WO2014175405A1 - ガス化発電プラントの制御装置、ガス化発電プラント、及びガス化発電プラントの制御方法 - Google Patents
ガス化発電プラントの制御装置、ガス化発電プラント、及びガス化発電プラントの制御方法 Download PDFInfo
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- WO2014175405A1 WO2014175405A1 PCT/JP2014/061635 JP2014061635W WO2014175405A1 WO 2014175405 A1 WO2014175405 A1 WO 2014175405A1 JP 2014061635 W JP2014061635 W JP 2014061635W WO 2014175405 A1 WO2014175405 A1 WO 2014175405A1
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- 238000002309 gasification Methods 0.000 title claims abstract description 181
- 238000000034 method Methods 0.000 title claims description 11
- 239000007789 gas Substances 0.000 claims abstract description 139
- 239000007800 oxidant agent Substances 0.000 claims abstract description 100
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 88
- 229910001882 dioxygen Inorganic materials 0.000 claims abstract description 88
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 65
- 229910001873 dinitrogen Inorganic materials 0.000 claims abstract description 61
- 238000000926 separation method Methods 0.000 claims abstract description 36
- 238000004519 manufacturing process Methods 0.000 claims abstract description 31
- 239000000567 combustion gas Substances 0.000 claims abstract description 15
- 230000001590 oxidative effect Effects 0.000 claims description 88
- 239000002893 slag Substances 0.000 claims description 41
- 238000002844 melting Methods 0.000 claims description 34
- 230000008018 melting Effects 0.000 claims description 34
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 33
- 239000001301 oxygen Substances 0.000 claims description 33
- 229910052760 oxygen Inorganic materials 0.000 claims description 33
- 239000000446 fuel Substances 0.000 claims description 32
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 30
- 229910052799 carbon Inorganic materials 0.000 claims description 30
- 239000002737 fuel gas Substances 0.000 claims description 15
- 238000000746 purification Methods 0.000 claims description 15
- 238000002485 combustion reaction Methods 0.000 claims description 13
- 238000007670 refining Methods 0.000 claims description 10
- 230000003068 static effect Effects 0.000 claims description 5
- 239000000155 melt Substances 0.000 claims description 2
- 239000003245 coal Substances 0.000 abstract description 122
- 239000006227 byproduct Substances 0.000 abstract description 4
- 230000004044 response Effects 0.000 abstract description 2
- 230000008859 change Effects 0.000 description 16
- 238000000605 extraction Methods 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- 239000000428 dust Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- 238000010248 power generation Methods 0.000 description 6
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 230000001052 transient effect Effects 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000004927 fusion Effects 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 230000010365 information processing Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 230000002123 temporal effect Effects 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
- F02C6/18—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use using the waste heat of gas-turbine plants outside the plants themselves, e.g. gas-turbine power heat plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/466—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
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
- F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
- F02C3/22—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being gaseous at standard temperature and pressure
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
- F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
- F02C3/26—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension
- F02C3/28—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension using a separate gas producer for gasifying the fuel before combustion
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C9/00—Controlling gas-turbine plants; Controlling fuel supply in air- breathing jet-propulsion plants
- F02C9/26—Control of fuel supply
- F02C9/40—Control of fuel supply specially adapted to the use of a special fuel or a plurality of fuels
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
- F23L7/007—Supplying oxygen or oxygen-enriched air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23N—REGULATING OR CONTROLLING COMBUSTION
- F23N5/00—Systems for controlling combustion
-
- 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
- C10J2300/1678—Integration of gasification processes with another plant or parts within the plant with air separation
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- 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
- F01K23/067—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 the combustion heat coming from a gasification or pyrolysis process, e.g. coal gasification
- F01K23/068—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 the combustion heat coming from a gasification or pyrolysis process, e.g. coal gasification in combination with an oxygen producing plant, e.g. an air separation plant
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F05—INDEXING SCHEMES RELATING TO ENGINES OR PUMPS IN VARIOUS SUBCLASSES OF CLASSES F01-F04
- F05D—INDEXING SCHEME FOR ASPECTS RELATING TO NON-POSITIVE-DISPLACEMENT MACHINES OR ENGINES, GAS-TURBINES OR JET-PROPULSION PLANTS
- F05D2220/00—Application
- F05D2220/70—Application in combination with
- F05D2220/72—Application in combination with a steam turbine
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
Definitions
- the present invention relates to a gasification power plant control device, a gasification power plant, and a gasification power plant control method.
- an integrated coal gasification combined cycle (IGCC) plant has been developed and put into practical use.
- This IGCC plant is obtained by recovering the exhaust heat of a gas turbine that operates with combustible gas obtained by refining the product gas obtained by gasifying coal in a gasification furnace in a gas purification facility. And a steam turbine that is operated by the generated steam.
- coal gas is produced by gasifying coal using oxygen or oxygen-enriched air produced by an oxygen producing apparatus that fractionates nitrogen and oxygen in the air by utilizing the difference in boiling point, and generating power by a gas turbine.
- a power plant is disclosed.
- Patent Document 2 there is an apparatus in which a slag melting burner is installed at the lower part of a coal gasification furnace. Normally, the temperature in the combustor of the coal gasifier is maintained to be equal to or higher than the melting temperature of the ash in the coal, but the ash in the coal is temporarily poorly discharged due to changes in operating conditions and coal properties. It may become. In such a case, the slag is melted by the slag melting burner installed at the lower part of the slag discharge port.
- the oxygen concentration is a parameter that defines the heat input to the gasification furnace.
- the supply amount of the oxidizing agent is feedback controlled (constant oxygen concentration control) so as to be constant with respect to (Gasifier Input Demand) (see FIG. 12).
- the oxygen concentration referred to here is the oxygen concentration in the total gas amount of the oxidant such as air and oxygen gas supplied to the combustor part of the coal gasifier and the inert gas represented by the nitrogen gas for transportation. is there.
- the extracted air from the compressor of the gas turbine is repressurized and used by the air booster, and the oxygen gas is used in the air separation facility (ASU).
- ASU air separation facility
- the flow rate of the oxidant supplied to the coal gasifier is controlled as shown in FIG. 13 so as to increase or decrease in accordance with the load of the coal gasifier.
- the amount of nitrogen gas required to calculate the oxygen concentration is calculated based on various state quantities because it is difficult to measure with high accuracy.
- the amount of nitrogen gas calculated by this also varies.
- the command value of the oxidant flow rate such as the air flow rate and the oxygen flow rate also varies with the variation of the nitrogen gas amount.
- the above-described air flow rate that is used by repressurizing the bleed air from the gas turbine with an air booster can be adjusted relatively easily by adjusting the opening and closing of the IGV of the air booster.
- an air separation facility using a cryogenic separation system or the like has a slow response, and therefore, it is necessary to operate by constantly discharging oxygen and nitrogen in consideration of the fluctuation of the oxygen flow rate command value in advance.
- a slag melting burner In an apparatus in which a slag melting burner is installed in the lower part of a coal gasification furnace, high temperature is required for melting slag, so oxygen gas produced by air separation equipment is used.
- oxygen gas produced by air separation equipment In such an apparatus, for the slag melting burner whose use time is difficult to predict, it is necessary to always discharge the oxygen gas flow rate used by the slag melting burner, which increases the power of the air separation facility. .
- the slag melting burner is used for heating and improving the dischargeability when the dischargeability of the molten slag is temporarily deteriorated due to fluctuations in the state quantity of the gasification furnace and the coal properties.
- the coal gasifier will use the coal associated with the GID so that the coal gasifier outlet pressure maintains the set value. Control is based on the flow rate and the oxidant flow rate. However, GID also has a lot of fluctuations, which also contributes to fluctuations in the oxygen gas flow rate.
- the present invention has been made in view of such circumstances, and can control the release of oxygen gas produced from air to a minimum, a control device for a gasification power plant, a gasification power plant, And it aims at providing the control method of a gasification power plant.
- control device for a gasification power plant the gasification power plant, and the control method for a gasification power plant according to the present invention employ the following means.
- a control device for a gasification power plant includes an air separation device that separates oxygen gas and nitrogen gas from air, a gasification furnace that gasifies carbon-containing fuel using the oxygen gas as an oxidant, And a control device for a gasification power plant comprising a gas turbine driven by a combustion gas obtained by burning a fuel gas obtained by refining the gas produced by the gasification furnace with a gas purification facility, the air separation device An air separation amount determination unit that determines a production amount of the nitrogen gas produced by the gasification power plant according to an operation load of the gasification power plant, and a production amount of the nitrogen gas determined by the air separation amount determination unit Accordingly, the entire amount of oxygen gas by-produced is supplied to the gasifier.
- a gasification power plant is generated by an air separation device that separates oxygen gas and nitrogen gas from air, a gasification furnace that gasifies carbon-containing fuel using oxygen gas as an oxidant, and a gasification furnace.
- a gas turbine that is driven by a combustion gas obtained by combusting a fuel gas obtained by purifying the generated gas with a gas purification facility.
- the carbon-containing fuel is, for example, coal.
- the amount of carbon-containing fuel supplied to the gasification furnace is determined according to the operating load of the gasification power plant, and nitrogen gas is required to convey the determined amount of carbon-containing fuel. Then, oxygen gas is produced from the air by an air separation device together with nitrogen gas for transportation.
- nitrogen gas produced by an air separation device has been produced excessively together with oxygen gas in order to cope with fluctuations on the consumption side, and the excess nitrogen gas and oxygen gas have been discharged.
- the amount of nitrogen gas produced by the air separation device is determined according to the operating load of the gasification power plant by the air separation amount determination unit described above, and by-produced according to the amount of nitrogen gas produced.
- the entire amount of oxygen gas is supplied to the gasifier. Accordingly, the oxygen gas is not produced excessively together with the nitrogen gas, and the entire amount of the oxygen gas produced as a by-product is supplied to the gasification furnace. Can be minimized.
- the total amount of oxidant supplied to the gasifier is adjusted by the amount of air extracted from the gas turbine.
- the oxygen concentration in the gas supplied to the gasifier is controlled by extracting air from the gas turbine to the gasifier. Without making it possible, oxygen that satisfies the amount of oxygen gas consumed in the gasifier can be supplied to the gasifier.
- the operation load of the gasification power plant is an output command value for the gasification power plant.
- the production amount of nitrogen gas is determined based on the output command value for the gasification power plant.
- the production amount of oxygen gas is uniquely determined.
- the output command value shows a more stable value than the gas furnace input command value, which is a parameter that regulates the heat input to the gasifier, so the production amount of nitrogen gas and oxygen gas is also more stable. It becomes a thing.
- the gasification furnace includes a slag melting burner that melts slag in the gasification furnace, and when the slag melting burner is used, the oxygen gas produced by the air separation device contains carbon. It is preferable that the slag melting burner is supplied in preference to the burner for gasifying the fuel.
- the produced oxygen gas is supplied to the slag melting burner in preference to the burner that gasifies the carbon-containing fuel. There is no need to supply gas. Alternatively, in consideration of the amount of oxygen gas used in the slag melting burner, there is no need to constantly blow oxygen gas.
- the gasification power plant includes an oxidant supply path that supplies air extracted from an air compressor of the gas turbine or oxygen separated from the air as an oxidant of the gasification furnace,
- an air ratio fixed mode is adopted in which an air ratio that is a ratio of an oxidant amount supplied to the gasification furnace to a theoretical combustion oxidant amount of the carbon-containing fuel is fixed.
- the air ratio variation mode in which the air ratio can be varied.
- a gasification power plant burns a fuel gas obtained by refining a gas generated by a gasification furnace with a gas refining facility using a oxidizer to gasify a carbon-containing fuel.
- a gas turbine driven by the generated combustion gas, and an oxidant supply passage for supplying air extracted from an air compressor of the gas turbine or oxygen separated from the air as an oxidant of the gasification furnace.
- the carbon-containing fuel is, for example, coal.
- the air ratio is fixed, which is the same as when the gasification power plant is in a static state. It was controlled by mode.
- the operating state quantity of the gasification furnace is, for example, the calorific value of the gas generated in the gasification furnace (generated gas calorific value). Therefore, according to the present invention, when the operation state quantity of the gasification furnace or the load of the gasification power plant changes, the operation mode is switched from the air ratio fixed mode to the air ratio fluctuation mode in which the air ratio can be changed.
- the oxidant amount fluctuates according to the load by entering the air ratio fluctuation mode, so that overshoot of the oxidant amount is suppressed. .
- the amount of oxidant with respect to the amount of carbon-containing fuel supplied to the gasifier is reduced by suppressing the overshoot of the amount of oxidant, combustible gas (for example, in the gas generated in the gasifier) Since the generated amount of CO) increases, the generated gas calorific value increases faster than before, and the gasification power plant settles in a shorter time.
- the overshoot tolerance to be considered with respect to the capacity of the oxidant supply facility is reduced, so that the capacity of the supply facility can be reduced as compared with the conventional case. Further, the smaller the overshoot tolerance is, the more the deviation between the facility planned point of the supply facility and the operating point during normal operation is suppressed.
- this configuration can quickly stabilize the control of the entire plant without increasing the capacity of the oxidizer supply facility.
- the gasification power plant includes an oxidant supply path that supplies air extracted from an air compressor of the gas turbine or oxygen separated from the air as an oxidant of the gasification furnace,
- a gasification power plant burns a fuel gas obtained by refining a gas generated by a gasification furnace with a gas refining facility using a oxidizer to gasify a carbon-containing fuel.
- a gas turbine driven by the generated combustion gas, and an oxidant supply passage for supplying air extracted from an air compressor of the gas turbine or oxygen separated from the air as an oxidant of the gasification furnace.
- the oxidizing agent is, for example, air or oxygen
- the carbon-containing fuel is, for example, coal.
- the air ratio (the amount of the theoretical combustion oxidant of carbon-containing fuel relative to the gasifier is used to keep the gasifier operating state constant, even when the gasifier operating state and the load of the gasification power plant fluctuate.
- the ratio of the amount of oxidant supplied to the gasification furnace) was controlled at a predetermined set value.
- the operating state quantity of the gasification furnace is, for example, the calorific value of the gas generated in the gasification furnace (generated gas calorific value).
- the present invention allows the oxidant amount control means to allow a transient change in the operation state of the gasifier according to the change in the operation state amount of the gasifier or the load of the gasification power plant, that is, The amount of oxidant supplied to the gasifier is controlled within a predetermined upper limit value while allowing the air ratio to deviate from a predetermined set value.
- the upper limit value is based on the amount of air that the air compressor can send to the gasification furnace.
- the upper limit value is a value with a margin for the maximum air volume of the air compressor.
- the allowable range of deviation from a predetermined set value is, for example, 3%, preferably 5%, as a relative ratio to the set value.
- the present invention allows the air ratio to deviate from a predetermined set value, and sets an upper limit value for the amount of oxidant supplied to the gasification furnace. Without increasing, control of the entire plant can be quickly stabilized.
- a gasification power plant includes an air separation device that separates oxygen gas and nitrogen gas from air, a gasification furnace that gasifies carbon-containing fuel using the oxygen gas as an oxidant, A gas turbine driven by a combustion gas obtained by burning a fuel gas obtained by purifying a gas generated by a gasification furnace with a gas purification facility, and the control device described above.
- a control method for a gasification power plant includes an air separation device that separates oxygen gas and nitrogen gas from air, a gasification furnace that gasifies carbon-containing fuel using the oxygen gas as an oxidant, And a control method of a gasification power plant comprising a gas turbine driven by a combustion gas obtained by burning a fuel gas obtained by refining the gas generated by the gasification furnace with a gas purification facility, the air separation device The first step of determining the amount of nitrogen gas produced according to the operation load of the gasification power plant and the amount of nitrogen gas produced as a by-product according to the amount of nitrogen gas determined by the air separation amount determination unit And a second step of supplying the entire amount of oxygen gas to the gasification furnace.
- the present invention is a gasification furnace that gasifies a carbon-containing fuel using an oxidant, and combustion that is obtained by burning a fuel gas obtained by purifying gas generated by the gasification furnace in a gas purification facility.
- IGCC plant gasification combined cycle power plant
- An example of the oxidizing agent is air and oxygen
- an example of the carbon-containing fuel is coal.
- FIG. 1 is a diagram illustrating an overall schematic configuration of an IGCC plant 1 according to the present embodiment.
- the IGCC plant 1 according to this embodiment mainly includes a coal gasification furnace 3, a gas turbine facility 5, a steam turbine facility 7, and an exhaust heat recovery boiler (hereinafter referred to as “HRSG”). 30.
- HRSG exhaust heat recovery boiler
- a coal supply facility 10 for supplying pulverized coal to the coal gasifier 3 is provided on the upstream side of the coal gasifier 3.
- the coal supply facility 10 includes a pulverizer (not shown) that pulverizes raw coal into pulverized coal of several ⁇ m to several hundred ⁇ m.
- the pulverized coal pulverized by the pulverizer is a plurality of hoppers 11. It is to be stored in.
- the pulverized coal stored in each hopper 11 is conveyed to the coal gasification furnace 3 together with nitrogen gas supplied from an air separation facility (hereinafter referred to as “ASU”) 15 at a constant flow rate.
- ASU air separation facility
- the ASU 15 is a device that separates nitrogen gas and oxygen gas from air and supplies them to the coal gasification furnace 3, and valves 15A for discharging the excessively generated nitrogen gas and oxygen gas to the outside, respectively.
- 15B is provided in the supply line to the coal gasification furnace 3. Note that the IGCC plant 1 according to the present embodiment minimizes air discharge without generating excessive nitrogen gas and oxygen gas as will be described in detail later.
- the coal gasification furnace 3 is connected to the coal gasification unit 3a formed so that gas flows from below to above and to the downstream side of the coal gasification unit 3a, and gas flows from above to below.
- the heat exchange part 3b formed in this way is provided.
- the coal gasification unit 3a is provided with a combustor 13 and a reductor 14 from below.
- the combustor 13 burns a part of the pulverized coal and char to generate CO 2 , and the rest is a portion that is released as volatile components (CO, H 2 , lower hydrocarbons) by thermal decomposition.
- the combustor 13 has a spouted bed. However, the combustor 13 may be a fluidized bed type or a fixed bed type.
- the combustor 13 and the reductor 14 are respectively provided with a combustor burner 13a and a reductor burner 14a, and pulverized coal is supplied from the coal supply facility 10 to the combustor burner 13a and the reductor burner 14a.
- the combustor burner 13a is supplied with the air extracted from the air compressor 5c of the gas turbine equipment 5 as an oxidant together with the oxygen gas separated in the ASU 15 via the air booster 17 and the oxidant supply path 8. It has become.
- the combustor burner 13a is supplied with air having an adjusted oxygen concentration.
- the air extracted from the air compressor 5 c may be separated from oxygen by the ASU 15, and the separated oxygen may be supplied to the combustor burner 13 a via the oxidant supply path 8.
- the pulverized coal is gasified by the high-temperature combustion gas from the combustor 13.
- the combustible gas as a gaseous fuel 2 such as CO and H from coal is produced.
- the coal gasification reaction is an endothermic reaction in which pulverized coal and char carbon react with CO 2 and H 2 O in a high-temperature gas to generate CO and H 2 .
- the coal gasification furnace 3 generates gas by reacting the supply air supplied from the air compressor 5c with coal.
- a plurality of heat exchangers (not shown) are installed in the heat exchange section 3b of the coal gasification furnace 3, and sensible heat is obtained from the generated gas guided from the reductor 14 to generate steam. It is like that.
- the steam generated in the heat exchanger is mainly used as driving steam for the steam turbine 7b.
- the generated gas that has passed through the heat exchanging unit 3 b is guided to the dust removal equipment 20.
- the dust removal equipment 20 includes a porous filter, and captures and collects char containing unburned components mixed in the generated gas by passing the generated gas through the porous filter.
- the captured char is deposited on the porous filter to form a char layer. In the char layer, the Na and K components contained in the product gas are condensed, and as a result, the Na and K components are also removed in the dust removal equipment 20.
- the char collected in this way is returned to the char burner 21 of the coal gasifier 3 together with the nitrogen gas supplied from the ASU 15 and recycled.
- the Na and K components returned to the char burner 21 together with the char are discharged from below the coal gasification unit 3a together with the finally melted ash of pulverized coal.
- the molten and discharged ash is quenched with water and crushed into glassy slag.
- the produced gas that has passed through the dust removal equipment 20 is purified by the gas purification equipment 22 and sent to the combustor 5a of the gas turbine equipment 5 as fuel gas.
- the gas turbine equipment 5 sends high-pressure air to the combustor 5a in which the fuel gas obtained by refining the product gas in the gas purification equipment 22 is combusted, the gas turbine 5b driven by the combustion gas, and the combustor 5a. And an air compressor 5c.
- the gas turbine 5b and the air compressor 5c are connected by the same rotating shaft 5d.
- the air compressed in the air compressor 5c is extracted and guided to the air booster 17 separately from the combustor 5a.
- the combustion exhaust gas that has passed through the gas turbine 5b is guided to the HRSG 30.
- the steam turbine 7b of the steam turbine equipment 7 is connected to the same rotating shaft 5d as the gas turbine equipment 5, and is a so-called single-shaft combined system.
- High-pressure steam is supplied to the steam turbine 7b from the coal gasification furnace 3 and the HRSG 30.
- the present invention is not limited to a single-shaft combined system, and may be a two-shaft combined system.
- a generator G that outputs electricity from a rotating shaft 5 d driven by the gas turbine 5 b and the steam turbine 7 b is provided on the opposite side of the gas turbine equipment 5 with the steam turbine equipment 7 interposed therebetween.
- the arrangement position of the generator G is not limited to this position, and may be any position as long as an electric output can be obtained from the rotating shaft 5d.
- the HRSG 30 generates steam from the combustion exhaust gas from the gas turbine 5b and releases the combustion exhaust gas from the chimney 31 to the atmosphere.
- the raw coal is pulverized by a pulverizer (not shown) and then led to the hopper 11 to be stored.
- the pulverized coal stored in the hopper 11 is supplied to the reductor burner 14a and the combustor burner 13a together with the nitrogen gas separated in the ASU 15. Further, the char collected in the dust removal equipment 20 is supplied to the char burner 21.
- the oxygen gas extracted from the air compressor 5c of the gas turbine equipment 5 and further pressurized by the air booster 17 is added with the oxygen gas separated in the ASU 15 and used. .
- pulverized coal and char are partially combusted by combustion air to generate CO 2 , and the remainder is thermally decomposed into volatile components (CO, H 2 , lower hydrocarbons).
- the reductor 14 the pulverized coal supplied from the reductor burner 14a and the char that has released volatile matter in the combustor 13 are gasified by the high-temperature gas rising from the combustor 13, and combustible gases such as CO and H 2 are generated.
- the product gas that has passed through the reductor 14 gives its sensible heat to each heat exchanger while passing through the heat exchange section 3b of the coal gasification furnace 3, thereby generating steam.
- the steam generated in the heat exchange unit 3b is mainly used for driving the steam turbine 7b.
- the product gas that has passed through the heat exchange unit 3b is guided to the dust removal equipment 20, and the char is recovered.
- the Na and K contents in the product gas are condensed here and taken into the char.
- the recovered char containing Na and K is returned to the coal gasifier 3.
- the product gas that has passed through the dust removal equipment 20 is purified by the gas purification equipment 22 and then guided to the combustor 5a of the gas turbine equipment 5, where it is burned together with the compressed air supplied from the air compressor 5c.
- the gas turbine 5b is rotated by the combustion gas, and the rotating shaft 5d is driven.
- the combustion exhaust gas that has passed through the gas turbine 5b is guided to the HRSG 30, and steam is generated by utilizing the sensible heat of the combustion exhaust gas.
- the steam generated in the HRSG 30 is mainly used for driving the steam turbine 7b.
- the steam turbine 7 b is rotated by the steam from the coal gasification furnace 3 and the steam from the HRSG 30, and drives the same rotating shaft 5 d as the gas turbine equipment 5.
- the rotational force of the rotating shaft 5d is converted into an electrical output by the generator G.
- FIG. 2 is a diagram illustrating a path of gas supplied to the slag melting burner 40 included in the coal gasification furnace 3.
- FIG. 2 also shows the path of the gas supplied to the combustor burner 13a together with the slag melting burner 40.
- the combustor burner 13 a is supplied with coal from the coal supply facility 10, air from the air booster 17, and oxygen gas produced by the ASU 15.
- the slag melting burner 40 is supplied with oxygen gas produced by the ASU 15 together with the fuel gas.
- the air supply line to the combustor burner 13a is provided with a flow rate adjusting valve 42a
- the oxygen gas supply line to the combustor burner 13a is provided with a flow rate adjusting valve 42b
- the oxygen gas supply line to the slag melting burner 40 is provided. Is provided with a flow rate adjusting valve 42c.
- a flow rate adjustment valve similar to the flow rate adjustment valve 42a is also provided in the air supply line to the char burner 21, and a flow rate adjustment similar to the flow rate adjustment valve 42b is also provided to the oxygen gas supply line to the char burner 21.
- a valve is provided.
- FIG. 3 is a block diagram illustrating functions of the control device 50 that controls the IGCC plant 1.
- the control device 50 includes, for example, a CPU (Central Processing Unit), a RAM (Random Access Memory), and a computer-readable recording medium.
- a series of processes for realizing various functions of an air separation amount determination unit 52, a necessary oxidant flow rate determination unit 54, an extraction amount determination unit 56, and a burner valve opening determination unit 58, which will be described later, are a program, for example.
- Various functions are realized by the CPU reading this program into the RAM or the like and executing information processing / arithmetic processing.
- the air separation amount determination unit 52 determines the production amount (flow rate) of nitrogen gas by the ASU 15 according to the operation load of the IGCC plant 1. It should be noted that the production amount (flow rate) of oxygen gas by the ASU 15 is uniquely determined along with the production amount of nitrogen gas.
- the necessary oxidant flow rate determination unit 54 determines an oxidant flow rate (hereinafter referred to as “necessary oxidant flow rate”) required by the coal gasification furnace 3 according to the operation load of the IGCC plant 1.
- the extraction amount determination unit 56 calculates the air flow rate that satisfies the deficient oxygen gas amount based on the difference between the amount of oxygen gas produced by the ASU 15 and the required oxygen amount, that is, the shortage of the required oxidant flow rate, and the gas turbine equipment The amount of bleed from the air compressor 5c included in the coal gasifier 3 to the coal gasifier 3 is determined. That is, the total amount of oxidant supplied to the coal gasification furnace 3 is adjusted by the amount of air extracted from the gas turbine equipment 5.
- the burner valve opening degree determination unit 58 determines the opening degree of a flow rate adjusting valve (flow rate adjusting valves 42a, 42b, 42c, etc.) provided in a gas supply line to various burners.
- FIG. 4 is a flowchart showing a flow of processing relating to determination of the oxygen amount (hereinafter referred to as “oxygen amount determination processing”) executed by the control device 50.
- an output command for the IGCC plant 1 (a power generation output command value, hereinafter referred to as “MWD”) is determined as an index indicating the operation load of the IGCC plant 1.
- MWD power generation output command value
- GID gasifier input command
- step 102 the amount of nitrogen gas produced by the ASU 15 based on the determined MWD is determined.
- FIG. 5 is a graph showing the relationship between MWD and consumption of nitrogen gas.
- the consumption amount of nitrogen gas for transporting coal and char to the gasification furnace 13 has a width as shown in FIG. 5 due to transient fluctuations.
- step 104 the maximum value of the width is determined as the amount of nitrogen gas produced by the ASU 15. Note that the larger the MWD, the greater the amount of nitrogen gas produced.
- FIG. 6 is a graph showing the relationship between the production amount of nitrogen gas and the production amount of oxygen gas. As shown in FIG. 6, the production amount of oxygen gas is uniquely determined by the characteristics of the ASU 15 according to the production amount of nitrogen gas.
- FIG. 7 is a graph showing the relationship between MWD and oxygen gas production. As shown in FIG. 7, the production amount of oxygen gas is set as a function with respect to MWD. By using this set function, the control device 50 can easily determine the production amount of oxygen gas.
- the processing in steps 102 and 104 corresponds to the function of the air separation amount determination unit 52.
- step 106 after step 100, the required oxidant flow rate is calculated based on the MWD. Step 106 is performed in parallel with steps 102 and 104. Note that the processing of step 106 corresponds to the function of the necessary oxidant flow rate determination unit 54.
- step 108 the shortage of the necessary oxidant flow rate is calculated.
- the IGCC plant 1 which concerns on this embodiment supplies the whole quantity of manufactured oxygen gas to the coal gasification furnace 3, since not all the required oxidizing agent flow rates can be covered with manufactured oxygen gas, required oxidizing agent flow volume Calculate the shortage of.
- the amount of air extracted from the air compressor 5c to the coal gasifier 3 is determined based on the shortage of the necessary oxidant flow rate. Thereby, the air ratio control of the coal gasification furnace 3 is adjusted by the air extracted from the gas turbine 5b, and the oxygen concentration itself is not controlled.
- steps 108 and 110 corresponds to the function of the extraction amount determination unit 56.
- control device 50 operates the ASU 15 based on the MWD, supplies the entire amount of the produced oxygen gas and nitrogen gas to the coal gasification furnace 3, and outputs the coal from the air compressor 5c based on the calculated extraction amount. Air is supplied to the gasification furnace 3. Therefore, the IGCC plant 1 does not produce excessive oxygen gas together with nitrogen gas, and the entire amount of produced oxygen gas is supplied to the coal gasification furnace 3, so that the oxygen gas produced from the air is discharged. Can be minimized.
- the produced oxygen gas is supplied to the slag melting burner 40 in preference to the combustor burner 13a and the char burner 21.
- the IGCC plant 1 does not need to always supply oxygen gas to the slag melting burner 40.
- FIG. 8 is a diagram showing changes in the opening degree of the flow rate adjusting valves 42a, 42b, and 42c when the slag melting burner 40 is used.
- the fuel gas is supplied to the slag melting burner 40, the flow rate adjustment valve 42c is opened, and the oxygen gas produced by the ASU 15 is supplied to the slag melting burner 40.
- the flow rate adjusting valve 42b for adjusting the oxygen gas flow rate to the combustor burner 13a is throttled according to the oxygen gas flow rate flowing through the flow rate adjusting valve 42c.
- the opening degree of the flow rate adjusting valve 42a that adjusts the air flow rate to the combustor burner 13a does not change. That is, the oxidant flow rate to the combustor burner 13a temporarily decreases.
- FIG. 9 is a diagram showing another form of change in the opening degree of the flow rate adjusting valves 42a, 42b, 42c when the slag melting burner 40 is used.
- the flow rate adjustment valve 42a is opened so as to compensate for the reduced oxygen gas amount by restricting the flow rate adjustment valve 42b. Thereby, the amount of oxygen contained in the oxidizing agent supplied to the combustor burner 13a is maintained.
- the IGCC plant 1 includes an ASU 15 that separates oxygen gas and nitrogen gas from air, a coal gasifier 3 that gasifies coal using an oxidizer, and a coal gasifier. 3 is provided with a gas turbine 5b that is driven by a combustion gas obtained by burning a fuel gas obtained by refining the gas generated by the gas 3 in the gas purification facility 22.
- the control device 50 of the IGCC plant 1 includes an air separation amount determination unit 52 that determines the production amount of nitrogen gas produced by the ASU 15 according to the operation load of the IGCC plant 1, and depends on the decided production amount of nitrogen gas. Then, the entire amount of oxygen gas by-produced is supplied to the coal gasification furnace 3. Therefore, the IGCC plant 1 can minimize the release of oxygen gas produced from air.
- the control device 50 sets the operation mode of the IGCC plant 1 to an air ratio fixed mode in which the air ratio is fixed when the IGCC plant 1 is in a static state, and operates the coal gasifier 3.
- the air ratio variation mode may be adopted in which the air ratio can be varied.
- the air ratio is the ratio of the oxidant flow rate supplied to the coal gasifier 3 to the theoretical combustion oxidant flow rate of the carbon-containing fuel.
- the air ratio was controlled in a fixed air ratio mode.
- the control with a fixed air ratio is, in other words, control for keeping the air ratio constant.
- overshoot may occur in other control amounts (for example, oxidant flow rate) in the coal gasification furnace 3, and it may take time to stabilize the control of the entire IGCC plant 1. It was.
- control device 50 switches the operation mode from the air ratio fixed mode to the air ratio fluctuation mode in which the air ratio can be varied when the fluctuation of the operation state quantity of the coal gasification furnace 3 or the load of the IGCC plant 1 fluctuates. .
- the oxidant flow rate fluctuates according to the load by entering the air ratio fluctuation mode, so that overshoot of the oxidant flow rate is suppressed.
- the oxidant flow rate with respect to the carbon-containing fuel amount supplied to the coal gasification furnace 3 is reduced by suppressing the overshoot of the oxidant flow rate, the combustible gas in the gas generated in the coal gasification furnace 3 is reduced. Since the production amount of the property gas (for example, CO) increases, the generated gas calorific value increases more quickly than before, and the IGCC plant 1 settles in a shorter time.
- the property gas for example, CO
- the overshoot tolerance to be considered with respect to the capacity of the air booster 17 that is an oxidant supply facility is reduced. It can be made smaller. Further, the smaller the overshoot tolerance is, the more the deviation between the facility planned point of the air booster 17 and the operating point during normal operation is suppressed.
- the IGCC plant 1 can quickly stabilize the control of the entire plant without increasing the capacity of the air booster 17.
- the reason why the operating state quantity of the coal gasification furnace 3 fluctuates in other words, the cause of occurrence of hunting in the power generation output of the IGCC plant 1 is as follows.
- the amount of fuel supplied to the gas turbine 5b increases, the actual gasifier pressure (measured value) and the set value of the gasifier pressure, as shown in the region A of the time change of the gasifier pressure in FIG. The deviation of increases.
- region B of the oxidant flow rate change with time in FIG. 10 the amount of extraction from the air compressor 5c of the gas turbine 5b increases and the power generation output of the IGCC plant 1 decreases.
- the reason why the operating state quantity of the coal gasifier 3 fluctuates is that a deviation between the measured value of the gasifier pressure and the set value of the gasifier pressure becomes large.
- the deviation from the set value of the gasifier pressure is 0 or small.
- control device 50 determines that the load of the IGCC plant 1 has fluctuated when the deviation between the measured value of the gasifier pressure and the set value of the gasifier pressure is larger than that at the time of stabilization, and determines the operation mode. Is set to the air ratio fluctuation mode.
- the IGCC plant 1 there is a plant in which the drive shaft of the steam turbine equipment 7 is not coaxial with the drive shaft of the gas turbine 5b.
- the load of the IGCC plant 1 fluctuates, it is assumed that the output of the gas turbine 5b does not increase while the GID increases.
- the GID increases, the coal flow rate increases as shown by the region C of the temporal change in the coal flow rate in FIG.
- the control device 50 of the IGCC plant 1 determines that the load of the IGCC plant 1 has fluctuated when the GID increases while the output of the gas turbine 5b does not increase, and changes the operation mode to the air ratio fluctuation mode. Set.
- control device 50 allows the air ratio to deviate from a predetermined set value in accordance with a change in the operating state quantity of the coal gasification furnace 3 or a change in the load of the IGCC plant 1.
- the oxidant flow rate supplied to the coal gasification furnace 3 is controlled within a predetermined upper limit value.
- the air ratio is set to a predetermined value so as to keep the operating state of the coal gasifier 3 constant. It was controlled to keep on.
- overshoot may occur in other control amounts (for example, oxidant flow rate) in the coal gasification furnace 3, and it may take time for the control of the entire IGCC plant 1 to be stabilized. there were.
- the control device 50 allows a transient change in the operation state of the coal gasification furnace 3 according to the change in the operation state amount of the coal gasification furnace 3 or the change in the load of the IGCC plant 1, that is, the air.
- the oxidant flow rate supplied to the coal gasification furnace 3 is controlled within a predetermined upper limit value while allowing the ratio to deviate from a predetermined set value (see the time variation of the oxidant flow rate in FIGS. 10 and 11). ).
- the upper limit value is based on the air volume that can be supplied to the coal gasification furnace 3 by the air compressor 5c. Specifically, the upper limit value is a value with a margin for the maximum air volume of the air compressor 5c.
- the allowable range of deviation from a predetermined set value is, for example, 3%, preferably 5%, as a relative ratio to the set value.
- the overshoot tolerance to be considered with respect to the capacity of the air booster 17 is reduced.
- control device 50 allows the air ratio to deviate from a predetermined set value and sets an upper limit value for the oxidant flow rate supplied to the coal gasification furnace 3. Control of the entire plant can be quickly stabilized without increasing the capacity.
- each said embodiment demonstrated the form which supplies the total amount of the oxygen gas byproduced according to the production amount of the nitrogen gas manufactured by ASU15 to the coal gasification furnace 3, this invention is based on this.
- the present invention is not limited thereto, and a configuration may be adopted in which substantially the entire amount of oxygen gas by-produced according to the production amount of nitrogen gas is supplied to the coal gasification furnace 3.
- substantially in the total amount means that oxygen gas leakage or the like in the oxygen gas supply line is allowed.
- the mode of determining the extraction amount from the necessary oxidant flow rate calculated based on the MWD has been described.
- the present invention is not limited to this, and the extraction amount for each MWD is determined. It is good also as a form which determines beforehand and determines the amount of extraction based on MWD.
- each said embodiment demonstrated the form which judges the presence or absence of the fluctuation
- the deviation between the measured value and the set value of the outlet pressure of the coal gasification furnace 3, the deviation between the measured value and the set value of the outlet pressure of the gas purification facility 22, or the inlet of the gas turbine 5b It is good also as a form determined based on the deviation of the measured value and setting value of a pressure.
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Abstract
Description
特に、空気吹きのIGCCプラントでは、石炭ガス化炉へ供給される空気として、ガスタービンが有する圧縮機からの抽気を空気昇圧機にて再加圧して使用し、酸素ガスは空気分離設備(ASU)で窒素ガスを製造する際に副生するものを使用している。また、石炭ガス化炉へ供給する酸化剤流量は、石炭ガス化炉の負荷見合いで増減するべく、図13に示されるように制御している。
また、ガスタービンからの抽気を空気昇圧機にて再加圧して使用する上述の空気流量は、空気昇圧機が有するIGVの開閉調整により比較的容易に調整できる。一方、深冷分離方式等による空気分離設備は、応答が遅いため、酸素流量指令値の変動分を予め考慮し、常時酸素及び窒素を放風して運転する必要がある。
なお、スラグ溶融バーナは、ガス化炉の状態量や石炭性状の変動により、一時的に溶融スラグの排出性が悪くなったときに、加熱し排出性を改善するために使用するものである。
これにより、窒素ガスと共に酸素ガスが余剰に製造されることが無く、副生された酸素ガスの全量がガス化炉へ供給されるので、本発明は、空気から製造された酸素ガスの放風を最小限にすることができる。
そこで、本発明は、ガス化炉の運転状態量又はガス化発電プラントの負荷が変動した場合、空気比固定モードから空気比を変動可能とする空気比変動モードへ運転モードが切り替えられる。
また、酸化剤量のオーバーシュートが抑制されるため、酸化剤の供給設備の容量に対して考慮するオーバーシュート裕度が小さくなるので、該供給設備の容量を従来に比べて小さくできる。また、オーバーシュート裕度が小さくなるほど、該供給設備の設備計画点と通常運転時の運転点とのずれが抑制される。
ガス化炉に供給する酸化剤量の制御量に積極的に上限値が設けられることによって、酸化剤量のオーバーシュートが抑制される。また、上限値が設けられることによって、ガス化炉に供給される炭素含有燃料量に対する酸化剤量が小さくなるため、ガス化炉で生成されるガス中の可燃性ガス(例えばCO)の生成量が増加するので生成ガス発熱量が従来に比べてより速く増加し、より短時間でガス化発電プラントが静定する。
また、上限値が設けられることによって、酸化剤量のオーバーシュートが抑制されるため、酸化剤の供給設備の容量に対して考慮するオーバーシュート裕度が小さくなるので、該供給設備の容量を従来に比べて小さくできる。また、オーバーシュート裕度が小さくなるほど、該供給設備の設備計画点と通常運転時の運転点とのずれが抑制される。
本実施形態では、本発明を、酸化剤を用いて炭素含有燃料をガス化させるガス化炉、ガス化炉によって生成されたガスをガス精製設備で精製して得られる燃料ガスを燃焼させた燃焼ガスによって駆動するガスタービン、及びガス化炉及びガスタービンの排ガスにより加熱された蒸気によって駆動する蒸気タービンを備えるガス化複合発電プラント(以下、「IGCCプラント」という。)に適用した場合について説明する。なお、酸化剤の一例を空気及び酸素とし、炭素含有燃料の一例を石炭とする。
図1に示されるように、本実施形態に係るIGCCプラント1は、主として、石炭ガス化炉3、ガスタービン設備5、蒸気タービン設備7、及び排熱回収ボイラ(以下、「HRSG」という。)30を備えている。
各ホッパ11に貯留された微粉炭は、一定流量ずつ空気分離設備(以下、「ASU」という。)15から供給される窒素ガスと共に石炭ガス化炉3へと搬送される。ASU15は、空気から窒素ガス及び酸素ガスを分離し、これらを石炭ガス化炉3へ供給する装置であり、余剰に生成された窒素ガス及び酸素ガスを各々外部へ放風するための弁15A,15Bが石炭ガス化炉3への供給ラインに設けられている。なお、本実施形態に係るIGCCプラント1は、詳細を後述するように窒素ガス及び酸素ガスを余剰に生成することなく、放風を最小限にする。
石炭ガス化部3aには、下方から、コンバスタ13及びリダクタ14が設けられている。コンバスタ13は、微粉炭及びチャーの一部分を燃焼させてCO2を生成し、残りは熱分解により揮発分(CO、H2、低級炭化水素)として放出させる部分である。コンバスタ13には噴流床が採用されている。しかし、コンバスタ13は、流動床式や固定床式であっても構わない。
コンバスタバーナ13aには、ガスタービン設備5の空気圧縮機5cより抽気した空気が空気昇圧機17及び酸化剤供給路8を介して、ASU15において分離された酸素ガスと共に酸化剤として供給されるようになっている。このようにコンバスタバーナ13aには酸素濃度が調整された空気が供給されるようになっている。なお、空気圧縮機5cより抽気した空気は、ASU15にて酸素が分離され、分離された酸素が酸化剤供給路8を介して、コンバスタバーナ13aに供給されてもよい。
蒸気タービン設備7の蒸気タービン7bは、ガスタービン設備5と同じ回転軸5dに接続されており、いわゆる一軸式のコンバインドシステムとなっている。蒸気タービン7bには、石炭ガス化炉3及びHRSG30から高圧蒸気が供給される。なお、一軸式のコンバインドシステムに限らず、二軸式のコンバインドシステムであっても構わない。
ガスタービン5b及び蒸気タービン7bによって駆動される回転軸5dから電気を出力する発電機Gが、蒸気タービン設備7を挟んでガスタービン設備5の反対側に設けられている。なお、発電機Gの配置位置については、この位置に限られず、回転軸5dから電気出力が得られるようであればどの位置であっても構わない。
HRSG30は、ガスタービン5bからの燃焼排ガスによって蒸気を発生すると共に、燃焼排ガスを煙突31から大気へと放出する。
原料炭は粉砕機(図示せず)で粉砕された後、ホッパ11へと導かれて貯留される。ホッパ11に貯留された微粉炭は、ASU15において分離された窒素ガスと共に、リダクタバーナ14a及びコンバスタバーナ13aへと供給される。さらに、チャーバーナ21には、除塵設備20において回収されたチャーが供給される。
リダクタ14では、リダクタバーナ14aから供給された微粉炭及びコンバスタ13内で揮発分を放出したチャーが、コンバスタ13から上昇してきた高温ガスによりガス化され、COやH2等の可燃性ガスが生成される。
熱交換部3bを通過した生成ガスは、除塵設備20へと導かれ、チャーが回収される。生成ガス中のNa分及びK分は、ここで凝縮してチャーに取り込まれる。回収されたNa分及びK分を含むチャーは、石炭ガス化炉3へと返送される。
蒸気タービン7bは、石炭ガス化炉3からの蒸気及びHRSG30からの蒸気によって回転させられ、ガスタービン設備5と同一の回転軸5dを駆動させる。回転軸5dの回転力は、発電機Gによって電気出力へと変換される。
図2に示されるように、コンバスタバーナ13aには石炭供給設備10からの石炭、空気昇圧機17からの空気、及びASU15で製造された酸素ガスが供給される。また、スラグ溶融バーナ40には燃料ガスと共にASU15で製造された酸素ガスが供給される。
コンバスタバーナ13aへの空気の供給ラインには流量調整弁42aが設けられ、コンバスタバーナ13aへの酸素ガスの供給ラインには流量調整弁42bが設けられ、スラグ溶融バーナ40への酸素ガスの供給ラインには流量調整弁42cが設けられている。
制御装置50は、例えば、CPU(Central Processing Unit)、RAM(Random Access Memory)、及びコンピュータ読み取り可能な記録媒体等から構成されている。そして、後述する空気分離量決定部52、必要酸化剤流量決定部54、抽気量決定部56、及びバーナ弁開度決定部58の各種機能を実現するための一連の処理は、一例として、プログラムの形式で記録媒体等に記録されており、このプログラムをCPUがRAM等に読み出して、情報の加工・演算処理を実行することにより、各種機能が実現される。
ここで、IGCCプラント1の運転負荷を示す指標として、MWDの他に、例えば石炭ガス化炉3に投入される入熱を規定するパラメータであるガス化炉入力指令(以下、「GID」という。)がある。MWDは、GIDに比べて、より安定した値を示すので、ASU15による窒素ガス並びに酸素ガスの製造量もより安定したものとなる。
図5は、MWDと窒素ガスの消費量との関係を示すグラフである。石炭及びチャーをガス化炉13へ搬送するための窒素ガスの消費量は、過渡的な変動により、図5に示されるように幅を有している。このためステップ104では、該幅の最大値をASU15による窒素ガスの製造量として決定する。なお、MWDが大きいほど、窒素ガスの製造量は多くなる。
図6は、窒素ガスの製造量と酸素ガスの製造量との関係を示すグラフである。図6に示されるように、窒素ガスの製造量に応じて酸素ガスの製造量がASU15の特性により一意に決定される。
図7は、MWDと酸素ガスの製造量との関係を示すグラフである。図7に示されるように、酸素ガスの製造量は、MWDに対する関数として設定されることとなる。この設定した関数を用いることにより、制御装置50は、簡易に酸素ガスの製造量を決定することができる。
なお、ステップ106の処理は、必要酸化剤流量決定部54の機能に相当する。
これにより、石炭ガス化炉3の空気比制御は、ガスタービン5bから抽気した空気により調整されることとなり、酸素濃度そのものは制御されないこととなる。
従って、IGCCプラント1は、窒素ガスと共に酸素ガスを余剰に製造することが無く、製造された酸素ガスの全量が石炭ガス化炉3へ供給するので、空気から製造された酸素ガスの放風を最小限にすることができる。
図9に示される形態では、スラグ溶融バーナ40を用いる場合、流量調整弁42bを絞ることにより減少した酸素ガス量を補うように、流量調整弁42aが開かれる。これにより、コンバスタバーナ13aへ供給される酸化剤に含まれる酸素量が維持される。
従って、IGCCプラント1は、空気から製造された酸素ガスの放風を最小限にすることができる。
上記実施形態の制御に加えて制御装置50は、IGCCプラント1の運転モードを、IGCCプラント1が静定状態の場合、空気比を固定とする空気比固定モードとし、石炭ガス化炉3の運転状態量又はIGCCプラント1の負荷が変動した場合、空気比を変動可能とする空気比変動モードとしてもよい。なお、空気比は、炭素含有燃料の理論燃焼酸化剤流量に対して石炭ガス化炉3に供給される酸化剤流量の比である。
ガスタービン5bへの燃料供給量が増加すると、図10のガス化炉圧力の時間変化の領域Aで示されるように、実際のガス化炉圧力(計測値)とガス化炉圧力の設定値との偏差が拡大する。これに伴い、図10の酸化剤流量の時間変化の領域Bで示されるように、ガスタービン5bの空気圧縮機5cからの抽気量が増加し、IGCCプラント1の発電出力が減少する。
すなわち、石炭ガス化炉3の運転状態量が変動する原因は、ガス化炉圧力の計測値とガス化炉圧力の設定値との偏差が大きくなることにあると考えられる。なお、IGCCプラント1が静定時の場合は、ガス化炉圧力の設定値との偏差は0又は小さい。
上記実施形態の制御に加えて制御装置50は、石炭ガス化炉3の運転状態量の変動又はIGCCプラント1の負荷の変動に応じて、空気比が予め定められた設定値からずれることを許容して、石炭ガス化炉3に供給する酸化剤流量を所定の上限値内で制御する。
なお、略全量における略とは、酸素ガスの供給ラインにおける酸素ガスの漏れ等を許容する意味である。
3 石炭ガス化炉
5b ガスタービン
15 ASU
22 ガス精製設備
40 スラグ溶融バーナ
50 制御装置
52 空気分離量決定部
Claims (8)
- 空気から酸素ガスと窒素ガスとを分離する空気分離装置、前記酸素ガスを酸化剤として炭素含有燃料をガス化させるガス化炉、及び前記ガス化炉によって生成されたガスをガス精製設備で精製して得られる燃料ガスを燃焼させた燃焼ガスによって駆動するガスタービンを備えるガス化発電プラントの制御装置であって、
前記空気分離装置によって製造される前記窒素ガスの製造量を、前記ガス化発電プラントの運転負荷に応じて決定する空気分離量決定部を備え、
前記空気分離量決定部によって決定された前記窒素ガスの製造量に応じて副生された酸素ガスの全量を、前記ガス化炉へ供給するガス化発電プラントの制御装置。 - 前記ガス化炉へ供給される酸化剤の合計量を、前記ガスタービンから抽気される空気量によって調整する請求項1記載のガス化発電プラントの制御装置。
- 前記ガス化発電プラントの運転負荷は、前記ガス化発電プラントに対する出力指令値である請求項1又は請求項2記載のガス化発電プラントの制御装置。
- 前記ガス化炉は、ガス化炉内のスラグを溶融するスラグ溶融バーナを備え、
前記スラグ溶融バーナが用いられる場合、前記空気分離装置で製造された酸素ガスは、炭素含有燃料をガス化させるバーナよりも前記スラグ溶融バーナに優先して供給される請求項1から請求項3の何れか1項記載のガス化発電プラントの制御装置。 - 前記ガス化発電プラントは、前記ガスタービンの空気圧縮機より抽気した空気又は該空気より分離される酸素を前記ガス化炉の酸化剤として供給する酸化剤供給路を備え、
前記ガス化発電プラントが静定状態の場合、炭素含有燃料の理論燃焼酸化剤量に対して前記ガス化炉に供給される酸化剤量の比である空気比を固定とする空気比固定モードとし、前記ガス化炉の運転状態量又は前記ガス化発電プラントの負荷が変動した場合、前記空気比を変動可能とする空気比変動モードとする請求項1から請求項4の何れか1項記載のガス化発電プラントの制御装置。 - 前記ガス化発電プラントは、前記ガスタービンの空気圧縮機より抽気した空気又は該空気より分離される酸素を前記ガス化炉の酸化剤として供給する酸化剤供給路を備え、
前記ガス化炉の運転状態量の変動又は前記ガス化発電プラントの負荷の変動に応じて、炭素含有燃料の理論燃焼酸化剤量に対して前記ガス化炉に供給される酸化剤量の比である空気比が予め定められた設定値からずれることを許容して、前記ガス化炉に供給する酸化剤量を所定の上限値内で制御する請求項1から請求項4の何れか1項記載のガス化発電プラントの制御装置。 - 空気から酸素ガスと窒素ガスとを分離する空気分離装置と、
前記酸素ガスを酸化剤として炭素含有燃料をガス化させるガス化炉と、
前記ガス化炉によって生成されたガスをガス精製設備で精製して得られる燃料ガスを燃焼させた燃焼ガスによって駆動するガスタービンと、
請求項1から請求項6の何れか1項記載の制御装置と、
を備えるガス化発電プラント。 - 空気から酸素ガスと窒素ガスとを分離する空気分離装置、前記酸素ガスを酸化剤として炭素含有燃料をガス化させるガス化炉、及び前記ガス化炉によって生成されたガスをガス精製設備で精製して得られる燃料ガスを燃焼させた燃焼ガスによって駆動するガスタービンを備えるガス化発電プラントの制御方法であって、
前記空気分離装置によって製造される窒素ガスの製造量を、前記ガス化発電プラントの運転負荷に応じて決定する第1工程と、
前記空気分離量決定部によって決定された窒素ガスの製造量に応じて副生された酸素ガスの全量を、前記ガス化炉へ供給する第2工程と、
を含むガス化発電プラントの制御方法。
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