CN112174363A - LNG cold energy utilization coproduction fresh water and carbon dioxide sealing device - Google Patents
LNG cold energy utilization coproduction fresh water and carbon dioxide sealing device Download PDFInfo
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- CN112174363A CN112174363A CN201910601185.4A CN201910601185A CN112174363A CN 112174363 A CN112174363 A CN 112174363A CN 201910601185 A CN201910601185 A CN 201910601185A CN 112174363 A CN112174363 A CN 112174363A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 61
- 239000013505 freshwater Substances 0.000 title claims abstract description 46
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 37
- 238000007789 sealing Methods 0.000 title abstract description 7
- 239000013535 sea water Substances 0.000 claims abstract description 56
- 239000003546 flue gas Substances 0.000 claims abstract description 47
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 45
- 239000007789 gas Substances 0.000 claims abstract description 43
- 238000002485 combustion reaction Methods 0.000 claims abstract description 32
- 235000002639 sodium chloride Nutrition 0.000 claims abstract description 31
- 238000010612 desalination reaction Methods 0.000 claims abstract description 26
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 23
- 239000011780 sodium chloride Substances 0.000 claims abstract description 23
- 238000001816 cooling Methods 0.000 claims abstract description 16
- 239000000203 mixture Substances 0.000 claims abstract description 10
- 238000002156 mixing Methods 0.000 claims abstract description 4
- 239000003949 liquefied natural gas Substances 0.000 claims description 124
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 32
- 239000003507 refrigerant Substances 0.000 claims description 31
- 239000006200 vaporizer Substances 0.000 claims description 28
- 239000002918 waste heat Substances 0.000 claims description 25
- 230000009919 sequestration Effects 0.000 claims description 16
- 239000003345 natural gas Substances 0.000 claims description 15
- 238000012546 transfer Methods 0.000 claims description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 238000000354 decomposition reaction Methods 0.000 claims description 8
- 150000003839 salts Chemical class 0.000 claims description 8
- 239000002994 raw material Substances 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 239000000446 fuel Substances 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 230000008901 benefit Effects 0.000 abstract description 5
- 238000005516 engineering process Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000011833 salt mixture Substances 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 15
- 239000012071 phase Substances 0.000 description 12
- 230000008569 process Effects 0.000 description 11
- 239000012267 brine Substances 0.000 description 9
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 9
- 150000004677 hydrates Chemical class 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- -1 and then the hydrate Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
-
- 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
- B01D53/002—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 condensation
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/04—Purification or separation of nitrogen
- C01B21/0405—Purification or separation processes
- C01B21/0494—Combined chemical and physical processing
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/22—Treatment of water, waste water, or sewage by freezing
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
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- Environmental & Geological Engineering (AREA)
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
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Abstract
The invention relates to the technical field of LNG cold energy utilization and hydrate technology application in an LNG receiving station, and discloses a device for joint production of fresh water and carbon dioxide for sealing and storing by LNG cold energy utilization, which comprises an LNG cooling system, a flue gas generation system, a sea salt water desalination system and a hydrate generator, wherein the LNG cooling system is respectively used for providing cold energy for the sea salt water desalination system and the flue gas generation system; the flue gas generation system is used for conveying flue gas generated after LNG combustion into the hydrate generator(ii) a The sea salt water desalination system is used for conveying sea salt water into a hydrate generator and mixing flue gas with the sea salt water to generate CO2Hydrate, N2And a salt mixture to obtain fresh water after separating and decomposing the mixture respectively. The device has the advantages of realizing the high-efficiency utilization of LNG cold energy of the gas power plant and CO-producing seawater desalination and CO2And (4) sealing and storing.
Description
Technical Field
The invention relates to the technical field of LNG cold energy utilization and hydrate technology application in an LNG receiving station, in particular to a device for joint production of fresh water and carbon dioxide by LNG cold energy utilization.
Background
LNG (liquefied natural gas) is low-temperature liquid at the temperature of-162 ℃ under normal pressure, about 240kWh (kilowatt-hour) of cold energy can be generated when each ton of LNG is gasified, and considerable economic benefit can be generated by reasonably utilizing the cold energy. In particular, the cold energy can be used in the fields of seawater desalination, air separation, power generation and the like.
The seawater desalination, namely the seawater desalination is used for producing fresh water, is an open source increment technology for realizing water resource utilization, can increase the total amount of the fresh water, is not influenced by time, space and climate, can ensure stable water supply such as coastal resident drinking water and industrial boiler water supplement, and has higher operation cost. The hydrate method seawater desalination is characterized in that according to the salt elimination effect generated by hydrates, a proper hydration agent is selected to generate hydrate crystals with water in seawater under the conditions of certain temperature and pressure, the salinity of the residual seawater is increased, and the hydrates are decomposed by increasing the temperature to obtain fresh water after solid-liquid separation by methods such as hydrate cleaning and the like, so that the energy conservation and the environmental protection are realized.
The emission of greenhouse gases mainly comprising carbon dioxide is the main cause of global warming and climate change, wherein the carbon dioxide emitted by the combustion of fossil energy accounts for about 2/3 of total emission, and carbon capture and storage are the more feasible CO in the prior art2(carbon dioxide) emission reduction method using CO in flue gas2The characteristic of easy generation of hydrate is that CO is easily generated2In waterEnrichment in the compound phase, thereby allowing CO to be generated2And N2(Nitrogen) separation. CO removal by hydrate process2The technology can be realized at the temperature of more than 0 ℃ and under lower pressure, has the characteristics of energy conservation, high efficiency, safety and the like, also has the advantages of small pressure loss, high separation efficiency and short industrial test flow, has competitive advantages under specific background and has good research and application values.
Disclosure of Invention
Technical problem to be solved
The invention aims to provide a device for utilizing LNG cold energy to coproduce fresh water and carbon dioxide for storage, which at least solves one of the technical problems that some coastal LNG gas power plants in the prior art cannot efficiently utilize the cold energy generated during LNG vaporization, and cannot coproduce fresh water and realize the storage of carbon dioxide in flue gas at the same time.
(II) technical scheme
In order to solve the technical problems, the invention provides an LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration device, which comprises an LNG cooling system, a flue gas generation system, a sea brine desalination system and a hydrate generator, wherein the LNG cooling system is respectively used for providing cold energy for the sea brine desalination system and the flue gas generation system; the flue gas generation system is used for conveying flue gas generated after LNG combustion into the hydrate generator; the sea salt water desalination system is used for conveying sea salt water into a hydrate generator and mixing flue gas with the sea salt water to generate CO2Hydrate, N2And a salt mixture to obtain fresh water after separating and decomposing the mixture respectively.
The LNG cooling system comprises a high-pressure pump, an LNG vaporizer, a refrigerant pump, a first heat exchanger, a second heat exchanger and a third heat exchanger; the sea salt water desalination system comprises a sea water input main pipe, a hydrate decomposer and a hydrate separator; the flue gas generating system comprises an air compressor, a combustion chamber and a compressor which are sequentially connected, wherein an inlet of the hydrate generator is connected with an outlet of a combustion chamber exhaust pipeline cooled by LNG, and an outlet of the hydrate generator is connected with an inlet of a hydrate separator.
The first inlet of the LNG vaporizer is connected with an LNG conveying pipeline, the second inlet of the LNG vaporizer is connected with the refrigerant output pipeline of the hydrate generator through a refrigerant pump, the first outlet of the LNG vaporizer is connected with the first inlet of the first heat exchanger, the second outlet of the LNG vaporizer is connected with the refrigerant input pipeline of the hydrate generator, and the third outlet of the LNG vaporizer is connected with the first inlet of the third heat exchanger.
And a second inlet of the first heat exchanger is connected with a first outlet of the second heat exchanger, a first outlet of the first heat exchanger is connected with a first inlet of the third heat exchanger after being converged with a third outlet of the LNG vaporizer, and a second outlet of the first heat exchanger is connected with a water phase input pipeline of the hydrate generator.
Wherein the outlet of the second heat exchanger is respectively connected with a hydrate decomposition water output pipeline and CO2The sealed output pipeline is connected, and the inlet of the second heat exchanger is respectively connected with the decomposed water conveying pipeline of the hydrate decomposer, the seawater input main pipe and the CO of the hydrate decomposer2The conveying pipelines are communicated.
And a second inlet of the third heat exchanger is connected with the exhaust gas pressurized by the compressor, a first outlet of the third heat exchanger is connected with a fuel inlet of the combustion chamber, and a second outlet of the third heat exchanger is connected with a feed gas input pipeline of the hydrate generator.
The first inlet is connected with a seawater pipeline, and the second inlet is connected with an outlet of a decomposed water conveying pipeline of the hydrate decomposer; a second outlet of the other second heat exchanger and CO2The first inlet is connected with the seawater input main pipe, and the second inlet is connected with CO of the hydrate decomposer2The conveying pipelines are connected.
Wherein the inlet of the combustor is connected with an LNG supply source through an LNG transfer pipeline; the inlet of the combustion chamber is also connected with the outlet of the air compressor, and the outlet of the combustion chamber is connected with the inlet of the turboexpander.
The flue gas generating system further comprises a turbine expander, an inlet of the turbine expander is connected with an outlet of the combustion chamber, an outlet of the turbine expander is connected with an inlet of the compressor, and the turbine expander is used for generating power by high-temperature flue gas generated after natural gas is combusted in the combustion chamber.
The flue gas generating system further comprises an air heat exchanger, an inlet of the air compressor is connected with the air conveying pipeline, and an outlet of the air compressor is connected with a first inlet of the air heat exchanger; and a second inlet of the air heat exchanger is connected with an outlet of a gas phase conveying pipeline of the hydrate separator, a first outlet of the air compressor is connected with an air inlet of the combustion chamber, and a second outlet of the air compressor is connected with the atmosphere.
The device also comprises a waste heat utilization structure; and the inlet of the waste heat utilization structure is connected with the outlet of the turboexpander, and the outlet of the waste heat utilization structure is connected with the compressor.
Wherein the apparatus further comprises a steam turbine; the waste heat utilization structure comprises a waste heat boiler, and an outlet of the waste heat boiler is connected with the steam turbine.
The first inlet of the hydrate generator is connected with a refrigerant input pipeline of the hydrate generator, the second inlet of the hydrate generator is connected with a seawater input pipeline which is refrigerated by the first heat exchanger, the third inlet of the hydrate generator is connected with a raw material gas input pipeline of the hydrate generator which is heat exchanged by the third heat exchanger, the first outlet of the hydrate generator is connected with a refrigerant output pipeline of the hydrate generator, and the second outlet of the hydrate generator is connected with a hydrate conveying pipeline.
Wherein the inlet of the hydrate separator is connected with the second outlet of the hydrate generator through a hydrate conveying pipeline, and the first outlet is connected with CO2The hydrate conveying pipeline is connected, the second outlet is connected with the sea salt conveying pipeline, and the third outlet is connected with the nitrogen conveying pipeline.
Wherein the hydrate decomposerInlet of (2) and CO2The hydrate conveying pipeline is connected, the first outlet is connected with the decomposed water conveying pipeline of the hydrate decomposer, and the second outlet is connected with CO of the hydrate decomposer2The conveying pipelines are connected.
(III) advantageous effects
Compared with the prior art, the LNG cold energy utilization and fresh water and carbon dioxide cogeneration device has the following advantages:
in the application, LNG is pressurized, so that the pressure of the LNG is increased, the cold energy of the LNG is utilized step by step to gradually cool flue gas and seawater, and cold energy is provided for the LNG in the process of generating hydrates to generate CO2Hydrate, N2And the sea salt water desalination system is used for separating and decomposing the mixture to obtain fresh water so as to realize the carbon dioxide sealing and the utilization of the cold energy of decomposed products, so that the cascade efficient utilization of the LNG cold energy is realized, the fresh water is produced in parallel, and the carbon dioxide sealing is realized. Therefore, in the invention, the cold energy cascade utilization of LNG, the high-energy consumption desalination process and the flue gas decarburization process are perfectly combined, the LNG cold energy of the gas power plant is efficiently utilized in the same process, carbon dioxide in flue gas generated after LNG is combusted is sealed and stored, and fresh water is co-produced, so that the device with high energy utilization rate and energy environment protection is provided for the gas power plant.
Drawings
Fig. 1 is a schematic structural diagram of an overall LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant according to an embodiment of the present application.
In the figure, 1: LNG; 2: a high pressure pump; 3: an LNG transfer pipeline; 4: an LNG vaporizer; 5: a natural gas output pipeline; 6: a first heat exchanger; 7: a third heat exchanger; 8: a refrigerant pump; 9: a hydrate generator; 10: a hydrate separator; 11: CO 22A hydrate delivery conduit; 12: n is a radical of2A delivery conduit; 13: a hydrate decomposer; 14: decomposed CO2A delivery conduit; 15: fresh water conveying pipelines after decomposition; 16-1: one of the second heat exchangers; 16-2: in addition, theA second heat exchanger; 17: a seawater input pipeline; 18: a raw material gas input pipeline; 19: a refrigerant output conduit; 20: a refrigerant input pipe; 21: a seawater input main pipe; 22: an air inlet duct; 23: an air compressor; 24: an air heat exchanger; 25: a combustion chamber; 26: a turbo expander; 27: a waste heat utilization structure; 28: a compressor; 29: sea salt pipeline.
Detailed Description
The following detailed description of embodiments of the present invention is provided in connection with the accompanying drawings and examples. The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention.
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, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; 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 specific cases to those skilled in the art.
As shown in fig. 1, the LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant is schematically shown to comprise an LNG cooling system, a flue gas generation system, a sea brine desalination system and a hydrate generator 9.
In an embodiment of the application, the LNG cooling system is used to provide cooling to the sea brine desalination system and the flue gas generation system, respectively.
The flue gas generation system is used for conveying flue gas generated after the LNG is combusted into the hydrate generator 9.
The sea brine desalination system is used for conveying sea brine into the hydrate generator 9 and mixing flue gas with the sea brine to generate CO2Hydrate, N2And a mixture of salts to obtain fresh water after separating and decomposing the mixture, respectively. Specifically, in the present application, LNG1 is increased in pressure by pressurizing LNG1, through a step ladderThe stage uses the cold energy of LNG1 to cool the flue gas and seawater gradually and provide cold energy for the flue gas and seawater in the process of generating the hydrate to generate CO2Hydrate, N2And the mixture is separated and decomposed respectively by a sea brine desalination system to obtain fresh water, so that the carbon dioxide is sealed, and the cold energy of the decomposed product is utilized, so that the LNG cold energy is efficiently utilized in a cascade manner, the fresh water is produced, and the carbon dioxide is sealed. Therefore, in the invention, the cold energy cascade utilization of LNG, the high-energy consumption desalination process and the flue gas decarburization process are perfectly combined, the LNG cold energy of the gas power plant is efficiently utilized in the same process, carbon dioxide in flue gas generated after LNG is combusted is sealed and stored, and fresh water is co-produced, so that the device with high energy utilization rate and energy environment protection is provided for the gas power plant.
In an embodiment of the present application, the LNG cooling system includes a high-pressure pump 2, an LNG vaporizer 4, a refrigerant pump 8, a first heat exchanger 6, a second heat exchanger, and a third heat exchanger 7.
The sea salt water desalination system comprises a sea water input main pipe 21, a hydrate decomposer 13 and a hydrate separator 10. It should be noted that the structures and operation principles of the hydrate decomposition 13, the hydrate separator 10 and the hydrate generator 9 are well known to those skilled in the art, and are not described in detail herein for the sake of brevity.
The flue gas generation system comprises an air compressor 23, a combustor 25 and a compressor 28 which are connected in sequence, wherein the inlet of the hydrate generator 9 is connected with the outlet of the combustor exhaust line cooled by LNG1, and the outlet of the hydrate generator 9 is connected with the inlet of the hydrate separator 10.
The LNG vaporizer 4 has a first inlet connected to the LNG transfer line 3, a second inlet connected to the refrigerant output line of the hydrate generator 9 via the refrigerant pump 8, a first outlet connected to the first inlet of the first heat exchanger 6, a second outlet connected to the refrigerant input line of the hydrate generator 9, and a third outlet connected to the first inlet of the third heat exchanger 7.
The second inlet of the first heat exchanger 6 is connected with the first outlet of the second heat exchanger, the first outlet is merged with the third outlet of the LNG vaporizer 4 and then connected with the first inlet of the third heat exchanger 7, and the second outlet is connected with the water phase input pipeline of the hydrate generator 9.
The outlet of the second heat exchanger is respectively connected with a hydrate decomposition water output pipeline and CO2The sealed output pipeline is connected, and the inlets of the second heat exchanger are respectively connected with the decomposed water conveying pipeline of the hydrate decomposer 13, the seawater input main pipe 21 and the CO of the hydrate decomposer2The conveying pipelines are communicated.
The second inlet of the third heat exchanger 7 is connected to the exhaust gas pressurized by the compressor 28, the first outlet is connected to the fuel inlet of the combustion chamber 25, and the second outlet is connected to the raw gas input pipeline of the hydrate generator 9.
The application adopts the cold energy in the LNG vaporization process according to local conditions. The LNG fed into the LNG vaporizer 4 transfers the cold energy to the first heat exchanger 6, the second heat exchanger and the third heat exchanger 7 in sequence, so that the cold energy is utilized in a cascade manner, the purpose of efficiently utilizing the cold energy of the LNG is achieved, and the energy utilization rate of the whole gas power plant is greatly improved.
A first inlet of the LNG vaporizer 4 is connected to the LNG transfer line 3, a second inlet of the LNG vaporizer 4 is connected to a refrigerant outlet line 19 of the hydrate generator 9 via a refrigerant pump 8, a first outlet of the LNG vaporizer 4 is connected to a first inlet of the first heat exchanger 6, a second outlet of the LNG vaporizer 4 is connected to a refrigerant inlet line 20 of the hydrate generator 9, and a third outlet of the LNG vaporizer 4 is connected to a first inlet of the third heat exchanger 7. The second inlet of the first heat exchanger 6 is connected with the first outlet of the second heat exchanger, the first outlet of the first heat exchanger 6 is merged with the third outlet of the LNG vaporizer 4 and then connected with the first inlet of the third heat exchanger 7, and the second outlet of the first heat exchanger 6 is connected with the seawater input pipeline 17 of the hydrate generator 9.
In a preferred embodiment of the present application, as shown in fig. 1, there are two second heat exchangers, one is a second heat exchanger 16-1, the other is a second heat exchanger 16-2, the second outlet of the second heat exchanger 16-1 is connected to the hydrate splitting water output pipeline, the first inlet of the second heat exchanger 16-1 is connected to the seawater input manifold 21, and the second inlet of the second heat exchanger 16-1 is connected to the outlet of the split fresh water conveying pipeline 15 of the hydrate splitter 13.
A second outlet of the second heat exchanger 16-2 and CO2The first inlet of the second heat exchanger 16-2 is connected with the seawater input manifold 21, the second inlet of the second heat exchanger 16-2 is connected with the CO of the hydrate decomposer 132The conveying pipelines are connected.
The second inlet of the third heat exchanger 7 is connected to the exhaust gas pressurized by the compressor 28, the first outlet of the third heat exchanger 7 is connected to the fuel inlet of the combustion chamber 25, and the second outlet of the third heat exchanger 7 is connected to the raw gas input pipeline 18 of the hydrate generator 9.
Specifically, the LNG1 is pressurized by the high-pressure pump 2, and then sent to the LNG vaporizer 4 through the LNG transfer pipe 3 to vaporize and release heat, the released heat is absorbed by the refrigerant and then input to the hydrate generator 9 through the refrigerant input pipe 20, and the cold released by the refrigerant is absorbed by the hydrate generator 9 and then output to the LNG vaporizer 4 through the refrigerant output pipe 19.
A portion of the LNG1 after vaporization is input via a natural gas export line 5 into a first heat exchanger 6 for cooling the seawater input via a seawater input line 17 into a hydrate generator 9. The other part of the vaporized natural gas is mixed with the natural gas passing through the first heat exchanger 6 and then is input into the third heat exchanger 7 together for cooling the pressurized feed gas.
The "raw gas" refers to CO generated by burning natural gas in the combustion chamber 252、N2And water vapor.
On the basis of the above embodiment, with reference to fig. 1, a first inlet of the hydrate generator 9 is connected to a refrigerant input pipeline 20 of the hydrate generator 9, a second inlet of the hydrate generator 9 is connected to a seawater input pipeline 17 cooled by the first heat exchanger 6, a third inlet of the hydrate generator 9 is connected to a raw material gas input pipeline 18 of the hydrate generator 9 subjected to heat exchange by the third heat exchanger 7, a first outlet of the hydrate generator 9 is connected to a refrigerant output pipeline 19 of the hydrate generator 9, and a second outlet of the hydrate generator 9 is connected to a hydrate conveying pipeline.
The first inlet of the hydrate separator 10 is connected with a hydrate conveying pipeline, and the first outlet of the hydrate separator 10 is connected with CO2The hydrate conveying pipeline 11 is connected, the second outlet of the hydrate separator 10 is connected with the sea salt conveying pipeline 29, and the third outlet of the hydrate separator 10 is connected with the N2The delivery pipes 12 are connected.
The inlet of the hydrate decomposer 13 and CO2The hydrate conveying pipeline 11 is connected, the first outlet is connected with the decomposed fresh water conveying pipeline 15 of the hydrate decomposer 13, and the second outlet of the hydrate decomposer 13 is connected with the decomposed CO of the hydrate decomposer 132The delivery pipes 14 are connected.
Specifically, after seawater is respectively sent into a second heat exchanger 16-1 and a second heat exchanger 16-2 through a seawater input header pipe 21, the seawater is subjected to secondary refrigeration under the action of the second heat exchanger 16-1 and the second heat exchanger 16-2, the cooled seawater is sent into a first heat exchanger 6 to be continuously cooled, namely, the seawater is subjected to tertiary refrigeration under the action of the first heat exchanger 6, the seawater subjected to tertiary refrigeration is sent into a hydrate generator 9 through a seawater input pipeline 17, a feed gas is sent into the hydrate generator 9 after being cooled by a third heat exchanger 7, corresponding components in the feed gas react with water in the seawater in the hydrate generator 9 to generate hydrate, gas and salt, and then the hydrate, gas and salt are sent into a hydrate separator 10 to be separated, and the hydrate separator 10 separates the feed into gas, solid and solution phases, gas phase is passed through N2Transporting the solid phase out through sea salt transporting pipeline 29 and transporting the hydrate slurry phase out through CO through transporting pipeline 122The hydrate conveying pipeline 11 is conveyed to a hydrate decomposer 13 after being conveyed outside, the hydrate decomposer 13 decomposes the hydrate into gas and water, and the gas is decomposed into CO2The transport pipe 14 is directed out into a second heat exchanger 16-2 for cooling the seawater.
The decomposed water phase is transported to a second heat exchanger 16-1 through a fresh water transport pipeline 15 so as to cool the seawater.
Based on the above embodiment, and with reference to fig. 1, in a preferred embodiment, the combustor 25 may be a gas turbine, and the inlet of the combustor is connected to a supply of LNG1 through a transfer line of LNG1, a transfer line of LNG 3, and a natural gas export line 5, respectively.
The inlet of the combustion chamber 25 is also connected to the outlet of the air compressor 23, and the outlet of the combustion chamber 25 is connected to the inlet of the turboexpander 26.
The combustion chamber 25 is used for burning natural gas to generate high-temperature flue gas, so that the turbo expander 26 generates electricity by using the high-temperature flue gas.
An inlet of the air compressor 23 is connected to the air inlet conduit 22, and an outlet of the air compressor 23 is connected to a first inlet of the air heat exchanger 24.
The second inlet of the air heat exchanger 24 is connected with the N of the hydrate separator 102The outlet of the transfer duct 12 is connected, a first outlet of the air heat exchanger 24 is connected to the air intake of the combustion chamber 25, and a second outlet of the air heat exchanger 24 is connected to the atmosphere.
In a preferred embodiment, the device further comprises a waste heat utilization structure 27. The waste heat utilization structure 27 may include a waste heat boiler and waste heat utilization.
The inlet of the waste heat utilization structure 27 is connected to the outlet of the turbo expander 26, and the outlet of the waste heat utilization structure 27 is connected to the compressor 28.
In another preferred embodiment, the apparatus further comprises a steam turbine (not shown). The outlet of the waste heat boiler device can be connected with a steam turbine. Accordingly, the outlet of the steam turbine is connected to the inlet of the waste heat utilization, which may be connected to a heating system (not shown) to provide heat to the heating system.
Specifically, after being sent into an air compressor 23 through an air inlet pipeline 22 to be pressurized, the air is sent into an air heat exchanger 24, after being cooled, the air is sent into a combustion chamber 25, natural gas is also sent into the combustion chamber 25 after being heated by a third heat exchanger 7, after being combusted in the combustion chamber 25, the natural gas and the air are sent into a waste heat utilization structure 27 to be utilized by waste heat after being generated by a turbine expander 26, after being pressurized by a compressor 28, the flue gas is sent into the third heat exchanger 7, after being cooled, the flue gas is sent into a hydrate generator 9 through a raw material gas input pipeline 18 to be reacted.
In a specific example, LNG1 (liquefied natural gas) was supplied at 3MPa, -159 ℃, the molar composition of LNG1 was as follows: 88.77% of methane, 7.54% of ethane, 2.59% of propane, 0.45% of isobutane, 0.56% of n-butane and 0.08% of nitrogen.
LNG1 is pressurized to 5Mpa and 158 ℃ by a high-pressure pump 2, is sent into an LNG vaporizer 4 through an LNG conveying pipeline 3 to be vaporized and released heat, the temperature of the LNG1 after heat release is increased to-90 ℃, the released heat is absorbed by refrigerant and then is input into a hydrate generator 9 through a refrigerant input pipeline 20, and the cold energy released by the refrigerant is absorbed by the hydrate generator 9, so that the temperature of the hydrate generator 9 can be kept at about 1 ℃.
Part of the vaporized LNG1 is input to the first heat exchanger 6 through the natural gas output line 5 to cool the seawater input to the hydrate generator 9 through the seawater input line 17, at which time the temperature of the part of LNG1 is raised to-60 ℃, and the other part of the vaporized LNG1 is mixed with the natural gas passing through the first heat exchanger 6 and input to the third heat exchanger 7 to cool the pressurized feed gas, at which time the temperature of the part of the vaporized LNG1 is raised to 15 ℃.
Seawater is respectively sent into a second heat exchanger 16-1 and a second heat exchanger 16-2 through a seawater input header pipe 21 and then is cooled, the seawater cooled to 10 ℃ is sent into a first heat exchanger 6 to be continuously cooled, the seawater cooled to 1 ℃ is sent into a hydrate generator 9 through a seawater input pipe 17, a feed gas is sent into the hydrate generator 9 after being cooled to 1 ℃ through a third heat exchanger 7, an accelerant is generally adopted in the hydrate generation process, the accelerant is preferably an environment-friendly accelerant, and the corresponding component CO in the feed gas2Reacts with water in the seawater in the hydrate generator 9 to generate CO2Hydrate, N2After being mixed with salt, can be coveredIs fed into a hydrate separator 10, which hydrate separator 10 separates the feed into a gas N2Solid salt and solution phase CO2Hydrate slurry, gas phase through N2Transporting the solid phase out through sea salt transporting pipeline 29, transporting the hydrate slurry phase out through hydrate transporting pipeline 13, decomposing the hydrate into CO at 7 deg.C by external heat source (such as sea water) in hydrate decomposer 132And water, decomposed CO2The seawater is transported out to a second heat exchanger 16-2 to cool the seawater, and the temperature of the seawater is reduced to 13 ℃.
The water phase is transported into a second heat exchanger 16-1 through the decomposed fresh water transport pipeline 15 to cool the seawater, and the temperature of the seawater is reduced to 13 ℃. Air is fed into an air compressor 23 through the air inlet pipeline 22 to be pressurized, then is fed into an air heat exchanger 24, is cooled and then is fed into a combustion chamber 25, natural gas is heated by a third heat exchanger 7 and then is fed into the combustion chamber 25, the natural gas and the air are combusted in the combustion chamber 25 to generate 1500 ℃ feed gas, and the feed gas consists of CO2And N2And the water vapor is sent into the waste heat utilization structure 27 for waste heat utilization after being generated by the turbine expansion machine 26, the temperature of the water vapor is reduced to 40 ℃, the utilized flue gas is pressurized to 1.5Mpa by the compressor 28, then sent into the third heat exchanger 7 for cooling to 1 ℃, and then sent into the hydrate generator 9 for reaction by the feed gas input pipeline 18.
In summary, in the present application, the LNG1 is pressurized to increase the pressure by pressurizing the LNG1, the flue gas and the seawater are gradually cooled by using the cold energy of the LNG1 in a stepwise manner, and the cold energy is provided to the flue gas and the seawater during the hydrate generation process to generate CO2Hydrate, N2And the mixture of the salt and the LNG1 is separated and decomposed by a sea brine desalination system respectively to obtain fresh water, so that the carbon dioxide is sealed, and the cold energy of the decomposed product is utilized, thereby realizing the cascade efficient utilization of the cold energy of the LNG1, the parallel production of the fresh water and the sealing of the carbon dioxide. It can be seen that in the present invention, the cold energy cascade utilization of LNG1 is associated with high energy consumptionThe desalination process and the flue gas decarbonization process are perfectly combined, the LNG1 cold energy of the gas power plant is efficiently utilized in the same process, carbon dioxide in flue gas generated after LNG1 is combusted is sealed and stored, and fresh water is co-produced, so that the device with high energy utilization rate and energy environmental protection is provided for the gas power plant.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (15)
1. The utility model provides a LNG cold energy utilizes coproduction fresh water and carbon dioxide to seal up and deposits device, includes LNG cooling system, its characterized in that still includes:
the system comprises a flue gas generation system, a sea salt water desalination system and a hydrate generator, wherein the LNG cooling system is respectively used for providing cold energy for the sea salt water desalination system and the flue gas generation system;
the flue gas generation system is used for conveying flue gas generated after LNG is combusted into the hydrate generator;
the sea salt water desalination system is used for conveying sea salt water into the hydrate generator and mixing flue gas with the sea salt water to generate CO2Hydrate, N2And a mixture of salts to obtain fresh water after separation and decomposition of the mixture, respectively.
2. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant of claim 1, wherein said LNG cooling system comprises a high pressure pump, an LNG vaporizer, a refrigerant pump, a first heat exchanger, a second heat exchanger, and a third heat exchanger;
the sea salt water desalination system comprises a sea water input main pipe, a hydrate decomposer and a hydrate separator;
the flue gas generating system comprises an air compressor, a combustion chamber and a compressor which are sequentially connected, wherein an inlet of the hydrate generator is connected with an outlet of a combustion chamber exhaust pipeline cooled by LNG, and an outlet of the hydrate generator is connected with an inlet of a hydrate separator.
3. The LNG cold energy utilization and fresh water and carbon dioxide cogeneration device according to claim 2, wherein the first inlet of the LNG vaporizer is connected to an LNG transfer pipeline, the second inlet of the LNG vaporizer is connected to the refrigerant output pipeline of the hydrate generator through a refrigerant pump, the first outlet of the LNG vaporizer is connected to the first inlet of the first heat exchanger, the second outlet of the LNG vaporizer is connected to the refrigerant input pipeline of the hydrate generator, and the third outlet of the LNG vaporizer is connected to the first inlet of the third heat exchanger.
4. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant of claim 3, characterized in that the second inlet of the first heat exchanger is connected with the first outlet of the second heat exchanger, the first outlet of the first heat exchanger is connected with the first inlet of the third heat exchanger after being merged with the third outlet of the LNG vaporizer, and the second outlet of the first heat exchanger is connected with the water phase input pipeline of the hydrate generator.
5. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant of claim 4, characterized in that the outlet of the second heat exchanger is connected with the hydrate decomposition water export pipeline and the CO export pipeline, respectively2The sealed output pipeline is connected, and the inlet of the second heat exchanger is respectively connected with the decomposed water conveying pipeline of the hydrate decomposer, the seawater input main pipe and the CO of the hydrate decomposer2The conveying pipelines are communicated.
6. An LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant as claimed in claim 5, characterized in that the second inlet of said third heat exchanger is connected to the exhaust gas pressurized by the compressor, the first outlet of said third heat exchanger is connected to the fuel inlet of the combustor, and the second outlet of said third heat exchanger is connected to the raw gas input pipeline of the hydrate generator.
7. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant according to claim 5, characterized in that the number of said second heat exchangers is two, wherein the second outlet of one of the second heat exchangers is connected to the hydrate decomposition water export pipeline, the first inlet is connected to the seawater pipeline, and the second inlet is connected to the outlet of the hydrate decomposition water delivery pipeline;
a second outlet of the other second heat exchanger and CO2The first inlet is connected with the seawater input main pipe, and the second inlet is connected with CO of the hydrate decomposer2The conveying pipelines are connected.
8. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant of claim 2, wherein the inlet of said combustor is connected to an LNG supply via an LNG transfer conduit;
the inlet of the combustion chamber is also connected with the outlet of the air compressor, and the outlet of the combustion chamber is connected with the inlet of the turboexpander.
9. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant of claim 8, wherein the flue gas generation system further comprises the turboexpander, an inlet of the turboexpander is connected with an outlet of a combustion chamber, an outlet of the turboexpander is connected with an inlet of the compressor, and the turboexpander is used for generating power from high temperature flue gas generated after natural gas is combusted in the combustion chamber.
10. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant of claim 2, wherein said flue gas generation system further comprises an air heat exchanger, an inlet of said air compressor is connected to an air delivery conduit, and an outlet of said air compressor is connected to a first inlet of said air heat exchanger; and a second inlet of the air heat exchanger is connected with an outlet of a gas phase conveying pipeline of the hydrate separator, a first outlet of the air heat exchanger is connected with an air inlet of the combustion chamber, and a second outlet of the air heat exchanger is connected with the atmosphere.
11. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant of claim 9, characterized in that said plant further comprises a waste heat utilization structure; and the inlet of the waste heat utilization structure is connected with the outlet of the turboexpander, and the outlet of the waste heat utilization structure is connected with the compressor.
12. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant of claim 11, characterized in that said plant further comprises a steam turbine; the waste heat utilization structure comprises a waste heat boiler, and an outlet of the waste heat boiler is connected with the steam turbine.
13. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration device according to claim 2, wherein the first inlet of the hydrate generator is connected to a refrigerant input pipeline of the hydrate generator, the second inlet is connected to a seawater input pipeline refrigerated by the first heat exchanger, the third inlet is connected to a raw material gas input pipeline of the hydrate generator heat-exchanged by the third heat exchanger, the first outlet is connected to a refrigerant output pipeline of the hydrate generator, and the second outlet is connected to a hydrate delivery pipeline.
14. The LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant of claim 2, wherein the hydrate separator inlet is connected to the hydrate generator second outlet via a hydrate transfer conduit, and the first outlet is connected to the CO generator2The hydrate conveying pipeline is connected, the second outlet is connected with the sea salt conveying pipeline, and the third outlet is connected with the nitrogen conveying pipeline.
15. An LNG cold energy utilization cogeneration fresh water and carbon dioxide sequestration plant as claimed in claim 2Characterized in that the inlet of the hydrate decomposer is connected with CO2The hydrate conveying pipeline is connected, the first outlet is connected with the decomposed water conveying pipeline of the hydrate decomposer, and the second outlet is connected with CO of the hydrate decomposer2The conveying pipelines are connected.
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