WO1999035436A1 - A method of and apparatus for returning a boil-off gas to its liquid phase - Google Patents

A method of and apparatus for returning a boil-off gas to its liquid phase Download PDF

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Publication number
WO1999035436A1
WO1999035436A1 PCT/GB1998/003794 GB9803794W WO9935436A1 WO 1999035436 A1 WO1999035436 A1 WO 1999035436A1 GB 9803794 W GB9803794 W GB 9803794W WO 9935436 A1 WO9935436 A1 WO 9935436A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
vaporised
stream
pressure
liquefied gas
Prior art date
Application number
PCT/GB1998/003794
Other languages
French (fr)
Inventor
Anthony Richard Alderson
Richard Allen Brown
David Alan Hayes
Deborah Julie Brown
Original Assignee
Bg Plc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Bg Plc filed Critical Bg Plc
Publication of WO1999035436A1 publication Critical patent/WO1999035436A1/en

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Classifications

    • 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
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • 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
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • 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
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/033—Small pressure, e.g. for liquefied gas
    • 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
    • F17C2265/02—Mixing fluids
    • F17C2265/022—Mixing fluids identical fluid
    • 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
    • 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

Definitions

  • This invention relates to a method of and apparatus for returning a vapourised gas and particularly a boil off gas to its liquid phase.
  • LNG liquified natural gas
  • Reciprocating compressors are relatively expensive and it is an object of the present invention to provide a method of and apparatus for returning a boil off gas to the liquid phase which is cheaper than using a reciprocating compressor.
  • a method of returning a vaporised gas to its liquid phase comprising forming at least one stream of liquefied gas from a supply of liquefied gas, supplying the vaporised gas at a supply pressure to the or each stream, entraining the vaporised gas in the or each stream so that a mixed stream of liquefied gas and entrained vaporised gas is formed and causing the pressure of the or each mixed stream to increase beyond that of the supply pressure of the vaporised gas so that the entrained vaporised gas returns to its liquid phase.
  • apparatus for returning a vaporised gas to its liquid phase comprising means for forming at least one stream of liquefied gas from a supply of liquefied gas, means for supplying the vaporised gas at a supply pressure to the or each stream, means for entraining the vaporised gas in the or each stream so that a mixed stream or streams of liquefied gas is or are formed and means for causing the pressure of the mixed stream or streams to increase beyond that of the supply pressure of the vaporised gas so that the entrained vaporised gas returns to its liquid phase.
  • an installation is shown at 2 for storing and supplying which in this case is cryogenic liquefied gas.
  • That gas may be liquefied fuel gas, for example liquefied natural gas (LNG).
  • the installation 2 includes a heat insulated storage vessel or storage tank 4 to contain the cryogenic liquefied gas at low temperature eg - 160°C and at a pressure a which may be substantially atmospheric pressure or substantially 1.0 bar.
  • the upper part of the tank 4 provides an internal region 4a in which boil off gas from the liquefied gas in the lower part of the tank can collect.
  • the pressure of the boil off gas in region 4a is b which is equal to pressure a.
  • a liquid jet pump or liquid jet compressor 6 is provided and has a low pressure inlet 8 connected to the region 4a by a pipe 10.
  • the inlet 8 opens into a side of a chamber 12 containing at least one nozzle or jet 14 facing towards a venturi passage 16.
  • An inlet 18 of the jet compressor 6 supplies the jet 14 with liquefied gas at low temperature, the liquefied gas being supplied to the inlet 18 by a pipe 20 receiving the output from a pump 22 which has an inlet 24 in the tank 4.
  • the pump 22 delivers liquefied gas at a pressure c which is greater than pressure a or pressure b.
  • Liquefied fuel gas issuing at low temperature from the jet 14 as a stream entrains therein boil off gas drawn from the region 4a to the chamber 12 via the inlet 8 to form a mixed stream of the liquefied gas and the boil off gas.
  • the entrained boil off gas resumes its liquid phase in the cold liquefied gas which has issued as a stream from the jet 14.
  • the liquefied gas at low temperature is output, from an outlet 26, at a pressure d to a pipe 28 leading to another pump 30 which may be a high pressure pump raising the pressure of the liquefied gas output in output pipe 32 to a pressure e for onward supply.
  • Output pressure d from the jet compressor 6 may be less than the input pressure c, and pressure e output from the pump 30 may be greater than pressure c.
  • the temperature of the boil off gas and that of the liquefied gas pumped through the system from pump inlet 24 to pump outlet pipe 32 may be substantially the same as that of the liquefied gas in the tank 4.
  • the liquefied gas in the tank 4 is LNG its temperature may be substantially -160°C which is also substantially the temperature of the boil off gas.
  • the pressure a and b_of the LNG in the tank 4 may be substantially 1.1 bar.
  • Output pressure c of the pump 22 may be in the range of substantially 3.0 to substantially 7.0 bar, say substantially 7.0 bar, and the temperature of the LNG supplied to the inlet 18 of the jet compressor 16 may, as indicated above, be substantially -160° C.
  • Output pressure d from the jet compressor 16 may be substantially 2.0 bar, and the output pressure e of LNG from the pump 30 may be in the range substantially 70 to substantially 80 bar.
  • each storage vessel may supply liquefied and boil off gas to a single jet or nozzle serving all the vessels via a pump which may also serve all the vessels or each vessel may be provided with its own individual pump for supplying the gases to the single jet or nozzle.
  • each vessel could be provided with its own individual jet or nozzle and its own individual pump for each nozzle.
  • liquefied gas and the boil off gas may be derived from different vessels or sources and indeed the liquefied gas may even be a different gas to the boil off gas though still physically compatible therewith.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

A method of returning boil-off gas from stored cryogenic liquefied gas to its liquid phase and an installation for storing and supplying cryogenic liquefied gas. An installation (2) for the storage and supply of a cryogenic liquified gas, for example liquefiednatural gas, comprises storage tank (4) for the liquefied gas at low temperature having an upper internal region (4a) in which the boil-off gas collects. That boil-off gas is supplied by pipe (10) to an inlet (8) of a liquid jet pump or liquid jet compressor (6). Liquefied gas is conveyed from the tank (4) by pump (22) and pipe (20) to a jet (14) of the jet compressor (6). The boil-off gas is entrained by the cold liquefied gas leaving the jet (14) in a venturi (16) to form a stream, the pressure of which is higher than that of the supply pressure of the vaporised gas so that the gas resumes its liquid phase, and the liquefied gas is raised to high pressure by high pressure pump (30) for onward supply.

Description

A METHOD OF AND APPARATUS FOR RETURNING A BOIL-OFF GAS TO ITS LIQUID PHASE
This invention relates to a method of and apparatus for returning a vapourised gas and particularly a boil off gas to its liquid phase.
In installations for the storage and supply of liquified natural gas (LNG), some of the LNG in a storage tank boils off and collects as boil off gas in the upper part of the tank. A pump extracting LNG from the tank sends the pumped LNG to an absorber. The boil off gas is supplied to a reciprocating compressor which compresses the boil off gas and supplies it at suitable pressure to the absorber to produce an equilibrium mixture of LNG and boil off gas all in the liquid phase.
Reciprocating compressors are relatively expensive and it is an object of the present invention to provide a method of and apparatus for returning a boil off gas to the liquid phase which is cheaper than using a reciprocating compressor.
According to a first aspect of the invention there is provided a method of returning a vaporised gas to its liquid phase, the method comprising forming at least one stream of liquefied gas from a supply of liquefied gas, supplying the vaporised gas at a supply pressure to the or each stream, entraining the vaporised gas in the or each stream so that a mixed stream of liquefied gas and entrained vaporised gas is formed and causing the pressure of the or each mixed stream to increase beyond that of the supply pressure of the vaporised gas so that the entrained vaporised gas returns to its liquid phase. According to a second aspect of the present invention, there is provided apparatus for returning a vaporised gas to its liquid phase, the apparatus comprising means for forming at least one stream of liquefied gas from a supply of liquefied gas, means for supplying the vaporised gas at a supply pressure to the or each stream, means for entraining the vaporised gas in the or each stream so that a mixed stream or streams of liquefied gas is or are formed and means for causing the pressure of the mixed stream or streams to increase beyond that of the supply pressure of the vaporised gas so that the entrained vaporised gas returns to its liquid phase.
Each aspect of the invention will now be further described, by way of example with reference to the accompanying drawing in which an installation formed according to the second aspect of the invention is shown diagrammatically, and partly in section, in which the method according to the first aspect of the invention can be performed.
With reference to the drawing, an installation is shown at 2 for storing and supplying which in this case is cryogenic liquefied gas.
That gas may be liquefied fuel gas, for example liquefied natural gas (LNG). The installation 2 includes a heat insulated storage vessel or storage tank 4 to contain the cryogenic liquefied gas at low temperature eg - 160°C and at a pressure a which may be substantially atmospheric pressure or substantially 1.0 bar. The upper part of the tank 4 provides an internal region 4a in which boil off gas from the liquefied gas in the lower part of the tank can collect. The pressure of the boil off gas in region 4a is b which is equal to pressure a. A liquid jet pump or liquid jet compressor 6 is provided and has a low pressure inlet 8 connected to the region 4a by a pipe 10. The inlet 8 opens into a side of a chamber 12 containing at least one nozzle or jet 14 facing towards a venturi passage 16. An inlet 18 of the jet compressor 6 supplies the jet 14 with liquefied gas at low temperature, the liquefied gas being supplied to the inlet 18 by a pipe 20 receiving the output from a pump 22 which has an inlet 24 in the tank 4. The pump 22 delivers liquefied gas at a pressure c which is greater than pressure a or pressure b. Liquefied fuel gas issuing at low temperature from the jet 14 as a stream entrains therein boil off gas drawn from the region 4a to the chamber 12 via the inlet 8 to form a mixed stream of the liquefied gas and the boil off gas. As a result of passage through the chamber 12 and the venturi passage 16 the entrained boil off gas resumes its liquid phase in the cold liquefied gas which has issued as a stream from the jet 14. Now the liquefied gas at low temperature is output, from an outlet 26, at a pressure d to a pipe 28 leading to another pump 30 which may be a high pressure pump raising the pressure of the liquefied gas output in output pipe 32 to a pressure e for onward supply. Output pressure d from the jet compressor 6 may be less than the input pressure c, and pressure e output from the pump 30 may be greater than pressure c. The temperature of the boil off gas and that of the liquefied gas pumped through the system from pump inlet 24 to pump outlet pipe 32 may be substantially the same as that of the liquefied gas in the tank 4.
If the liquefied gas in the tank 4 is LNG its temperature may be substantially -160°C which is also substantially the temperature of the boil off gas. The pressure a and b_of the LNG in the tank 4 may be substantially 1.1 bar. Output pressure c of the pump 22 may be in the range of substantially 3.0 to substantially 7.0 bar, say substantially 7.0 bar, and the temperature of the LNG supplied to the inlet 18 of the jet compressor 16 may, as indicated above, be substantially -160° C. Output pressure d from the jet compressor 16 may be substantially 2.0 bar, and the output pressure e of LNG from the pump 30 may be in the range substantially 70 to substantially 80 bar.
While not shown it will be appreciated that there may be more than one storage vessel containing liquefied and boil off gas and each storage vessel may supply liquefied and boil off gas to a single jet or nozzle serving all the vessels via a pump which may also serve all the vessels or each vessel may be provided with its own individual pump for supplying the gases to the single jet or nozzle.
Alternatively each vessel could be provided with its own individual jet or nozzle and its own individual pump for each nozzle.
In addition the liquefied gas and the boil off gas may be derived from different vessels or sources and indeed the liquefied gas may even be a different gas to the boil off gas though still physically compatible therewith.

Claims

Claims
1. A method of returning a vaporised gas to its liquid phase, the method comprising forming at least one stream of liquefied gas from a supply of liquefied gas, supplying the vaporised gas at a supply pressure to the or each stream, entraining the vaporised gas in the or each stream so that a mixed stream of liquefied gas and entrained vaporised gas is formed and causing the pressure of the or each mixed stream to increase beyond that of the supply pressure of the vaporised gas so that the entrained vaporised gas returns to its liquid phase.
2. A method as claimed in claim 1 in which the stream or streams of liquefied gas is or are formed by passing the liquefied gas through at least one nozzle or jet.
3. A method as claimed in claim 1 or claim 2 in which the liquefied gas is supplied from at least one storage vessel and the vaporised gas also issues from a region within the same vessel or vessels.
4. A method as claimed in claim 3 in which the liquefied gas from the or each storage vessel is supplied at a first pressure and the vaporised gas in the region of the or each storage vessel is supplied at a second pressure which is lower than the first pressure.
5. A method as claimed in claim 4 in which the liquefied gas stream or streams is or are at a third pressure which is greater than the second pressure.
6. A method as claimed in any of the preceding claims in which the vaporised gas is boil off gas from a liquefied gas.
7. A method as claimed in any of the preceding claims in which the liquefied and vaporised gas is natural gas.
8. Apparatus for returning a vaporised gas to its liquid phase, the apparatus comprising means for forming at least one stream of liquefied gas from a supply of liquefied gas, means for supplying the vaporised gas at a supply pressure to the or each stream, means for entraining the vaporised gas in the or each stream so that a mixed stream or streams of liquefied gas is or are formed and means for causing the pressure of the mixed stream or streams to increase beyond that of the supply pressure of the vaporised gas so that the entrained vaporised gas returns to its liquid phase.
9. Apparatus as claimed in claim 8 in which the means for forming the or each stream of liquefied gas comprises at least one jet or nozzle.
10. Apparatus as claimed in claim 8 or claim 9 in which at least one storage vessel is provided from which the liquefied gas and the vaporised gas is supplied.
11. Apparatus as claimed in any of claims 8 to 10 in which the means for entraining the vaporised gas in the or each stream comprises a chamber for the or each stream, which chamber receives separately a stream of liquefied gas and a supply of vaporised gas to form a mixed stream of the liquefied gas and the vaporised gas.
12. Apparatus as claimed in any of claims 8 to 11 in which the means for causing the pressure of the or each mixed stream to increase beyond that of the supply pressure of the vaporised gas comprises a venturi.
13. A method of returning a vapourised gas to its liquid phase substantially as hereinbefore described with reference to the accompanying drawing.
14. Apparatus for returning a vapourised gas to its liquid phase substantially as hereinbefore described with reference to the accompanying drawing.
PCT/GB1998/003794 1998-01-08 1998-12-22 A method of and apparatus for returning a boil-off gas to its liquid phase WO1999035436A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB9800238.9 1998-01-08
GBGB9800238.9A GB9800238D0 (en) 1998-01-08 1998-01-08 Jet extractor compression

Publications (1)

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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008085348A2 (en) * 2006-12-28 2008-07-17 Kellogg Brown & Root Llc Methods for pressurizing boil off gas
CN103225740A (en) * 2013-04-22 2013-07-31 中国海洋石油总公司 BOG processing system utilizing pressure energy of LNG receiving station
CN103225739A (en) * 2013-04-22 2013-07-31 中国海洋石油总公司 Energy-saving processing system for vapor of LNG receiving station
JP2014159859A (en) * 2013-02-20 2014-09-04 Jfe Engineering Corp Apparatus for re-liquefaction/pressure-rise of boil-off gas of low-temperature liquid gas
JP2015190598A (en) * 2014-03-28 2015-11-02 千代田化工建設株式会社 Vaporized gas re-liquefaction facility and vaporized gas re-liquefaction method
CN105953072A (en) * 2016-06-30 2016-09-21 日照海达尔加气设备有限公司 Gas dispenser for injecting liquefied natural gas while gas is mixed in
CN106288478A (en) * 2016-09-28 2017-01-04 中国海洋石油总公司 A kind of injector for normal-temperature natural-gas injection LNG cold boil-off gas
CN109578806A (en) * 2018-12-07 2019-04-05 江苏中圣压力容器装备制造有限公司 A kind of process unit of LNG flash steam (BOG) pressurization condensing recovery
CN111561657A (en) * 2020-05-21 2020-08-21 大连海洋大学 Boil-off gas treatment device for liquefied natural gas device
WO2021121013A1 (en) * 2019-12-16 2021-06-24 南京扬子石油化工设计工程有限责任公司 Low-temperature full-capacity tank for realizing low liquid level material extraction function by using pump column
WO2024127643A1 (en) * 2022-12-16 2024-06-20 株式会社荏原製作所 Liquefied gas transportation system

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MY123311A (en) 1999-01-15 2006-05-31 Exxon Production Research Co Process for producing a pressurized methane-rich liquid from a methane-rich gas
GB0001801D0 (en) 2000-01-26 2000-03-22 Cryostar France Sa Apparatus for reliquiefying compressed vapour
US6672104B2 (en) 2002-03-28 2004-01-06 Exxonmobil Upstream Research Company Reliquefaction of boil-off from liquefied natural gas
KR101018742B1 (en) 2010-12-30 2011-03-04 삼성물산 주식회사 The facilities for offshre lng floating storage with jack-up platform regasification unit
FR3005135B1 (en) 2013-04-30 2019-03-29 Cryostar Sas METHOD AND DEVICE FOR REFUELING CRYOGENIC LIQUID, IN PARTICULAR LIQUEFIED NATURAL GAS
KR20160015699A (en) * 2014-07-31 2016-02-15 대우조선해양 주식회사 Fuel Supply System And Method
CN113028276A (en) * 2021-02-24 2021-06-25 四川汇众力低温科技有限公司 Low-temperature gas recovery device

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US5228295A (en) * 1991-12-05 1993-07-20 Minnesota Valley Engineering No loss fueling station for liquid natural gas vehicles
WO1996001391A1 (en) * 1994-07-01 1996-01-18 Chicago Bridge & Iron Technical Services Company Method and apparatus for fueling vehicles with liquefied cryogenic fuel
US5590535A (en) * 1995-11-13 1997-01-07 Chicago Bridge & Iron Technical Services Company Process and apparatus for conditioning cryogenic fuel to establish a selected equilibrium pressure

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008085348A2 (en) * 2006-12-28 2008-07-17 Kellogg Brown & Root Llc Methods for pressurizing boil off gas
WO2008085348A3 (en) * 2006-12-28 2008-10-16 Kellogg Brown & Root Llc Methods for pressurizing boil off gas
JP2014159859A (en) * 2013-02-20 2014-09-04 Jfe Engineering Corp Apparatus for re-liquefaction/pressure-rise of boil-off gas of low-temperature liquid gas
CN103225740A (en) * 2013-04-22 2013-07-31 中国海洋石油总公司 BOG processing system utilizing pressure energy of LNG receiving station
CN103225739A (en) * 2013-04-22 2013-07-31 中国海洋石油总公司 Energy-saving processing system for vapor of LNG receiving station
JP2015190598A (en) * 2014-03-28 2015-11-02 千代田化工建設株式会社 Vaporized gas re-liquefaction facility and vaporized gas re-liquefaction method
CN105953072A (en) * 2016-06-30 2016-09-21 日照海达尔加气设备有限公司 Gas dispenser for injecting liquefied natural gas while gas is mixed in
CN106288478A (en) * 2016-09-28 2017-01-04 中国海洋石油总公司 A kind of injector for normal-temperature natural-gas injection LNG cold boil-off gas
CN109578806A (en) * 2018-12-07 2019-04-05 江苏中圣压力容器装备制造有限公司 A kind of process unit of LNG flash steam (BOG) pressurization condensing recovery
CN109578806B (en) * 2018-12-07 2024-01-23 江苏中圣压力容器装备制造有限公司 LNG flash evaporation vapour (BOG) supercharging condensation recovery process device
WO2021121013A1 (en) * 2019-12-16 2021-06-24 南京扬子石油化工设计工程有限责任公司 Low-temperature full-capacity tank for realizing low liquid level material extraction function by using pump column
CN111561657A (en) * 2020-05-21 2020-08-21 大连海洋大学 Boil-off gas treatment device for liquefied natural gas device
WO2024127643A1 (en) * 2022-12-16 2024-06-20 株式会社荏原製作所 Liquefied gas transportation system

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GB9800238D0 (en) 1998-03-04
GB9828120D0 (en) 1999-02-17
GB2333149A (en) 1999-07-14

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