CN113738467B - Integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas - Google Patents

Integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas Download PDF

Info

Publication number
CN113738467B
CN113738467B CN202111112458.2A CN202111112458A CN113738467B CN 113738467 B CN113738467 B CN 113738467B CN 202111112458 A CN202111112458 A CN 202111112458A CN 113738467 B CN113738467 B CN 113738467B
Authority
CN
China
Prior art keywords
lng
oxygen
air
carbon
power generation
Prior art date
Legal status (The legal status 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 status listed.)
Active
Application number
CN202111112458.2A
Other languages
Chinese (zh)
Other versions
CN113738467A (en
Inventor
杨敬东
刘清友
杨晓明
汤晓勇
田静
陆永康
廖勇
赵石兵
顾爱英
王亮
周亚洲
刘洪�
汪宏伟
朱海燕
汪兴明
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Southwest Branch Of China Petroleum Engineering & Construction Corp
Zhejiang Zheneng Wenzhou Lng Co ltd
Chengdu Univeristy of Technology
Original Assignee
Southwest Branch Of China Petroleum Engineering & Construction Corp
Zhejiang Zheneng Wenzhou Lng Co ltd
Chengdu Univeristy of Technology
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 Southwest Branch Of China Petroleum Engineering & Construction Corp, Zhejiang Zheneng Wenzhou Lng Co ltd, Chengdu Univeristy of Technology filed Critical Southwest Branch Of China Petroleum Engineering & Construction Corp
Priority to CN202111112458.2A priority Critical patent/CN113738467B/en
Publication of CN113738467A publication Critical patent/CN113738467A/en
Application granted granted Critical
Publication of CN113738467B publication Critical patent/CN113738467B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

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
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0266—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 characterised by the separated product stream separation of carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
    • F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
    • F01D15/10—Adaptations for driving, or combinations with, electric generators
    • 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
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
    • 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
    • F25J3/04272—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons and comprising means for reducing the risk of pollution of hydrocarbons into the air fractionation
    • 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
    • F25J3/04278—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using external refrigeration units, e.g. closed mechanical or regenerative refrigeration units
    • 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
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • 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
    • F25J3/044—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 using a single pressure main column system only
    • 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
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • 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
    • 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
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • 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
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration 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
    • 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

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Environmental & Geological Engineering (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

The invention discloses an integrated system for carrying out carbon-carrying capture power generation by utilizing liquefied natural gas, which comprises an LNG gasification and cold energy utilization system, an air separation oxygen generation system, an oxygen-enriched combustion turbine circulation power generation and tail gas carbon recovery system. Compared with the prior art, the invention has the following positive effects: the invention integrates LNG gasification, cold energy oxygen production, oxygen-enriched power generation and carbon capture, and has the advantages that the energy consumption in LNG gasification, oxygen production and carbon capture links can be greatly reduced, the LNG cold energy utilization rate is improved, the power generation efficiency is improved, and the zero-carbon emission power generation effect can be realized by injecting captured carbon dioxide into the underground salt water for sealing. According to the invention, pure oxygen is prepared by utilizing LNG cold energy, the pure oxygen and natural gas participate in oxygen-enriched combustion turbine to circularly generate power, and the generated tail gas is subjected to carbon dioxide capture, so that the energy consumption of LNG gasification, oxygen production and carbon capture links is reduced, a zero-carbon power generation technology is created, the social requirement of future carbon neutralization is met, and the application prospect is wide.

Description

Integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas
Technical Field
The invention relates to an integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas, in particular to a system for carrying out carbon dioxide capturing by utilizing LNG cold energy to prepare pure oxygen, wherein the pure oxygen, the natural gas and carbon dioxide participate in oxygen-enriched combustion turbine to circularly generate power.
Background
In recent years, the greenhouse effect has been paid attention to, and researches have shown that CO in the atmosphere 2 Is one of the gases with the greatest influence on the greenhouse effect. The heating effect produced by the method is about 63% of the total heating effect. China is used as a country with large carbon emission, and faces severe carbon emission reduction pressure.
Liquefied natural gas (Liquefied Natural Gas, abbreviated as LNG) contains methane as a main component, and the atmospheric boiling point of methane is-161 ℃. The manufacturing process is that natural gas produced by a gas field is purified (dehydrated, dealkylated and deacidified), and then methane is changed into liquid by adopting the processes of throttling, expanding and externally adding cold source refrigeration, and external heating is needed for regasification when the natural gas is used. The liquefied natural gas has the advantages of no impurity and pure components, and the amount of the greenhouse gas released in the combustion process is far smaller than that of other fossil fuels, so that the liquefied natural gas is an ideal clean and efficient power generation fuel. The LNG can release about 830kJ/kg of cold energy in the gasification process, and has great utilization value. But from the global aspect, the utilization degree of LNG cold energy is only about 20 percent, the cold energy resource development and utilization rate is low, and the cold energy is low
Figure BDA0003274351880000011
Waste is serious. Carbon Capture and Sequestration (CCS) technology is considered one of the primary measures for carbon emission reduction in electric power, with oxycombustion technology being considered the most readily available carbon capture technology for industrialization and scale-up. The main factors limiting the popularization of the oxygen-enriched combustion technology at present are large energy consumption and mainly concentrate on air separation oxygen production and CO production 2 Compressing and capturing links.
There are many kinds of oxygen-enriched combustion turbine cycles, and the best-known Allam-Fetvedt cycle is taken as an example, and Allam-Fetvedt cycle is a Brayton cycle technology, and "ten breakthrough technologies worldwide" in Massa technology comment in 2018 have been selected. The technology adopts oxygen-enriched combustion and supercritical CO 2 As a working fluid, it is capable of recovering waste heat and eliminating conventional pollutants and CO 2 And (5) discharging. As a by-product, pipeline CO is produced which can be used for sealing 2 . According to the measurement and calculation of foreign well-known institutions, the power supply efficiency of the Allam-Fetvedt cycle at the working pressure of 30MPa and the turbine inlet temperature of 1100 ℃ is 2.3 percent higher than that of the natural gas combined cycle of the existing F-level gas turbine, and the Allam-Fetvedt cycle can be used for burning daysThe gas or the coal synthesis gas realizes complete carbon capture and NO emission of pollutants such as NOx and the like.
The invention combines the LNG gasification, cold energy oxygen production, oxygen-enriched power generation, carbon capture and other technical cross fields, and has the advantages that the energy consumption in the LNG gasification, oxygen production and carbon capture links can be greatly reduced, the LNG cold energy utilization rate is improved, the power generation efficiency is improved, and the zero-carbon emission power generation effect can be realized by injecting captured carbon dioxide into the underground salt water for sealing; meanwhile, the system adopts a multi-stage heat exchange thought, so that the heat exchange temperature difference is reduced on one hand, and the heat exchanger is improved
Figure BDA0003274351880000021
Efficiency, on the other hand, reduces the compression power consumption of the compressor. Compared with the traditional gas power plant technology, the invention can realize zero-carbon emission power generation, has high efficiency, is clean and environment-friendly, is safe and reliable, has good economic benefit, and can be conveniently moved to other areas to continue service when the demand changes.
Disclosure of Invention
In order to develop the technology for reducing the electricity generation and decarbonization cost of liquefied natural gas, the invention provides an integrated system for carrying out carbon-carrying capture electricity generation by utilizing liquefied natural gas, pure oxygen is prepared by utilizing LNG cold energy, the pure oxygen and the natural gas participate in oxygen-enriched combustion turbine circulation electricity generation, and the electricity generation tail gas carries out carbon dioxide capture, so that the energy consumption of LNG gasification, oxygen production and carbon capture links is reduced, a zero-carbon electricity generation technology is created, the social requirement of future carbon neutralization is met, and the application prospect is wide.
The technical scheme adopted for solving the technical problems is as follows: an integrated system for carrying out carbon-carrying capture power generation by utilizing liquefied natural gas comprises an LNG gasification and cold energy utilization system, an air separation oxygen generation system, an oxygen-enriched combustion turbine cycle power generation and tail gas carbon recovery system, wherein:
the LNG gasification and cold energy utilization system comprises an LNG storage tank, an LNG booster pump, a cold box and a heat exchanger which are sequentially connected; the nitrogen circulation loop is composed of a nitrogen compressor, a first heat exchanger, a first cold box, a liquid nitrogen separator, a second cold box and a nitrogen compressor;
the air separation oxygen generation system comprises an air filtering device, an air compressor, a second heat exchanger, an air dehydration device, a third heat exchanger, a second cold box, an air expander and an air rectifying tower which are sequentially connected, wherein an upper outlet of the air rectifying tower is sequentially connected with the second cold box and the third heat exchanger, the bottom of the air rectifying tower is respectively connected with an inlet of the second cold box and an inlet of a liquid oxygen booster pump, an outlet of the second cold box is connected with an inlet of the air rectifying tower, and an outlet of the liquid oxygen booster pump is connected with an inlet of the second heater;
the oxygen-enriched combustion turbine cyclic power generation and tail gas carbon recovery system comprises an LNG storage tank, a second LNG booster pump, a first heater, a mixed burner, a turbine generator, a fourth heat exchanger, a first cooler, a carbon dioxide separator, a carbon dioxide compressor and a second cooler which are sequentially connected, wherein an outlet of the second cooler is divided into two paths, one path is connected into an external transmission and storage channel, and the other path is sequentially connected with the carbon dioxide booster pump, the fourth heat exchanger and the mixed burner; the outlet of the second heater is connected with the inlet of the mixing burner.
Compared with the prior art, the invention has the following positive effects:
the invention integrates LNG gasification, cold energy oxygen production, oxygen-enriched power generation and carbon capture, and has the advantages that the energy consumption in LNG gasification, oxygen production and carbon capture links can be greatly reduced, the LNG cold energy utilization rate is improved, the power generation efficiency is improved, and the zero-carbon emission power generation effect can be realized by injecting captured carbon dioxide into the underground salt water for sealing. The LNG gasification considers cold energy utilization, adopts two-stage cooling, reduces the oxygen temperature by reducing the temperature of ethylene glycol, and avoids explosion hazard caused by direct contact of oxygen and LNG. The invention also considers the bearing capacity of the pressure vessel, utilizes a plurality of compression devices to adjust the inlet pressure, and avoids the operation of the devices in high-load and high-pressure dangerous states. Meanwhile, the system adopts a multi-stage heat exchange thought, so that the heat exchange temperature difference is reduced on one hand, and the heat exchanger is improved
Figure BDA0003274351880000031
Efficiency, on the other hand, reduces the compression power consumption of the compressor. The invention also considers that methane is in excess of the critical pointBoundary CO 2 Laminar flame propagation velocity ratio in atmosphere at subcritical CO 2 100 times higher in the air mixture and no rich flameout limit; methane in supercritical CO 2 The direct combustion in the atmosphere heats up, has good combustion heat exchange efficiency, supports the turbine power generation at the back and obtains superior power generation efficiency; natural gas in supercritical CO 2 And the pure oxygen mixture is combusted, and the tail gas has no NOx emission problem; the inlet and outlet of the turbine are in supercritical and subcritical states respectively, the output power of the turbine is high, the turbine is very beneficial to removing moisture in the combustion tail gas through the cooler and the separator, and in order to keep the total flow of the circulating working medium unchanged, carbon dioxide increment generated by combustion is continuously discharged out of the system and is trapped, so that 100% of carbon trapping of the power generation tail gas can be realized.
Drawings
The invention will now be described by way of example and with reference to the accompanying drawings in which:
FIG. 1 is a schematic diagram of an integrated system for carbon-bearing capture power generation using liquefied natural gas;
reference numerals in the drawings include: LNG storage tank 1, LNG booster pump 2, cold box 3, heat exchanger 4, nitrogen compressor 5, air filter 6, air compressor 7, heat exchanger 8, air dewatering device 9, heat exchanger 10 No. three, cold box 11 No. two, air expander 12, air rectifying column 13, first governing valve 14, second governing valve 15, liquid nitrogen separator 16, liquid oxygen booster pump 17, ethylene glycol booster pump 18, LNG booster pump 19 No. two, heater 20 No. two, heater 21, hybrid combustor 22, turbine generator 23, heat exchanger 24 No. four, cooler 25 No. one, carbon dioxide separator 26, carbon dioxide compressor 27, cooler 28 No. two, carbon dioxide booster pump 29.
Detailed Description
As shown in FIG. 1, the integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas comprises an LNG gasification and cold energy utilization system, an air separation oxygen generation system, an oxygen-enriched combustion turbine cycle power generation and tail gas carbon recovery system; wherein:
1. LNG gasification and cold energy utilization system
The LNG gasification and cold energy utilization system comprises an LNG storage tank 1, an LNG booster pump 2, an LNG cold box 3, an heat exchanger 4, a nitrogen compressor 5, a second regulating valve 15 and a liquid nitrogen separator 16;
the connection mode of equipment in the LNG gasification and cold energy utilization system is as follows: an LNG storage tank 1 is arranged at the inlet of a first LNG booster pump 2, and then is connected with a first cold box 3 and a first heat exchanger 4 in sequence; the outlet of the nitrogen compressor 5 is connected with a first heat exchanger 4 and then is connected with a first cold box 3, the outlet of the first cold box 3 is connected with a second regulating valve 15 and then is connected with a liquid nitrogen separator 16, the liquid nitrogen separator is provided with two outlets, the two outlets are connected with different inlets of a second cold box 11, and pipelines of the two outlets corresponding to the second cold box 11 are combined and then are connected with the nitrogen compressor 5 to form a closed loop.
In LNG gasification and cold energy utilization systems:
the low-pressure LNG with the pressure of 0.4-1.0 MPa is formed into high-pressure LNG with the pressure of 100MPa and 162 ℃ below zero by passing through a pipeline through an LNG booster pump 2 from an LNG storage tank 1, then the high-pressure LNG is sent to a first cold box 3 for cold energy recovery, the high-pressure LNG is formed into low-temperature high-pressure natural gas with the pressure of 10MPa after exiting the first cold box 3, and the low-pressure natural gas with the pressure of 0 ℃ is subjected to heat exchange with nitrogen through a first heat exchanger 4 for secondary cold energy recovery, and then the natural gas is subjected to normal-temperature high-pressure natural gas output;
the nitrogen with the pressure of 0.5MPa and the temperature of minus 40 ℃ is pressurized to 4.5MPa by a nitrogen compressor 5, the nitrogen enters a first heat exchanger 4 to exchange heat with low-temperature high-pressure natural gas for the first time to obtain 4.5MPa, the nitrogen with the temperature of minus 150 ℃ enters a first cold box 3 to exchange heat with LNG to obtain 4.5MPa, the liquid nitrogen with the temperature of minus 150 ℃ is depressurized by a second regulating valve 15, the pressure and the temperature of minus 179 ℃ are delivered to a liquid nitrogen separator 16 to carry out gas-liquid separation, the nitrogen is separated by the liquid nitrogen separator 16 and then is respectively delivered to a second cold box 11 to be respectively converted into nitrogen and normal-temperature nitrogen after cold energy recovery, and the nitrogen and the normal-temperature nitrogen are delivered to the nitrogen compressor 5 to complete nitrogen recycling.
2. Air separation oxygen generation system
The air separation oxygen generation system comprises a second cold box 11, an air filtering device 6, an air compressor 7, a second heat exchanger 8, a third heat exchanger 10, an air dehydration device 9, an air expander 12, an air rectifying tower 13, a liquid oxygen booster pump 17, a first regulating valve 14 and an ethylene glycol booster pump 18;
the equipment connection mode in the air separation oxygen production system is as follows: the inlet of the ethylene glycol booster pump 18 is connected with the second heat exchanger 8, the inlet of the second heat exchanger 8 is connected with the first cold box outlet 3, and the inlet of the first cold box 3 is connected with the outlet of the ethylene glycol pump 18 to form a closed loop; the outlet of the air filtering device 6 is connected with the inlet of the air compressor 7, the outlet of the air compressor 7 is connected with the second heat exchanger 8, the second heat exchanger 8 is connected with the inlet of the air dehydration device 9, the outlet of the air dehydration device 9 is connected with the inlet of the second cold box 11 after being connected with the third heat exchanger 10, the outlet of the second cold box 11 is connected with the inlet 12 of the air expander, the outlet of the air expander 12 is connected with the air rectifying tower 13, the upper outlet of the air rectifying tower 13 is connected with the inlet of the second cold box 11, the outlet of the second cold box 11 is connected with the third heat exchanger 10, the bottom of the air rectifying tower 13 is respectively connected with the inlet of the second cold box 11 and the liquid oxygen booster pump 17, the outlet of the second cold box 11 is connected with the rectifying tower 13 after being connected with the first regulating valve 14, and the outlet of the liquid oxygen booster pump 17 is connected with the second heater 21.
In an air separation oxygen production system:
ethylene glycol at the normal temperature of 20 ℃ is pressurized to 1.6MPa by an ethylene glycol booster pump 18 and then is sent to a first cold box 3 for heat exchange, the temperature of the ethylene glycol after the exchange is-40 ℃, and the ethylene glycol after the temperature reduction is sent to a second heat exchanger 8 for heat exchange with air and then returns to the ethylene glycol booster pump 18 to complete the ethylene glycol circulation; the air is sequentially filtered by an air filtering device 6 and then is conveyed to an air compressor 7 to be pressurized to 5MPa, the temperature is 700 ℃, then the air is conveyed to an air dehydration device 9 to remove water after being subjected to heat exchange with ethylene glycol through a second heat exchanger 8 and then is conveyed to a third heat exchanger 10 to be subjected to heat exchange with low-temperature nitrogen, then the air is conveyed to a second cold box 11 to be subjected to heat exchange again and then is subjected to temperature reduction to-170 ℃, the low-temperature air after heat exchange enters an air expansion machine 12 to generate electricity, electric power is output, and low-pressure air (liquid air) which is discharged from the air expansion machine 12 enters an air rectifying tower 13 to be rectified;
the air is separated into rising-183 ℃ low-temperature nitrogen and liquid oxygen with the bottom of-183 ℃ in the air rectifying tower 13; the low-temperature nitrogen is pumped from the upper part and conveyed to the second cold box 11 to recover cold energy, then the cold energy is conveyed to the third heat exchanger 10 to exchange heat with air, then the cold energy is directly discharged, liquid oxygen is pumped from the bottom and is divided into two liquid oxygen with the pressure of 0.1MPa, one liquid oxygen enters the second cold box 11 to recover cold energy, then the cold energy is reduced in pressure through the first regulating valve 14 and is conveyed back to the air rectifying tower 13, the other liquid oxygen is pressurized to 3MPa by the liquid oxygen booster pump 17 and then becomes high-pressure liquid oxygen, the high-pressure liquid oxygen enters the second heater 21 to exchange heat with hot water, the hot water is cooled to be cold water to be discharged after heat exchange, and the high-pressure liquid oxygen is heated to become high-pressure oxygen and then conveyed to the mixed combustor 22.
3. Oxygen-enriched combustion turbine cyclic power generation and tail gas carbon recovery system
The oxygen-enriched combustion turbine cyclic power generation and tail gas carbon recovery system comprises: a LNG booster pump 19, a heater 20, a heater 21, a hybrid combustor 22, a turbine generator 23, a carbon dioxide compressor 27, a carbon dioxide separator 26, a cooler 25, a heat exchanger 24, a carbon dioxide booster pump 29, and a cooler 28;
the connection mode of the oxygen-enriched combustion turbine cyclic power generation and tail gas carbon recovery system is as follows: the inlet of the second LNG booster pump 19 is connected with the LNG storage tank 1, the outlet of the second LNG booster pump 19 is connected with the first heater 20, the first heater 20 is connected with the mixed combustor 22, the outlet of the mixed combustor 22 is connected with the turbine generator 23, the outlet of the turbine generator 23 is connected with the fourth heat exchanger 24, the fourth heat exchanger 24 is connected with the inlet of the first cooler 25, the outlet of the first cooler 25 is connected with the carbon dioxide separator 26, the outlet of the carbon dioxide separator 26 is connected with the carbon dioxide compressor 27, the carbon dioxide compressor 27 is connected with the inlet of the second cooler 28, the outlet of the second cooler 28 is connected with the carbon dioxide booster pump 29 or the external transmission, and the outlet of the carbon dioxide booster pump 29 is connected with the fourth heat exchanger 24 and then connected with the mixed combustor 22 to form a closed loop; the outlet of the second heater 21 is connected with the inlet of the mixing burner 22.
In the oxygen-enriched combustion turbine cycle power generation and tail gas carbon recovery system:
the reaction pressure of the mixing burner 22 was 3MPa. LNG is output from an LNG storage tank 1, pressurized to 3MPa through a second LNG booster pump 19, preheated by a first heater 20 to generate high-pressure natural gas, and then conveyed to a mixing combustor 22; the high-pressure oxygen after heat exchange by the second heater 21 is sent to the mixing burner 22 and CO 2 Mixing natural gas at a certain proportion, wherein carbon dioxide is 94%, and the mixture is used for daily useThe gas accounts for 1.25 percent, the oxygen accounts for 4.75 percent, and when the reaction occurs, the components can form dynamic change due to the reaction process; the waste heat is fed into a first cooler 25 to heat cold water again after exiting the fourth heat exchanger 24, the waste heat is fed into a carbon dioxide separator 26 to separate out water, the carbon dioxide is fed into a carbon dioxide compressor 27 to be compressed, the carbon dioxide is fed into a second cooler 28 to be preheated by hot water to be supercritical carbon dioxide, a part of the supercritical carbon dioxide is fed into the fourth heat exchanger 24 to be heated again to be high-temperature high-pressure carbon dioxide through a carbon dioxide booster pump 29 and then fed into a mixed combustor 22, and the other part of the supercritical carbon dioxide is fed to be sealed.

Claims (8)

1. An integrated system for carrying out carbon-containing capture power generation by utilizing liquefied natural gas, which is characterized in that: the system comprises an LNG gasification and cold energy utilization system, an air separation oxygen production system, an oxygen-enriched combustion turbine cyclic power generation and tail gas carbon recovery system, wherein:
the LNG gasification and cold energy utilization system comprises an LNG storage tank, an LNG booster pump, a cold box and a heat exchanger which are sequentially connected; the nitrogen circulation loop is composed of a nitrogen compressor, a first heat exchanger, a first cold box, a liquid nitrogen separator, a second cold box and a nitrogen compressor; the liquid nitrogen separator of the nitrogen circulation loop is provided with two outlets, the two outlets are connected with different inlets of a second cold box, and pipelines of the two outlets corresponding to the second cold box are combined and then connected to a nitrogen compressor;
the air separation oxygen generation system comprises an air filtering device, an air compressor, a second heat exchanger, an air dehydration device, a third heat exchanger, a second cold box, an air expander and an air rectifying tower which are sequentially connected, wherein an upper outlet of the air rectifying tower is sequentially connected with the second cold box and the third heat exchanger, the bottom of the air rectifying tower is respectively connected with an inlet of the second cold box and an inlet of a liquid oxygen booster pump, an outlet of the second cold box is connected with an inlet of the air rectifying tower, and an outlet of the liquid oxygen booster pump is connected with an inlet of the second heater; the air separation oxygen generation system comprises an ethylene glycol circulation loop consisting of an ethylene glycol booster pump, a first cold box and a second heat exchanger;
the oxygen-enriched combustion turbine cyclic power generation and tail gas carbon recovery system comprises an LNG storage tank, a second LNG booster pump, a first heater, a mixed burner, a turbine generator, a fourth heat exchanger, a first cooler, a carbon dioxide separator, a carbon dioxide compressor and a second cooler which are sequentially connected, wherein an outlet of the second cooler is divided into two paths, one path is connected into an external transmission and storage channel, and the other path is sequentially connected with the carbon dioxide booster pump, the fourth heat exchanger and the mixed burner; the outlet of the second heater is connected with the inlet of the mixing burner.
2. An integrated system for carbon-bearing capture power generation using lng as in claim 1, wherein: and a regulating valve is arranged between the first cold box of the nitrogen circulation loop and the liquid nitrogen separator.
3. An integrated system for carbon-bearing capture power generation using lng as in claim 1, wherein: and a regulating valve is arranged between the outlet of the second cold box and the inlet of the air rectifying tower.
4. An integrated system for carbon-bearing capture power generation using lng as in claim 1, wherein: in the LNG gasification and cold energy utilization system, low-pressure LNG is subjected to a first LNG booster pump to form high-pressure LNG with the pressure of 100MPa and 162 ℃ and then is sent to a first cold box for cold energy recovery, the high-pressure LNG is subjected to a first cold box to form low-temperature high-pressure natural gas with the pressure of 10MPa and 0 ℃ and then is subjected to cold energy recovery through a first heat exchanger to form normal-temperature high-pressure natural gas for output.
5. An integrated system for carbon-bearing capture power generation using lng as in claim 1, wherein: in the LNG gasification and cold energy utilization system, nitrogen with the pressure of 0.5MPa and the temperature of 40 ℃ is pressurized to 4.5MPa by a nitrogen compressor, the nitrogen enters a first heat exchanger for heat exchange and cooling to 4.5MPa, the nitrogen enters a first cold box for heat exchange with LNG at the temperature of 30 ℃ to form liquid nitrogen with the pressure of 4.5MPa and the temperature of 150 ℃, the liquid nitrogen is depressurized and cooled to 0.5MPa and the temperature of 179 ℃ and then is conveyed to a liquid nitrogen separator for gas-liquid separation, and the low-temperature gas nitrogen and the liquid nitrogen are respectively conveyed to a second cold box for cold energy recovery and then are respectively conveyed to a nitrogen compressor for nitrogen recycling.
6. An integrated system for carbon-bearing capture power generation using lng as in claim 1, wherein: in the air separation oxygen production system, air is sequentially filtered by an air filtering device and then is conveyed to an air compressor to be pressurized to 5MPa and 700 ℃, then is conveyed to an air dehydration device to remove water after being subjected to heat exchange and cooling to-30 ℃ by a second heat exchanger, is conveyed to a third heat exchanger to be subjected to heat exchange, and is conveyed to a second cold box to be subjected to heat exchange and cooling to-170 ℃ again, low-temperature air after heat exchange enters an air expander to be subjected to power generation, and low-pressure air discharged from the air expander enters an air rectifying tower to be rectified: the air is separated into rising low-temperature nitrogen with the temperature of minus 183 ℃ and liquid oxygen with the temperature of minus 183 ℃ at the bottom in an air rectifying tower, wherein the low-temperature nitrogen is pumped out from the upper part and conveyed to a second cooling box, and the cold energy is recovered and then conveyed to a third heat exchanger to exchange heat with the air, and then the cold energy is converted into normal-temperature nitrogen to be directly discharged; the liquid oxygen is pumped out from the bottom and is divided into two liquid oxygen with the pressure of 0.1MPa, one liquid oxygen enters a second cold box for cold energy recovery and is then depressurized and conveyed back to an air rectifying tower, the other liquid oxygen is pressurized to 3MPa by a liquid oxygen booster pump and becomes high-pressure liquid oxygen, the high-pressure liquid oxygen enters a second heater for heat exchange, and the high-pressure liquid oxygen is heated to become high-pressure oxygen and is then conveyed to a mixed combustor.
7. An integrated system for carbon-bearing capture power generation using lng as in claim 1, wherein: in the air separation oxygen generation system, ethylene glycol at the normal temperature of 20 ℃ is pressurized to 1.6MPa by an ethylene glycol booster pump and then is sent to a first cold box for heat exchange, the ethylene glycol temperature is reduced to-40 DEG and then is sent to a second heat exchanger for heat exchange, and then the ethylene glycol returns to the ethylene glycol booster pump for completing the ethylene glycol circulation.
8. An integrated system for carbon-bearing capture power generation using lng as in claim 1, wherein: in the oxygen-enriched combustion turbine cyclic power generation and tail gas carbon recovery system, the reaction pressure of a mixed combustor is 3MPa, LNG is pressurized to 3MPa by a second LNG booster pump and then preheated by a first heater to generate high-pressure natural gas, and the high-pressure natural gas is conveyed to the mixed combustor; high-pressure oxygen after heat exchange by a second heater is sent to a mixing burner to be mixed with CO 2 Natural gas is mixed, combusted and expanded and then is conveyed to a turbine generator, power generation is carried out through gas expansion, current is conveyed outwards, then high-temperature tail gas is conveyed to a fourth heat exchanger for heat exchange, the tail gas enters a first cooler for heating cold water again by using waste heat after exiting the fourth heat exchanger, the tail gas enters a carbon dioxide separator for separating out water after exiting the first cooler, enters a carbon dioxide compressor, carbon dioxide is conveyed to a second cooler for preheating by hot water after being compressed, one part of the tail gas serves as supercritical carbon dioxide to be conveyed outwards for sealing, and the other part of the tail gas is conveyed to the fourth heat exchanger for heating again to become high-temperature high-pressure carbon dioxide and then is conveyed to a mixed combustor.
CN202111112458.2A 2021-09-23 2021-09-23 Integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas Active CN113738467B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202111112458.2A CN113738467B (en) 2021-09-23 2021-09-23 Integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202111112458.2A CN113738467B (en) 2021-09-23 2021-09-23 Integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas

Publications (2)

Publication Number Publication Date
CN113738467A CN113738467A (en) 2021-12-03
CN113738467B true CN113738467B (en) 2023-07-14

Family

ID=78740505

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202111112458.2A Active CN113738467B (en) 2021-09-23 2021-09-23 Integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas

Country Status (1)

Country Link
CN (1) CN113738467B (en)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114922715B (en) * 2022-05-12 2024-08-06 江苏科技大学 Low-temperature carbon trapping system for dual-fuel ship and working 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
CN115263466A (en) * 2022-07-13 2022-11-01 江苏科技大学 Low-temperature carbon capture coupling cold energy and waste heat cascade utilization system of LNG power ship

Citations (6)

* 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
CN105115245A (en) * 2015-08-11 2015-12-02 中海油能源发展股份有限公司北京冷能利用研究所 System device for trapping liquefied carbon dioxide by using cold energy of liquefied natural gas and method of device
CN105605602A (en) * 2016-01-28 2016-05-25 华中科技大学 Natural gas oxygen-enriched combustion system capable of using liquefied natural gas (LNG) cold energy for air separation oxygen-making and carbon capture
CN109812304A (en) * 2019-03-06 2019-05-28 上海发电设备成套设计研究院有限责任公司 The peaking generation system and method for integrated carbon dioxide recycle and liquefied air energy storage
CN209586523U (en) * 2019-01-28 2019-11-05 华北电力大学 A kind of oxygen-enriched combusting electricity generation system that integrated solar methane dry type is reformed
CN215907932U (en) * 2021-09-23 2022-02-25 浙江浙能温州液化天然气有限公司 Integrated system for carbon-carrying capture power generation by utilizing liquefied natural gas

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2776683B1 (en) * 2011-10-22 2020-12-30 Sustainable Energy Solutions, LLC Systems and methods for integrated energy storage and cryogenic carbon capture

Patent Citations (6)

* 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
CN105115245A (en) * 2015-08-11 2015-12-02 中海油能源发展股份有限公司北京冷能利用研究所 System device for trapping liquefied carbon dioxide by using cold energy of liquefied natural gas and method of device
CN105605602A (en) * 2016-01-28 2016-05-25 华中科技大学 Natural gas oxygen-enriched combustion system capable of using liquefied natural gas (LNG) cold energy for air separation oxygen-making and carbon capture
CN209586523U (en) * 2019-01-28 2019-11-05 华北电力大学 A kind of oxygen-enriched combusting electricity generation system that integrated solar methane dry type is reformed
CN109812304A (en) * 2019-03-06 2019-05-28 上海发电设备成套设计研究院有限责任公司 The peaking generation system and method for integrated carbon dioxide recycle and liquefied air energy storage
CN215907932U (en) * 2021-09-23 2022-02-25 浙江浙能温州液化天然气有限公司 Integrated system for carbon-carrying capture power generation by utilizing liquefied natural gas

Also Published As

Publication number Publication date
CN113738467A (en) 2021-12-03

Similar Documents

Publication Publication Date Title
JP7112378B2 (en) Method and system for power generation with improved efficiency
CN113738467B (en) Integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas
US10054046B2 (en) System and method for high efficiency power generation using a nitrogen gas working fluid
JP6153231B2 (en) Carbon dioxide capture system and method in a low emission turbine system
CN107108233B (en) Production of low pressure liquid carbon dioxide from power generation systems and methods
CN108439336B (en) Zero-emission hydrogen electric cogeneration system
AU2012200096B2 (en) Carbon dioxide liquefaction system
CN114046172B (en) System and method for treating and utilizing coal fire based on carbon dioxide process and modularized design
US20120009075A1 (en) Systems for compressing a gas
CN215907932U (en) Integrated system for carbon-carrying capture power generation by utilizing liquefied natural gas
CN114382562B (en) Shunt recompression pure oxygen combustion circulation system
CN109350988B (en) CO (carbon monoxide) 2 IGFC power generation system and method with liquefaction process and cryogenic air separation coupling
Mathieu et al. New concept of CO2 removal technologies in power generation, combined with fossil fuel recovery and long term CO2 sequestration
CN109184830B (en) Fuel and oxygen combustion product and CO2Mixed working medium circulation power generation device
CN109812335B (en) Zero-carbon-emission integrated coal gasification-steam combined cycle power generation process
CN114776392A (en) System and method for generating power based on integrated coal gasification and complete carbon capture cycle
CN117928172A (en) High-purity liquid CO utilizing LNG cold energy2Production method and system
CN116517653A (en) Coal supercritical water gasification power generation system for circulating supercritical carbon dioxide working medium and operation method
CN115930550A (en) System for carrying out carbon capture by utilizing liquefied natural gas
VanOsdol et al. Using Staged Compression to Increase the System Efficiency of a Coal Based Gas Turbine Fuel Cell Hybrid Power Generation System With Carbon Capture

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant