertical sectional view of the coal gasifier of the second embodiment.
  • FIG. 9 is a schematic longitudinal sectional view of the coal gasifier of the third embodiment.
  • H 2 0 and C0 2 produced in volatiles of combustion of H 2 and CO (2), (3) reacts with unburned carbon (Chiya I) in a high temperature atmosphere as shown by the combustible gas Form.
  • the temperature of the coal is set to a temperature that is sufficient to melt the ash in the reaction stage, the ash is melted and taken out as a liquid slag, and the harmful metal is encapsulated by cooling it into a slag. Discharge.
  • the coal gasifier of the present invention is a gas-bed type two-stage gasifier, which divides the inside of the gasifier into upper and lower parts, and supplies coal and a small amount of oxidizing agent from the upper part and coal and a large amount of oxidizing agent from the lower part. As a result, the temperature in the lower stage is sufficient for the ash in the coal to melt.
  • FIG. 1 schematically shows a gasification reaction state of the gasification apparatus of the present invention.
  • Coal supplied from the lower parner reacts with a large amount of oxidizing agent to generate product gas and molten ash (slag).
  • coal supplied from the upper parner produces fine char due to the endothermic reaction.
  • the char generated in the upper part of the gasification furnace adheres as powder to the surface of the slag generated in the lower part of the gasification furnace, and has an action and an effect of suppressing adhesion to the furnace wall and the heat recovery part.
  • the coal gasifier of the present invention can prevent the slag generated in the gasifier from adhering to the heat recovery unit by reducing the slag generated in the gasifier.
  • the heat recovery section heat transfer tube
  • Figure 2 shows the relationship between the ratio of carbon and ash in coal ash (char) and the adhesion of ash to temperature.
  • the horizontal axis shows the carbon concentration of the ash, and the vertical axis shows the temperature.
  • the ash adhesion is high in the shaded area. In other words, it indicates that in the region where the temperature is high and the carbon concentration in the ash is low, the ash in the generated gas tends to adhere to the heat recovery section (heat transfer tube). On the other hand, when the temperature is low (below 90 CTC) or when the carbon concentration in the ash is high (over 10%), the adhesion of the ash in the produced gas is low. That is, it shows that it is hard to adhere to the heat transfer tube. From the above, by increasing the ratio of carbon to ash in the generated gas, it is possible to suppress ash from adhering to the heat recovery section such as a heat transfer tube. This This makes it possible to provide a compact coal gasifier in which a heat recovery section for recovering the heat generated in the reaction is integrally disposed immediately after the gasifier.
  • coal gasifier of the present invention supply of a cooling gas or the like is not required, or even if it is supplied, the amount thereof can be reduced. Therefore, subsequent equipment can be downsized.
  • the heat recovery unit provided directly after the gasification reaction unit of the present invention includes:
  • first heat recovery section and the second heat recovery section having a lower temperature than the surface of the first heat recovery section are provided at a subsequent stage of the first heat recovery section.
  • the first and second heat recovery sections are installed in the gas flow so as to be orthogonal to the gas flow direction.
  • TC temperature of the generated gas
  • TC temperature reduced to 900 ° C.
  • high-temperature steam can be obtained.
  • the second heat recovery section the generated heat is generated.
  • Gas temperature 900 ° C is cooled to 40 (TC.
  • the reason for this configuration is to increase the heat transfer efficiency and to make more effective use of the volume.
  • the heat recovery section is a two-stage heat recovery section with different temperatures in order to recover the heat of the generated gas most efficiently.
  • a spiral or zigzag metallic heat transfer tube is preferable.
  • the formation density can be set arbitrarily according to the capacity of the gasification furnace.
  • High-temperature water (or high-temperature steam) is supplied to the heat transfer tube serving as the first heat recovery unit, and low-temperature water (or high-temperature water) is supplied to the heat transfer tube serving as the second heat recovery unit.
  • low-temperature steam to recover heat from the gasification reaction. That is, the first heat recovery unit is used as an evaporator or a super heater, and the second heat recovery unit is used as an evaporator or a economizer.
  • FIG. 3 shows a schematic longitudinal sectional view of the coal gasifier of the present invention.
  • the coal gasifier has a gasification reaction section surrounded by the vessel 51 and a heat recovery section arranged directly connected to the subsequent stage.
  • the gasification reaction section (hereinafter referred to as gasification furnace) consists of a furnace upper part 28 and a furnace lower part 29.
  • An upper nozzle 31 is installed in the furnace upper part 28, and a lower nozzle 32 is installed in the furnace lower part 29.
  • a recycle nozzle 6 is provided at the upper end of the gasifier 25, at the upper end of the gasifier 25, a recycle nozzle 6 is provided. At the lower end of the gasifier 25, a slag tap 26 is provided, and the diameter of the gasifier 25 is reduced at these points.
  • a slag water cooling tank 30 is provided below the gasification furnace 25. Further, a high-temperature heat recovery section 23 and a low-temperature heat recovery section 22 are provided immediately above the gasification furnace 25.
  • the inner wall of the gasifier 25 is protected by a water-cooled wall 24 cooled by water and a refractory material 60 on its surface.
  • Fig. 4 shows a cross-sectional view of the gasification furnace.
  • A Figure shows the part where the recycle nozzle 6 for supplying the recycle gas is provided,
  • (b) shows the part where the upper nozzle 31 is provided, and
  • (c) shows the part where the lower nozzle 32 is provided. It is a cross-sectional view of each of the parts.
  • each nozzle is oriented so that it is supplied to the center in the order of (a), (b), and (c) as shown in the swirl diameters 41 to 43 of the gas flow.
  • the furnace wall can be covered in the order of the recycle gas, the upper product gas, and the lower product gas from the side closer to the furnace wall. That is, the lower temperature gas is made to be on the furnace wall side to protect the furnace wall 44.
  • coal 9 and the oxygen 8 are supplied at a predetermined ratio so that the temperature of the coal 9 and the oxygen 8 does not melt the ash in the coal. From the lower nozzle 32, both coal 9 and oxygen 8 are supplied at a predetermined ratio so as to reach a temperature at which ash is melted.
  • an additive 11 made of limestone or the like for lowering the melting point of the ash or assisting a reaction such as desulfurization in a furnace may be supplied together with the coal.
  • steam 10 may be supplied as a furnace temperature control and an oxidizing agent.
  • the recycled charcoal 13 recovered by the equipment (dust removal device) at the latter stage of the coal gasifier is supplied from below the gasifier 25.
  • a reaction zone having a temperature lower than the melting point of the ash is formed in the furnace upper part 28.
  • a reaction region having a temperature higher than the melting point of the ash is formed in the lower furnace part 29, and a molten slag is formed between this region and the furnace wall.
  • the above-mentioned recycle channel is mainly composed of unburned carbon and ash.
  • Table 1 shows an example of the operating conditions of the above coal gasifier.
  • coal was supplied in equal amounts to the upper part 28 and the lower part 29 of the furnace.
  • Oxygen is supplied in sufficient quantity to gasify the supplied coal.
  • the ratio of total oxygen and total coal under these operating conditions is 0.8 by weight.
  • the ratio of oxygen-free coal was set to 0.58 in order to supply oxygen in an amount that would not melt the ash in the coal.
  • the amount of oxygen supplied to the lower part 29 of the furnace is supplied by subtracting the amount of oxygen supplied to the upper part of the furnace from the total amount of oxygen. Therefore, the ratio of oxygen coal in the lower part 29 of the furnace under the operating conditions is 1.02.
  • the ratio of oxygen supplied together with the recycling channel is included in the total oxygen amount.
  • the temperature of the lower furnace part 29 is about 156 ° C., which is a temperature sufficient to melt the ash in the coal.
  • the upper part 28 of the furnace is in a temperature range (900 to 140 ° C) lower than the melting point of ash, char is generated, and the slag generated in the lower part of the furnace is Adheres as powder on the surface of.
  • the heat recovery sections 23 and 22 heat transfer tubes installed above the gasifier 25, it does not adhere to them. Therefore, it is possible to improve a decrease in heat transfer due to slag adhering to the surface of the heat transfer tube.
  • the carbon powder helps to destroy the boundary layer of the attached matter, so that the heat transfer coefficient of the heat transfer tube can be favorably maintained.
  • the product gas containing slag with low adhesion wrapped in carbon powder is discharged from the outlet throttle section 27 of the gasifier 25 and cooled by the high-temperature heat recovery section 23 cooled first by high-temperature water 5. Heat is recovered as high-pressure steam 4. Next, it is further cooled by the low-temperature heat exchanger 22 cooled by the low-temperature water 3 and recovered as low-pressure steam 2.
  • the product gas cooled as described above is sent to equipment provided downstream of the gasifier outlet 21.
  • Fig. 5 shows the configuration of an integrated coal gasification combined cycle system using the coal gasifier of this embodiment.
  • This power generation system is composed of a coal gasifier, a gas purifier, a combined gas turbine / steam turbine generator, and the like.
  • Oxygen is supplied to the coal gasifier 82 by the oxygen generator 81.
  • Coal is atomized and supplied from a coal hopper 80, pressurized with excess nitrogen generated in an oxygen production unit 81, and compressed by an upper nozzle 31 and a lower nozzle 32 of a coal gasifier 82. Will be re-supplied.
  • the amount of coal supplied to the upper nozzle 31 is adjusted by the upper coal supply controller 92.
  • the amount of coal supplied to the lower nozzle 32 is similarly adjusted by the lower coal supply controller 93.
  • the gasifier 25 in the coal gasifier 82 is recovered as low-pressure water vapor 2 by a heat recovery unit (22, 23 in Fig. 1) that absorbs heat by convection and radiation. Is done.
  • a heat recovery unit 22, 23 in Fig. 1
  • Dust is removed from the generated gas by a dedusting device 83 composed of a cyclone, a high-temperature bag filter, or a high-temperature electrostatic precipitator. Further, sulfides such as H 2 S and COS are removed by a desulfurization device 84 such as a wet desulfurization device that desulfurizes by absorbing liquid or a dry desulfurization device that desulfurizes by using a solid desulfurizing agent.
  • a dedusting device 83 composed of a cyclone, a high-temperature bag filter, or a high-temperature electrostatic precipitator.
  • sulfides such as H 2 S and COS are removed by a desulfurization device 84 such as a wet desulfurization device that desulfurizes by absorbing liquid or a dry desulfurization device that desulfurizes by using a solid desulfurizing agent.
  • the resulting gas, from which dust and sulfur compounds have been removed and purified, is supplied to the combustor of gas turbine 85, which directly burns and drives the turbine and converts it into electric power. Is done.
  • the gas turbine re-loiling temperature must be about 40 (TC or less) for reasons such as valve reliability.
  • the air 61 is compressed to form compressed air.
  • the gas is supplied to the oxygen production unit 81 or the coal gasification unit 82.
  • a part of the purified gas is pressurized by a compressor 101 and supplied to a coal gasifier 82 from a recycling nozzle 6. This is used to cool the gas produced in the gasifier 25.
  • the high-temperature exhaust gas from the gas turbine 85 is recovered as steam by the heat recovery poir 86.
  • the recovered steam is supplied to the steam turbine 87 and converted into electric power.
  • Steam generated by the heat exchanger directly connected to the gasifier is also supplied to the steam turbine to generate power.
  • the coal gasifier of the present invention since the generated gas is efficiently cooled by the heat recovery unit provided directly, the supply amount of the cooling gas can be reduced. . Because of this, the amount of gas other than coal gas passing through the dust removal device 83 and the desulfurization device 84 is small, so that these gas purification devices can be downsized, and the integrated coal gasification combined cycle system can be integrated. It can be downsized.
  • FIG. 6 compares the operating temperatures of the coal gasifier of the present embodiment and the conventional example.
  • the gas temperature at the outlet of the gasifier is as high as about 150 ° C. Therefore, before the product gas reaches the heat exchanger, reduce the temperature to 900 ° C or less. Need to use large amounts of cooling gas. This temperature is shown in FIG.
  • the temperature force at the outlet 27 of the gasification furnace 25 is already as low as 40 CTC, and the ratio of carbon to ash in the generated gas Is large, the adhesion to the heat recovery section and the like is suppressed.
  • the temperature entering the heat recovery section may be about 1200 ° C. Therefore, even when the cooling gas is supplied, the amount may be small.
  • FIG. 7 is a graph comparing the size of the gasifier of the present embodiment with that of the conventional example (including the heat recovery unit).
  • Conventional example 1 is a case where a radiation type heat recovery unit is used in a single-stage reaction type gasification furnace, and since the radiation surface per unit cross-sectional area cannot be increased, the furnace becomes large.
  • Conventional example 2 is a two-stage reaction type gasification furnace, in which the temperature at the outlet of the furnace can be lowered, so that the heat recovery unit can be made relatively small.
  • the heat recovery section can use a convection heat transfer section in addition to the radiant heat transfer section, making the gasification apparatus extremely compact.
  • a gasification zone is formed in the upper and lower stages, only coal is supplied in the upper reaction zone, all ash formed in the upper reaction zone is discharged outside the furnace, and unreacted carbon catalyst collected outside the system is collected. Is collected and supplied to the lower reaction zone as a recycling channel 13. In the lower reaction zone 29, oxygen 8 and coal 9 are supplied, and combustion reaction mainly occurs. reaction A gasification reaction mainly occurs in the upper reaction zone 28 formed in the upper part of the furnace 25.
  • the specific effect of the present embodiment is that the combustible gas formed in the upper reaction zone 28 is discharged without any contact with the oxidizing agent, so that the calorific value of the generated gas can be increased.
  • Embodiment 3 will be described with reference to FIG.
  • This embodiment is a one-stage reaction type coal gasifier.
  • Reaction zone 33 is supplied with coal 9 and oxygen 8. Reduces the ratio of oxygen to coal, forms unreacted carbon, and suppresses adhesion to the heat recovery section. Unreacted carbon is collected by a dust removal device at the subsequent stage and supplied as a recycling channel.
  • ADVANTAGE OF THE INVENTION According to this invention, generation

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Industrial Gases (AREA)

Abstract

L'invention porte sur un appareil de gazéification du charbon construit de manière à ce que le fourneau de gazéification et l'unité de récupération de la chaleur provenant de la réaction de gazéification dans le fourneau soient intégralement compris dans une seule enceinte sans imposer de charge à l'équipement suivant. L'unité de récupération de chaleur, placée immédiatement au-dessus du fourneau, se compose de tubes de chauffe perpendiculaires au flux des gaz produits, tandis que le fourneau de gazéification se compose d'une partie basse et d'une partie haute . Une tuyère d'étage supérieur est placée dans la partie haute, tandis qu'une tuyère d'étage inférieur l'est dans la partie basse. La partie basse fournit du charbon et une grande partie de l'oxydant par l'intermédiaire de la tuyère de l'étage inférieur, de manière à produire une température suffisante pour la fusion du contenu de cendres, tandis que la partie haute fournit du charbon et une faible partie de l'oxydant par l'intermédiaire de la tuyère de l'étage inférieure de manière à produire une température insuffisante pour faire fondre le contenu de cendres. On empêche ainsi le dépôt de cendres sur les parois du four. Par ailleurs, les tubes de chauffe formant l'unité de récupération de chaleur comprennent deux étages de température superficielle différente ce qui permet d'abaisser efficacement la température du gaz produit et d'atténuer les influences sur les matériaux constitutifs de l'équipement suivant.
PCT/JP1997/001668 1996-05-20 1997-05-19 Appareil de gazeification du charbon, procede de gazeification et centrale integree de production d'energie a gazeification de charbon a cycle combine WO1997044412A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AU27900/97A AU730980B2 (en) 1996-05-20 1997-05-19 Coal gasification apparatus and a coal gasification hybrid power generation system
JP54199397A JP4150937B2 (ja) 1996-05-20 1997-05-19 石炭ガス化装置および石炭ガス化方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP8/124396 1996-05-20
JP12439696 1996-05-20

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WO1997044412A1 true WO1997044412A1 (fr) 1997-11-27

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KR (1) KR20000015802A (fr)
CN (1) CN1221446A (fr)
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Cited By (6)

* Cited by examiner, † Cited by third party
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JP2002001103A (ja) * 2000-06-14 2002-01-08 Osaka Gas Co Ltd ２段反応装置の制御方法
WO2003068894A1 (fr) * 2002-02-12 2003-08-21 Hitachi, Ltd. Procede et dispositif de gazeification
JP2008231295A (ja) * 2007-03-22 2008-10-02 Electric Power Dev Co Ltd ガス化炉
CN101608136B (zh) * 2008-06-19 2012-10-24 侯长连 高效煤炭气化炉
JP2012251169A (ja) * 2012-09-24 2012-12-20 Electric Power Dev Co Ltd ガス化炉
CN105779007A (zh) * 2016-03-25 2016-07-20 北京澳柯清洁煤气工程技术有限公司 有余热利用的粉煤灰再气化成煤气的方法

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JP4898759B2 (ja) 2008-10-22 2012-03-21 三菱重工業株式会社 石炭ガス化炉
CN102892870A (zh) * 2010-04-16 2013-01-23 新日铁住金工程技术株式会社 煤气化炉
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JP5818704B2 (ja) * 2012-01-25 2015-11-18 三菱日立パワーシステムズ株式会社 ガス化炉、ガス化発電プラント
JP5518161B2 (ja) * 2012-10-16 2014-06-11 三菱重工業株式会社 ガス化装置
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JP6637797B2 (ja) * 2016-03-11 2020-01-29 三菱日立パワーシステムズ株式会社 炭素含有原料ガス化システム及びその酸化剤分配比設定方法
CN106590760A (zh) * 2017-01-10 2017-04-26 北京清创晋华科技有限公司 一种恒定液位带废锅气化炉
CN109373313B (zh) * 2018-12-03 2024-03-22 北京京诚泽宇能源环保工程技术有限公司 一种净化回收一体化加热炉系统
KR20230067743A (ko) * 2021-11-08 2023-05-17 주식회사 선진티에스 무함수 석탄을 이용한 가스화기-용광로 복합시스템 및 이를 이용한 방법

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JPS5529593A (en) * 1978-08-18 1980-03-01 Metallgesellschaft Ag Gasifying of solid fuel
JPS57179289A (en) * 1981-04-28 1982-11-04 Agency Of Ind Science & Technol Recovering method of heat from gasified product of hydrocarbon
JPS58127789A (ja) * 1982-01-20 1983-07-29 ル−ルコ−レ・アクチエンゲゼルシヤフト 石炭ガス化における急冷方法
JPS58194987A (ja) * 1982-04-26 1983-11-14 シエル・インタ−ナシヨネイル・リサ−チ・マ−チヤツピイ・ベ−・ウイ 固体の炭素含有燃料のガス化法
JPS59172589A (ja) * 1983-03-23 1984-09-29 Hitachi Ltd 石炭ガス化方法
JPS60158293A (ja) * 1984-01-11 1985-08-19 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 合成ガスの製造方法および装置
JPS61207492A (ja) * 1985-03-13 1986-09-13 Mitsubishi Heavy Ind Ltd 石炭ガス化装置
JPS61228093A (ja) * 1985-04-01 1986-10-11 Mitsubishi Heavy Ind Ltd 燃料ガス化装置
JPH0797579A (ja) * 1993-09-28 1995-04-11 Hitachi Ltd 石炭ガス化装置
JPH07286186A (ja) * 1994-04-20 1995-10-31 Hitachi Ltd 石炭ガス化発電プラント
JPH07332612A (ja) * 1994-06-13 1995-12-22 Mitsubishi Heavy Ind Ltd ＣａＳの酸化装置及びその運転方法
JPH0873869A (ja) * 1994-09-06 1996-03-19 Mitsubishi Heavy Ind Ltd 二段噴流床石炭ガス化炉
JPH08104882A (ja) * 1994-10-05 1996-04-23 Hitachi Ltd 噴流層石炭ガス化炉及び石炭ガス化方法

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002001103A (ja) * 2000-06-14 2002-01-08 Osaka Gas Co Ltd ２段反応装置の制御方法
WO2003068894A1 (fr) * 2002-02-12 2003-08-21 Hitachi, Ltd. Procede et dispositif de gazeification
JP2008231295A (ja) * 2007-03-22 2008-10-02 Electric Power Dev Co Ltd ガス化炉
CN101608136B (zh) * 2008-06-19 2012-10-24 侯长连 高效煤炭气化炉
JP2012251169A (ja) * 2012-09-24 2012-12-20 Electric Power Dev Co Ltd ガス化炉
CN105779007A (zh) * 2016-03-25 2016-07-20 北京澳柯清洁煤气工程技术有限公司 有余热利用的粉煤灰再气化成煤气的方法
CN105779007B (zh) * 2016-03-25 2019-02-01 北京澳柯清洁煤气工程技术有限公司 有余热利用的粉煤灰再气化成煤气的方法

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CN1221446A (zh) 1999-06-30
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JP4150937B2 (ja) 2008-09-17
AU2790097A (en) 1997-12-09

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