US2937504A - Process for the vaporisation of liquefied low-boiling gases - Google Patents

Process for the vaporisation of liquefied low-boiling gases Download PDF

Info

Publication number
US2937504A
US2937504A US615188A US61518856A US2937504A US 2937504 A US2937504 A US 2937504A US 615188 A US615188 A US 615188A US 61518856 A US61518856 A US 61518856A US 2937504 A US2937504 A US 2937504A
Authority
US
United States
Prior art keywords
pressure
temperature
liquefied
working medium
energy
Prior art date
Legal status (The legal status 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 status listed.)
Expired - Lifetime
Application number
US615188A
Other languages
English (en)
Inventor
Riediger Bruno
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
GEA Group AG
Original Assignee
Metallgesellschaft AG
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 Metallgesellschaft AG filed Critical Metallgesellschaft AG
Application granted granted Critical
Publication of US2937504A publication Critical patent/US2937504A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • F17C9/04—Recovery of thermal energy
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0107—Single phase
    • F17C2225/0123—Single phase gaseous, e.g. CNG, GNC
    • 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
    • F17C2227/0171—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
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0309—Heat exchange with the fluid by heating using another 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
    • 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
    • F17C2227/0323—Heat exchange with the fluid by heating using another fluid in a closed loop
    • 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
    • F17C2265/05—Regasification
    • 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

Definitions

  • temperatures employed for the liquefied gases should be below their critical temperature.
  • the present invention aims at recovering a major part of the energy which has been expended in the liquefaction of low-boiling substances such as natural gas, methane,
  • the vaporis'ation or heating of the liquefied substances is carried out in conjunction with a cyclic process in which a working medium is cooled and then heated again. It is effective ifthe liquefied substances, are utilised as cooling agents, preferably at fairly low temperatures, in one or more cyclic processes, e.g. inone of these in which a vaporous medium which'has done work is completely or partially condensed by cooling, the condensate formed from the vapour being subsequently vaporised again.
  • acondensate is vapourised, the vapours of which are supp1ied,'undei' the pressure generated by the evaporation,
  • pressure gradients and possibly, before being utilised for the generation of energy, they can be heated further and their enthalpy raised, by the application of heat, to such a value that the gases, after expansion in the engine, are available with the required conditions (pressure and temperature) so that they are ready for further use.
  • liquefied substances in succession in two or more cyclic processes, by so selecting the working media in the successive cyclic processes that they are condensed at temperatures which are higher from one cyclic process to the next. If, for example, it is desired to utilise the cold content of liquefied ethane which has been transported in ships in the liquid state at atmospheric pressure, this is available at the site of utilisation at a temperature the maximum of which is approximately- -88 C. In view of the need for a most favourable pressure gradient in the cyclic process it appears advisable to choose as working medium for this the hydrocarbon next above ethane as regards boiling, point viz. propane.
  • the condensation temperature for the propane will then lie, for example, above approximately -40 C. if, for reasons which will be understood, it is desired to avoid a vacuum in the system.
  • the propane can then be vaporised at temperatures up to +96 C. and then superheated.
  • the pressure to be applied is arbitrary and can i also be above the critical pressure. Thus there is an even greater enthalpy gradient available for the generation of energy.
  • the transport temperature at atmospheric pressure lies around -160 C.
  • Fig. 2 represents the utilisation of the cold of liquefied methane in the same manner
  • Fig. 3 is a diagrammatic exemplification of another embodiment of the invention in which the liquefied gas itself is also utilised in an energy generating plant as the working medium.
  • the liquefied ethane passes at a temperature of -88,, C. and under a pressure of atmospheres gauge, through a conduit 17 into the condenser 1 where it serves forjthe; condensation of propane vapour coming through a couduit 12 from an expansion engine 2 at a temperature of 25 C. and under a pressure of 2 atmospheres absolute.
  • the propane vapour is condensed; the condensate flows through conduit 13 to apump 5 which brings it to a pressure of about 65 atm. absolute and leads it through a conduit 14 to a vaporiser 3.
  • the propane vapour which is drawn off from this vaporiser through conduit 15 is raised to a temperature of about 125 C.
  • the heating agent in the first place may be air drawn from the ambient atmosphere but it must be absolutely dry so as to avoid the formation of ice on the heat-exchange surfaces.
  • the further heating can also be effected by means of waste energy, e.g. in the form of hot water from the condensers of steam turbines or the cooling water system of diesel engines or waste steam under low pressure.
  • the heating agent enters the vaporiser through conduit 19 and leaves itv through conduit 20.
  • the highest working pressure in the propane cycle is given as 60 atm. absolute and the highest temperature 125 C. There is no reason why even higher working pressures should not be employed.
  • the criterion for a suitable choice of the maximum working pressure is the amount of the throughput, so that the blades in the first stage of the turbine have lengths with which favourable turbine efficiencies can be reached.
  • the feed pump can also consist of two units if a storage tank for the circulating fluid has to be interposed between the condenser and the vaporiser, one of these units being located before the reservoir and one after it.
  • Liquid methane passes through a conduit 31 at a temperature of about l6 0 C. and under a pressure of about 90 atm. gauge into a condenser 21. It flows out from said condenser 21 through a conduit 42 into a condenser 26, which it enters at about 100 C. and leaves at a temperature of -40 C. through conduit 43 to be conducted to the point of its further exploitation or utilisation.
  • the pressure drop of the methane during its passage through the condensers amounts to about 10 atm. absolute, so that the vaporised methane in the conduit 43 is under a pressure of about atm. gauge.
  • the working medium is ethane
  • propane is used. Both cycles can be designed on the diagram of the cycle shown in Fig. 1 and in the same manner.
  • the primary cycle is provided with an expansion engine 22 together with the plant 37 for producing electrical energy, the feed pump 25, the vaporiser 23 and the superheater 24, and the cycle II with the same equipment 27, 41, 26, 10, 28 and 29, which are connected by means of the conduits 32, 33, 34, 35, 36 and 52, 53, 54, 55 and 56, respectively.
  • the ethane in cycle I enters the expansion engine 22 at a temperature of 80 C. and a pressure of 60 atm. absolute and leaves it under a pressure of 2 atm. absolute and a temperature of 75 C.
  • the condensate passes at the same temperature from the condenser 21 to the feed pump 25 in which its pressure is raised to approximately 65 atm. absolute.
  • the propane cycle II shown in Fig. 2 can work with the same pressures as the cycle in Fig. 1 and corresponding temperatures.
  • the low temperature of a liquid hydrocarbon or mixture of hydrocarbons or of substances with similar physical properties can be utilised for producing energy, in a way which is particularly favourable from both the economical and technical standpoints, from amounts of heat which shall be drawn off at a low temperature and which represent either a desired cooling performance or a waste energy which cannot be utilised readily.
  • the liquefied gas is thereby vaporised and brought to a higher tem perature.
  • the temperature desired for the vaporised methane, etc. is near the ambient temperature and higher than can be attained by the examples described with reference to Figs. 1 and 2, this can be achieved, for example, by raising the pressure in the cyclic system and hence the temperatures in the condensers. Alternatively it can be effected by the addition of a third, for example an analogous cycle, for butane, for example, thus obtaining an outlet temperature for the gas leaving the condenser of, for example, +5 C.
  • the liquefied gas is passed through the condensers under fairly high pressure. Since, initially, it is liquid which has to be conveyed, this conveyance under pressure only requires low energy rates. This conveyance under pressure can be utilised with advantage for the further recovery of energy from the liquefied and re-vaporised gas. It can also be of advantage in other cases, however, for example, when it is required to shift the start of vaporisation of the liquefied gas to higher temperature ranges. This again has the advantage that the flow cross sections in one part of the installation can be kept smaller and the heat transfer coefiicients which are more favourable with liquids can be utilised in a wider temperature range.
  • a pump 62 which is provided inside a ship 61 or other storage container pumps the liquefied gas first through an installation K which may take the form illustrated in Fig. 1 or 2 and in which the liquefied gas is vaporised and heated. From this installation K the gas passes through a conduit 63, for example with a temperature of a little over 0 C. and under a pressure of 80 atm. gauge, into the heater, for example the tubular heater 64 or into an apparatus of similar action.
  • a conduit 63 for example with a temperature of a little over 0 C. and under a pressure of 80 atm. gauge
  • this heater the gas is brought, by means of external heat, to such a temperature that, after expansion in an engine 65, it reaches a desired condition, making it suitable, for example, for its further conveyance through a distribution system to the consumers.
  • the inlet temperature to the heater 64 should preferably be chosen a little above freezing point so as to avoid icing of the tube system by the steam contained in the flue gases.
  • the choice of this temperature point is more or less arbitrary, however, and has no great influence on the results obtainable. The higher the temperature point due to the supply of heat in the preceding part of the installation K, the less heat will be necessary to supply to the heater 64. If, for example, at the outlet from the energy generating plant 65, the gas is to be available at 20 C., 1 atm.
  • the process of the present invention has the great advantage over the latter, however, in that no vaporisation heat needs to be supplied to the working medium in the tubular heater since this heat can be withdrawn from the surrounding air in the preceding processes or can be made available from waste heat.
  • a method of recovering energy from liquefied low boiling gases which comprises vaporising such liquefied low boiling gases in heat exchange relationship with a gaseous working medium which is condensed during such vaporisation, raising the pressure of the thus condensed working medium to a higher pressure, then vaporising said condensed working medium at said higher pressure, expanding said vaporised working medium to recover energy and then recycling the vaporized working medium to the condensation step where it is recondensed to provide a cyclic process.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
US615188A 1955-10-10 1956-10-10 Process for the vaporisation of liquefied low-boiling gases Expired - Lifetime US2937504A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE1165066X 1955-10-10

Publications (1)

Publication Number Publication Date
US2937504A true US2937504A (en) 1960-05-24

Family

ID=6734485

Family Applications (1)

Application Number Title Priority Date Filing Date
US615188A Expired - Lifetime US2937504A (en) 1955-10-10 1956-10-10 Process for the vaporisation of liquefied low-boiling gases

Country Status (4)

Country Link
US (1) US2937504A (en, 2012)
BE (1) BE551602A (en, 2012)
FR (1) FR1165066A (en, 2012)
GB (1) GB814209A (en, 2012)

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3018634A (en) * 1958-04-11 1962-01-30 Phillips Petroleum Co Method and apparatus for vaporizing liquefied gases and obtaining power
US3068659A (en) * 1960-08-25 1962-12-18 Conch Int Methane Ltd Heating cold fluids with production of energy
US3123983A (en) * 1961-01-16 1964-03-10 Means for removal of liquefied gas
US3154928A (en) * 1962-04-24 1964-11-03 Conch Int Methane Ltd Gasification of a liquid gas with simultaneous production of mechanical energy
US3183666A (en) * 1962-05-02 1965-05-18 Conch Int Methane Ltd Method of gasifying a liquid gas while producing mechanical energy
US3183677A (en) * 1960-06-16 1965-05-18 Conch Int Methane Ltd Liquefaction of nitrogen in regasification of liquid methane
DE2506333A1 (de) * 1975-02-07 1976-08-19 Sulzer Ag Verfahren und anlage zur verdampfung und erwaermung von fluessigem naturgas
US4438729A (en) * 1980-03-31 1984-03-27 Halliburton Company Flameless nitrogen skid unit
US4458633A (en) * 1981-05-18 1984-07-10 Halliburton Company Flameless nitrogen skid unit
AT383884B (de) * 1985-10-24 1987-09-10 Messer Griesheim Austria Ges M Verfahren zur rueckgewinnung von bei der luftzerlegung nach verfluessigung aufgewendeter verfluessigungsenergie
EP1672270A2 (fr) 2004-12-17 2006-06-21 Snecma Système de compression-évaporation pour gaz liquéfié
US20070044485A1 (en) * 2005-08-26 2007-03-01 George Mahl Liquid Natural Gas Vaporization Using Warm and Low Temperature Ambient Air
US20070271932A1 (en) * 2006-05-26 2007-11-29 Chevron U.S.A. Inc. Method for vaporizing and heating a cryogenic fluid
WO2007144103A1 (en) * 2006-06-14 2007-12-21 Eni S.P.A. Process and plant for the vaporization of liquefied natural gas and storage thereof
EP2278210A1 (en) * 2009-07-16 2011-01-26 Shell Internationale Research Maatschappij B.V. Method for the gasification of a liquid hydrocarbon stream and an apparatus therefore
WO2011084066A1 (en) * 2010-01-06 2011-07-14 Moss Maritime As Lng re-gasification system for supplying vaporized lng to a natural gas piping distribution system
JP2014142161A (ja) * 2012-12-28 2014-08-07 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude 低温圧縮ガスまたは液化ガスの製造装置および製造方法
US9932799B2 (en) 2015-05-20 2018-04-03 Canadian Oilfield Cryogenics Inc. Tractor and high pressure nitrogen pumping unit

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2751642C3 (de) * 1977-11-17 1981-10-29 Borsig Gmbh, 1000 Berlin Verfahren zur Umwandlung einer tiefsiedenden Flüssigkeit, insbesondere unter Atmosphärendruck stehendem Erdgas oder Methan, in den gasförmigen Zustand mit anschließender Erwärmung
US4519213A (en) * 1983-08-01 1985-05-28 Zwick Energy Research Organization, Inc. Ambient air heated electrically assisted cryogen vaporizer

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR736736A (fr) * 1931-09-07 1932-11-28 Procédé pour la production, le stockage et le transport des fluides liquéfiés ou solidifiés par le froid
US2175267A (en) * 1934-10-09 1939-10-10 David H Killeffer Method of and apparatus for refrigeration
US2273257A (en) * 1940-07-15 1942-02-17 Griscom Russell Co Evaporation of liquefied gases
US2328647A (en) * 1941-08-06 1943-09-07 James O Jackson Method and apparatus for storing gaseous materials in the liquid phase
US2530443A (en) * 1949-09-17 1950-11-21 James S Walker Air conditioning cooling system for steam condensers
US2658360A (en) * 1946-05-08 1953-11-10 Chemical Foundation Inc Transportation of natural gas

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR736736A (fr) * 1931-09-07 1932-11-28 Procédé pour la production, le stockage et le transport des fluides liquéfiés ou solidifiés par le froid
US2175267A (en) * 1934-10-09 1939-10-10 David H Killeffer Method of and apparatus for refrigeration
US2273257A (en) * 1940-07-15 1942-02-17 Griscom Russell Co Evaporation of liquefied gases
US2328647A (en) * 1941-08-06 1943-09-07 James O Jackson Method and apparatus for storing gaseous materials in the liquid phase
US2658360A (en) * 1946-05-08 1953-11-10 Chemical Foundation Inc Transportation of natural gas
US2530443A (en) * 1949-09-17 1950-11-21 James S Walker Air conditioning cooling system for steam condensers

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3018634A (en) * 1958-04-11 1962-01-30 Phillips Petroleum Co Method and apparatus for vaporizing liquefied gases and obtaining power
US3183677A (en) * 1960-06-16 1965-05-18 Conch Int Methane Ltd Liquefaction of nitrogen in regasification of liquid methane
US3068659A (en) * 1960-08-25 1962-12-18 Conch Int Methane Ltd Heating cold fluids with production of energy
US3123983A (en) * 1961-01-16 1964-03-10 Means for removal of liquefied gas
US3154928A (en) * 1962-04-24 1964-11-03 Conch Int Methane Ltd Gasification of a liquid gas with simultaneous production of mechanical energy
DE1214256B (de) * 1962-04-24 1966-04-14 Conch Int Methane Ltd Verfahren zum Verdampfen verfluessigter Gase
US3183666A (en) * 1962-05-02 1965-05-18 Conch Int Methane Ltd Method of gasifying a liquid gas while producing mechanical energy
DE2506333A1 (de) * 1975-02-07 1976-08-19 Sulzer Ag Verfahren und anlage zur verdampfung und erwaermung von fluessigem naturgas
US4438729A (en) * 1980-03-31 1984-03-27 Halliburton Company Flameless nitrogen skid unit
US5551242A (en) * 1980-03-31 1996-09-03 Halliburton Company Flameless nitrogen skid unit
US4458633A (en) * 1981-05-18 1984-07-10 Halliburton Company Flameless nitrogen skid unit
AT383884B (de) * 1985-10-24 1987-09-10 Messer Griesheim Austria Ges M Verfahren zur rueckgewinnung von bei der luftzerlegung nach verfluessigung aufgewendeter verfluessigungsenergie
EP1672270A2 (fr) 2004-12-17 2006-06-21 Snecma Système de compression-évaporation pour gaz liquéfié
US20060222523A1 (en) * 2004-12-17 2006-10-05 Dominique Valentian Compression-evaporation system for liquefied gas
US7406830B2 (en) 2004-12-17 2008-08-05 Snecma Compression-evaporation system for liquefied gas
US20070044485A1 (en) * 2005-08-26 2007-03-01 George Mahl Liquid Natural Gas Vaporization Using Warm and Low Temperature Ambient Air
US20070271932A1 (en) * 2006-05-26 2007-11-29 Chevron U.S.A. Inc. Method for vaporizing and heating a cryogenic fluid
WO2007144103A1 (en) * 2006-06-14 2007-12-21 Eni S.P.A. Process and plant for the vaporization of liquefied natural gas and storage thereof
US20090199576A1 (en) * 2006-06-14 2009-08-13 Eni S.P.A. Process and plant for the vaporization of liquefied natural gas and storage thereof
AU2007260273B2 (en) * 2006-06-14 2012-08-30 Eni S.P.A. Process and plant for the vaporization of liquefied natural gas and storage thereof
EP2278210A1 (en) * 2009-07-16 2011-01-26 Shell Internationale Research Maatschappij B.V. Method for the gasification of a liquid hydrocarbon stream and an apparatus therefore
WO2011084066A1 (en) * 2010-01-06 2011-07-14 Moss Maritime As Lng re-gasification system for supplying vaporized lng to a natural gas piping distribution system
JP2014142161A (ja) * 2012-12-28 2014-08-07 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude 低温圧縮ガスまたは液化ガスの製造装置および製造方法
US9932799B2 (en) 2015-05-20 2018-04-03 Canadian Oilfield Cryogenics Inc. Tractor and high pressure nitrogen pumping unit

Also Published As

Publication number Publication date
BE551602A (en, 2012)
GB814209A (en) 1959-06-03
FR1165066A (fr) 1958-10-17

Similar Documents

Publication Publication Date Title
US2937504A (en) Process for the vaporisation of liquefied low-boiling gases
US2975607A (en) Revaporization of liquefied gases
KR101641394B1 (ko) 액화 천연 가스 변환 방법 및 장치
US7900451B2 (en) Power and regasification system for LNG
US3068659A (en) Heating cold fluids with production of energy
US9903232B2 (en) Power and regasification system for LNG
US3292380A (en) Method and equipment for treating hydrocarbon gases for pressure reduction and condensate recovery
US4437312A (en) Recovery of power from vaporization of liquefied natural gas
US7493763B2 (en) LNG-based power and regasification system
US3479832A (en) Process for vaporizing liquefied natural gas
US3413817A (en) Liquefaction of natural gas at supercritical pressure employing a single refrigeration cycle
US3505810A (en) System for generating power
CN101454608B (zh) 蒸发和加热深冷流体的方法
CN109386316B (zh) 一种lng冷能和bog燃烧能联合利用系统及方法
US3182461A (en) Natural gas liquefaction and separation
US20030005698A1 (en) LNG regassification process and system
US3018634A (en) Method and apparatus for vaporizing liquefied gases and obtaining power
EP0009387A1 (en) Process for obtaining energy during the regasification of liquefied gases
WO2014165188A1 (en) Combined heat and power technology for natural gas liquefaction plants
US3228189A (en) Binary cycle engine heat recovery system
US11585597B2 (en) Hydrocarbon distillation
NO170364B (no) Anordning for idriftssettelse og/eller rekalibrering av et slavesystem innen treghetsnavigasjon
RU2212600C1 (ru) Установка для сжижения природного газа и его регазификации
US606326A (en) Absorption refrige-rating-machine
US564506A (en) Motive-power apparatus