KR20180046751A - Boil-Off Gas Re-liquefaction System and Method - Google Patents
Boil-Off Gas Re-liquefaction System and Method Download PDFInfo
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- KR20180046751A KR20180046751A KR1020160142312A KR20160142312A KR20180046751A KR 20180046751 A KR20180046751 A KR 20180046751A KR 1020160142312 A KR1020160142312 A KR 1020160142312A KR 20160142312 A KR20160142312 A KR 20160142312A KR 20180046751 A KR20180046751 A KR 20180046751A
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- Prior art keywords
- gas
- heat exchanger
- storage tank
- liquefied
- evaporated
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- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000001704 evaporation Methods 0.000 claims abstract description 75
- 230000008020 evaporation Effects 0.000 claims abstract description 72
- 238000007906 compression Methods 0.000 claims abstract description 44
- 230000006835 compression Effects 0.000 claims abstract description 44
- 238000004781 supercooling Methods 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims description 25
- 239000003507 refrigerant Substances 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 16
- 239000013505 freshwater Substances 0.000 claims description 6
- 239000013535 sea water Substances 0.000 claims description 6
- 230000005611 electricity Effects 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 200
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 22
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 17
- 239000003915 liquefied petroleum gas Substances 0.000 description 17
- 239000012530 fluid Substances 0.000 description 13
- 239000001294 propane Substances 0.000 description 11
- 239000003949 liquefied natural gas Substances 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 5
- 239000005977 Ethylene Substances 0.000 description 5
- 238000005057 refrigeration Methods 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 239000001273 butane Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 4
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 4
- 238000005259 measurement Methods 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- 239000000969 carrier Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000003209 petroleum derivative Substances 0.000 description 2
- 230000000704 physical effect Effects 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- MWRWFPQBGSZWNV-UHFFFAOYSA-N Dinitrosopentamethylenetetramine Chemical compound C1N2CN(N=O)CN1CN(N=O)C2 MWRWFPQBGSZWNV-UHFFFAOYSA-N 0.000 description 1
- 229940112112 capex Drugs 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- FEBLZLNTKCEFIT-VSXGLTOVSA-N fluocinolone acetonide Chemical compound C1([C@@H](F)C2)=CC(=O)C=C[C@]1(C)[C@]1(F)[C@@H]2[C@@H]2C[C@H]3OC(C)(C)O[C@@]3(C(=O)CO)[C@@]2(C)C[C@@H]1O FEBLZLNTKCEFIT-VSXGLTOVSA-N 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 239000013526 supercooled liquid Substances 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
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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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
- F25J1/0025—Boil-off gases "BOG" from storages
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B25/00—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby
- B63B25/02—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods
- B63B25/08—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid
- B63B25/12—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed
- B63B25/16—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed heat-insulated
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C13/00—Details of vessels or of the filling or discharging of vessels
- F17C13/004—Details of vessels or of the filling or discharging of vessels for large storage vessels not under pressure
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C6/00—Methods and apparatus for filling vessels not under pressure with liquefied or solidified gases
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
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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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
- F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
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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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
- F25J1/0277—Offshore use, e.g. during shipping
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
- F17C2227/01—Propulsion of the fluid
- F17C2227/0128—Propulsion of the fluid with pumps or compressors
- F17C2227/0171—Arrangement
- F17C2227/0185—Arrangement comprising several pumps or compressors
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
- F17C2227/03—Heat exchange with the fluid
- F17C2227/0302—Heat exchange with the fluid by heating
- F17C2227/0306—Heat exchange with the fluid by heating using the same fluid
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
- F17C2227/03—Heat exchange with the fluid
- F17C2227/0302—Heat exchange with the fluid by heating
- F17C2227/0309—Heat exchange with the fluid by heating using another fluid
- F17C2227/0316—Water heating
- F17C2227/0318—Water heating using seawater
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/03—Treating the boil-off
- F17C2265/032—Treating the boil-off by recovery
- F17C2265/033—Treating the boil-off by recovery with cooling
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/03—Treating the boil-off
- F17C2265/032—Treating the boil-off by recovery
- F17C2265/037—Treating the boil-off by recovery with pressurising
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/03—Treating the boil-off
- F17C2265/032—Treating the boil-off by recovery
- F17C2265/038—Treating the boil-off by recovery with expanding
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2270/00—Applications
- F17C2270/01—Applications for fluid transport or storage
- F17C2270/0102—Applications for fluid transport or storage on or in the water
- F17C2270/0105—Ships
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/62—Ethane or ethylene
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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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
Abstract
Description
The present invention relates to a system and a method for re-liquefying an evaporation gas, and more particularly, to a re-liquefaction system and method for re-liquefying an evaporation gas in a low temperature liquefied gas carrier.
Natural gas is usually liquefied and transported over a long distance in the form of Liquefied Natural Gas (LNG). Liquefied natural gas is obtained by cooling natural gas at a cryogenic temperature of about -163 ° C at normal pressure. It is very suitable for long distance transportation through the sea because its volume is greatly reduced as compared with the gas state.
Liquefied petroleum gas (LPG) is generally referred to as Liquefied Propane Gas (LPG), and is a natural gas which is cooled at -200 ° C. and discharged at about room temperature And is compressed and liquefied at 7 to 10 atmospheres.
Propane, propylene, butane, butylene and the like are main components of the petroleum gas. When the propane is liquefied at about 15 ° C under a pressure of 7 to 10 atm, the volume is reduced to about 1/260. When the butane is liquefied at about 15 ° C, / 230. Therefore, for convenience of storage and transport, petroleum gas is also used as liquefied natural gas.
Liquefied natural gas, liquefied petroleum gas and other liquefied gases are stored in storage tanks and supplied to the demand of land. Even if the storage tanks are insulated, there is a limit to completely shut off the external heat. The liquefied gas is continuously vaporized in the storage tank. The liquefied gas vaporized inside the storage tank is referred to as boil-off gas (BOG).
When the pressure of the storage tank becomes higher than the set pressure due to the generation of the evaporation gas, the evaporated gas is discharged to the outside of the storage tank and used as the fuel of the ship or is re-liquefied and returned to the storage tank. A re-liquefaction system for re-liquefying the evaporated gas generated from the gaseous cargo and returning it to the storage tank is provided.
Liquefied gas (LPGC) is mainly composed of propane and the like, and since liquefied petroleum gas contains a large amount of components having relatively high molecular weight as compared with liquefied natural gas, liquefied petroleum gas Gasification is easier than liquefied natural gas. The liquefied petroleum gas carrier carries liquefied gas cargo with a liquefaction temperature of about -30 ° C or higher under 1 atmospheric pressure, and the liquefied petroleum gas carrier carries the liquefied petroleum gas carrier liquefied gas, System is provided.
On the other hand, the liquefied gas cargo carried as a cargo on a Liquefied Ethane Gas Carrier (LEGC) has a liquefying temperature lower than that of the liquefied gas cargo loaded on the liquefied petroleum gas carrier. Thus, (Hereinafter referred to as " ethane evaporation gas ") containing ethylene as a main component, the ethane evaporation gas must be cooled to approximately -100 [deg.] C or lower, It is necessary to further cool down the heat of the liquefied petroleum gas evaporating gas.
Therefore, a separate independent cold / hot supply cycle for supplying additional cold heat is added to the liquefied petroleum gas re-liquefaction process and used as the ethane re-liquefaction process. Generally, a propane refrigeration cycle is used as the heat and cold supply cycle.
On the other hand, in the liquefied petroleum gas carrier, after the evaporation gas generated in the liquefied gas storage tank is compressed, the refrigerant is heat-exchanged with the seawater to cool it, and a part of the compressed evaporated gas is expanded to be used as a refrigerant of the uncompressed compressed evaporative gas A method of re-liquefying the evaporation gas has also been proposed. However, in the case of the ethane-evaporated gas having a low boiling point, the evaporation gas re-liquefaction system of the liquefied petroleum gas carrier is not evaporated unless a separate independent cold / Gas was not re-injected.
However, if an additional independent cold / hot supply cycle is added to re-liquefy the evaporative gas, especially the ethane vapor, which is low in boiling point, which is generated in a liquefied gas storage tank having a low temperature liquefaction point, such as liquefied ethane gas, There is a problem that the space for installing the necessary devices, the installation cost (CAPEX), and the operating cost (OPEX) such as energy consumption become very large.
SUMMARY OF THE INVENTION Accordingly, it is an object of the present invention to provide an evaporative gas re-liquefaction system capable of re-liquefying evaporative gas generated in a liquefied gas having a low boiling point without adding a separate independent cold / And a method therefor.
According to an aspect of the present invention, there is provided a system for re-liquefying an evaporated gas generated in a liquefied gas storage tank, the system comprising: a first heat exchanger for recovering the cold heat of the evaporated gas generated in the liquefied gas storage tank; And a second heat exchanger; A multi-stage compression unit for compressing the heated evaporative gas passing through at least one of the first heat exchanger and the second heat exchanger; And an intermediate cooler for supercooling the evaporated gas compressed by the multi-stage compressing unit, wherein the second heat exchanger is provided in parallel with the first heat exchanger, or is provided in series in the front end or the rear end of the first heat exchanger, A gas remelting system is provided.
Preferably, in the first heat exchanger, the evaporated gas compressed in the multi-stage compression section and the evaporated gas generated in the liquefied gas storage tank undergo heat exchange, and in the second heat exchanger, , Fresh water or electricity.
Advantageously, said second heat exchanger can not operate said first heat exchanger or can operate upon an initial start-up of said remanufacturing system.
Preferably, the apparatus further includes third expansion means for expanding the evaporated gas which has passed through the intermediate cooler and is subcooled, so that evaporated gas in the liquid state expanded in the third expansion means can be recovered to the liquefied gas storage tank .
Preferably, the expansion device further includes expansion means for branching and expanding at least a part of the evaporation gas supplied to the intercooler, wherein in the intercooler, the expanded evaporation gas is used as a refrigerant and the evaporation gas to be expanded and the evaporation The gas can be branched and the remaining evaporation gas can be heat-exchanged.
Preferably, the evaporation gas is a low temperature evaporation gas having a liquefaction temperature of 1 atm to -110 deg. C or higher, and the multi-stage compression section may not be provided for low temperature.
According to another aspect of the present invention, there is provided a refrigeration apparatus for recovering cold heat of an evaporated gas generated in a liquefied gas storage tank, multi-stage compressing the evaporated gas, cooling the compressed evaporated gas, The cold heat of the evaporated gas generated in the gas storage tank is recovered by cooling the compressed evaporated gas in the first heat exchanger and the seawater, fresh water or electric energy is recovered in the second heat exchanger when the compressed evaporated gas can not be supplied There is provided a method of re-liquefying an evaporation gas.
Preferably, the evaporation gas produced in the liquefied gas storage tank may have a liquefaction temperature of 1 atm to -110 < 0 > C or higher.
Preferably, at least a part of the cooled evaporated gas is branched and expanded by using the evaporated gas as a refrigerant, the remaining evaporated gas is subcooled, and the re-liquefied evaporated gas can be recovered to the storage tank.
Preferably, the pressure of the multi-stage compressed evaporated gas is controlled using a flash gas generated from the supercooled evaporated gas, and at least a part of the evaporated gas in the liquid state separated from the flash gas is branched to expand the evaporated gas As the refrigerant, the remaining vaporized gas can be subcooled and recovered to the storage tank.
According to the evaporation gas re-liquefaction system and method of the present invention, there is no need to provide a separate independent cold / heat supply cycle, so that the installation cost can be reduced and the evaporation gas such as ethane is re-liquefied by self- The re-liquefaction efficiency equivalent to that of the conventional re-liquefying device can be achieved without a supply cycle.
In addition, since there is no need to install a cold / hot supply cycle, the number of equipment to be installed can be reduced, and in particular, the compressor for the cold / hot supply cycle can be eliminated.
Further, the total liquefied flow rate can be increased by supercooling the condensed vaporized gas.
In addition, since the amount of expansion of the evaporation gas to be supplied to the refrigerant can be optimized, the flow rate of the evaporation gas supplied to the multi-stage compression section can be reduced and the power and power of the multi-stage compression section can be reduced.
Further, since a receiver can be provided to control the pressure at the downstream end of the multi-stage compressor, an optimum performance coefficient (COP) can be achieved, and a re-liquefying device with improved refrigeration effect can be constructed.
Further, it is not necessary to provide a compressor for compressing the evaporation gas as an expensive cryogenic compressor. Even if the first heat exchanger can not be operated due to a failure of the first heat exchanger or the like, I can drive.
FIG. 1 is a schematic view illustrating a vaporization gas remelting system according to an embodiment of the present invention. Referring to FIG.
In order to fully understand the operational advantages of the present invention and the objects attained by the practice of the present invention, reference should be made to the accompanying drawings, which illustrate preferred embodiments of the present invention, and to the contents of the accompanying drawings.
Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. In the drawings, like reference numerals refer to like elements throughout. The same elements are denoted by the same reference numerals even though they are shown in different drawings.
The evaporation gas re-liquefaction system and method of the present invention can be applied to a variety of applications on ships equipped with liquefied gas hold windows and onshore. Especially ships such as FPSO, FSRU, including ships such as all types of ships and offshore structures, ie liquefied gas carriers, Liquefied Ethane Gas (LEG) carriers, with storage tanks capable of storing low temperature liquid cargo or liquefied gas It can be applied to marine structures.
In the description of the present invention, the term " flow " means a fluid flowing along a line, that is, an evaporation gas. In each line, a fluid may be in a liquid state, a gas-liquid mixed state, State, or the like.
The liquefied gas stored in the
In addition, the following examples can be modified in various forms, and the scope of the present invention is not limited to the following examples.
Hereinafter, the re-liquefaction of the evaporated gas in the liquefied ethane gas carrier will be described as an example. In the following embodiments, the evaporated gas may be a single component or a mixed component including ethane, ethylene, propane or butane.
FIG. 1 is a schematic view illustrating a vaporization gas remelting system according to an embodiment of the present invention. Referring to FIG.
Referring to FIG. 1, the evaporation gas re-liquefaction system of this embodiment is for re-liquefying the evaporation gas generated in the liquefied
In the present embodiment, the evaporated gas generated in the
The
The evaporation gas discharged from the
The
The
The downstream end of the
The refrigerant that cools the evaporated gas in the
In this embodiment, the pressure of the evaporation gas compressed and discharged in the rearmost compressor of the
The
The ethane or ethylene component contained in the evaporation gas may be passed through the
That is, according to the present invention, the evaporation gas compressed in the
Further, the low-temperature evaporation gas, that is, the a-stream discharged from the
For example, after the evaporated gas generated in the
That is, the evaporation gas generated in the
1, a second heat exchanger (not shown) for recovering the cold heat of the evaporated gas supplied from the liquefied
During the initial start-up of the re-liquefaction system, since the evaporated gas, that is, the b-stream compressed by the
Therefore, according to the present embodiment, when the cold heat of the a flow can not be recovered in the
In the second heat exchanger (40), the heat medium recovering cold heat from the a stream may be seawater, fresh water or electricity.
1, the
That is, according to the present embodiment, the
The
According to the present embodiment, a liquid component such as a droplet or a mist, which may be contained in the a flow fed through the
Therefore, according to the present embodiment, only the gas component can be supplied to the
1, the evaporation gas re-liquefaction system according to the present embodiment is configured so that the b-flow in which the refrigerant passes through the
The first flow b1 discharged from the
In this embodiment, the first expansion means 71 for expanding the first flow b1 branched from the b flow, which is cooled and discharged after the heat exchange in the
The first expansion means 71 inflates the first flow b1 branched from the b flow cooled in the
In this embodiment, the first flow b1 is supplied to the first expansion means 71 under the condition of about 40 to 100 bara, about 12 to 45 캜, expanded by 4 to 15 bara by the first expansion means 71, Can be cooled or supercooled by the first
The first flow b1 discharged from the first
According to the present embodiment, a first temperature gauge (not shown) for measuring the temperature of the second flow b2, which is provided on the redistribution line at the rear end of the
The flow rate of the first flow (b1) branching from the flow can be controlled by a control unit (not shown) using the measurement value of the first temperature meter, and the control unit can control the flow rate of the first flow BL of the first flow b2 or to control the first expansion means 71 so as to supercool the second flow b2 in the first
For example, in order to cool the evaporation gas to a lower temperature in the first
Therefore, according to the present invention, the first expansion means (71) is controlled to the temperature of the second flow (b2) that is supercooled and discharged in the first intermediate cooler (41) It is possible to optimize the flow rate and degree of expansion of the
1, the evaporation gas remelting system of the present embodiment includes a second intercooler 42 (also referred to as " second intercooler ") 42 which is provided in the refueling line and further cools the second stream b2 that has passed through the
According to the present embodiment, the second flow b2 having passed through the
A second expansion means 72 for expanding the third flow c1 is provided on the third flow line CL which provides the flow of the third flow c1 branched from the second flow b2, The third stream c1 expanded in the expansion means 72 and lowered in temperature is supplied to the second
The third flow c1 discharged from the second
According to the present embodiment, the third flow c1 is expanded to about 2 to 5 bara in the second expansion means 72, is supplied to the second intermediate cooler 42 while being lowered in temperature by the expansion, And supercooling the fourth flow c2 supplied to the
The third flow c1 discharged from the
However, the third flow c1 discharged from the
Likewise, according to the present embodiment, a second temperature gauge (not shown) for measuring the temperature of the fourth flow c2, which is provided on the liquid refining line at the rear end of the
The flow rate of the third flow c1 branched from the flow of b2 discharged from the
For example, to cool the evaporation gas to a lower temperature in the
The first expansion means 71 and the second expansion means 72 described above may be an expansion valve, a line-Thomson valve or an expander.
1, the fourth flow c2 discharged from the
1, the evaporation gas remelting system of the present embodiment further includes a
The liquid discharged from the
The first
In the present embodiment, the
As described above, the
On the other hand, the efficiency of the cooling system of the fluid is expressed by a coefficient of performance (COP) representing the ratio of the cooling effect to the compression work, and the coefficient of performance is improved as the cooling effect is increased or the compression work is made smaller. The performance coefficient of the re-liquefaction system depends on the pressure of the fluid flowing along the fluid line of the re-liquefaction system, and a pressure range in which the performance coefficient has an optimum value exists. Accordingly, in this embodiment, And the fluid flowing through the line connected from the rear end to the
The
That is, the second flow b2 cooled and discharged in the
Therefore, in this embodiment, the
That is, in this embodiment, the control unit measures the internal pressure of the
The pressure control line PL supplies the fluid discharged from the
For example, when the internal pressure of the
At this time, according to the present embodiment, the pressure set value at the rear end of the compressor may be 40 to 100 bara, and more preferably 80 bara. That is, the internal pressure setting value of the
It is necessary to control the level of the
For example, a control unit (not shown) measures the level of the
According to the present embodiment, since the compressed evaporation gas is further cooled by the
It is possible to constitute a re-liquefaction system together with the
In contrast, when it is assumed that the evaporation gas having the same flow rate and physical condition conditions generated from the same liquefied gas is liquefied, in the case where a separate refrigerant cycle is additionally provided as in the prior art without the
In addition, by making the
Further, when the liquefied gas is propane without requiring an additional refrigerant cycle by the
In addition, if a conventional liquefied petroleum gas carrier was able to load only liquid cargo under the conditions of a liquefaction temperature of -30 ° C and a liquefaction temperature of 1 atm, the liquefied ethane gas carrier to which the evaporation gas re-liquefaction system and method according to the present invention is applied, It is applicable to liquid cargoes having a liquefaction temperature of -110 ° C. or higher, and thus the spectrum of cargo that can be carried can be broadened.
The evaporated gas is cooled at least once by heat exchange through the
It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit and scope of the invention. It is.
10: Liquefied gas storage tank
20: Multistage compression section
21d: Aftercooler
30: first heat exchanger
40: second heat exchanger
41: first intercooler
42: second intercooler
71: first expansion means
72: second expansion means
90: Receiver
PL: pressure control line
Claims (10)
A first heat exchanger for recovering cold and hot of the evaporated gas generated in the liquefied gas storage tank; And a second heat exchanger;
A multi-stage compression unit for compressing the heated evaporative gas passing through at least one of the first heat exchanger and the second heat exchanger; And
And an intermediate cooler for supercooling the evaporated gas compressed by the multi-stage compressing unit,
Wherein the second heat exchanger is provided in parallel with the first heat exchanger or in series at a front end or a rear end of the first heat exchanger.
In the first heat exchanger, the evaporated gas compressed in the multi-stage compression unit and the evaporated gas generated in the liquefied gas storage tank heat-
And the evaporated gas generated in the liquefied gas storage tank is heated by seawater, fresh water or electricity in the second heat exchanger.
Wherein the second heat exchanger is incapable of operating the first heat exchanger or operates upon an initial start-up of the re-liquefaction system.
And third expansion means for expanding the supercooled evaporated gas passing through the intermediate cooler,
And the evaporated gas in the liquid state expanded in the third expansion means is returned to the liquefied gas storage tank.
And expansion means for branching and expanding at least a part of the evaporation gas supplied to the intermediate cooler,
Wherein the intermediate cooler uses the expanded evaporative gas as a refrigerant to divert the expanded evaporative gas and the expanded evaporative gas and heat exchange the remaining remaining evaporative gas.
The evaporation gas is a low temperature evaporation gas having a liquefaction temperature of 1 atm to -110 deg.
Wherein the multi-stage compression section is not provided for low temperature.
The evaporation gas is subjected to multi-stage compression,
Cooling the compressed evaporated gas,
The cold gas of the evaporated gas generated in the liquefied gas storage tank is cooled,
Recovering the compressed evaporated gas by cooling in a first heat exchanger,
And recovering the evaporated gas using seawater, fresh water, or electric energy in the second heat exchanger when the compressed evaporated gas can not be supplied.
Wherein the evaporation gas produced in the liquefied gas storage tank has a liquefaction temperature of greater than or equal to 1 atm.
And evaporating the re-liquefied evaporated gas into the storage tank by supercooling the remaining evaporated gas by using the evaporated gas expanded by branching at least a part of the cooled evaporated gas as a refrigerant.
The pressure of the multi-stage compressed evaporated gas is controlled by using a flash gas generated from the supercooled evaporated gas,
Wherein the flash gas is divided into at least a portion of the evaporated gas in the liquid state, and the expanded gas is expanded into a refrigerant, and the remaining evaporated gas is subcooled and recovered into the storage tank.
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KR20150049748A (en) * | 2013-10-31 | 2015-05-08 | 현대중공업 주식회사 | A Treatment System of Liquefied Gas |
KR20160044101A (en) * | 2014-10-14 | 2016-04-25 | 현대중공업 주식회사 | A Treatment System Of Liquefied Gas |
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KR20150049748A (en) * | 2013-10-31 | 2015-05-08 | 현대중공업 주식회사 | A Treatment System of Liquefied Gas |
KR20160044101A (en) * | 2014-10-14 | 2016-04-25 | 현대중공업 주식회사 | A Treatment System Of Liquefied Gas |
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WO2020204677A1 (en) * | 2019-04-04 | 2020-10-08 | 지에스건설 주식회사 | Evaporation gas compression equipment |
KR20200117518A (en) * | 2019-04-04 | 2020-10-14 | 지에스건설 주식회사 | Boil-off gas compression installation |
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