CN113897229A - Marine LNG gas supply system with carbon capture function - Google Patents
Marine LNG gas supply system with carbon capture function Download PDFInfo
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- CN113897229A CN113897229A CN202111307724.7A CN202111307724A CN113897229A CN 113897229 A CN113897229 A CN 113897229A CN 202111307724 A CN202111307724 A CN 202111307724A CN 113897229 A CN113897229 A CN 113897229A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
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Abstract
The invention discloses a marine LNG (liquefied natural gas) supply system with a carbon capture function, which comprises a flue gas quenching system, a gas quenching system and a quenching water heat exchanger, wherein tail gas of a marine main engine enters from a gas inlet of a quenching tower and is discharged from a gas outlet of the quenching tower; the quenching water heat exchanger is connected between a hot water outlet and a quenching water inlet of the quenching tower, and fluid provided by the quenching water inlet is contacted with the tail gas and discharged from the hot water outlet; and an LNG storage tank in communication with the chilled water heat exchanger, the LNG storage tank removing heat from fluid provided from a hot water outlet of the quench tower to LNG provided by the marine vessel host. The invention can fully utilize a large amount of waste heat in the tail gas to achieve the purposes of energy conservation and emission reduction.
Description
Technical Field
The invention belongs to the technical field of marine LNG supply, and particularly relates to a marine LNG supply system with a carbon capture function.
Background
When a conventional dual fuel ship type uses LNG as fuel, it is usually necessary to provide a FGSS gas supply system. The gas supply system comprises a glycol water system and an LNG gasification system, and the environment is protected by the fact that the tail gas of the main engine contains more carbon dioxide (more than 6%) after combustion, greenhouse gas emission is controlled, and huge pressure is brought.
The existing dual-fuel ship gas supply system does not contain a carbon dioxide recovery system, a large amount of carbon dioxide is discharged, and LNG uses a glycol system to supply heat, so that the purpose of vaporizing LNG is achieved. The existing gas supply system usually comprises two sets of glycol systems, and the glycol solution exchanges heat with the ring to gasify and heat the LNG to the use temperature of the host.
For a container ship with 14000 tanks, about 6000kg of LNG is consumed per hour, while about 17000kg of carbon dioxide emissions are present in the flue gas. If the ship is sailing at sea for one month, carbon dioxide 8500t will be discharged, calculated as LNG fuel usage 70% of the time.
In summary, although the conventional dual-fuel ship type is equipped with a water glycol system, the flue gas emission contains a large amount of carbon dioxide, and a large amount of waste heat is not fully utilized and directly discharged.
Disclosure of Invention
This section is for the purpose of summarizing some aspects of embodiments of the invention and to briefly introduce some preferred embodiments. In this section, as well as in the abstract and the title of the invention of this application, simplifications or omissions may be made to avoid obscuring the purpose of the section, the abstract and the title, and such simplifications or omissions are not intended to limit the scope of the invention.
The present invention has been made keeping in mind the above and/or other problems occurring in the prior art.
The invention aims to provide a marine LNG (liquefied natural gas) supply system with a carbon capture function, which is characterized in that carbon dioxide in combustion tail gas of a marine main engine is removed by using an absorption solvent, the removed carbon dioxide is purified, dried and pressurized, and finally liquefied into liquid carbon dioxide by using cold energy of LNG (liquefied natural gas), and the liquid carbon dioxide enters a storage tank for storage, and the LNG exchanges heat with the purified carbon dioxide to achieve the purpose of gasification.
In order to solve the technical problems, the invention provides the following technical scheme: a marine LNG supply system with a carbon capture function comprises,
the flue gas quenching system comprises a quenching tower and a quenching water heat exchanger, wherein tail gas of the marine main engine enters from a gas inlet of the quenching tower and is discharged from a gas outlet of the quenching tower; the quenching water heat exchanger is connected between a hot water outlet and a quenching water inlet of the quenching tower, and fluid provided by the quenching water inlet is contacted with the tail gas and discharged from the hot water outlet; and the number of the first and second groups,
an LNG storage tank in communication with the chilled water heat exchanger, the LNG storage tank removing heat to LNG provided by the marine vessel host from fluid provided by a hot water outlet of the quench tower.
As a preferable aspect of the marine LNG supply system having a carbon capture function of the present invention, there is provided: and a cooler is connected between the quenching tower and the quenching water heat exchanger.
As a preferable aspect of the marine LNG supply system having a carbon capture function of the present invention, there is provided: also comprises a decarburization system, which comprises,
an absorption tower, wherein a gas inlet of the absorption tower is communicated with a gas outlet of the quenching tower, and the tail gas is contacted with a decarbonized solvent provided by a solvent inlet of the absorption tower and discharged from an outlet of the absorption tower; and the number of the first and second groups,
and the inlet of the separator is communicated with the outlet of the absorption tower, and the separated tail gas is discharged from the discharge outlet of the separator.
As a preferable aspect of the marine LNG supply system having a carbon capture function of the present invention, there is provided: the absorption tower further comprises a re-separator, and the liquid outlet of the absorption tower and the liquid outlet of the separator are both connected with the re-separator.
As a preferable aspect of the marine LNG supply system having a carbon capture function of the present invention, there is provided: also includes a solvent regeneration system, the solvent regeneration system includes,
a regeneration tower, wherein a decarbonization solvent outlet of the regeneration tower is communicated with a solvent inlet of the absorption tower, and an inlet of the regeneration tower is communicated with an outlet of the separator; the stripped carbon dioxide is discharged from a gas outlet of the regeneration tower; and the number of the first and second groups,
a solvent heat exchanger receiving a lean fluid provided from a decarbonized solvent outlet of the regeneration column and a rich fluid provided from a drain of the re-separator, the rich fluid removing heat from the lean fluid.
As a preferable aspect of the marine LNG supply system having a carbon capture function of the present invention, there is provided: the system further comprises a carbon dioxide pretreatment system, the carbon dioxide pretreatment system comprises a pre-compressor and a drying tower which are connected with each other, an inlet of the pre-compressor is connected with a gas outlet of the regeneration tower, and dry carbon dioxide is discharged from a gas outlet of the drying tower.
As a preferable aspect of the marine LNG supply system having a carbon capture function of the present invention, there is provided: the carbon dioxide pretreatment system further includes a pretreatment heat exchanger connected between the pre-compressor and the drying tower, the cooling medium removing heat from carbon dioxide provided by the pre-compressor.
As a preferable aspect of the marine LNG supply system having a carbon capture function of the present invention, there is provided: the drying tower further comprises a carbon dioxide collecting system, wherein the carbon dioxide collecting system comprises a carbon dioxide compressor, a carbon dioxide heat exchanger and a carbon dioxide storage tank, the carbon dioxide compressor is communicated with a gas outlet of the drying tower, and the carbon dioxide compressor is communicated with the carbon dioxide storage tank through the carbon dioxide heat exchanger;
wherein the LNG storage tank is in communication with the chilled water heat exchanger through the carbon dioxide heat exchanger, the LNG storage tank removing heat from the fluid provided at the outlet of the carbon dioxide compressor to the LNG provided at the chilled water heat exchanger.
Compared with the prior art, the invention has the following beneficial effects:
the invention can fully utilize a large amount of waste heat in the tail gas to achieve the purposes of energy conservation and emission reduction.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without inventive exercise. Wherein:
fig. 1 is a schematic structural diagram of embodiment 1 of the present invention.
Fig. 2 is a schematic structural diagram of embodiment 2 of the present invention.
Fig. 3 is a schematic structural diagram of embodiment 3 of the present invention.
Fig. 4 is a schematic structural diagram of embodiment 4 of the present invention.
Fig. 5 is a schematic structural diagram of a carbon dioxide collecting system added to embodiment 4 of the present invention.
Detailed Description
In order to make the aforementioned objects, features and advantages of the present invention more comprehensible, specific embodiments thereof are described in detail below with reference to examples of the specification.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, but the present invention may be practiced in other ways than those specifically described and will be readily apparent to those of ordinary skill in the art without departing from the spirit of the present invention, and therefore the present invention is not limited to the specific embodiments disclosed below.
Furthermore, reference herein to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one implementation of the invention. The appearances of the phrase "in one embodiment" in various places in the specification are not necessarily all referring to the same embodiment, nor are separate or alternative embodiments mutually exclusive of other embodiments.
Example 1
Referring to fig. 1, a first embodiment of the present invention provides a marine LNG gas supply system with a carbon capture function, which includes a flue gas quenching system 100 and an LNG storage tank 200, wherein the LNG storage tank 200 is used to provide LNG to a marine main engine 300, combustion air enters the marine main engine 300 and is used to provide oxygen to the LNG entering the marine main engine 300, and exhaust gas discharged after combustion of the marine main engine 300 is discharged from the marine main engine 300, and the temperature of the exhaust gas is up to 230 ℃; the flue gas quenching system 100 uses quenching water to rapidly cool the high-temperature tail gas discharged by the marine main engine 300;
the flue gas quenching system 100 comprises a quenching tower 101 and a quenching water heat exchanger 102, tail gas discharged by the marine main engine 300 enters the quenching tower 101, contacts with quenching water entering the quenching tower 101 for cooling, and the cooled tail gas is discharged from the quenching tower 101; the quench water used for cooling is collected and sent to the quench tower 101 again by the quench water pump 103 for recycling.
The temperature of the discharged quenching water is 40-50 ℃, the heat of the quenching water can be fully utilized to gasify the LNG discharged from the LNG storage tank 200 into natural gas, and the temperature of the natural gas entering the ship main engine 300 is the temperature required by the main engine. Therefore, a quenching water heat exchanger 102 is provided, quenching water discharged from the quenching tower 101 is used as a heat medium of the quenching water heat exchanger 102, and LNG discharged from the LNG tank 200 is used as a refrigerant of the quenching water heat exchanger 102, and exchanges heat with the quenching water by the LNG to gasify the LNG into natural gas.
Specifically, the quenching tower 101 adopted in this embodiment is a high-efficiency packed tower, and is cooled rapidly by spraying quenching water, and the high-temperature tail gas is cooled to about 40 ℃ by the quenching water, and meanwhile, impurities such as dust can be removed.
The quench water temperature after exchanging heat with the LNG is unstable, therefore, increase cooler 104 between quench water heat exchanger 102 and quench tower 101, the refrigerant is provided by cooling water system 800, with the temperature stable control of quench water at 35 ~ 40 ℃, flow back to in the quench tower 101 again.
The cooling water system 800 includes a cooling water tank 801 and a cooling water pump 802, the cooling water in the cooling water tank 801 is sent to the cooler 104 by the cooling water pump 802, and the cooling water after heat exchange flows back to the cooling water tank 801.
It should be noted that the cooling water mentioned in the following examples is provided by the present cooling water system 800.
Example 2
Referring to fig. 2, this embodiment is different from the first embodiment in that: the overall system also includes a decarbonization system 400; since the cooled off-gas discharged from the quenching tower 101 still contains a large amount of carbon dioxide when it is discharged as it is, the decarbonization system 400 is added to the embodiment 1 in the present embodiment 2.
Specifically, the decarbonization system 400 comprises an absorption tower 401 and a separator 402, wherein the absorption tower 401 is communicated with the quenching tower 101, tail gas enters the absorption tower 401 and contacts with a decarbonization solvent entering the absorption tower 401, carbon dioxide is dissolved in the decarbonization solvent to realize tail gas decarbonization, and the decarbonization solvent adsorbing carbon dioxide is discharged from the absorption tower 401 and collected or directly recycled; the remaining tail gas (mainly nitrogen, combusted oxygen and residual carbon dioxide) enters the separator 402 from the absorber 401, passes through the water separator and is discharged to the atmosphere; the separator 402 used in this embodiment is a vertical gravity separator for separating the water vapor and solvent entrained by the absorber tower, reducing water and solvent losses.
It should be noted that the absorption tower 401 in this embodiment is a structured packing tower, which is filled with structured packing, and the tower plate may be selected according to different working conditions; the decarbonizing solvent includes, but is not limited to, amines such as MEA, DEA, MDEA, etc., and may be pure decarbonizing solvent water solution, or may have piperazine, etc. added into it, and the mixture is reasonably mixed according to the fume treating amount and the required carbon dioxide recovering rate.
The temperature of the tail gas discharged from the absorption tower 401 is about 55 ℃, in order to adapt to the working temperature of the separator 402, a tail gas cooler 403 may be added between the absorption tower 401 and the separator 402, and the cooling medium is provided by cooling water to cool the tail gas to 40 ℃, and then the tail gas enters the separator 402.
In another embodiment, since the decarbonizing solvent discharged from the absorption tower 401 may further contain a part of undissolved carbon dioxide, and a part of decarbonizing solvent may further be contained in the liquid separated by the separator 402, a re-separator 404 is added, the absorption tower 401 and the separator 402 are connected to the re-separator 404 to be separated again, the separated off gas is discharged to the atmosphere from the exhaust port of the re-separator 404, and the separated decarbonizing solvent is collected.
Example 3
Referring to fig. 3, this embodiment differs from the above embodiment in that: the overall system also includes a solvent regeneration system 500; the solvent regeneration system 500 evaporates carbon dioxide in the decarbonization solvent by using a heating and gas stripping mode to recover the absorption capacity of the decarbonization solvent to the carbon dioxide; different decarbonization solvents have different regeneration conditions; the principle is that carbon dioxide is regenerated by heating or decompressing with the absorption capacity of carbon dioxide being low under low pressure and heating state, and the required heat source includes but is not limited to steam, electricity, heat conducting oil, etc.
Specifically, the solvent regeneration system 500 includes a regeneration tower 501 and a solvent heat exchanger 502, the decarbonized solvent adsorbing carbon dioxide discharged from the absorption tower 401 or the re-separator 404 enters the regeneration tower 501 through a solvent pump 503, the desorbed carbon dioxide is discharged from the regeneration tower 501 and collected, and the regenerated decarbonized solvent is circulated into the absorption tower 401.
The temperature of the regenerated decarbonization solvent discharged from the regeneration tower 501 reaches 120 ℃, and the solvent needs to be heated in the regeneration tower 501, so that the heat of the regenerated decarbonization solvent can be fully utilized, the regenerated decarbonization solvent is used as a heating medium of the solvent heat exchanger 502, the decarbonization solvent adsorbing carbon dioxide is used as a cooling medium of the solvent heat exchanger 502, and the decarbonization solvent adsorbing carbon dioxide after heat exchange enters the regeneration tower 501 again, so that the energy consumption can be reduced;
the temperature of the regenerated decarbonization solvent after heat exchange reaches 80 ℃, in order to meet the temperature requirement of the absorption tower 401, a solvent cooler 504 is added between the solvent heat exchanger 502 and the absorption tower 401, the regenerated decarbonization solvent is used as a heating medium of the solvent cooler 504, a cooling medium is provided by cooling water, the regenerated decarbonization solvent is cooled to 50 ℃, and then the cooled decarbonization solvent enters the absorption tower 401.
It should be noted that the heat source of the regeneration tower 501 in this embodiment is provided by low-pressure steam in the ship.
Since the carbon dioxide partially dissolved may remain in the decarbonizing solvent regenerated by the regeneration tower 501, the reboiler 506 is additionally provided, the low-pressure steam in the vessel and the regenerated decarbonizing solvent are respectively introduced into the reboiler 506 to exchange heat, the carbon dioxide dissolved in the solvent is desorbed, and the regenerated decarbonizing solvent is sent to the absorption tower 401 by the regeneration pump 505.
The carbon dioxide removed through the regeneration tower 501 also contains part of water, a condenser 507 is additionally arranged at the gas outlet of the regeneration tower 501, the carbon dioxide is discharged after passing through the condenser 507, and water doped in the carbon dioxide is condensed and flows back into the regeneration tower 501, so that the water loss of the system water is ensured to be small, and the heat balance of the regeneration tower is favorably ensured.
Example 4
Referring to fig. 4 and 5, this embodiment differs from the above-described embodiment in that: the whole system further comprises a carbon dioxide pretreatment system 600, the carbon dioxide pretreatment system 600 comprises a precompressor 601 and a drying tower 602 which are connected with each other, an inlet of the precompressor 601 is connected with a gas outlet of the regeneration tower 501, carbon dioxide discharged from the regeneration tower 501 enters the precompressor, and the carbon dioxide is compressed to 0.8MPa by the precompressor, so that the pressure of the pressurized carbon dioxide is easy to liquefy, the temperature required by liquefaction is increased, and the energy consumption of liquefaction is saved.
The pre-compressed carbon dioxide enters a drying tower 602 to separate most of the water, and finally a molecular sieve is used to remove trace water, so that the aim of drying is to prevent water from generating ice under a low-temperature condition and freezing and blocking liquefaction equipment. The dried carbon dioxide is discharged from the drying tower 602.
A pre-treatment heat exchanger 603 is added between the pre-compressor 601 and the drying tower 602, a refrigerant of the pre-treatment heat exchanger 603 is provided by cooling water, and the cooling water removes heat from carbon dioxide provided by the pre-compressor 601, so that the carbon dioxide enters the drying tower 602 after being cooled.
Further, as shown in fig. 5, the drying tower further comprises a carbon dioxide collecting system 700, the carbon dioxide collecting system 700 comprises a carbon dioxide compressor 701, a carbon dioxide heat exchanger 702 and a carbon dioxide storage tank 703, the carbon dioxide compressor 701 is communicated with the gas outlet of the drying tower 602, and the carbon dioxide compressor 701 is communicated with the carbon dioxide storage tank 703 through the carbon dioxide heat exchanger 702; wherein the LNG storage tank 200 is in communication with the chilled water heat exchanger 102 through a carbon dioxide heat exchanger 702, and the LNG supplied from the LNG storage tank 200 to the chilled water heat exchanger 102 removes heat from the fluid supplied from the outlet of the carbon dioxide compressor 701.
Specifically, the dried carbon dioxide is discharged from the drying tower 602 and then further compressed to 1.8MPa by a carbon dioxide compressor 701, and then exchanges heat with LNG at the temperature of-160 ℃, at this time, the carbon dioxide is liquefied into liquid carbon dioxide, and the liquid carbon dioxide enters a carbon dioxide storage tank for storage;
the LNG after heat exchange is heated to about-150 ℃ and enters the quenching water heat exchanger 102 to exchange heat with the quenching water discharged from the quenching tower 101, so that the LNG is gasified into natural gas, and the temperature of the natural gas entering the marine main engine 300 is 20-25 ℃.
The invention can fully utilize a large amount of waste heat in the tail gas to achieve the purposes of energy conservation and emission reduction.
It should be noted that the above-mentioned embodiments are only for illustrating the technical solutions of the present invention and not for limiting, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions may be made on the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention, which should be covered by the claims of the present invention.
Claims (8)
1. The utility model provides a marine LNG gas supply system with carbon capture function which characterized in that: comprises the steps of (a) preparing a mixture of a plurality of raw materials,
the flue gas quenching system (100) comprises a quenching tower (101) and a quenching water heat exchanger (102), wherein tail gas of the marine main engine (300) enters from a gas inlet of the quenching tower (101) and is discharged from a gas outlet of the quenching tower (101); the quenching water heat exchanger (102) is connected between a hot water outlet and a quenching water inlet of the quenching tower (101), and fluid provided by the quenching water inlet is contacted with the tail gas and discharged from the hot water outlet; and the number of the first and second groups,
an LNG storage tank (200), the LNG storage tank (200) in communication with the chilled water heat exchanger (102), the LNG provided by the LNG storage tank (200) to the marine main unit (300) removing heat from a fluid provided by a hot water outlet of the quench tower (101).
2. The system for supplying LNG to a ship with a carbon capture function according to claim 1, wherein: a cooler (104) is also connected between the quenching tower (101) and the quenching water heat exchanger (102).
3. The marine LNG supply system with a carbon capture function according to claim 1 or 2, wherein: further comprising a decarbonization system (400), the decarbonization system (400) comprising,
an absorption tower (401), wherein a gas inlet of the absorption tower (401) is communicated with a gas outlet of the quenching tower (101), and the tail gas is contacted with a decarbonized solvent provided by a solvent inlet of the absorption tower (401) and discharged from an outlet of the absorption tower (401); and the number of the first and second groups,
a separator (402), wherein the inlet of the separator (402) is communicated with the outlet of the absorption tower (401), and the separated tail gas is discharged from the discharge port of the separator (402).
4. The system for supplying LNG to a ship with a carbon capture function according to claim 3, wherein: the device also comprises a re-separator (404), wherein the liquid outlet of the absorption tower (401) and the liquid outlet of the separator (402) are both connected with the re-separator (404).
5. The system for supplying LNG to a ship with a carbon capture function according to claim 4, wherein: further comprising a solvent regeneration system (500), said solvent regeneration system (500) comprising,
a regeneration tower (501), wherein a decarbonized solvent outlet of the regeneration tower (501) is communicated with a solvent inlet of the absorption tower (401), and an inlet of the regeneration tower (501) is communicated with an outlet of the separator (402); the stripped carbon dioxide is discharged from a gas outlet of the regeneration tower (501); and the number of the first and second groups,
a solvent heat exchanger (502), the solvent heat exchanger (502) receiving a lean fluid provided from a decarbonized solvent outlet of the regeneration column (501) and a rich fluid provided from a drain of the re-separator (404), the rich fluid removing heat from the lean fluid.
6. The marine LNG supply system with carbon capture function according to any one of claims 1, 2, 4, and 5, wherein: the system further comprises a carbon dioxide pretreatment system (600), wherein the carbon dioxide pretreatment system (600) comprises a pre-compressor (601) and a drying tower (602) which are connected with each other, an inlet of the pre-compressor (601) is connected with a gas outlet of the regeneration tower (501), and dried carbon dioxide is discharged from a gas outlet of the drying tower (602).
7. The system for supplying LNG to a ship with a carbon capture function according to claim 6, wherein: the carbon dioxide pre-treatment system (600) further comprises a pre-treatment heat exchanger (603), the pre-treatment heat exchanger (603) being connected between the pre-compressor (601) and the drying tower (602), a cooling medium removing heat from carbon dioxide provided by a pre-compressor (601).
8. The system for supplying LNG with carbon capture function for a ship according to any one of claims 1, 2, 4, 5 and 7, wherein: the system also comprises a carbon dioxide collecting system (700), wherein the carbon dioxide collecting system (700) comprises a carbon dioxide compressor (701), a carbon dioxide heat exchanger (702) and a carbon dioxide storage tank (703), the carbon dioxide compressor (701) is communicated with a gas outlet of the drying tower (602), and the carbon dioxide compressor (701) is communicated with the carbon dioxide storage tank (703) through the carbon dioxide heat exchanger (702);
wherein the LNG storage tank (200) is in communication with the chilled water heat exchanger (102) through the carbon dioxide heat exchanger (702), the LNG provided by the LNG storage tank (200) to the chilled water heat exchanger (102) removing heat from the fluid provided by the outlet of the carbon dioxide compressor (701).
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| CN202111307724.7A CN113897229A (en) | 2021-11-05 | 2021-11-05 | Marine LNG gas supply system with carbon capture function |
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Cited By (1)
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|---|---|---|---|---|
| CN115265095A (en) * | 2022-08-01 | 2022-11-01 | 中国石油大学(华东) | System and process for decarbonizing tail gas by using LNG cold energy based on LNG power ship |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115265095A (en) * | 2022-08-01 | 2022-11-01 | 中国石油大学(华东) | System and process for decarbonizing tail gas by using LNG cold energy based on LNG power ship |
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