CN115930550A - System for carrying out carbon capture by utilizing liquefied natural gas - Google Patents

System for carrying out carbon capture by utilizing liquefied natural gas Download PDF

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Publication number
CN115930550A
CN115930550A CN202211451112.XA CN202211451112A CN115930550A CN 115930550 A CN115930550 A CN 115930550A CN 202211451112 A CN202211451112 A CN 202211451112A CN 115930550 A CN115930550 A CN 115930550A
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seabed
heat exchanger
air
carbon dioxide
natural gas
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CN202211451112.XA
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Chinese (zh)
Inventor
管恩勇
梁光川
周军
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Southwest Petroleum University
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Southwest Petroleum University
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    • 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
    • F25J3/04248—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
    • F25J3/044—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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) 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
    • 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.
    • 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

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention discloses a system for capturing carbon by using liquefied natural gas, which comprises a cold box, an air rectifying tower, a mixed combustor, a turbine, a heat exchanger, a waste cooler, a gas separation device, a supercritical carbon dioxide compressor, a seabed heat exchanger, a supercritical carbon dioxide turbine, a seabed cooler and a seabed cavern gas storage. Compared with the prior art, the invention has the following positive effects: the invention integrates LNG cold energy utilization, air oxygen production, oxygen-enriched power generation and seabed carbon sequestration, has the advantages of reducing equipment load through multi-stage heat exchange, improving the utilization rate of cold energy, realizing zero emission of carbon dioxide by seabed carbon sequestration, and has wide application prospect, low carbon, environmental protection and high utilization rate.

Description

System for carrying out carbon capture by utilizing liquefied natural gas
Technical Field
The invention relates to a system for capturing carbon by using liquefied natural gas, in particular to a system for capturing carbon dioxide by using LNG cold energy to prepare pure oxygen, burning for power generation and capturing tail gas for seabed sealing.
Background
The natural gas is a mixture of different components according to a certain proportion, and the main component of the natural gas is hydrocarbon, including methane, ethane, propane, butane and the like, wherein the methane accounts for more than 90 percent. LNG, i.e., liquefied Natural Gas (Liquefied Natural Gas), is Natural Gas produced in a Gas field, which is purified and Liquefied at a series of ultra-low temperatures to obtain Natural Gas that is liquid at normal pressure, and is known as the cleanest fossil energy source on the earth. Typically, liquefied natural gas is liquefied at normal atmospheric pressure by reducing the temperature to about-162 c.
In recent years, attention has been paid to the greenhouse effect, and studies have shown that atmospheric CO 2 Is one of the most influential gases on the greenhouse effect. The heating effect produced by the temperature-increasing device is about 63 percent of the total heating effect. China faces a severe carbon emission reduction pressure as a carbon emission big country. Geothermal energy is used as pollution-free clean energy, has huge reserves and is an important development direction of renewable biogenic sources. The earth's surface covered by the ocean has a richer geothermal resource on the ocean floor.
The invention combines the technologies of LNG gasification, cold energy oxygen production, LNG power generation, seabed carbon sequestration and the like in cross-field, has the advantages of reducing energy consumption, improving the utilization rate of cold energy and realizing zero emission of carbon.
Disclosure of Invention
In order to solve the problems, the invention provides a system for capturing carbon by using liquefied natural gas, which is an integrated system for sealing and storing seabed with carbon capture by using liquefied natural gas cold energy, is used for liquefying air to prepare pure oxygen by using LNG cold energy, mixing and burning the pure oxygen and the natural gas to generate electricity, capturing carbon dioxide by using tail gas after the electricity generation, and sealing and storing the tail gas in a seabed waste gas exhausted gas storage.
The invention is realized by adopting the following technical scheme:
a system for capturing carbon by utilizing liquefied natural gas comprises an LNG storage tank, a booster pump, a cold box, a first heat exchanger, an air rectifying tower, an air filtering device, an air compressor, an air drying device, a second heat exchanger, an air expander, a mixed combustor, a turbine, a third heat exchanger, a waste gas cooler, a supercritical carbon dioxide compressor, a seabed heat exchanger, a supercritical carbon dioxide turbine, a seabed cooler and a seabed cavern gas storage.
The LNG storage tank is connected with a booster pump, the outlet of the booster pump is connected with a cold box, the outlet of the cold box is connected with a first heat exchanger, and the outlet of the heat exchanger is connected with a mixed combustor; the air filtering device is sequentially connected with an air compressor, an air drying device, a second heat exchanger, a cold box, an air expander and a liquid phase inlet of the air rectifying tower; a gas phase outlet at the upper part of the air rectifying tower is sequentially connected with a first heat exchanger, a cold box and a second heat exchanger; a liquid phase outlet at the lower part of the air rectifying tower is sequentially connected with the cold box and the third heat exchanger mixed burner; the waste gas outlet of the mixed combustor is sequentially connected with a turbine, a third heat exchanger, a waste gas cooler, a gas separation device, a supercritical carbon dioxide compressor, a supercritical carbon dioxide turbine, a seabed cooler and a seabed rock cavern gas storage.
Compared with the prior art, the invention has the following positive effects:
the invention integrates the utilization of LNG cold energy for oxygen generation, oxygen-enriched power generation, tail gas recovery and carbon seabed storage, has the advantages of fully utilizing the cold energy during LNG gasification, capturing carbon dioxide and storing the carbon dioxide in the seabed gas storage of waste gas, and can improve the utilization rate of the LNG cold energy and the power generation efficiency on the premise of low carbon and environmental protection.
Furthermore, the invention adopts a multi-stage heat exchange scheme, on one hand, the temperature difference is reduced by considering the bearing temperature of equipment, and on the other hand, the temperature of the heat exchanger is improved
Figure BDA0003944775760000021
Efficiency, reduced equipment work load and prolonged equipment service life.
Furthermore, the tail gas stripping device provided by the invention utilizes the selective permeation film, and compared with the traditional process, the tail gas stripping device is quicker and simpler, reduces the cost, and is safer and more green.
Furthermore, the carbon dioxide is safer to store in the form of hydrate, the carbon dioxide is not easy to leak, and the water quality and the ecological environment cannot be influenced.
Furthermore, the large seabed pressure can reduce the pressure difference of carbon dioxide storage and reduce the strength requirement of the transportation pipeline.
Drawings
Fig. 1 is a schematic diagram of a carbon capture system using lng:
in the figure: 1LNG storage tank, 2 booster pumps, 3 cold boxes, 4 first heat exchangers, 5 pressure reducing valves, 6 air rectifying towers, 7 air filtering devices, 8 air compressors, 9 air drying devices, 10 second heat exchangers, 11 air expanders, 12 mixed combustors, 13 turbines, 14 third heat exchangers, 15 waste gas coolers, 16 gas separation devices, 17 supercritical carbon dioxide compressors, 18 subsea heat exchangers, 19 supercritical carbon dioxide turbines, 20 subsea coolers, 21 subsea cavern gas storages
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on those shown in the drawings, and are used only for convenience in describing the present invention and for simplicity in description, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and thus, are not to be construed as limiting the present invention. Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or to implicitly indicate the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified. In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in a specific case to those of ordinary skill in the art.
A system for capturing carbon by using liquefied natural gas comprises an LNG storage tank 1, a booster pump 2, a cold box 3, a first heat exchanger 4, an air rectifying tower 6, an air filtering device 7, an air compressor 8, an air drying device 9, a second heat exchanger 10, an air expander 11, a mixed combustor 12, a turbine 13, a third heat exchanger 14, an exhaust gas cooler 15, an exhaust gas cooler 16, a supercritical carbon dioxide compressor 17, a seabed heat exchanger 18, a supercritical carbon dioxide turbine 19, a seabed cooler 20 and a seabed cave gas storage 21.
Wherein, the outlet of the LNG storage tank 1 is connected with a booster pump 2, the outlet of the booster pump 2 is connected with a cold box 3, the outlet of the cold box 3 is connected with a first heat exchanger 4 and is connected with a mixed combustor 12 after passing through a pressure reducing valve; the air filtering device 7 is sequentially connected with an air compressor 8, an air drying device 9, a second heat exchanger 10, a cold box 3, an air expansion 11 and a liquid phase inlet of an air rectifying tower 6; the gas phase outlet at the upper part 6 of the air rectifying tower is sequentially connected with a first heat exchanger 10, a cold box 3 and a second heat exchanger 10; a liquid phase outlet at the lower part of the air rectifying tower 6 is sequentially connected with the cold box 3, the third heat exchanger 14 and the mixed combustion 12; the waste gas outlet of the mixed combustor 12 is sequentially connected with a turbine 13, a third heat exchanger 14, a waste gas cooler 15, a gas separation device 16, a supercritical carbon dioxide compressor 17, a seabed heat exchanger 18, a supercritical carbon dioxide turbine 19, a seabed cooler 20 and a seabed cavern gas storage 21.
The low-pressure LNG from the LNG storage tank 1 is pressurized to a high-pressure state through the booster pump 2 and passes through the cold box 3 to recycle cold energy, the LNG is gasified into low-temperature high-pressure natural gas after the cold energy recycling, the low-temperature high-pressure natural gas is subjected to heat exchange with low-temperature nitrogen from an outlet at the upper part of the air rectifying tower 6 through the first heat exchanger 4 to carry out secondary cold energy recycling, and the low-temperature high-pressure natural gas subjected to the heat exchange is subjected to pressure reduction through the pressure reducing valve 5 and is conveyed to the hybrid combustor 12 to carry out oxygen-enriched combustion; air filters particles in the air through an air filtering device 7, the primarily filtered air enters an air compressor 8 and is compressed into high-pressure air which is conveyed to an air drying device 9, water formed in the compression process is dried, the dried air exchanges heat with low-temperature nitrogen from a cold box 3 through a second heat exchanger 10, the temperature of the air is reduced, the high-pressure air with the reduced temperature enters the cold box 3 and further reduces the temperature through the heat exchange with cold energy in the cold box 3, the low-temperature high-pressure air out of the cold box passes through an air expander 11, the pressure is reduced, the low-temperature high-pressure air does work outwards, the low-temperature low-pressure air with the reduced pressure enters an air rectifying tower 6 for rectification, the low-temperature nitrogen flows out of an upper outlet of the air rectifying tower 6, enters the cold box 3 after exchanging heat with natural gas through a first heat exchanger 4, the low-temperature high-pressure air enters a second heat exchanger 10 to exchange heat with the air, and the low-temperature nitrogen becomes normal-temperature nitrogen for emptying; liquid oxygen flows out from a liquid phase outlet at the lower part of the air rectifying tower 6 and enters the cold box 3, the cold box 3 recovers the cold energy of the liquid oxygen, and low-temperature oxygen is preheated by the third heat exchanger 14 and then is conveyed to the mixed combustor 12 after being recovered; oxygen-enriched combustion is carried out in the mixed combustor 12, high-temperature tail gas after combustion enters the turbine 13 to be subjected to power generation and output, the tail gas passing through the turbine 13 is subjected to heat exchange with low-temperature oxygen through the third heat exchanger 14, the temperature of the tail gas is preliminarily reduced, and the tail gas is conveyed to the waste gas cooler 15 to be further reduced in temperature and then conveyed to the gas separation device 16. The gas separation device 16 only separates out carbon dioxide, the separated carbon dioxide enters a supercritical carbon dioxide compressor 17 to be compressed to a low-temperature high-pressure state, then is conveyed to a seabed heat exchanger 18 to exchange heat and keep cold with seawater, and then is conveyed to a medium-supercritical carbon dioxide turbine 19 to perform expansion work to provide electric energy for seabed equipment, and then is conveyed to a seabed cooler 20 to reach a low-temperature state required by the production of carbon dioxide hydrate, and finally is sealed in a seabed cave gas storage 21.
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention, and all the changes or substitutions should be covered within the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.

Claims (2)

1. A system for capturing carbon by using liquefied natural gas is characterized by comprising an LNG storage tank 1, a booster pump 2, a cold box 3, a first heat exchanger 4, a pressure reducing valve 5, an air rectifying tower 6, an air filtering device 7, an air compressor 8, an air drying device 9, a second heat exchanger 10, an air expander 11, a mixed combustor 12, a turbine 13, a third heat exchanger 14, an exhaust gas cooler 15, an exhaust gas cooler 16, a supercritical carbon dioxide compressor 17, a seabed heat exchanger 18, a supercritical carbon dioxide turbine 19, a seabed cooler 20 and a seabed cavern gas storage 21.
2. The system for capturing carbon by using liquefied natural gas according to claim 1, wherein a pressure reducing valve 5 is provided between the first heat exchanger 4 and the mixing burner 12.
CN202211451112.XA 2022-11-15 2022-11-15 System for carrying out carbon capture by utilizing liquefied natural gas Withdrawn CN115930550A (en)

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Application Number Priority Date Filing Date Title
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