WO2012104202A1 - 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
WO2012104202A1
WO2012104202A1 PCT/EP2012/051267 EP2012051267W WO2012104202A1 WO 2012104202 A1 WO2012104202 A1 WO 2012104202A1 EP 2012051267 W EP2012051267 W EP 2012051267W WO 2012104202 A1 WO2012104202 A1 WO 2012104202A1
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WO
WIPO (PCT)
Prior art keywords
power plant
heat exchanger
natural gas
combined cycle
cooling
Prior art date
Application number
PCT/EP2012/051267
Other languages
French (fr)
Inventor
Manfred Wirsum
Christoph Ruchti
Hongtao Li
François Droux
Frederic Zenon Kozak
Alexander Zagorskiy
Original Assignee
Alstom Technology Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Alstom Technology Ltd filed Critical Alstom Technology Ltd
Priority to CN2012800073139A priority Critical patent/CN103459784A/en
Priority to EP12703480.9A priority patent/EP2673478A1/en
Priority to JP2013552159A priority patent/JP2014512471A/en
Publication of WO2012104202A1 publication Critical patent/WO2012104202A1/en
Priority to US13/953,143 priority patent/US20130312386A1/en

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Classifications

    • 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

Definitions

  • the present invention pertains to a combined cycle power plant for the generation of electric power having a gas turbine, a steam turbine, and a heat recovery steam generator, and furthermore a plant for the capture and compression of carbon dioxide.
  • the invention pertains in particular to an integration of a liquefied natural gas processing system with the power plant.
  • Combined cycle power plants for the generation of electricity are known to include a gas turbine, a steam turbine, and a heat recovery steam generator utilizing the hot flue gases emitted by the gas turbine to generate steam to drive the steam turbine.
  • various measures have been proposed to minimize the amount of carbon dioxide emitted into the atmosphere.
  • Such measures include the arrangement of systems in the power plant that capture and process C02 contained in the flue gases exhausted by a heat recovery steam generator HRSG or a coal-fired boiler.
  • C02 capture processes operate for example on the basis of chilled ammonia or amine processes. In order to work effectively, both of these processes require that the flue gases are cooled to temperatures below 10°C.
  • the captured C02 is transported and stored economically, it is purified, separated from water, chilled, compressed, and liquefied. For this, among others, sufficiently cold heat exchange media need to be provided at economical conditions.
  • a C02 capture plant of this type requires a given amount of energy, which reduces the overall efficiency of the power plant. In order to design a combined cycle power plant with C02 capture more energy efficiently, it has been proposed to use the cold energy from the LNG regasification for some power plant processes.
  • JP2000024454 discloses the use of vaporization heat of LNG to cool waste gases and solidify carbon dioxide contained in the waste gases.
  • JP60636999 discloses the use of cold heat generated upon the evaporation of LNG to recover carbon dioxide from exhaust gas as liquefied carbon dioxide.
  • WO 2008/009930 discloses the use of such cold energy in an air separation unit to produce nitrogen and oxygen.
  • US 6,367,258 discloses the vaporization of liquefied natural gas for a combined cycle power plant, where the cold energy of the vaporization is utilized for the chilling of gas turbine intake air, steam turbine condenser cooling water, or a first heat transfer fluid intended to cool components in the gas turbine.
  • Velautham et al. «Zero emission combined Power cycle using LNG cold » JSME International Journal, Series B, Vol. 44, No.4, 2001 , discloses the use of liquefied natural gas cold for cooling air in heat exchange with air in view of separating oxygen from the air for further use in a combined cycle power plant.
  • the use of liquefied natural gas cold reduces the energy consumption of the oxygen-air-separation process.
  • the use of liquefied natural gas cold energy in heat exchange with C02 for its liquefication is also disclosed.
  • the WO2007/148984 discloses a LNG regasification plant in which natural gas is burned in pure oxygen.
  • the plant also comprises a boiler and a steam turbine to generate electricity from the hot combustion gases. From the resulting flue gas C02 is separated by condensation of water vapor. Further, C02 is cooled against LNG for liquefaction.
  • the US5467722 discloses a combined cycle power plant with a subsequent C02 capture system and a LNG regasification plant.
  • the C02 capture system comprises heat exchangers, which cool the flue gas for cryogenic C02 capture using liquid LNG as a heat sink.
  • a combined cycle power plant comprises a gas turbine, a steam turbine, and a heat recovery steam generator (HRSG), both turbines driving a generator.
  • the power plant comprises furthermore a C02 capture system operating on the basis of a chilled ammonia or an amine process and arranged to process exhaust gases from the HRSG.
  • the combined cycle power plant comprises a liquefied natural gas regasification system, which comprises heat exchangers operatively connected with one or more heat exchangers within the C02 capture system.
  • the regasification of the liquefied natural gas LNG provides the cold energy necessary to operate cooling processes in the C02 capture system.
  • the heat gained by the heat exchange medium in that cooling process is in turn used to support the regasification process of the LNG.
  • the LNG regasification system and the cooling systems of the C02 capture system are integrated in a closed circuit system. This integration reduces the amount of energy needed to operate the C02 capture system and LNG system, which otherwise would to be provided by other means, for example by steam extraction and electricity from the power plant. It therefore mitigates the efficiency reduction due to the C02 capture process and LNG regasification processes.
  • the LNG regasification system comprises one or more heat exchangers, configured for the operation at a specific temperature range of the natural gas in a cascaded arrangement, form a LNG inlet temperature up to ambient temperature, for heat exchange between the LNG on the cold stream side and a heat exchange medium on the hot stream side of the heat exchanger.
  • the heat exchange medium on the hot stream side has cryogenic or chilling temperatures at the output of the heat exchanger depending on the cold requirements of the process.
  • the chilling temperatures can be for example in the range from above a cryogenic temperature (cryogenic temperatures are temperatures below -150 °C) up to ⁇ ⁇ ⁇ or even up to ambient temperature, or in an embodiment in a range from 5°C to 2°C for chilled ammonia process applications.
  • the C02 capture system is arranged for the chilled ammonia process.
  • the power plant comprises lines to direct the heat exchange medium from this regasification heat exchanger generating a medium having cryogenic or chilling temperatures to one or more refrigeration systems within the C02 capture system, where the refrigeration systems are
  • a cooler for cooling part of a rich absorption solution flow for the purpose of regulating the temperature thereof.
  • the C02 absorption system is a system for the removal of the C02 from flue gases by means of an amine process and the system for the LNG regasification is operatively connected to cooling systems within this C02 absorption system.
  • This amine process system requires a heat exchange medium for cooling the absorption lean solution to temperatures of about 45°C.
  • lines lead from the heat exchanger of the LNG system to a cooler for amine process lean solution and back to the heat exchanger.
  • the heat exchangers are arranged in a cascaded way (the natural gas output temperature of a heat exchanges is the input temperature of the subsequent heat exchanger, and the natural gas is heated up form an LNG inlet cryogenic temperature up to -10°C or more, preferably up to 0°C or up to ambient temperature), and each of the heat exchangers of the LNG regasification system is configured and arranged for heat exchange within a specific temperature range based on load and temperature
  • the natural gas temperature range in the first heat exchanger is defined by the cryogenic inlet temperature of the LNG as well as the requirements of the cold utility and heat exchange medium on the hot stream side of this first heat exchanger.
  • the boiling temperature of the LNG at the regasification pressure can be used as the natural gas outlet design temperature for this first heat exchanger.
  • the natural gas outlet temperature of the first range can be higher, typically 10°C to 50 °C higher that the LNG boiling temperature
  • This first heat exchanger will provide cryogenic cold or very low temperature chilling power to the cold utility which requires extremely low temperature cold such as an air separation unit, etc.
  • the natural gas inlet temperature of the second temperature range is the outlet temperature of the first range and the output temperature of the second range is the inlet temperature of the third range.
  • This heat exchanger can be designed to provide very low temperature chilling power, at a temperature higher than the first heat exchanger.
  • the natural gas inlet temperature of the third temperature range is the outlet temperature of the second range.
  • This heat exchanger can be designed to provide chilling power, which has a higher temperature than the second heat exchanger.
  • first natural gas temperature range -165°C to -120 °C
  • second temperature range - 120 ⁇ ⁇ to -80 ° C
  • third temperature range -80 °C to 0°C.
  • Each one of these heat exchangers can comprise one or more heat exchange apparatuses, which can be arranged either in series or in parallel to one another. Such arrangements allow flexibility in flow and temperature control of the heat exchange medium and allow flexibility in control in different operation modes of the power plant.
  • the LNG regasification system comprises cold storage units for the storage of LNG, which are arranged for providing cold heat exchange media to the above-mentioned cooling systems within the power plant.
  • the cold energy contained in these cold storage units can be used for the C02 liquefication process, thereby enabling reduction of power consumption of the C02 absorption system.
  • the LNG regasification system in particular a heat exchanger arranged for operation with a heat exchange medium having chilling temperatures at its output, is additionally operatively connected with a system for cooling the inlet air to the gas turbine of the combined cycle power plant.
  • temperatures of the medium can be in a range of 1 0°C or less, or in a range from 5 °C to 2 °C.
  • the LNG regasification system is additionally operatively connected with one or more of the following systems associated with the process of the capture of C02 from the flue gas from the combined cycle power plant:
  • the LNG regasification system is additionally operatively connected with a cooling water system for the steam turbine condenser. This further increases the overall efficiency by effectively using the cold energy available for cooling and in turn using the low-level heat available from the condensation for the LNG regasification process.
  • the return heat exchange medium is directed back to the heat exchanger within the LNG regasification system.
  • the LNG regasification system can thereby be operated with the heat provided by the cooler and chiller systems of the combined cycle power plant.
  • the cooler and chiller systems can be operated with the cold energy provided by the LNG.
  • the system for LNG regasification comprises a heat exchanger configured and arranged for the liquefication of C02 extracted by the C02 capture system.
  • the power plant with such LNG system requires no, or fewer, compressors for the liquefaction of the C02.
  • that heat exchanger of the LNG regasification system is provided with heat from the C02 liquefaction process.
  • the power plant comprises lines to direct the heat exchange medium from the first heat exchanger of the liquefied natural gas regasification system to an air separation unit.
  • the heat exchange medium has cryogenic temperatures
  • the chilling power from the first heat exchanger of the liquefied natural gas regasification system is exchanged to the inlet air of the air separation unit and the chilling power from a second heat exchanger of the liquefied natural gas regasification system is used to cool the outlet air of the first compressor of the air separation unit.
  • Figure 1 shows a schematic of the combined cycle power plant with C02 capture system according to the invention and in particular the operative connections between the LNG regasification system and the cooling systems within the power plant.
  • FIG. 2 shows a detailed schematic of a C02 capture system, in particular of chilled ammonia system and the operative connections between the LNG system and this C02 capture system.
  • FIG. 3 shows a detailed schematic of a C02 capture system, in particular of a system based on an amine process and the operative connections between the LNG system and this C02 capture system.
  • Figure 4 shows a schematic of the combined cycle power plant with C02 capture system according to a further embodiment of the invention and in particular the operative connections between the LNG regasification system and the cooling systems within the power plant.
  • FIG. 1 depicts a combined cycle power plant 10 for the generation of electricity with a gas turbine GT provided with ambient air A, a heat recovery steam generator HRSG, which generated steam using the hot exhaust gases from the gas turbine, and steam turbine ST driven by steam generated in the HRSG.
  • a condenser 1 condenses the expanded steam and the condensate is directed as feedwater to the HRSG thereby completing the water/steam cycle of the steam turbine.
  • the power plant furthermore comprises a C02 capture system 5A, 5B, which can be either a system operating on the basis of a chilled ammonia process (as shown in as 5A in figure 2) or a system based on a amine process (as shown as 5B in figure 3).
  • the gas turbine of power plant 10 is operated with natural gas supplied by the liquefied natural gas LNG regasification plant 20.
  • the power plant 10 is operatively connected with a LNG processing system 20 having one more stages, which vaporizes cryogenic liquefied natural gas LNG for use in the gas turbine combustion chamber CC.
  • the LNG regasification processes in system 20 is integrated with one or more cooling and chilling systems within the power plant 1 0 in order to optimize the overall power plant efficiency.
  • the LNG system 20 comprises several stages 21 - 23, which are arranged in series, where each stage is dedicated to the regasification of the LNG within a range about a specific temperature level.
  • the cooling or chilling systems within the C02 capture system are integrated in closed heat exchange circuits with the LNG regasification system 20.
  • a first embodiment comprises a power plant with a C02 capture system 5a, which is a system operating on the basis of a chilled ammonia process, as shown in figure 2.
  • the system 5a comprises a C02 absorption column A preceded by a direct contact cooler DCC, which cools the flue gas directed from the HRSG via line G1 from a temperature in the range from 1 20 * ⁇ to Q0 °C down to a temperature of 10 °C or less, as it is required to successfully operate the chilled ammonia process.
  • a cooler 31 is arranged in cooling circuit of the direct contact cooler DCC and is configured to use the cold energy from heat exchanger 23 of the LNG regasification system 20.
  • the heat exchanger 23 generates a chilled flow medium of 10 ⁇ or less, for example from 2-5 °C, which is used in a cooler 33 to cool the flue gas to a temperature of less than 10 °C.
  • Gas that is free of C02 exits from the column A via line G5 and is directed to a water wash WW, from which a gas line G6 for cleaned flue gas extends to the direct contact cooler DCC2. Finally, the cleaned flue gas is directed from the direct contact cooler DCC via line G7 to a stack S and the atmosphere.
  • the water wash W W is operatively connected to a stripper St and a water cooler 32 via water lines W.
  • a line for a pure C02 flow leads from the stripper St to a regenerator RG.
  • the C02 captured from the flue gas is finally released at the top of the regenerator RG, from where it is directed to further processing, for example compression, drying, or chilling.
  • the C02 absorption column A is connected with a system for the regeneration of the chilled ammonia, its absorption solution.
  • the C02-rich absorption solution RS is reheated by means of a regenerator RG in order to release the C02 and produce a C02-lean solution LS to be reused in the absorption column A.
  • the absorption solution regeneration system comprises additionally a cooler 33 for the rich solution RS.
  • Each of the above-mentioned coolers 31 , 32, 33 within the chilled ammonia C02 capture system 5A require chilling water as cooling medium having temperatures of less than
  • each of these coolers is connected in a closed circuit with heat exchanger 23 by means of lines 25 and 26.
  • the C02 capture system can also be a system 5B based on an amine process, as shown Figure 3. It includes a C02 absorber B, which is provided with a flow of water via line W and lean absorption agent flow LS'. Flue gas from the HRSG is directed to the bottom of the absorber B and raises up through the apparatus in counter-current to the lean solution LS'. Clean flue gas exits at the top of the apparatus and is directed to the atmosphere via a stack S. The rich solution resulting from the absorption process is directed via line RS' and a heat exchanger LRX to an amine regenerator column ARC.
  • the absorption column ARC is further connected with a circuit containing a reboiler RB, from which a lean solution flow is directed via line LS' to the heat exchanger LRX, where the lean solution LS' exchanges heat with the rich solution RS' thereby preheating the rich solution prior to its entry to the amine regenerator column ARC.
  • the lean solution LS' needs to be further cooled prior to its use in the absorber column B. For this, it is directed through a heat exchanger LSC, which is configured to cool the lean solution by means of chilling water in line 25 from stage 23 of the LNG system.
  • the heated water from the heat exchanger LSC is directed back to stage 23 for chilling again in stage 23, thereby closing the circuit.
  • the C02 extracted from the flue gas exits from the regenerator column ARC and is directed to further processing such as compression, drying, or chilling.
  • the flue gas from the HRSG should be cooled to specific temperature ranges prior to its processing within that system.
  • the flue gas In the case of chilled ammonia process, the flue gas has a preferred temperature from of less than10 °C prior to entering the absorber.
  • the flue gas In the case of an amine process, the flue gas should have a temperature of ca. 50°C in order to assure optimal operation.
  • the power plant comprises a flue gas cooler 3A, or if necessary, additionally a flue gas chiller 3B arranged in the flue gas line for cooling or chilling the flue gas prior to its processing in the C02 capture processing.
  • the cold energy therefore may be entirely drawn from the LNG system.
  • the cooler/chiller system 3A, 3B in turn supports the LNG system with heat gained from the flue gas and directed to the LNG system via line 26.
  • the power plant comprises several further cooling systems connected or associated with the C02 capture system, which can be integrated with the LNG system, in addition to the cooling systems of the C02 capture system itself.
  • the C02 capture system 5A, 5B is connected to a C02 drying and cooling system 6 for processing the captured C02, which has been separated from the flue gas in the C02 capture system.
  • An optional compressor for C02 compression may be arranged following the cooling system 6.
  • the power plant 1 0 can furthermore comprise a flue gas recirculation system, which can include a line branching off the exhaust line from the HRSG, which directs untreated flue gas back to the gas turbine inlet via a flue gas cooler 4a followed by an optional flue gas chiller 4b. Cooled or chilled flue gas exiting from the flue gas cooler or flue gas chiller respectively is directed and admixed to the inlet air flow A intended for the gas turbine compressor.
  • a flue gas recirculation system can include a line branching off the exhaust line from the HRSG, which directs untreated flue gas back to the gas turbine inlet via a flue gas cooler 4a followed by an optional flue gas chiller 4b. Cooled or chilled flue gas exiting from the flue gas cooler or flue gas chiller respectively is directed and admixed to the inlet air flow A intended for the gas turbine compressor.
  • the power plant can comprise an inlet air chilling system 2, which cools the inlet air for example in case of high ambient air temperatures using a chilled medium from heat exchanger 23 via line 25.
  • the heated medium is returned to heat exchanger 23 via line 26.
  • the power plant is operatively connected with the liquefied natural gas processing system 20, which vaporizes cryogenic liquefied natural gas LNG for use in the gas turbine combustion chamber CC and/or for export via a gas pipeline.
  • the regasification processes and the various cooling and chilling systems within the power plant 10 are integrated in a manner to optimize the overall power plant efficiency.
  • the LNG system 20 comprises for example several stages 21 -23, which are arranged in series, where each stage vaporizes the LNG to a different temperature level.
  • a first stage 21 is configured and arranged to vaporize the LNG and is operatively connected in a closed circuit to an air separation unit ASU within power plant 10 via lines 27 and 28.
  • Line 27 directs cryogenic cold via a flow medium to operate the ASU, where a line 28 directs the heat generated in the ASU back to vaporizer stage 21 to vaporize the LNG.
  • the air separation unit ASU is arranged in a line for ambient air, which branches off the inlet airflow line A for the gas turbine compressor. Pure oxygen extracted from ambient air is directed either back to the ambient air line to the compressor, and/or the combustion chamber CC of the gas turbine, and /or the heat recovery steam generator HRSG to support supplementary firing.
  • a second heat exchanger 22 of the LNG system 20, as shown in figure 1 is operatively connected with the C02 drying and cooling system 6.
  • the cold energy of the LNG heat exchanger 22 is used to liquefy the C02 captured from the gas turbine exhaust gas after the C02 has been compressed sufficiently in a compressor 37.
  • the liquefied C02 may be directed to a transportation facility T or any other facility for processing or storing C02.
  • the integration of the second heat exchanger 22 of the LNG vaporizer into the C02 processing of the power plant allows a liquefaction of the C02 without the need of additional C02 compressors and intercoolers to compress the C02 to higher pressures. This arrangement allows a significant savings in investment and operating cost as well as plant efficiency.
  • the third heat exchanger 23 of the LNG regasification system 20 is operatively connected by means of lines 25 and 26 with cooler systems of the C02 capture system 5A or 5B.
  • further cooling systems within the power plant 10 can be integrated in similar manner. These systems include for example the cooling system for the steam turbine condenser 1 .
  • Each one of the heat exchangers 21 -23 may in themselves comprise one or more vaporizer units, where in the case of several units, the units can be arranged in series or in parallel. Such arrangements allow for flexible control of the LNG and heat exchange flows and the respective temperatures.
  • the last heat exchanger 23 may be combined with a cold storage unit 24, which is also connected by lines to lines 25 and 26.
  • heat exchanger 22 may be connected with a cold storage unit 35, which is connected with lines to compressor 37 and the transport facility T.
  • the heat exchanger 21 may be combined with a cold storage unit 36, which is connected via lines to lines 27 and 28. This configuration allows the operation of the cooling and chilling systems within the power plant during a shutdown of the LNG regasification process or insufficient cold available from the process.
  • FIG. 4 shows a further exemplary embodiment of the power plant 10 with a variant of the LNG regasification plant 20'.
  • This variant comprises two heat exchangers 21 and 23 for LNG regasification with optional cold storage units 24 and 36.
  • the power plant comprises a system of compressors 37 with an intercooler 34 arranged after the drying and chilling system 6.
  • the intercooler is supplied with cold via line 25 from heat exchanger 23.

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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 C02 capture plant
Technical Field
The present invention pertains to a combined cycle power plant for the generation of electric power having a gas turbine, a steam turbine, and a heat recovery steam generator, and furthermore a plant for the capture and compression of carbon dioxide. The invention pertains in particular to an integration of a liquefied natural gas processing system with the power plant.
Background Art Combined cycle power plants for the generation of electricity are known to include a gas turbine, a steam turbine, and a heat recovery steam generator utilizing the hot flue gases emitted by the gas turbine to generate steam to drive the steam turbine. In order to reduce emissions that contribute to the greenhouse effect, various measures have been proposed to minimize the amount of carbon dioxide emitted into the atmosphere. Such measures include the arrangement of systems in the power plant that capture and process C02 contained in the flue gases exhausted by a heat recovery steam generator HRSG or a coal-fired boiler. Such C02 capture processes operate for example on the basis of chilled ammonia or amine processes. In order to work effectively, both of these processes require that the flue gases are cooled to temperatures below 10°C.
Furthermore, for the captured C02 to be transported and stored economically, it is purified, separated from water, chilled, compressed, and liquefied. For this, among others, sufficiently cold heat exchange media need to be provided at economical conditions. A C02 capture plant of this type requires a given amount of energy, which reduces the overall efficiency of the power plant. In order to design a combined cycle power plant with C02 capture more energy efficiently, it has been proposed to use the cold energy from the LNG regasification for some power plant processes.
JP2000024454 discloses the use of vaporization heat of LNG to cool waste gases and solidify carbon dioxide contained in the waste gases. JP60636999 discloses the use of cold heat generated upon the evaporation of LNG to recover carbon dioxide from exhaust gas as liquefied carbon dioxide. WO 2008/009930 discloses the use of such cold energy in an air separation unit to produce nitrogen and oxygen.
US 6,367,258 discloses the vaporization of liquefied natural gas for a combined cycle power plant, where the cold energy of the vaporization is utilized for the chilling of gas turbine intake air, steam turbine condenser cooling water, or a first heat transfer fluid intended to cool components in the gas turbine.
Velautham et al., «Zero emission combined Power cycle using LNG cold », JSME International Journal, Series B, Vol. 44, No.4, 2001 , discloses the use of liquefied natural gas cold for cooling air in heat exchange with air in view of separating oxygen from the air for further use in a combined cycle power plant. The use of liquefied natural gas cold reduces the energy consumption of the oxygen-air-separation process. The use of liquefied natural gas cold energy in heat exchange with C02 for its liquefication is also disclosed.
The WO2007/148984 discloses a LNG regasification plant in which natural gas is burned in pure oxygen. The plant also comprises a boiler and a steam turbine to generate electricity from the hot combustion gases. From the resulting flue gas C02 is separated by condensation of water vapor. Further, C02 is cooled against LNG for liquefaction.
The US5467722 discloses a combined cycle power plant with a subsequent C02 capture system and a LNG regasification plant. The C02 capture system comprises heat exchangers, which cool the flue gas for cryogenic C02 capture using liquid LNG as a heat sink.
Summary of Invention
It is an object of the present invention to provide a combined cycle power plant operating with a C02 capture plant having increased power plant efficiency over known power plants of this type.
A combined cycle power plant comprises a gas turbine, a steam turbine, and a heat recovery steam generator (HRSG), both turbines driving a generator. The power plant comprises furthermore a C02 capture system operating on the basis of a chilled ammonia or an amine process and arranged to process exhaust gases from the HRSG. According to the invention the combined cycle power plant comprises a liquefied natural gas regasification system, which comprises heat exchangers operatively connected with one or more heat exchangers within the C02 capture system.
The regasification of the liquefied natural gas LNG provides the cold energy necessary to operate cooling processes in the C02 capture system. The heat gained by the heat exchange medium in that cooling process is in turn used to support the regasification process of the LNG. The LNG regasification system and the cooling systems of the C02 capture system are integrated in a closed circuit system. This integration reduces the amount of energy needed to operate the C02 capture system and LNG system, which otherwise would to be provided by other means, for example by steam extraction and electricity from the power plant. It therefore mitigates the efficiency reduction due to the C02 capture process and LNG regasification processes.
In an embodiment of the invention, the LNG regasification system comprises one or more heat exchangers, configured for the operation at a specific temperature range of the natural gas in a cascaded arrangement, form a LNG inlet temperature up to ambient temperature, for heat exchange between the LNG on the cold stream side and a heat exchange medium on the hot stream side of the heat exchanger. The heat exchange medium on the hot stream side has cryogenic or chilling temperatures at the output of the heat exchanger depending on the cold requirements of the process.
The chilling temperatures can be for example in the range from above a cryogenic temperature (cryogenic temperatures are temperatures below -150 °C) up to Ι Ο Ό or even up to ambient temperature, or in an embodiment in a range from 5°C to 2°C for chilled ammonia process applications.
In a further embodiment, the C02 capture system is arranged for the chilled ammonia process. In order to support this process, the power plant comprises lines to direct the heat exchange medium from this regasification heat exchanger generating a medium having cryogenic or chilling temperatures to one or more refrigeration systems within the C02 capture system, where the refrigeration systems are
- a cooler in a cooling circuit of a flue gas direct contact cooler,
- a water cooler arranged prior to a flue gas water wash apparatus,
- a cooler for cooling part of a rich absorption solution flow for the purpose of regulating the temperature thereof.
In a further embodiment of the invention, the C02 absorption system is a system for the removal of the C02 from flue gases by means of an amine process and the system for the LNG regasification is operatively connected to cooling systems within this C02 absorption system. This amine process system requires a heat exchange medium for cooling the absorption lean solution to temperatures of about 45°C. As is the case in the embodiments above, the use of cooling power from the LNG system mitigates the efficiency reduction due to the C02 capture process. In a particular embodiment of the invention, lines lead from the heat exchanger of the LNG system to a cooler for amine process lean solution and back to the heat exchanger.
The heat exchangers are arranged in a cascaded way (the natural gas output temperature of a heat exchanges is the input temperature of the subsequent heat exchanger, and the natural gas is heated up form an LNG inlet cryogenic temperature up to -10°C or more, preferably up to 0°C or up to ambient temperature), and each of the heat exchangers of the LNG regasification system is configured and arranged for heat exchange within a specific temperature range based on load and temperature
requirements of the cold utilities (such as an air separation unit, a C02 liquefaction process, a chilled ammonia C02 capture process, cooling requirements in combined cycle power plants, etc) optimized via process integration. More specifically in one exemplary embodiment the natural gas temperature range in the first heat exchanger is defined by the cryogenic inlet temperature of the LNG as well as the requirements of the cold utility and heat exchange medium on the hot stream side of this first heat exchanger. The boiling temperature of the LNG at the regasification pressure can be used as the natural gas outlet design temperature for this first heat exchanger. In order to reduce equipment size the natural gas outlet temperature of the first range can be higher, typically 10°C to 50 °C higher that the LNG boiling temperature This first heat exchanger will provide cryogenic cold or very low temperature chilling power to the cold utility which requires extremely low temperature cold such as an air separation unit, etc.
The natural gas inlet temperature of the second temperature range is the outlet temperature of the first range and the output temperature of the second range is the inlet temperature of the third range. This heat exchanger can be designed to provide very low temperature chilling power, at a temperature higher than the first heat exchanger.
The natural gas inlet temperature of the third temperature range is the outlet temperature of the second range. This heat exchanger can be designed to provide chilling power, which has a higher temperature than the second heat exchanger.
In such a cascaded arrangement, the exergy losses of the LNG chilling power is minimized when providing cold to different cold utilizes. Specifically the following temperature ranges are used in an exemplary embodiment: First natural gas temperature range: -165°C to -120 °C, second temperature range: - 120 <Ό to -80 ° C, and third temperature range: -80 °C to 0°C. Each one of these heat exchangers can comprise one or more heat exchange apparatuses, which can be arranged either in series or in parallel to one another. Such arrangements allow flexibility in flow and temperature control of the heat exchange medium and allow flexibility in control in different operation modes of the power plant. In a further embodiment of the invention, the LNG regasification system comprises cold storage units for the storage of LNG, which are arranged for providing cold heat exchange media to the above-mentioned cooling systems within the power plant. In case of non-operation of LNG regasification or regasification, the cold energy contained in these cold storage units can be used for the C02 liquefication process, thereby enabling reduction of power consumption of the C02 absorption system.
In a further embodiment of the invention, the LNG regasification system, in particular a heat exchanger arranged for operation with a heat exchange medium having chilling temperatures at its output, is additionally operatively connected with a system for cooling the inlet air to the gas turbine of the combined cycle power plant. The chilling
temperatures of the medium can be in a range of 1 0°C or less, or in a range from 5 °C to 2 °C.
In a further exemplary embodiment of the invention, the LNG regasification system is additionally operatively connected with one or more of the following systems associated with the process of the capture of C02 from the flue gas from the combined cycle power plant:
- a system for flue gas cooling and /or chilling prior to its entry to the C02 capture system in order to fulfill temperature requirement for the C02 capture process,
- a system for the cooling of flue gas recirculated after the HRSG back to the gas turbine inlet,
- a system for the chilling of flue gas recirculated after the HRSG back to the gas turbine inlet,
- a system for cooling of C02 extracted by the C02 capture system.
- a system for drying C02 by means of chilling.
The recirculation of flue gas increases the C02 concentration in the flue gas and thereby increases the C02 capture process efficiency. In a further exemplary embodiment of the invention, the LNG regasification system is additionally operatively connected with a cooling water system for the steam turbine condenser. This further increases the overall efficiency by effectively using the cold energy available for cooling and in turn using the low-level heat available from the condensation for the LNG regasification process.
From all of the above-mentioned cooling systems, the return heat exchange medium is directed back to the heat exchanger within the LNG regasification system.
The LNG regasification system can thereby be operated with the heat provided by the cooler and chiller systems of the combined cycle power plant. In return, the cooler and chiller systems can be operated with the cold energy provided by the LNG.
The use of the cold energy available from the LNG regasification system in any of the above cooling systems increases the overall power plant efficiency as these cooling systems no longer have to be operated with energy taken from other sources of the power plant. The heat taken back from the above-mentioned cooling systems on the other hand provide a heat source for the LNG regasification. Therefore, no or less steam extraction from the combined cycle power plant will be needed to operate the LNG regasification. The power plant's performance (efficiency and power output) can be improved.
In a further exemplary embodiment of the invention the system for LNG regasification comprises a heat exchanger configured and arranged for the liquefication of C02 extracted by the C02 capture system. The power plant with such LNG system requires no, or fewer, compressors for the liquefaction of the C02. In addition, that heat exchanger of the LNG regasification system is provided with heat from the C02 liquefaction process.
In a further embodiment, the power plant comprises lines to direct the heat exchange medium from the first heat exchanger of the liquefied natural gas regasification system to an air separation unit. The heat exchange medium has cryogenic temperatures
(temperatures below -150 °C) at the output of that heat exchanger and is used for the operation of the air separation process thereby reducing the energy required to operate that unit. A further line for the return heat exchange medium from the air separation unit leads back to that first heat exchanger and provides its heat to the liquefied natural gas regasification process. In an alternative embodiment the chilling power from the first heat exchanger of the liquefied natural gas regasification system is exchanged to the inlet air of the air separation unit and the chilling power from a second heat exchanger of the liquefied natural gas regasification system is used to cool the outlet air of the first compressor of the air separation unit.
Brief Description of the Drawings
Figure 1 shows a schematic of the combined cycle power plant with C02 capture system according to the invention and in particular the operative connections between the LNG regasification system and the cooling systems within the power plant.
Figure 2 shows a detailed schematic of a C02 capture system, in particular of chilled ammonia system and the operative connections between the LNG system and this C02 capture system.
Figure 3 shows a detailed schematic of a C02 capture system, in particular of a system based on an amine process and the operative connections between the LNG system and this C02 capture system.
Figure 4 shows a schematic of the combined cycle power plant with C02 capture system according to a further embodiment of the invention and in particular the operative connections between the LNG regasification system and the cooling systems within the power plant.
Best Modes for Carrying out the Invention Figure 1 depicts a combined cycle power plant 10 for the generation of electricity with a gas turbine GT provided with ambient air A, a heat recovery steam generator HRSG, which generated steam using the hot exhaust gases from the gas turbine, and steam turbine ST driven by steam generated in the HRSG. A condenser 1 condenses the expanded steam and the condensate is directed as feedwater to the HRSG thereby completing the water/steam cycle of the steam turbine. The power plant furthermore comprises a C02 capture system 5A, 5B, which can be either a system operating on the basis of a chilled ammonia process (as shown in as 5A in figure 2) or a system based on a amine process (as shown as 5B in figure 3).
The gas turbine of power plant 10 is operated with natural gas supplied by the liquefied natural gas LNG regasification plant 20. The power plant 10 is operatively connected with a LNG processing system 20 having one more stages, which vaporizes cryogenic liquefied natural gas LNG for use in the gas turbine combustion chamber CC. According to the invention, the LNG regasification processes in system 20 is integrated with one or more cooling and chilling systems within the power plant 1 0 in order to optimize the overall power plant efficiency. For this, the LNG system 20 comprises several stages 21 - 23, which are arranged in series, where each stage is dedicated to the regasification of the LNG within a range about a specific temperature level. In particular, the cooling or chilling systems within the C02 capture system are integrated in closed heat exchange circuits with the LNG regasification system 20.
A first embodiment comprises a power plant with a C02 capture system 5a, which is a system operating on the basis of a chilled ammonia process, as shown in figure 2. The system 5a comprises a C02 absorption column A preceded by a direct contact cooler DCC, which cools the flue gas directed from the HRSG via line G1 from a temperature in the range from 1 20 *Ό to Q0 °C down to a temperature of 10 °C or less, as it is required to successfully operate the chilled ammonia process. A cooler 31 is arranged in cooling circuit of the direct contact cooler DCC and is configured to use the cold energy from heat exchanger 23 of the LNG regasification system 20. The heat exchanger 23 generates a chilled flow medium of 10 Ό or less, for example from 2-5 °C, which is used in a cooler 33 to cool the flue gas to a temperature of less than 10 °C.
Gas that is free of C02 exits from the column A via line G5 and is directed to a water wash WW, from which a gas line G6 for cleaned flue gas extends to the direct contact cooler DCC2. Finally, the cleaned flue gas is directed from the direct contact cooler DCC via line G7 to a stack S and the atmosphere.
The water wash W W is operatively connected to a stripper St and a water cooler 32 via water lines W. A line for a pure C02 flow leads from the stripper St to a regenerator RG. The C02 captured from the flue gas is finally released at the top of the regenerator RG, from where it is directed to further processing, for example compression, drying, or chilling.
The C02 absorption column A is connected with a system for the regeneration of the chilled ammonia, its absorption solution. The C02-rich absorption solution RS is reheated by means of a regenerator RG in order to release the C02 and produce a C02-lean solution LS to be reused in the absorption column A. The absorption solution regeneration system comprises additionally a cooler 33 for the rich solution RS.
Each of the above-mentioned coolers 31 , 32, 33 within the chilled ammonia C02 capture system 5A require chilling water as cooling medium having temperatures of less than
10 °C, which can be provided by the heat exchanger 23 of the LNG system 20. Each of these coolers is connected in a closed circuit with heat exchanger 23 by means of lines 25 and 26.
According to a further embodiment of the invention, the C02 capture system can also be a system 5B based on an amine process, as shown Figure 3. It includes a C02 absorber B, which is provided with a flow of water via line W and lean absorption agent flow LS'. Flue gas from the HRSG is directed to the bottom of the absorber B and raises up through the apparatus in counter-current to the lean solution LS'. Clean flue gas exits at the top of the apparatus and is directed to the atmosphere via a stack S. The rich solution resulting from the absorption process is directed via line RS' and a heat exchanger LRX to an amine regenerator column ARC. There the C02 is released from the solution and directed via a condenser C to facilities for further processing or storing. The absorption column ARC is further connected with a circuit containing a reboiler RB, from which a lean solution flow is directed via line LS' to the heat exchanger LRX, where the lean solution LS' exchanges heat with the rich solution RS' thereby preheating the rich solution prior to its entry to the amine regenerator column ARC. The lean solution LS' needs to be further cooled prior to its use in the absorber column B. For this, it is directed through a heat exchanger LSC, which is configured to cool the lean solution by means of chilling water in line 25 from stage 23 of the LNG system. The heated water from the heat exchanger LSC is directed back to stage 23 for chilling again in stage 23, thereby closing the circuit. The C02 extracted from the flue gas exits from the regenerator column ARC and is directed to further processing such as compression, drying, or chilling.
Depending on the type of C02 capture system installed, the flue gas from the HRSG should be cooled to specific temperature ranges prior to its processing within that system. In the case of chilled ammonia process, the flue gas has a preferred temperature from of less than10 °C prior to entering the absorber. In the case of an amine process, the flue gas should have a temperature of ca. 50°C in order to assure optimal operation. For such flue gas cooling, the power plant comprises a flue gas cooler 3A, or if necessary, additionally a flue gas chiller 3B arranged in the flue gas line for cooling or chilling the flue gas prior to its processing in the C02 capture processing. The cold energy therefore may be entirely drawn from the LNG system. The cooler/chiller system 3A, 3B in turn supports the LNG system with heat gained from the flue gas and directed to the LNG system via line 26.
The power plant comprises several further cooling systems connected or associated with the C02 capture system, which can be integrated with the LNG system, in addition to the cooling systems of the C02 capture system itself.
The C02 capture system 5A, 5B is connected to a C02 drying and cooling system 6 for processing the captured C02, which has been separated from the flue gas in the C02 capture system. An optional compressor for C02 compression may be arranged following the cooling system 6.
In order to enhance the efficiency of the C02 capture process by means of increasing the C02 concentration in the flue gas, the power plant 1 0 can furthermore comprise a flue gas recirculation system, which can include a line branching off the exhaust line from the HRSG, which directs untreated flue gas back to the gas turbine inlet via a flue gas cooler 4a followed by an optional flue gas chiller 4b. Cooled or chilled flue gas exiting from the flue gas cooler or flue gas chiller respectively is directed and admixed to the inlet air flow A intended for the gas turbine compressor.
For a further power plant capacity increase, the power plant can comprise an inlet air chilling system 2, which cools the inlet air for example in case of high ambient air temperatures using a chilled medium from heat exchanger 23 via line 25. The heated medium is returned to heat exchanger 23 via line 26.
The power plant is operatively connected with the liquefied natural gas processing system 20, which vaporizes cryogenic liquefied natural gas LNG for use in the gas turbine combustion chamber CC and/or for export via a gas pipeline. The regasification processes and the various cooling and chilling systems within the power plant 10 are integrated in a manner to optimize the overall power plant efficiency. The LNG system 20 comprises for example several stages 21 -23, which are arranged in series, where each stage vaporizes the LNG to a different temperature level. A first stage 21 is configured and arranged to vaporize the LNG and is operatively connected in a closed circuit to an air separation unit ASU within power plant 10 via lines 27 and 28. Line 27 directs cryogenic cold via a flow medium to operate the ASU, where a line 28 directs the heat generated in the ASU back to vaporizer stage 21 to vaporize the LNG.
The air separation unit ASU is arranged in a line for ambient air, which branches off the inlet airflow line A for the gas turbine compressor. Pure oxygen extracted from ambient air is directed either back to the ambient air line to the compressor, and/or the combustion chamber CC of the gas turbine, and /or the heat recovery steam generator HRSG to support supplementary firing. A second heat exchanger 22 of the LNG system 20, as shown in figure 1 , is operatively connected with the C02 drying and cooling system 6. The cold energy of the LNG heat exchanger 22 is used to liquefy the C02 captured from the gas turbine exhaust gas after the C02 has been compressed sufficiently in a compressor 37. The liquefied C02 may be directed to a transportation facility T or any other facility for processing or storing C02. The integration of the second heat exchanger 22 of the LNG vaporizer into the C02 processing of the power plant allows a liquefaction of the C02 without the need of additional C02 compressors and intercoolers to compress the C02 to higher pressures. This arrangement allows a significant savings in investment and operating cost as well as plant efficiency.
The third heat exchanger 23 of the LNG regasification system 20 is operatively connected by means of lines 25 and 26 with cooler systems of the C02 capture system 5A or 5B. In order to additionally optimize the overall power plant efficiency, further cooling systems within the power plant 10 can be integrated in similar manner. These systems include for example the cooling system for the steam turbine condenser 1 .
Each one of the heat exchangers 21 -23 may in themselves comprise one or more vaporizer units, where in the case of several units, the units can be arranged in series or in parallel. Such arrangements allow for flexible control of the LNG and heat exchange flows and the respective temperatures.
Additionally, the last heat exchanger 23 may be combined with a cold storage unit 24, which is also connected by lines to lines 25 and 26. Also heat exchanger 22 may be connected with a cold storage unit 35, which is connected with lines to compressor 37 and the transport facility T. Similarly, the heat exchanger 21 may be combined with a cold storage unit 36, which is connected via lines to lines 27 and 28. This configuration allows the operation of the cooling and chilling systems within the power plant during a shutdown of the LNG regasification process or insufficient cold available from the process.
Figure 4 shows a further exemplary embodiment of the power plant 10 with a variant of the LNG regasification plant 20'. This variant comprises two heat exchangers 21 and 23 for LNG regasification with optional cold storage units 24 and 36. Instead of having a heat exchanger 22 used for C02 liquefaction, the power plant comprises a system of compressors 37 with an intercooler 34 arranged after the drying and chilling system 6. The intercooler is supplied with cold via line 25 from heat exchanger 23. Reference numerals used in figures
1 steam turbine condenser
2 inlet air chilling system
3A/3B flue gas cooler/ chiller
4A/4B recirculated flue gas cooler / chiller
5A C02 capture system - chilled ammonia system
5B C02 capture system - amine process
6 C02 drying and cooling system
10 combined cycle power plant
20,20' liquefied natural gas regasification system
21 first heat exchanger at cryogenic temperatures
22 second heat exchanger at chilling temperatures
23 third heat exchanger
24 cold storage unit
25 line for heat exchange medium from third heat exchanger to power plant
26 return line for heat exchange medium from power plant back to LNG regasification heat exchanger
27 line for cryogenic heat exchange medium from first LNG regasification heat exchanger to air separation unit
28 return line for heat exchange medium from air separation unit back to LNG regasification heat exchanger
31 -33 refrigeration systems within chilled ammonia C02 capture system
31 cooler in DCC cooling circuit within chilled ammonia C02 capture system
32 water cooler within chilled ammonia C02 capture system
33 rich solution cooler within chilled ammonia C02 capture system
34 C02 intercooler
35,36 cold storage unit
37 C02 compressor
GT gas turbine
ST steam turbine
HRSG heat recovery steam generator
A inlet air
ASU air separation unit
LNG liquefied natural gas
NG gasified natural gas
DCC direct contact cooler A C02 absorber
RG C02 absorption solution regenerator
RS line for C02 absorption rich solution
LS lien for C02 absorption lean solution
W water line
WW water wash apparatus
G1 .G2, G5, G6.G7 flue gas lines
B C02 absorber
RS' line for C02 absorption rich solution
LS' line for C02 absorption lean solution
ARC amine regenerator column
RB reboiler
C lean solution cooling system
S stack
T liquefied C02 transport system

Claims

Claims
1 . Combined cycle power plant (1 0) comprising a gas turbine (GT), a steam turbine (ST), a heat recovery steam generator (HRSG), a liquefied natural gas (LNG) regasification system (20), and
a C02 capture system (5A, 5B) arranged to process exhaust gases exhausted by the heat recovery steam generator (HRSG) characterized in that
the liquefied natural gas regasification system (20) comprises heat exchangers (21 , 22, 23) operatively connected with heat exchangers (31 , 32, 33, 36, LSC) within the C02 capture system (5A, 5B),
wherein one or more heat exchangers (21 , 22, 23) arranged in a cascaded way, configured for the operation at temperatures of the natural gas form an LNG inlet temperature up to at least -1 0°C and of which at least one heat exchanger (23) is configured and arranged for heat exchange between the liquefied natural gas and a heat exchange medium, where that heat exchange medium has cryogenic temperatures or chilling temperatures at the output from that at least one heat exchanger (21 ).
2. Combined cycle power plant (10) according to claim 1
characterized in that
the C02 capture system is a system (5A) arranged for a chilled ammonia process and the power plant (10) comprises lines (25, 26) to direct the heat exchange medium from this regasification heat exchanger (23) to one or more of the following refrigeration systems within the C02 capture system
- a cooler (31 ) integrated in a cooling circuit of a flue gas direct contact cooler (DCC),
- a water cooler (32) prior to a flue gas water wash apparatus (WW),
- a cooler (33) for the cooling of C02 rich absorption solution within the C02 capture system (5A).
3. Combined cycle power plant (1 0) according to claim 1
characterized in that
the C02 capture system is a system (5B) arranged for an amine process for the removal of C02 from flue gases and the liquefied natural gas regasification system (20) comprises one or more heat exchangers (21 , 22, 23) arranged in a cascaded way, configured for the operation of the natural gas from an LNG inlet temperature up to at least 0°C and of which at least one heat exchanger (21 ) is configured and arranged for heat exchange between the liquefied natural gas and a heat exchange medium, where that heat exchange medium has cryogenic temperature or chilling temperatures at the output from that at least one heat exchanger (23).
4. Combined cycle power plant (10) according to claim 3
characterized in that
the power plant (10) comprises lines (25, 26) to direct the heat exchange medium from this regasification heat exchanger (21 ) to a system (LSC) for cooling a C02 lean solution within the C02 capture amine process system (5B).
5. Combined cycle power plant (10) according to claims 1 or 3
characterized in that
the at least one heat exchanger (23), which is configured and arranged for heat exchange between the liquefied natural gas and a heat exchange medium that has a cryogenic temperature or a chilling temperature at the output from the heat exchanger, is operatively connected to a system (2) for cooling the inlet air to the gas turbine (GT) of the combined cycle power plant (10).
6. Combined cycle power plant (10) according to claim 5
characterized in that
the one or more heat exchangers (21 -23) of the liquefied natural gas regasification system are additionally operatively connected to one or more of the following systems of the combined cycle power plant (10):
- a system (3a) for flue gas cooling prior to its entry to the C02 capture system,
- a system (3b) for flue gas chilling prior to its entry to the C02 capture system.
- a cooling water system (1 ) for the steam turbine condenser,
- a system (4a) for the cooling of flue gas recirculated after the HRSG back to the gas turbine inlet,
- a system (4b) for the chilling of flue gas recirculated after the HRSG back to the gas turbine inlet,
- a system (6) for cooling of C02 extracted by the C02 capture system.
- a system (6) for drying C02 by means of chilling.
7. Combined cycle power plant (10) according to any of the foregoing claims 1 -6 characterized in that
the heat exchangers (21 -23) of the liquefied natural gas regasification system are arranged either in series or in parallel.
8. Combined cycle power plant (1 0) according to claim 7
characterized in that
each of the heat exchangers (21 , 22, 23) of the LNG regasification system (20) are configured and arranged for heat exchange within a given temperature range, where each one of the heat exchangers (21 , 22, 23) can comprise one or more heat exchange apparatuses, which can be arranged either in series or in parallel to one another.
9. Combined cycle power plant (1 0) according to claim 5
characterized in that
the liquefied natural gas regasification system (20) comprises one or more cold storage units for the storage of liquefied natural gas arranged in parallel to its heat exchangers (21 -23).
10. Combined cycle power plant (1 0) according to claims 1 or 3
characterized in that
the system for liquefied natural gas regasification comprises a heat exchanger (22) configured and arranged for the liquefaction of C02 extracted by the C02 capture system.
1 1 . Combined cycle power plant (1 0) according to claims 6 and 10
characterized in that
a line leads from the system (6) for drying and cooling C02 to the heat exchanger (22) for C02 liquefaction and a line for liquefied C02 leads from this heat exchanger (22) to a transport facility (T) or pump.
12. Combined cycle power plant (1 0) according to claim 1
characterized in that
the liquefied natural gas regasification system (20) comprises a heat exchanger (21 ) configured and arranged for heat exchange between liquefied natural gas and a medium having cryogenic temperatures at the output of said heat exchanger (21 ) and a line (27) for said heat exchange medium that leads to an air separation unit (27), and a line (28) leads from said air separation unit (ASU) back to said heat exchanger (21 ).
13. Combined cycle power plant (1 0) according to claim 5
characterized in that
the liquefied natural gas regasification system (21 -23) is additionally operatively connected to the cooling system for the steam turbine (ST) condenser (1 ).
PCT/EP2012/051267 2011-02-01 2012-01-26 Combined cycle power plant with co2 capture plant WO2012104202A1 (en)

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103628982A (en) * 2013-11-27 2014-03-12 暨南大学 Combined power circulating method capable of catching carbon dioxide (CO2) by using LNG (Liquefied Natural Gas) cold energy and system thereof
WO2014137573A3 (en) * 2013-03-04 2015-08-06 Exxonmobil Upstream Research Company Regasification plant
ES2580879A1 (en) * 2015-02-26 2016-08-29 Universidade Da Coruña Thermoelectric plant fed with environmental heat and cooled by regasification of liquefied natural gas (Machine-translation by Google Translate, not legally binding)
CN108579361A (en) * 2018-05-09 2018-09-28 常州大学 Carbon dioxide low energy consumption capturing device in a kind of power plants LNG tail gas
EP3090198B1 (en) * 2013-12-30 2019-07-17 William M. Conlon Liquid air power and storage
CN114909605A (en) * 2022-06-08 2022-08-16 江苏科技大学 LNG ship cold energy circulating storage and cold energy comprehensive utilization system and working method thereof
CN115014000A (en) * 2022-06-10 2022-09-06 国网浙江省电力有限公司电力科学研究院 Multi-energy combined supply zero-carbon emission system and operation control method thereof

Families Citing this family (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20140020388A1 (en) * 2012-07-19 2014-01-23 Miguel Angel Gonzalez Salazar System for improved carbon dioxide capture and method thereof
CN105008499A (en) 2013-03-08 2015-10-28 埃克森美孚上游研究公司 Power generation and methane recovery from methane hydrates
TW201500635A (en) 2013-03-08 2015-01-01 Exxonmobil Upstream Res Co Processing exhaust for use in enhanced oil recovery
EP3123011A1 (en) * 2014-03-26 2017-02-01 Exxonmobil Upstream Research Company System and method for the conditioning of recirculated exhaust gas
CN103867894B (en) * 2014-03-29 2016-02-10 辽宁石油化工大学 One utilizes cold energy of liquefied natural gas to generate electricity and CO 2the method and apparatus of trapping
WO2016195968A1 (en) 2015-06-01 2016-12-08 Conlon William M Part load operation of liquid air power and storage system
WO2016195999A1 (en) 2015-06-03 2016-12-08 Conlon William M Liquid air power and storage with carbon capture
WO2016204893A1 (en) 2015-06-16 2016-12-22 Conlon William M Cryogenic liquid energy storage
WO2017069922A1 (en) 2015-10-21 2017-04-27 Conlon William M High pressure liquid air power and storage
US10378763B2 (en) 2015-12-03 2019-08-13 General Electric Company Method and apparatus to facilitate heating feedwater in a power generation system
CA3006956C (en) * 2015-12-14 2020-10-27 Exxonmobil Upstream Research Company Expander-based lng production processes enhanced with liquid nitrogen
CN105605602B (en) * 2016-01-28 2017-10-31 华中科技大学 LNG cold energy is used for the natural gas oxygen-enriched combustion system that making oxygen by air separation and carbon are captured
JP6946012B2 (en) * 2017-02-09 2021-10-06 三菱重工業株式会社 CO2 liquefaction system and CO2 liquefaction method
IT201700073449A1 (en) * 2017-07-05 2019-01-05 Fpt Ind Spa VEHICLE EQUIPPED WITH HEAT RECOVERY SYSTEM (WHR)
CN107899375A (en) * 2017-11-25 2018-04-13 杨正山 A kind of coal-burning power plant's flue gas carbon dioxide mix trapping coupling microalgae carbon sequestration technique
CA3102635A1 (en) * 2018-06-06 2019-12-12 Saipem S.P.A. Post-combustion co2 capture with heat recovery and integration
CN109821341A (en) * 2019-03-20 2019-05-31 赫普科技发展（北京）有限公司 A kind of gas turbine utilizes LNG cold energy carbon capture system and carbon capture method
CN109876590A (en) * 2019-03-20 2019-06-14 赫普科技发展（北京）有限公司 A kind of thermal power plant utilizes LNG cold energy carbon capture system and carbon capture method
CN110711463A (en) * 2019-10-31 2020-01-21 上海海事大学 Gas power plant CO based on solar energy and LNG cold energy2Trapping system
CN110787594B (en) * 2019-11-25 2023-09-01 中冶京诚工程技术有限公司 CO in flue gas 2 Method and system for capturing and utilizing coupled LNG depressurization cycle
WO2022094605A1 (en) * 2020-10-30 2022-05-05 Colorado State University Research Foundation Synergistic heat pumped thermal storage and flexible carbon capture system
CN113669121B (en) * 2021-08-26 2022-06-14 江南大学 Power plant condensing system and process method
AU2022376162A1 (en) * 2021-10-25 2024-05-30 Bright Generation Holdings Llp Synergistic heat pumped thermal storage and flexible carbon capture system
WO2024039365A1 (en) * 2022-08-16 2024-02-22 General Electric Technology Gmbh System and method for multi-stage carbon capture
WO2024054119A1 (en) * 2022-09-06 2024-03-14 Capsol Technologies As Carbon capture for gas turbines
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Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4942734A (en) * 1989-03-20 1990-07-24 Kryos Energy Inc. Cogeneration of electricity and liquid carbon dioxide by combustion of methane-rich gas
JPH0448185A (en) * 1990-06-14 1992-02-18 Central Res Inst Of Electric Power Ind Recovering method of carbon dioxide discharged out of lng burning thermal power station
WO1995021683A1 (en) * 1994-02-15 1995-08-17 Kværner Water Systems A.S. A method for removing and preventing emissions into the atmosphere of carbon dioxide (co2) from exhaust gases from heat engines
US5467722A (en) 1994-08-22 1995-11-21 Meratla; Zoher M. Method and apparatus for removing pollutants from flue gas
WO1996038656A1 (en) * 1995-06-01 1996-12-05 Cabot Corporation A liquefied natural gas (lng) fueled combined cycle power plant and an lng fueled gas turbine plant
JP2000024454A (en) 1998-07-08 2000-01-25 Chugoku Electric Power Co Inc:The Treatment of waste combustion gas and apparatus therefor
US6367258B1 (en) 1999-07-22 2002-04-09 Bechtel Corporation Method and apparatus for vaporizing liquid natural gas in a combined cycle power plant
JP2006036999A (en) 2004-07-29 2006-02-09 Matsushita Electric Ind Co Ltd Method for gasifying organic material
WO2007148984A2 (en) 2006-06-20 2007-12-27 Aker Engineering & Technology As Method and plant for re-gasification of lng
WO2008009930A2 (en) 2006-07-18 2008-01-24 Ntnu Technology Transfer As Apparatus and methods for natural gas transportation and processing
WO2008090167A1 (en) * 2007-01-25 2008-07-31 Shell Internationale Research Maatschappij B.V. Process for producing a pressurised co2 stream in a power plant integrated with a co2 capture unit

Family Cites Families (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4433554A (en) * 1982-07-16 1984-02-28 Institut Francais Du Petrole Process for producing cold and/or heat by use of an absorption cycle with carbon dioxide as working fluid
US4995234A (en) * 1989-10-02 1991-02-26 Chicago Bridge & Iron Technical Services Company Power generation from LNG
WO1995016105A1 (en) * 1993-12-10 1995-06-15 Cabot Corporation An improved liquefied natural gas fueled combined cycle power plant
US5724805A (en) * 1995-08-21 1998-03-10 University Of Massachusetts-Lowell Power plant with carbon dioxide capture and zero pollutant emissions
JP2002541421A (en) * 1999-04-05 2002-12-03 レール・リキード−ソシエテ・アノニム・ア・ディレクトワール・エ・コンセイユ・ドゥ・スールベイランス・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード Variable production capacity fluid mixture separation apparatus and process
US7299619B2 (en) * 2003-12-13 2007-11-27 Siemens Power Generation, Inc. Vaporization of liquefied natural gas for increased efficiency in power cycles
MX2007000341A (en) * 2004-07-14 2007-03-27 Fluor Tech Corp Configurations and methods for power generation with integrated lng regasification.
US7637109B2 (en) * 2004-08-02 2009-12-29 American Air Liquide, Inc. Power generation system including a gas generator combined with a liquified natural gas supply
US7314847B1 (en) * 2004-10-21 2008-01-01 The United States Of America As Represented By The United States Department Of Energy Regenerable sorbents for CO2 capture from moderate and high temperature gas streams
US7288136B1 (en) * 2005-01-13 2007-10-30 United States Of America Department Of Energy High capacity immobilized amine sorbents
US7654320B2 (en) * 2006-04-07 2010-02-02 Occidental Energy Ventures Corp. System and method for processing a mixture of hydrocarbon and CO2 gas produced from a hydrocarbon reservoir
ITMI20061149A1 (en) * 2006-06-14 2007-12-15 Eni Spa PROCEDURE AND PLANT FOR THE REGASIFICATION OF NATURAL LIQUEFIED GAS AND THE SUOM STORAGE
US20080115531A1 (en) * 2006-11-16 2008-05-22 Bao Ha Cryogenic Air Separation Process and Apparatus
US7867322B2 (en) * 2007-01-31 2011-01-11 Alstom Technology Ltd Use of SO2 from flue gas for acid wash of ammonia
US20100267123A1 (en) * 2007-06-22 2010-10-21 Louis Wibberley Method for co2 transfer from gas streams to ammonia solutions
AU2008278901B2 (en) * 2007-07-25 2012-06-14 Bp Alternative Energy International Limited Separation of carbon dioxide and hydrogen
GB0721488D0 (en) * 2007-11-01 2007-12-12 Alstom Technology Ltd Carbon capture system
DE502007003785D1 (en) * 2007-11-16 2010-06-24 Linde Ag Method for controlling a pump arrangement and pump arrangement
US20090151318A1 (en) * 2007-12-13 2009-06-18 Alstom Technology Ltd System and method for regenerating an absorbent solution
US20090282977A1 (en) * 2008-05-14 2009-11-19 Alstom Technology Ltd Gas purification system having provisions for co2 injection of wash water
EP2282970A1 (en) * 2008-05-15 2011-02-16 Shell Internationale Research Maatschappij B.V. Method for recovering a natural gas contaminated with high levels of co2
US7846240B2 (en) * 2008-10-02 2010-12-07 Alstom Technology Ltd Chilled ammonia based CO2 capture system with water wash system

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4942734A (en) * 1989-03-20 1990-07-24 Kryos Energy Inc. Cogeneration of electricity and liquid carbon dioxide by combustion of methane-rich gas
JPH0448185A (en) * 1990-06-14 1992-02-18 Central Res Inst Of Electric Power Ind Recovering method of carbon dioxide discharged out of lng burning thermal power station
WO1995021683A1 (en) * 1994-02-15 1995-08-17 Kværner Water Systems A.S. A method for removing and preventing emissions into the atmosphere of carbon dioxide (co2) from exhaust gases from heat engines
US5467722A (en) 1994-08-22 1995-11-21 Meratla; Zoher M. Method and apparatus for removing pollutants from flue gas
WO1996038656A1 (en) * 1995-06-01 1996-12-05 Cabot Corporation A liquefied natural gas (lng) fueled combined cycle power plant and an lng fueled gas turbine plant
JP2000024454A (en) 1998-07-08 2000-01-25 Chugoku Electric Power Co Inc:The Treatment of waste combustion gas and apparatus therefor
US6367258B1 (en) 1999-07-22 2002-04-09 Bechtel Corporation Method and apparatus for vaporizing liquid natural gas in a combined cycle power plant
JP2006036999A (en) 2004-07-29 2006-02-09 Matsushita Electric Ind Co Ltd Method for gasifying organic material
WO2007148984A2 (en) 2006-06-20 2007-12-27 Aker Engineering & Technology As Method and plant for re-gasification of lng
WO2008009930A2 (en) 2006-07-18 2008-01-24 Ntnu Technology Transfer As Apparatus and methods for natural gas transportation and processing
WO2008090167A1 (en) * 2007-01-25 2008-07-31 Shell Internationale Research Maatschappij B.V. Process for producing a pressurised co2 stream in a power plant integrated with a co2 capture unit

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
AKIYA T ET AL: "HIGH PERFORMANCE ENERGY SUPPLY SYSTEM", AEROSPACE POWER SYSTEMS. BOSTON, AUG. 4 - 9, 1991; [PROCEEDINGS OF THE INTERSOCIETY ENERGY CONVERSION ENGINEERING CONFERENCE], NEW YORK, IEEE, US, vol. 6, 4 August 1991 (1991-08-04), pages 109 - 114, XP000313114, ISBN: 978-0-89448-163-5 *
DATABASE EPODOC [online] EUROPEAN PATENT OFFICE, THE HAGUE, NL; 18 February 1992 (1992-02-18), SHINODA MASAHARU: "Recovering method of carbon dioxide discharged out of lng burning thermalpower station", Database accession no. jp04048185 *
VELAUTHAM ET AL.: "Zero emission combined Power cycle using LNG cold", JSME INTERNATIONAL JOURNAL, SERIES B, vol. 44, no. 4, 2001

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014137573A3 (en) * 2013-03-04 2015-08-06 Exxonmobil Upstream Research Company Regasification plant
CN103628982A (en) * 2013-11-27 2014-03-12 暨南大学 Combined power circulating method capable of catching carbon dioxide (CO2) by using LNG (Liquefied Natural Gas) cold energy and system thereof
CN103628982B (en) * 2013-11-27 2015-09-09 暨南大学 Utilize combined power circulation method and the system thereof of cold energy of liquefied natural gas capturing carbon dioxide
EP3090198B1 (en) * 2013-12-30 2019-07-17 William M. Conlon Liquid air power and storage
ES2580879A1 (en) * 2015-02-26 2016-08-29 Universidade Da Coruña Thermoelectric plant fed with environmental heat and cooled by regasification of liquefied natural gas (Machine-translation by Google Translate, not legally binding)
CN108579361A (en) * 2018-05-09 2018-09-28 常州大学 Carbon dioxide low energy consumption capturing device in a kind of power plants LNG tail gas
CN114909605A (en) * 2022-06-08 2022-08-16 江苏科技大学 LNG ship cold energy circulating storage and cold energy comprehensive utilization system and working method thereof
CN114909605B (en) * 2022-06-08 2024-04-19 江苏科技大学 LNG ship cold energy circulating storage and cold energy comprehensive utilization system and working method thereof
CN115014000A (en) * 2022-06-10 2022-09-06 国网浙江省电力有限公司电力科学研究院 Multi-energy combined supply zero-carbon emission system and operation control method thereof
CN115014000B (en) * 2022-06-10 2023-12-26 国网浙江省电力有限公司电力科学研究院 Multi-energy combined supply zero-carbon emission system and operation control method thereof

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