CN103459784A - Combined cycle power plant with CO2 capture plant - Google Patents

Combined cycle power plant with CO2 capture plant Download PDF

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Publication number
CN103459784A
CN103459784A CN2012800073139A CN201280007313A CN103459784A CN 103459784 A CN103459784 A CN 103459784A CN 2012800073139 A CN2012800073139 A CN 2012800073139A CN 201280007313 A CN201280007313 A CN 201280007313A CN 103459784 A CN103459784 A CN 103459784A
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China
Prior art keywords
heat exchanger
lng
cooling
power plant
combined cycle
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Pending
Application number
CN2012800073139A
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Chinese (zh)
Inventor
M.沃森
C.鲁奇蒂
H.李
F.德鲁
F.Z.科札克
A.札戈斯基
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General Electric Technology GmbH
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Alstom Technology AG
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Publication of CN103459784A publication Critical patent/CN103459784A/en
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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
    • F01K23/10—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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • 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
    • F01K13/00—General layout or general methods of operation of complete plants
    • 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
    • F01K23/064—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 in combination with an industrial process, e.g. chemical, metallurgical
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • F22B1/1807—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines using the exhaust gases of combustion engines
    • F22B1/1815—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines using the exhaust gases of combustion engines using the exhaust gases of gas-turbines
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04533—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the direct combustion of fuels in a power plant, so-called "oxyfuel combustion"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04593—The air gas consuming unit is also fed by an air stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/102—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/70—Flue or combustion exhaust gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/02—Compressor intake arrangement, e.g. filtering or cooling
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/80—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/80—Hot exhaust gas turbine combustion engine
    • F25J2240/82—Hot exhaust gas turbine combustion engine with waste heat recovery, e.g. in a combined cycle, i.e. for generating steam used in a Rankine cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
    • 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
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • 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
    • Y02E20/14—Combined heat and power generation [CHP]
    • 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
    • Y02E20/32—Direct CO2 mitigation

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Treating Waste Gases (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

A combined cycle power plant (10) comprises a CO2 capture system (5A, 5B) operatively integrated with a liquefied natural gas LNG regasification system (20), where cold energy from the regasification process is used for cooling processes within the CO2 capture system or processes associated with it. These cooling systems include systems for cooling lean or rich absorption solutions for the CO2 capture or the cooling of flue gas. The LNG regasification system (20) is arranged in one or more heat exchange stages having (21-23) and one or more cold storage units (24, 35, 36). The power plant with CO2 capture (10) can be operated at improved overall efficiencies.

Description

Combined cycle power plant with CO2 catching apparatus
Technical field
The present invention relates to a kind of combined cycle power plant for generating, described combined cycle power plant has gas-turbine, steamturbine and heat recovery steam generator, also relates to a kind of equipment for trapping and compression arbon dioxide.Particularly, the present invention relates to the integrated of LNG Liquefied natural gas processing system and power generating equipment.
Background technique
The combined cycle power plant that becomes known for generating comprises gas-turbine, steamturbine and heat recovery steam generator, and this heat recovery steam generator utilizes the hot flue gases of gas-turbine discharge to produce steam to drive steamturbine.In order to reduce the discharge that causes greenhouse effect, proposed various measures and reduced as far as possible the amount that is discharged into the carbon dioxide in atmosphere.These measures are included in arrangement system in power generating equipment, the CO that its trapping and processing comprise in the vapor plume of heat recovery steam generator HRSG or discharged from coal-fired boiler 2.Such CO 2the trapping process is operated based on for example cold ammonia or amine absorption process.In order effectively to work, these two kinds of methods all need flue gas cools to the temperature lower than 10 ℃.In addition, in order to carry economically and store the CO of trapping 2, be purified, with moisture from, freezing, the compression and liquefaction.For this reason, also need under economic condition, provide enough cold heat exchange medium.Such CO 2catching apparatus needs the energy of specified rate, will reduce thus the overall efficiency of power generating equipment.In order to design the more efficiently CO of having in the energy utilization 2the combined cycle power plant of trapping, proposed to use for some power generating equipment processes the cold energy gasified again from LNG.
JP2000024454 discloses with the vaporization heat of LNG to carry out cooled exhaust air and be solidificated in the carbon dioxide comprised in waste gas.JP60636999 discloses the cold and hot amount produced when evaporation LNG be take from waste gas carbon dioxide recovery as liquefied carbon dioxide of using.WO 2008/009930 discloses in air gas separation unit and has produced nitrogen and oxygen with such cold energy.
US 6,367, and 258 disclose liquefied natural gas vaporization for combined cycle power plant, wherein utilize the cold energy of vaporization to come frozen gas turbine air amount, steamturbine condenser cooling water or for the first thermal fluid of the parts of cooled gas turbine.
The people such as Velautham, use the cooling zero-emission cogeneration circulation of LNG), JSME International Journal, Series B, the 44th volume, the 4th phase, 2001, disclose the cold energy that uses LNG Liquefied natural gas, by with air heat exchange, carrying out cooling-air, expected from air separation oxygen to be further used for combined cycle power plant.Use cold energy of liquefied natural gas to reduce the energy consumption of oxygen-air separation process.Use cold energy of liquefied natural gas and CO are also disclosed 2heat exchange is for CO 2liquefaction.
WO2007/148984 discloses a kind of LNG equipment for gasification again, and wherein rock gas burns in pure oxygen.This equipment also comprises boiler and steamturbine, with the combustion gas by hot, generates electricity.By condensed steam, by resulting vapor plume separation of C O 2.In addition, CO 2cooling and liquefy by LNG.
US5467722 discloses a kind of CO had subsequently 2trapping system and LNG be the combined cycle power plant of equipment for gasification again.CO 2trapping system comprises heat exchanger, and it comes cooling stack gas with trapping low temperature CO with liquid LNG as heat sink 2.
summary of the invention
An object of the present invention is to provide a kind of related CO 2the combined cycle power plant that catching apparatus operates together, compared with known such power generating equipment, combined cycle power plant of the present invention has the power generating equipment efficiency of raising.
Combined cycle power plant air inclusion turbine, steamturbine and heat recovery steam generator (HRSG), wherein two kinds of turbine drives electric organs.In addition, power generating equipment comprises CO 2trapping system, it is operated and is arranged for the treatment of the waste gas from HRSG based on cold ammonia or amine absorption process.
According to the present invention, combined cycle power plant comprises the lng regas system, and it comprises and CO 2the heat exchanger that one or more operation of heat exchanger in trapping system connect.
The gasification again of LNG Liquefied natural gas LNG is provided at CO 2carry out the necessary cold energy of cooling procedure in trapping system.The heat that heat exchange medium in this cooling procedure obtains and then for supporting the gasification again of LNG.CO 2the LNG of trapping system gasification system and cooling system again is integrated into closed circuit system.This integrated reduction operation CO 2trapping system and the required energy of LNG system, otherwise described energy will provide by alternate manner, and for example the electric power by steam extraction and power generating equipment provides.Therefore, it alleviates due to CO 2trapping process and the LNG Efficiency Decreasing that gasification causes again.
In one embodiment of the invention, LNG gasification system again comprises one or more heat exchangers, cascade arrangement, through operation the with the specific range of temperatures at rock gas (from the LNG inlet temperature to ambient temperature) is set, for heat exchange between the heat exchange medium of the LNG of the cold flow side at heat exchanger and hot-fluid side.In output place of heat exchanger, the heat exchange medium of hot-fluid side has low temperature (cryogenic temperature) or cryogenic temperature (chilling temperature), depends on the cold energy requirement of process.
Cryogenic temperature (chilling temperature) can be for example in following scope: from higher than cryogenic temperature (cryogenic temperature) (cryogenic temperature is the temperature lower than-150 ℃) to 10 ℃ or even to ambient temperature, perhaps in one embodiment, for cold ammonia absorption process application, 5 ℃ of-2 ℃ of scopes.
In another embodiment, arrange CO 2trapping system is for cold ammonia absorption process.In order to support the method, power generating equipment comprises pipeline, with this heat exchanger that gasifies again of the medium that heat exchange medium had to low temperature or cryogenic temperature from generation, guides CO into 2one or more refrigeration systems in trapping system, wherein refrigeration system is
-directly contact the cooler in the cooling circuit of cooler in vapor plume,
-be arranged on the water cooler before vapor plume water washing equipment,
-for the cooler of the rich absorbent solution of cooling part stream, for regulating the temperature of described rich absorbent solution stream.
In another embodiment of the present invention, CO 2absorption system is for adopting the amine absorption process for from vapor plume, removing CO 2system, and the system gasified again for LNG with at this CO 2cooling system operation in absorption system connects.The system of this employing amine absorption process needs heat exchange medium, for cooling poor absorbent solution to the about temperature of 45 ℃.As the situation in above embodiment, use and can alleviate due to CO from the cooling of LNG system 2the Efficiency Decreasing that the trapping process causes.In a specific embodiments of the present invention, pipeline leads to the cooler of the barren solution of amine absorption process from the heat exchanger of LNG system, and is back to heat exchanger.
Heat exchanger be take cascade system and is arranged (the input temp that the rock gas output temperature of heat exchange is heat exchanger subsequently, and by heated by natural gas, from LNG entrance cryogenic temperature to-10 ℃ or higher, preferably to 0 ℃ or to ambient temperature), and the load of the cooling infrastructure based on to through the method integrated optimization (cold utilities) and temperature requirement (for example air gas separation unit, CO 2liquefaction process, cold ammonia CO 2cooling requirement in trapping process, combined cycle power plant etc.), LNG again each heat exchanger of gasification system through arranging and arrange with heat exchange in specific temperature range.More specifically, in an exemplary, the natural gas temperature scope in First Heat Exchanger limits by the requirement of the low temperature inlet temperature of LNG and cooling infrastructure with at the heat exchange medium of the hot-fluid side of this First Heat Exchanger.Under vapor pressure again, the boiling temperature of LNG can be used as the gas outlet design temperature of this First Heat Exchanger.In order to reduce equipment size, the gas outlet temperature of the first scope can be higher, usually high 10 ℃-50 ℃ than LNG boiling temperature.This First Heat Exchanger will provide low temperature refrigeration energy or superfreeze energy for cooling infrastructure, and described cooling infrastructure needs utmost point low temperature refrigeration, such as air gas separation unit etc.
The outlet temperature that the gas inlet temperature of the second temperature range is the first scope, and the inlet temperature that the output temperature of the second scope is the 3rd scope.This heat exchanger can be designed to provide the superfreeze energy at the temperature higher than First Heat Exchanger.
The outlet temperature that the gas inlet temperature of the 3rd temperature range is the second scope.This heat exchanger can be designed to provide freezing energy, and it has the temperature higher than the second heat exchanger.
In such cascade arrangement, when the cooling infrastructure to different provides cooling, reduced most possibly the available loss of energy of the freezing energy of LNG.
Particularly, in an exemplary, use following temperature range:
The first natural gas temperature scope :-165 ℃ to-120 ℃, the second temperature range :-120 ℃ to-80 ℃, and the 3rd temperature range :-80 ℃ to 0 ℃.
Each in these heat exchangers can comprise one or more heat-exchange apparatus, and they can be one another in series or be arranged in parallel.Such layout allows flowing of heat exchange medium and temperature controlled flexibility and permission to control the flexibility of the different operation modes of power generating equipment.
In another embodiment of the present invention, LNG gasification system again comprises for storing the cold storage element of LNG, and it is arranged for the above-mentioned cooling system in power generating equipment provides cold heat exchange medium.In the situation that do not move, LNG gasifies again or gasification again, and the cold energy be included in these cold storage elements can be used for CO 2liquefaction process, thus CO can be reduced 2the power consumption of absorption system.
In another embodiment of the present invention, LNG is gasification system again, specifically be arranged as the heat exchanger (heat exchange medium has cryogenic temperature in heat exchanger output place) with heat exchange medium operation, also be connected with the system operation of intake air for the cooling gas-turbine that leads to combined cycle power plant.The cryogenic temperature of medium can be 10 ℃ or lower scope, or the scope of 5 ℃-2 ℃.
In another exemplary of the present invention, LNG gasification system more also is connected with one or more following systems operations, described system with trap CO from the vapor plume from combined cycle power plant 2procedure correlation:
-enter CO in vapor plume 2before trapping system for the system of its cooling and/or freezing (cooling and/or chilling), to meet CO 2the temperature requirement of trapping process,
-for the cooling system of returning to the vapor plume of gas-turbine entrance in HRSG recirculation afterwards,
-return to the system of the vapor plume of gas-turbine entrance for being chilled in recirculation after HRSG,
-for cooling CO 2the CO that trapping system extracts 2system,
-for by freezing, carrying out dry CO 2system.
The recirculation of vapor plume improves the CO in vapor plume 2concentration, thus CO improved 2the trapping process efficiency.
In another exemplary of the present invention, LNG gasification system more also is connected with the cooling water system operation for the steamturbine condenser.By effectively utilizing available cold energy for cooling, and and then utilize and can derive from the LNG low-level heat of the condensation of gasification again, this further improves overall efficiency.
By all above-mentioned cooling systems, by returning to heat exchange medium, draw back the LNG heat exchanger in gasification system again.
The LNG heat that thereby gasification system can provide by cooler and the chiller system of combined cycle power plant again operates.Conversely, the cold energy that cooler and chiller system can provide with LNG operates.
Because these cooling systems no longer need to use the energy extracted by other source of power generating equipment, operate, use can derive from LNG in above any cooling system again the cold energy of gasification system improve overall power generating equipment efficiency.On the other hand, the heat of being fetched by above-mentioned cooling system is provided for the origin of heat that LNG gasifies again.Therefore, do not need or the steam extraction from combined cycle power plant that needs are less operates LNG and gasifies.Can improve the performance (efficiency and power stage) of power generating equipment.
In another exemplary of the present invention, the system gasified again for LNG comprises heat exchanger, and it is through arranging and arrange for liquefying CO 2the CO that trapping system extracts 2.Power generating equipment with such LNG system do not need or needs less for the CO that liquefies 2compressor.In addition, from CO 2the heat of liquefaction process is provided for the LNG heat exchanger of gasification system again.
In another embodiment, power generating equipment comprises pipeline, to guide heat exchange medium into air gas separation unit from the First Heat Exchanger of lng regas system.In output place of heat exchanger, heat exchange medium has cryogenic temperature (temperature is lower than-150 ℃), and for the operation of air separation process, thereby reduce the required energy in this unit of operation.For from other pipeline that returns to heat exchange medium of air gas separation unit, leading to back this First Heat Exchanger, and provide its heat for the lng regas process.
In an alternate embodiment, from the freezing intake air that can exchange to air gas separation unit of the First Heat Exchanger of lng regas system, and from the freezing energy of the second heat exchanger of lng regas system the outlet air for the first compressor of cooling-air separative element.
the accompanying drawing summary
Fig. 1 shows to have CO according to the present invention 2the schematic diagram of the combined cycle power plant of trapping system, particularly LNG gasification system again are connected with the operation between cooling system in power generating equipment.
Fig. 2 shows CO 2the detailed maps of trapping system, particularly cold ammonia absorption system and at LNG system and this CO 2operation between trapping system connects.
Fig. 3 shows CO 2the detailed maps of trapping system, the particularly system based on the amine absorption process and at LNG system and this CO 2operation between trapping system connects.
Fig. 4 shows according to another embodiment of the present invention, has CO 2the schematic diagram of the combined cycle power plant of trapping system, particularly LNG gasification system again are connected with the operation between cooling system in power generating equipment.
implement best mode of the present invention
Fig. 1 describes the combined cycle power plant 10 for generating, it has provides the gas-turbine of ambient air A GT, use the heat recovery steam generator HRSG that produces steam from the hot waste gas of gas-turbine, and by the steam-powered steamturbine ST produced in HRSG.The steam that condenser 1 condensation is expanded, and guide condensation product into HRSG as feed water, thus complete the water/vapor recycle of steamturbine.In addition, power generating equipment comprises CO 2trapping system 5A, 5B, they can be system (5A as shown in FIG. 2) or the system based on the amine absorption process (5B as shown in Figure 3) operated based on cold ammonia absorption process.
The gas-turbine of power generating equipment 10 is used the LNG Liquefied natural gas LNG rock gas that equipment for gasification 20 is supplied again to be operated.Power generating equipment 10 is connected with LNG processing system 20 operations with one or more stages, and system 20 makes low-temperature liquefaction rock gas LNG vaporization, for gas-turbine firing chamber CC.According to the present invention, the LNG in system 20 is one or more cooling in gasification and power generating equipment 10 and refrigeration system is integrated again, to optimize overall power generating equipment efficiency.For this reason, LNG system 20 comprises several stage 21-23, their tandem arrangement, and wherein each stage is relevant to the LNG that gasifies again in particular temperature levels scope roughly.Particularly, CO 2with LNG, gasification system 20 is integrated again in closed heat exchange loop for cooling or refrigeration system in trapping system.
The first embodiment comprises and has CO 2the power generating equipment of trapping system 5a, its system for being operated based on cold ammonia absorption process, as shown in Figure 2.After directly contacting cooler DCC, system 5a comprises CO 2absorption tower A, directly contact vapor plume that cooler DCC will come from HRSG via pipeline G1 and be down to 10 ℃ or lower temperature from the temperature range of 120 ℃-80 ℃ is cooling, and this is that successfully to operate cold ammonia absorption process required.Cooler 31 be arranged in the cooling circuit of direct contact cooler DCC and through arranging so that use the cold energy of the heat exchanger 23 of gasification system 20 again from LNG.Heat exchanger 23 produces the freezing flowing medium of 10 ℃ or lower (for example 2-5 ℃), and it is for cooler 33, with cooling stack gas to the temperature lower than 10 ℃.
Not containing CO 2gas leave tower A via pipeline G5, and guide water washing WW into, by this water washing WW, clean vapor plume gas line G6 used extends to direct contact cooler DCC2.Finally, clean vapor plume is guided flue S and atmosphere from direct contact cooler DCC into via pipeline G7.
Via water pipeline W, with stripper St, with water cooler, 32 operations are connected water washing W W.For pure CO 2the pipeline of stream leads to regenerator RG from stripper St.
CO by the vapor plume trapping 2finally at the top of regenerator RG, discharge, thus it is guided into to further processing, for example compression, dry or freezing.
CO 2absorption tower A with for the cold ammonia (CO that regenerates 2absorbent solution) system connect.Heat again rich CO by regenerator RG 2absorbent solution RS, to discharge CO 2with the poor CO of generation 2solution LS, to be used further to absorption tower A.The absorbent solution regenerative system comprises the cooler 33 of mother solution RS in addition.
At cold ammonia CO 2each above-mentioned cooler 31,32,33 in trapping system 5A need chilled water as temperature the cooling medium lower than 10 ℃, it can provide by the heat exchanger 23 of LNG system 20.Each in these coolers is connected with heat exchanger 23 with 26 by pipeline 25 in closed-loop path.
According to another embodiment of the present invention, CO 2trapping system also can be the system 5B based on the amine absorption process, as shown in Figure 3.System 5B comprises CO 2adsorber B, it provides current and provides poor absorbent stream LS ' via pipeline W.To guide from the vapor plume of HRSG the bottom of adsorber B into, and rise by equipment, with barren solution, LS ' becomes adverse current.Clean vapor plume is left at the equipment top, and guides atmosphere into via flue S.Guide via pipeline RS ' and heat exchanger LRX the mother solution that derives from absorption process into amine regenerator column ARC.Discharge CO at this from solution 2and guide to equipment further to process or to store via condenser C '.Absorption tower ARC further is connected with the loop of containing reboiler RB, by reboiler RB, barren solution is flowed through and guided heat exchanger LRX into by pipeline LS ', wherein barren solution LS ' and mother solution RS ' heat-shift, thus before it enters amine regenering tower ARC the preheating mother solution.Before barren solution LS ' is for absorber column B, need to it is further cooling.For this reason, it is by heat exchanger LSC guiding, and this heat exchanger LSC is set to carry out cooling barren solution by the chilled water in the stage from the LNG system 23 in pipeline 25.To draw the stage of being back to 23 from the water heated of heat exchanger LSC, with again freezing in the stage 23, thus closed-loop path.
The CO extracted from vapor plume 2from regenering tower, ARC leaves, and is drawn towards further processing, for example compression, dry or freezing.
The CO that depends on installation 2the type of trapping system, be cooled to specific temperature range before processing in this system from the vapor plume Ying Qi of HRSG.In the situation that cold ammonia absorption process, before entering adsorber, the preferred temperature of vapor plume is lower than 10 ℃.In the situation that the amine absorption process, the temperature of vapor plume should be approximately 50 ℃, to guarantee optimum operation.For such flue gas cools, power generating equipment comprises flue gas cools device 3A, or if necessary, arranges in addition vapor plume freezer 3B in flue gas line, at CO 2vapor plume cooling or freezing vapor plume is before processed in trapping in processing.Therefore, can take out cold energy fully from the LNG system.Cooler/ chiller system 3A, 3B and then support the LNG system with heat, described heat obtains and guides the LNG system into via pipeline 26 from vapor plume.
Power generating equipment comprises several and CO 2trapping system connects or other relevant cooling system, except CO 2beyond the cooling system of trapping system self, they can with the LNG system intergration.
CO 2trapping system 5A, 5B and CO 2drying is connected with cooling system 6, for the treatment of the CO of trapping 2, it is at CO 2in trapping system, with vapor plume, separate.After cooling system 6, can arrange optional compressor, for CO 2compression.
For the CO by raising vapor plume 2concentration improves CO 2the efficiency of trapping process, power generating equipment 10 can comprise the vapor plume recirculating system in addition, it can comprise the pipeline separated from the discharge pipe line of HRSG, its by undressed vapor plume via flue gas cools device 4a and subsequently optional vapor plume freezer 4b draw return-air body turbine inlet.The cooling or freezing vapor plume that to leave from flue gas cools device or vapor plume freezer guides to respectively expection for the intake air stream A of gas-turbine compressor and mixes with it.
In order further to improve generating equipment capacity, power generating equipment can comprise entrance air freezing system 2, and it uses via pipeline 25 refrigerant from heat exchanger 23, carrys out the cooling for example inlet gas in high ambient air temperature situation.The medium heated returns to heat exchanger 23 via pipeline 26.
Power generating equipment is connected with 20 operations of LNG Liquefied natural gas processing system, and system 20 is used for low-temperature liquefaction rock gas LNG vaporization gas-turbine firing chamber CC and/or exports via gas line.It is integrated that gasification and a plurality of cooling and refrigeration system in power generating equipment 10 adopt the mode of optimizing overall power generating equipment efficiency again.LNG system 20 comprises for example several stage 21-23, their tandem arrangement, and wherein each stage vaporization LNG is to different temperature levels.First stage 21 is through arranging and arrange with gasification LNG, and operates and be connected with air gas separation unit ASU in power generating equipment 10 with 28 via pipeline 27 in closed loop.Pipeline 27 is via flowing medium guiding cryogenic freezing, and with operation A SU, the heat that wherein pipeline 28 will produce in ASU draws the vaporizer stage 21 that is back to, with gasification LNG.
Air gas separation unit ASU is arranged in the pipeline of ambient air, and it separates from the stream of the intake air for gas-turbine compressor pipeline A.The pure oxygen that will extract from ambient air draws winding border air line to compressor, and/or the firing chamber CC of gas-turbine, and/or heat recovery steam generator HRSG, to support aftercombustion.
As shown in Figure 1, the second heat exchanger 22 and CO of LNG system 20 2it is dry that with cooling system, 6 operations are connected.Fully compress CO in compressor 37 2afterwards, the CO that the cold energy of LNG heat exchanger 22 traps from gas-turbine waste gas for liquefaction 2.Can be by the CO of liquefaction 2guide conveying equipment T or any miscellaneous equipment into, for the treatment of or store CO 2.
CO in power generating equipment 2in processing, the second heat exchanger 22 of integrated LNG vaporizer makes the CO that can liquefy 2, and without other CO 2compressor and interstage cooler are by CO 2be compressed to higher pressure.This is arranged and allows significantly to save investment and running cost and device efficiency.
LNG again the 3rd heat exchanger 23 of gasification system 20 by pipeline 25 and 26 and CO 2the chiller system operation of trapping system 5A or 5B connects.For the overall power generating equipment efficiency of extra optimization, other cooling system in power generating equipment 10 can adopt similar mode integrated.These systems comprise for example cooling system, for steamturbine condenser 1.
Itself can comprise one or more gasifier units each in heat exchanger 21-23, and wherein in the situation that several unit, but described unit serial or parallel connection is arranged.Such layout makes can control LNG and heat exchange flow and relevant temperature neatly.
In addition, last heat exchanger 23 can combine with cold storage element 24, and cold storage element 24 also is connected with 26 with pipeline 25 by pipeline.Heat exchanger 22 also can be connected with cold storage element 35, and cold storage element 35 is connected with conveying equipment T with compressor 37 by pipeline.Similarly, heat exchanger 21 can combine with cold storage element 36, and cold storage element 36 is connected with 28 with pipeline 27 via pipeline.This be arranged so that can LNG again gasification parking or while there is no enough derived from processes freezing, the cooling and refrigeration system in the operation power generating equipment.
Fig. 4 shows another exemplary of power generating equipment 10, has the LNG change programme of equipment for gasification 20 ' again.This change programme comprises two heat exchangers 21 and 23 and gasifies for LNG again, has optional cold storage element 24 and 36.Power generating equipment does not have for CO 2the heat exchanger 22 of liquefaction, but the system that comprises compressor 37, compressor 37 has the interstage cooler 34 of arranging after dry and refrigeration system 6.Cooling by 23 pairs of middle cooler supplies of heat exchanger via pipeline 25.
The reference character used in figure
1 The steamturbine condenser
2 The intake air refrigeration system
3A/3B Flue gas cools device/freezer
4A/4B Flue gas cools device/the freezer of recirculation
5A CO 2Trapping system-cold ammonia absorption system
5B CO 2Trapping system-amine absorption process
6 CO 2Drying and cooling system
10 Combined cycle power plant
20，20’ The lng regas system
21 First Heat Exchanger under cryogenic temperature
22 The second heat exchanger under cryogenic temperature
23 The 3rd heat exchanger
24 Cold storage element
25 For the pipeline from the 3rd heat exchanger to the heat exchange medium of power generating equipment
26 For return to gasify the again return line of heat exchange medium of heat exchanger of LNG from power generating equipment
27 For the pipeline of heat exchanger to the Low Temperature Thermal exchange media of air gas separation unit that gasify again from a LNG
28 For return to gasify the again return line of heat exchange medium of heat exchanger of LNG from air gas separation unit
31-33 At cold ammonia CO 2Refrigeration system in trapping system
31 At cold ammonia CO 2Cooler in DCC cooling circuit in trapping system
32 At cold ammonia CO 2Water cooler in trapping system
33 At cold ammonia CO 2Mother solution cooler in trapping system
34 CO 2Interstage cooler
35，36 Cold storage element
37 CO 2Compressor
GT Gas-turbine
ST Steamturbine
HRSG The heat recovery steam generator
A Intake air
ASU Air gas separation unit
LNG LNG Liquefied natural gas
NG The gasification rock gas
DCC Directly contact cooler
A CO 2Adsorber
RG CO 2The absorbent solution regenerator
RS For CO 2Absorb the pipeline of mother solution
LS For CO 2Absorb the pipeline of barren solution
W Water pipeline
WW Water washing equipment
G1，G2，G5，G6，G7 Flue gas line
B CO 2Adsorber
RS’ For CO 2Absorb the pipeline of mother solution
LS’ For CO 2Absorb the pipeline of barren solution
ARC The amine regenerator column
RB Reboiler
C’ The barren solution cooling system
S Flue
T Liquefaction CO 2Transporting system

Claims (13)

1. combined cycle power plant (10), described equipment (10) air inclusion turbine (GT), steamturbine (ST), heat recovery steam generator (HRSG), LNG Liquefied natural gas (LNG) be gasification system (20) again, and
CO 2trapping system (5A, 5B), this CO 2trapping system (5A, 5B), through arranging to process the waste gas of described heat recovery steam generator (HRSG) discharge, is characterized in that
Described lng regas system (20) comprises and described CO 2heat exchanger in trapping system (5A, 5B) (31,32,33,36, the heat exchanger (21,22,23) that LSC) operation connects,
Wherein one or more heat exchangers (21,22,23) with cascade system, arrange, through being provided for operating rock gas under the temperature from the LNG inlet temperature at least-10 ℃, and wherein at least one heat exchanger (23) is through arranging and arrange that wherein this heat exchange medium has cryogenic temperature or cryogenic temperature in output place of this at least one heat exchanger (21) for carry out heat exchange between LNG Liquefied natural gas and heat exchange medium.
2. the combined cycle power plant of claim 1 (10),
It is characterized in that
Described CO 2trapping system is through arranging the system (5A) for cold ammonia absorption process, and described power generating equipment (10) comprises pipeline (25,26), to guide into following one or more at described CO by described heat exchange medium from this heat exchanger (23) that gasifies again 2refrigeration system in trapping system
-directly contact cooler integrated in the cooling circuit of cooler (DCC) (31) in vapor plume,
-the water cooler (32) before at vapor plume water washing equipment (WW),
-for cooling at described CO 2rich CO in trapping system (5A) 2the cooler of absorbent solution (33).
3. the combined cycle power plant of claim 1 (10)
It is characterized in that
Described CO 2trapping system is through arranging the system (5B) for the amine absorption process, for from vapor plume, removing CO 2and described lng regas system (20) comprises one or more heat exchangers (21 of arranging with cascade system, 22,23), through arranging to operate rock gas from the LNG inlet temperature at least 0 ℃, and wherein at least one heat exchanger (21) is through arranging and arrange that wherein this heat exchange medium has cryogenic temperature or cryogenic temperature in output place of this at least one heat exchanger (23) for carry out heat exchange between LNG Liquefied natural gas and heat exchange medium.
4. the combined cycle power plant of claim 3 (10),
It is characterized in that
Described power generating equipment (10) comprises pipeline (25,26), to guide described heat exchange medium into system (LSC) from this heat exchanger (21) that gasifies again, at described CO 2cooling poor CO in the system (5B) of trapping amine absorption process 2solution.
5. claim 1 or 3 combined cycle power plant (10),
It is characterized in that
Described at least one heat exchanger (23) is through arranging and arrange for carrying out heat exchange between LNG Liquefied natural gas and heat exchange medium, described heat exchange medium has cryogenic temperature or cryogenic temperature in output place of heat exchanger, and described at least one heat exchanger (23) is connected with system (2) operation of intake air for the cooling gas-turbine (GT) that enters described combined cycle power plant (10).
6. the combined cycle power plant of claim 5 (10),
It is characterized in that
One or more heat exchangers (21-23) of described lng regas system operate and are connected in addition with the one or more following system of described combined cycle power plant (10):
-system (3a), for entering described CO in vapor plume 2cooling stack gas before trapping system,
-system (3b), for entering described CO in vapor plume 2freezing vapor plume before trapping system,
-cooling water system (1), for the steamturbine condenser,
-system (4a), for the cooling vapor plume of returning to described gas-turbine entrance in HRSG recirculation afterwards,
-system (4b), return to the vapor plume of described gas-turbine entrance for being chilled in recirculation after HRSG,
-system (6), for cooling by described CO 2the CO that trapping system extracts 2,
-system (6), by freezing next dry CO 2.
7. the combined cycle power plant (10) of any one in aforementioned claim 1-6,
It is characterized in that
The heat exchanger of described lng regas system (21-23) is arranged with serial or parallel connection.
8. the combined cycle power plant of claim 7 (10),
It is characterized in that
Described LNG again each heat exchanger of gasification system (20) (21,22,23) through arranging and arranging with heat exchange in given temperature range, each heat exchanger (21 wherein, 22,23) can comprise one or more heat-exchange apparatus, they can be one another in series or be arranged in parallel.
9. the combined cycle power plant of claim 5 (10),
It is characterized in that
Described lng regas system (20) comprises one or more cold storage elements, for storing LNG Liquefied natural gas, with its heat exchanger (21-23), is arranged in parallel.
10. claim 1 or 3 combined cycle power plant (10),
It is characterized in that
The described system for lng regas comprises through arranging and arranging for the described CO that liquefies 2the CO that trapping system extracts 2heat exchanger (22).
11. the combined cycle power plant of claim 6 and 10 (10),
It is characterized in that
Have from for dry and cooling CO 2system (6) lead to for CO 2the pipeline of the heat exchanger (22) of liquefaction, and the liquefaction CO that leads to conveying equipment (T) or pump from this heat exchanger (22) 2pipeline.
12. the combined cycle power plant of claim 1 (10),
It is characterized in that
Described lng regas system (20) comprises: heat exchanger (21), and described heat exchanger (21) is through arranging and arrange with in LNG Liquefied natural gas with have in output place of described heat exchanger (21) between the medium of cryogenic temperature and carry out heat exchange; Pipeline (27) with the described heat exchange medium that leads to air gas separation unit (27); With lead to back the pipeline (28) of described heat exchanger (21) from described air gas separation unit (ASU).
13. the combined cycle power plant of claim 5 (10),
It is characterized in that
Described lng regas system (21-23) operates and is connected in addition with the cooling system for steamturbine (ST) condenser (1).
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