WO1994017325A1 - Procede et systeme servant respectivement a exploiter et a produire du gaz combustible - Google Patents

Procede et systeme servant respectivement a exploiter et a produire du gaz combustible Download PDF

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Publication number
WO1994017325A1
WO1994017325A1 PCT/NO1994/000020 NO9400020W WO9417325A1 WO 1994017325 A1 WO1994017325 A1 WO 1994017325A1 NO 9400020 W NO9400020 W NO 9400020W WO 9417325 A1 WO9417325 A1 WO 9417325A1
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WO
WIPO (PCT)
Prior art keywords
gas
boil
compressor
liquefied
heat exchanger
Prior art date
Application number
PCT/NO1994/000020
Other languages
English (en)
Inventor
Per E. Christiansen
Original Assignee
Kværner Moss Technology A.S.
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 Kværner Moss Technology A.S. filed Critical Kværner Moss Technology A.S.
Priority to AU60117/94A priority Critical patent/AU6011794A/en
Priority to DE69409504T priority patent/DE69409504T2/de
Priority to EP94906400A priority patent/EP0681671B1/fr
Priority to JP6516888A priority patent/JPH08505926A/ja
Publication of WO1994017325A1 publication Critical patent/WO1994017325A1/fr
Priority to FI953612A priority patent/FI953612A0/fi

Links

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
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/035—Propane butane, e.g. LPG, GPL
    • 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
    • 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
    • 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
    • F17C2227/0135—Pumps
    • 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
    • F17C2227/0157—Compressors
    • 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
    • F17C2227/0178—Arrangement in the vessel
    • 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
    • F17C2227/0367—Localisation of heat exchange
    • F17C2227/0388—Localisation of heat exchange separate
    • F17C2227/0393—Localisation of heat exchange separate using a vaporiser
    • 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
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/06—Controlling or regulating of parameters as output values
    • F17C2250/0605—Parameters
    • F17C2250/0621—Volume
    • 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
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/06—Controlling or regulating of parameters as output values
    • F17C2250/0605—Parameters
    • F17C2250/0631—Temperature
    • 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
    • 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
    • F17C2265/036—Treating the boil-off by recovery with heating
    • 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

  • the invention relates to a process for the utilization of boil-off (decoction) from liquefied petroleum gas as fuel gas in combination with gas produced by evaporation of the liquefied petroleum gas, where the boil-off and evaporated gas are brought together and compressed.
  • the invention also relates to a system for carrying out the method, wherein boil-off and evaporated gas are brought together and compressed, comprising a storage tank for liquefied petroleum gas, an outlet line for decoction from the storage tank, an outlet line for liquefied gas from the storage tank, an evaporator in the outlet line for liquefied gas, a flowline (header) connected to the two outlet lines, a compressor connected to the flowline, and a pressure pipe from the compressor.
  • a storage tank for liquefied petroleum gas comprising a storage tank for liquefied petroleum gas, an outlet line for decoction from the storage tank, an outlet line for liquefied gas from the storage tank, an evaporator in the outlet line for liquefied gas, a flowline (header) connected to the two outlet lines, a compressor connected to the flowline, and a pressure pipe from the compressor.
  • the point of departure is the situation currently found aboard LNG ships, i.e. , ships designed to carry liquefied natural gas.
  • Ships carrying liquefied natural gas (LNG ships) at atmospheric pressure normally are not equipped with recondensation systems. Therefore, the gas which boils off as a result of leakage of heat into the tanks, here defined as decoction (boil-off), is used as fuel gas in the ship's steam boiler.
  • decoction here defined as decoction (boil-off)
  • the temperature of the cargo at atmospheric pressure will be about minus 160°C for most LNG mixtures, while the gas temperature and pressure requirements at the inlet to the boiler burners are, respectively, plus 30°C and minimum 0.5 bar g.
  • the gas amount may be increased by evaporating LNG, here defined as gas produced by the evaporation of the liquefied gas, which is taken directly from the tanks.
  • LNG here defined as gas produced by the evaporation of the liquefied gas
  • a compressor maintains the desired tank pressure by evacuating boil-off.
  • the boil-off will receive some heat in the tank dome and the pipe system, causing the temperature at the inlet to a separator placed in front of the compressor to be increased from minus 160°C to about minus 120°C.
  • the pressure increase in the compressor causes a temperature rise of about 30°C.
  • a heat exchanger (heater) is installed after the compressor for further heating of the gas.
  • a pump suitable for this purpose is started in one of the tanks, and LNG at minus 160°C is sent on to an evaporator.
  • the gas is evaporated and overheated to about minus 60°C, prior to entering said separator and mixing with the boil-off.
  • the separator is considered necessary because LNG taken from the bottom of the tanks contains small amounts of heavier hydrocarbons which have a droplet form after the evaporation, or conceivably can condense in the inlet to the compressor and damage it.
  • boil-off is used alone, the separator per se is not necessary, nor is it necessary if the temperature is sufficiently high in front of the compressor, eliminating the danger of precipitation of liquid drops.
  • the system should be run either with boil-off alone or with evaporation of LNG.
  • the amounts will vary from 0 to 100 for both sources. If, for example, maximum gas consumption for the boilers is 5000 kg/hour and the boil-off amount is 4000 kg/hour, then 1000 kg/hour must be supplied via the evaporator. If the boil-off amount is 2000 kg/hour, then 3000 kg/hour must be supplied via the evaporator, etc.
  • the suction temperature for the compressor could vary between the extremes of minus 60°C and minus 120°C.
  • An existing system of this type involves an arrangement requiring four main components, namely: an evaporator, separa ⁇ tor, compressor and heater.
  • the operating temperatures are such that these components must be classified as cryogenic equipment, with special requirements with regard to materials and construction. This also applies to the pipework and instrumentation.
  • the purpose of the present invention is to simplify the process and the system.
  • the aforementioned system be designed such that the evaporator is constructed as a combined heat exchanger having two separate throughflow tube bundles disposed in a common surrounding shell, one said bundle being connected to the outlet line for liquefied gas for the evaporation thereof, and the other tube bundle being connected to the outlet line for boil-off for the overheating thereof, which tubes flow into a common mixing chamber which is connected to the flowline .
  • the process and the system are radically simplified. Because the suction temperature of the compressor is raised substantially, the separator may be omitted, and the compressor need not be cryogenic, with the special requirements for materials, construction and design associated therewith. Insulation of the pipelines may be omitted, and ice formation on the valves and expansion members is avoided. This simplification results in reduction of the amount of required space and a less complicated pipework system.
  • the combined heat exchanger can be supplied at a price which is not substantially higher than that of each of the heat exchangers (evaporator and heater) in use today. The overall capital costs and operating expenses (including maintenance) over the lifetime of the ship will be reduced substantially.
  • Thermal engineering calculations indicate that it is possible to construct the combined heat exchanger with dimensions covering all conditions from 0-100% boil-off and from 0-100% evaporation. Furthermore, the apparatus may be regulated such that the gas exiting the heat exchanger maintains a tempera ⁇ ture of plus 10°C, so that further heating of 20-30°C in the compressor will ensure that the gas supplied to the boilers has the correct temperature (and pressure).
  • Fig. 1 is a purely schematic view of a known system
  • Fig. 2 shows a system according to the invention
  • Fig. 3 shows the new combined heat exchanger with associated control system.
  • numeral 1 designates a storage tank for liquefied petroleum gas, for example a tank for LNG aboard an LNG ship.
  • boil-off decoction
  • This boil-off collects in the dome 2 of the storage tank and may be removed through an outlet line 3.
  • This outlet line 3 runs to a separator 4, from which runs a line 5 to a compressor 6.
  • compressor 6 In compressor 6 the boil-off is compressed, with an attendant increasing of the temperature. Further temperature increases take place in a heater 7, from which runs a line 8 carrying fuel gas.
  • Tank 1 contains liquefied natural gas having a temperature of around minus 160°.
  • the boil-off, which is removed through line 3, will as a result of the supply of heat in dome 2 and in line 3 have a temperature of around minus 120°C at separator 4.
  • compressor 6 the temperature increases to about minus 90°C, and in heater 7 the temperature is increased to plus 40°C.
  • the system is designed in such a way that if the decoction is insufficient, i.e., if greater amounts of fuel gas are needed than the boil-off can supply, then liquefied natural gas is extracted by means of a pump 9. From this submerged pump runs outlet line 10 for liquefied gas, on to an evaporator 11. From evaporator 11 runs a line 12 to separator 4. When the evaporated gas arrives at the separator it will have a temperature of about minus 60°C.
  • the separator is considered necessary because the liquefied gas removed from the bottom of tank 1 after the evaporation contains small amounts of liquid drops. These can conceivably condense in the inlet of compressor 6 and damage it. For boil-off alone the separator is not necessary, nor is it necessary if the temperature is sufficiently high prior to the compressor to ensure that there is no danger of precipitation of liquid drops.
  • FIG. 2 A schematic view of the system according to the invention is shown in Figure 2.
  • the system is intended to be connected to a storage tank 1 with a dome 2 and submerged pump 9 and an outlet line 3 for boil-off, as well as an outlet line 10 for liquefied petroleum gas, as in the system in Figure 1.
  • the two outlet lines 3 and 10 are led to a combined heat exchanger 13.
  • This has two separate tube bundles 14 and 15 in the same shell, namely a bundle 15 for the evaporation of the liquefied gas and a bundle 14 for the overheating of boil-off. Both tube bundles flow into a common mixing chamber 16. From there runs a line 17 to a compressor 18. From compressor 18 runs a fuel gas line 19.
  • the combined heat exchanger may be regulated such that the mixed gas in line 17 will have a temperature of plus 10°C.
  • the fuel gas supplied by compressor 18 will have a temperature of around 30°C.
  • the compressor in Figure 2 may be of a normal type since the suction temperature, as mentioned above, will be high (plus 10°C instead of minus 120°C as in Figure 1).
  • Volume control is effected in the system in Figure 1 by means of a control valve at the inlet of evaporator 11 and by regulation of the suction volume of compressor 6.
  • a line 20 branches off from line 10 to the mixing chamber 16 of the combined heat exchanger.
  • Quadrangle 21 represents a temperature control.
  • Quadrangle 22 represents a flow control.
  • the flow control directs a control valve 23 in the boil-off line 3 as well as a control valve 24 in line 10. Both of these control loops will in practice be integrated in a common data processor which also handles the other control functions in the system.
  • Temperature control out from the combined heat exchanger is carried out here by means of injection of liquefied petroleum gas through line 20 in mixing chamber 16 when the heat exchanger is working with both overheating of boil-off and the evaporation of liquefied gas.
  • the temperature is controlled by means of pressure adjustment of the supply of vapour through line 25. Condensate is eliminated through line 26.
  • the invention is not limited to LNG as gas.

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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

Système de production de gaz combustible à partir du gaz de décoction (d'évaporation) provenant du gaz de pétrole liquéfié, et éventuellement du gaz obtenu par l'évaporation du gaz liquéfié, dans lequel on utilise un échangeur thermique mixte (13) assurant le chauffage du gaz d'évaporation et du gaz de pétrole liquéfié. Un compresseur (18) peut être alimenté en un flux mixte de gaz surchauffé par l'intermédiaire d'une chambre commune de mélange (16) dans l'échangeur thermique mixte. Le compresseur (18) peut avantageusement être d'un type normal puisque sa température d'aspiration est suffisamment élevée pour le permettre, grâce, précisément, au chauffage et à l'évaporation dans l'échangeur thermique mixte.
PCT/NO1994/000020 1993-01-29 1994-01-25 Procede et systeme servant respectivement a exploiter et a produire du gaz combustible WO1994017325A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
AU60117/94A AU6011794A (en) 1993-01-29 1994-01-25 Process and system for, respectively, the utilization and provision of fuel gas
DE69409504T DE69409504T2 (de) 1993-01-29 1994-01-25 Verfahren und system für, beziehungsweise, die verwendung und bereitstellung von brennstoffgas
EP94906400A EP0681671B1 (fr) 1993-01-29 1994-01-25 Procede et systeme servant respectivement a exploiter et a produire du gaz combustible
JP6516888A JPH08505926A (ja) 1993-01-29 1994-01-25 燃料ガスの利用及び供給方法及びシステム
FI953612A FI953612A0 (fi) 1993-01-29 1995-07-28 Menetelmä ja järjestelmä polttokaasun käyttämiseksi ja hankkimiseksi

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NO930317A NO176454C (no) 1993-01-29 1993-01-29 Fremgangsmåte og anlegg for utnyttelse henholdsvis tilveiebringelse av brenngass
NO930317 1993-01-29

Publications (1)

Publication Number Publication Date
WO1994017325A1 true WO1994017325A1 (fr) 1994-08-04

Family

ID=19895791

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/NO1994/000020 WO1994017325A1 (fr) 1993-01-29 1994-01-25 Procede et systeme servant respectivement a exploiter et a produire du gaz combustible

Country Status (8)

Country Link
EP (1) EP0681671B1 (fr)
JP (1) JPH08505926A (fr)
AU (1) AU6011794A (fr)
DE (1) DE69409504T2 (fr)
ES (1) ES2115935T3 (fr)
FI (1) FI953612A0 (fr)
NO (1) NO176454C (fr)
WO (1) WO1994017325A1 (fr)

Cited By (16)

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WO1996028688A1 (fr) * 1995-03-16 1996-09-19 Kværner Maritime A.S Dispositif echangeur de chaleur
WO1997032157A1 (fr) * 1996-02-29 1997-09-04 Kværner Maritime A.S Procede d'utilisation de gaz evapores provenant de gaz liquides et appareil de mise en oeuvre de ce procede
FR2765238A1 (fr) * 1997-06-26 1998-12-31 Renault Nouveaux carburants constitues de gaz liquefies pour moteurs a combustion interne
EP1132698A1 (fr) * 2000-03-09 2001-09-12 Cryostar-France SA Reliquéfaction de vapeur comprimée
WO2003011420A1 (fr) * 2001-07-31 2003-02-13 Hamworthykse Gas Systems A.S Procede et appareil de recuperation de gaz de composes organiques volatils
US6530241B2 (en) 2000-01-26 2003-03-11 Cryostar-France Sa Apparatus for reliquefying compressed vapour
WO2005058692A1 (fr) * 2003-12-18 2005-06-30 Wärtsilä Finland Oy Dispositif d'alimentation en gaz d'un navire et procede d'alimentation en gaz dans un dispositif d'alimentation en gaz d'un navire
WO2006077094A1 (fr) * 2005-01-21 2006-07-27 Cryostar Sas Procédé et appareil d'alimentation en gaz naturel
EP1291576A3 (fr) * 2001-08-24 2008-12-10 Cryostar-France SA Appareil destiné à l'alimentation en gaz naturel
DE102007042158A1 (de) * 2007-09-05 2009-03-12 Man Diesel Se Gasversorgungsanlage für einen mit gasförmigen Treibstoff betriebenen Verbrennungsmotor
WO2009136793A1 (fr) * 2008-05-08 2009-11-12 Hamworthy Gas Systems As Systèmes de distribution de gaz pour moteurs à gaz
JP2010261595A (ja) * 2007-02-12 2010-11-18 Daewoo Shipbuilding & Marine Engineering Co Ltd 蒸発ガス処理方法
NO338121B1 (no) * 2004-03-12 2016-08-01 Gustomsc Resources Bv Apparat for sammenkopling av to offshore-enheter
FR3071276A1 (fr) * 2017-09-20 2019-03-22 Gaztransport Et Technigaz Dispositif et procede d'alimentation en gaz a indice de methane optimise d'au moins un moteur thermique, en particulier d'un navire de transport de gaz liquefie
CN113970065A (zh) * 2021-11-09 2022-01-25 新地能源工程技术有限公司 一种热值可调的lng应急气化装置及方法
RU2773583C2 (ru) * 2017-09-20 2022-06-06 Газтранспорт Эт Технигаз Устройство и способ подачи газа с метановым числом, оптимизированным для по меньшей мере одного теплового двигателя, в частности, судна для транспортировки сжиженного газа

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DE102006061251B4 (de) * 2006-12-22 2010-11-11 Man Diesel & Turbo Se Gasversorgungsanlage für einen Antrieb
KR100807963B1 (ko) * 2007-01-23 2008-02-28 현대중공업 주식회사 상온에서 운전되는 액화천연가스 연료공급장치
US10816140B2 (en) * 2015-10-16 2020-10-27 Cryostar Sas Method of an apparatus for treating boil-off gas for the purpose of supplying at least an engine
WO2023156934A1 (fr) * 2022-02-17 2023-08-24 Bennamann Services Ltd Systèmes et procédés de vaporisation d'un liquide

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US5819542A (en) * 1995-03-16 1998-10-13 Kvaerner Maritime As Heat exchanger device
WO1996028688A1 (fr) * 1995-03-16 1996-09-19 Kværner Maritime A.S Dispositif echangeur de chaleur
WO1997032157A1 (fr) * 1996-02-29 1997-09-04 Kværner Maritime A.S Procede d'utilisation de gaz evapores provenant de gaz liquides et appareil de mise en oeuvre de ce procede
FR2765238A1 (fr) * 1997-06-26 1998-12-31 Renault Nouveaux carburants constitues de gaz liquefies pour moteurs a combustion interne
WO1999000466A1 (fr) * 1997-06-26 1999-01-07 Renault Carburant constitue de gaz liquefies pour moteur a combustion interne
US6530241B2 (en) 2000-01-26 2003-03-11 Cryostar-France Sa Apparatus for reliquefying compressed vapour
EP1132698A1 (fr) * 2000-03-09 2001-09-12 Cryostar-France SA Reliquéfaction de vapeur comprimée
US6449983B2 (en) 2000-03-09 2002-09-17 The Boc Group, Inc. Reliquefaction of compressed vapor
US7032390B2 (en) 2001-07-31 2006-04-25 Hamworthykse Gas Systems A.S. Method for recovery of VOC gas and an apparatus for recovery of VOC gas
WO2003011420A1 (fr) * 2001-07-31 2003-02-13 Hamworthykse Gas Systems A.S Procede et appareil de recuperation de gaz de composes organiques volatils
GB2396572A (en) * 2001-07-31 2004-06-30 Hamworthy Kse Gas Systems As Method for recovery of voc-gas and an apparatus for recovery of voc-gas
GB2396572B (en) * 2001-07-31 2005-04-06 Hamworthy Kse Gas Systems As Method for recovery of voc-gas and an apparatus for recovery of voc-gas
EP1291576A3 (fr) * 2001-08-24 2008-12-10 Cryostar-France SA Appareil destiné à l'alimentation en gaz naturel
WO2005058692A1 (fr) * 2003-12-18 2005-06-30 Wärtsilä Finland Oy Dispositif d'alimentation en gaz d'un navire et procede d'alimentation en gaz dans un dispositif d'alimentation en gaz d'un navire
US7497180B2 (en) 2003-12-18 2009-03-03 Wartsila Finland Oy Gas supply arrangement of a marine vessel and method of providing gas in a gas supply arrangement of a marine vessel
NO338121B1 (no) * 2004-03-12 2016-08-01 Gustomsc Resources Bv Apparat for sammenkopling av to offshore-enheter
US8656726B2 (en) 2005-01-21 2014-02-25 Cryostar Sas Natural gas supply method and apparatus
WO2006077094A1 (fr) * 2005-01-21 2006-07-27 Cryostar Sas Procédé et appareil d'alimentation en gaz naturel
JP2010261595A (ja) * 2007-02-12 2010-11-18 Daewoo Shipbuilding & Marine Engineering Co Ltd 蒸発ガス処理方法
DE102007042158A1 (de) * 2007-09-05 2009-03-12 Man Diesel Se Gasversorgungsanlage für einen mit gasförmigen Treibstoff betriebenen Verbrennungsmotor
CN102084114A (zh) * 2008-05-08 2011-06-01 海威气体系统公司 气体发动机的气体供应系统
WO2009136793A1 (fr) * 2008-05-08 2009-11-12 Hamworthy Gas Systems As Systèmes de distribution de gaz pour moteurs à gaz
FR3071276A1 (fr) * 2017-09-20 2019-03-22 Gaztransport Et Technigaz Dispositif et procede d'alimentation en gaz a indice de methane optimise d'au moins un moteur thermique, en particulier d'un navire de transport de gaz liquefie
WO2019057541A1 (fr) * 2017-09-20 2019-03-28 Gaztransport Et Technigaz Dispositif et procede d'alimentation en gaz a indice de methane optimise d'au moins un moteur thermique, en particulier d'un navire de transport de gaz liquefie
CN111448385A (zh) * 2017-09-20 2020-07-24 气体运输技术公司 向特别是液化气运输船舶的至少一个热力发动机供应具优化甲烷值的气体的设备和方法
CN111448385B (zh) * 2017-09-20 2022-04-12 气体运输技术公司 向特别是液化气运输船舶的至少一个热力发动机供应具优化甲烷值的气体的设备和方法
RU2773583C2 (ru) * 2017-09-20 2022-06-06 Газтранспорт Эт Технигаз Устройство и способ подачи газа с метановым числом, оптимизированным для по меньшей мере одного теплового двигателя, в частности, судна для транспортировки сжиженного газа
CN113970065A (zh) * 2021-11-09 2022-01-25 新地能源工程技术有限公司 一种热值可调的lng应急气化装置及方法

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EP0681671A1 (fr) 1995-11-15
FI953612A (fi) 1995-07-28
NO930317L (no) 1994-08-01
NO930317D0 (no) 1993-01-29
NO176454B (no) 1994-12-27
DE69409504T2 (de) 1998-09-10
ES2115935T3 (es) 1998-07-01
NO176454C (no) 1995-04-05
EP0681671B1 (fr) 1998-04-08
JPH08505926A (ja) 1996-06-25
AU6011794A (en) 1994-08-15
DE69409504D1 (de) 1998-05-14
FI953612A0 (fi) 1995-07-28

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