US3253418A - Method of processing a mixture of liquefied gases - Google Patents

Method of processing a mixture of liquefied gases Download PDF

Info

Publication number
US3253418A
US3253418A US412383A US41238364A US3253418A US 3253418 A US3253418 A US 3253418A US 412383 A US412383 A US 412383A US 41238364 A US41238364 A US 41238364A US 3253418 A US3253418 A US 3253418A
Authority
US
United States
Prior art keywords
heat exchange
gas
temperature
residual liquid
exchange medium
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
US412383A
Inventor
Harmens Alexander
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.)
Conch International Methane Ltd
Original Assignee
Conch International Methane Ltd
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 Conch International Methane Ltd filed Critical Conch International Methane Ltd
Application granted granted Critical
Publication of US3253418A publication Critical patent/US3253418A/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
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/061—Natural gas or substitute natural gas
    • F25J3/0615—Liquefied natural gas
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/064—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • 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

Definitions

  • it concerns a method of vaporizing liquefied natural gas in such a way as to obtain its components in an advantageous gaseous form and at the same time make best use of the liquefied natural gas as a sink of heat, namely to utilize the cold inherent in the liquefied natural gas for external duty.
  • liquefied natural gas means a mixture of low molecular weight hydrocarbon gases obtainable from natural deposits of such gases in the ground or associated with crude oil.
  • a method of vaporizing liquefied natural gas comprises: heating the liquefied natural gas under constant pressure .to give a lean gas and leave a residual liquid, heat for the vaporization being provided by a first heat exchange medium which is-thereby cooled to give a first source of cold for external duty; and heating the residual liquid under constant pressure to give a rich gas, heat for the vaporization being provided by a second heat exchange medium which is thereby cooled to give a second source of cold for external duty.
  • the pressure on the residual liquid from the first stage of vaporization is preferably increased before the residual liquid is completely vaporized.
  • Increasing the pressure on the residual liquid will also provide a convenient way of adjusting the final temperature of the second heat exchange medium, because the greater the pressure on the residual liquid the higher will be the lowest temperature at which the residual liquid will be completely vaporized.
  • the mixture of liquefied gases is heated to a temperature of 160 F., half of the mixture being vaporized to give a lean gas mixture consisting of methane, 77.8 mol percent; ethane, 21.8 mol percent; and propane, 0.4 mol percent and leave a residual liquid consisting of methane, 2.2 mol percent; ethane, 58.2 'mol percent; and propane, 39.6 mol percent.
  • the lean gas mixture leaves the heat exchanger 2 via a gas line 3. The heat for producing the part vaporization.
  • gaseous ethylene under a pressure of 17 p.s.i.a condensing at a temperature of l50 F. in the warm side of the heat exchanger 2.
  • Liquid ethylene leaves the heat exchanger via a liquid line 4 to be used as a refrigerant.
  • Fresh gaseous ethylene enters the warm side of the heat exchanger 2 from a gas line 5.
  • the residual liquid in the cold side of the heat ex changer 2 is pumped into a liquid line 6 by a pump 7, and then passes via the pump 7 into a further liquid line 8 under a pressure of 26 p.s.i.a
  • the residual liquid then passes into the cold side of a heat exchanger 9 in which it'is heated to a temperature of 50 F. and completely vaporized to give a rich gas mixture.
  • the rich gas mixture passes from the heat exchanger 9 into a gas line 10.
  • the heat for producing the complete vaporization of the residual liquid in the cold side of the heat exchanger 9 is provided by a gaseous propane under a pressure of 16 p.s.i.a. condensing in the warm side of the heat exchanger 9 at a temperature at 40 F.
  • Liquid propane leaves the heat exchanger 9 via a liquid line 11 to be used as a refrigerant.
  • Fresh gaseous propane enters the warm side of the heat exchanger 9 from a gas line 12.
  • the pump 7 is not necessary but if it is omitted the temperature to which the residual liquid is heated in the cold side of the heat exchanger 9 is --75 P. not 50 F.
  • the gaseous propane in the warm side of the heat exchanger 9 still condenses at a temperature of 40 F. but it is also subcooled to a temperature of about F.
  • Method of vaporizing liquefied natural gas comprising (a) heating the LNG under constant pressure by heat exchange with a first heat exchange medium, at a temperature such as to convert the LNG into two major fractions, one of which is a lean gas and the other a residual liquid gas containing the heavier, more slowly vaporizable constituents of the original LNG,
  • step (a) heating the residual liquid gas from step (a), at constant pressure, by heat exchange with a second heat exchange medium, at a temperature such as to convert said residual liquid gas to a rich gas containing said heavier constituents,
  • step (d) and cooling said second heat exchange medium by the heat exchange of step (c) to provide a second source of low temperature, but at a higher temperature than that produced in step (b), for external duty.
  • a method as claimed inclaim 1 said first heat exchange medium being a gas prior to said heat exchange step and being liquefied during said first heat exchange step.
  • said LNG being composed of substantial par-ts of methane, ethane and propane; said lean gas being composed of methane and ethane with a negligible percentage of propane: said rich gas being composed of ethane and'propane with a negligible percentage of met-bane.

Description

y 1966 A. HARMENS 3,253,418
METHOD OF PROCESSING A MIXTURE 0F LIQUEFIED GASES Filed Nov. 19, 1964 Product Leon Gos Merhone 2 Mol.%
Erhone 58 Mol.% 9 Liquid Propane Propane 4O Mol.% W
Rich Gus Product INVENTOR A Iexonder Harmens ATTORNEY United States Patent Ofiiice 3,253,418 METHOD OF PROCESSING A MIXTURE F LIQUEFIED GASES Alexander Harmens, Purley, England, assignor to Conch International Methane Limited, Nassau, The Bahamas, a Bahamian company Filed Nov. 19, 1964, Ser. No. 412,383 Claims priority, application Great Britain, Feb. 11, 1964, 5,743/ 64 7 Claims. (Cl. 6252) This invention relates to a method of processing a mixture of liquefied gases. More particularly, it concerns a method of vaporizing liquefied natural gas in such a way as to obtain its components in an advantageous gaseous form and at the same time make best use of the liquefied natural gas as a sink of heat, namely to utilize the cold inherent in the liquefied natural gas for external duty.
In this specification, the expression liquefied natural gas means a mixture of low molecular weight hydrocarbon gases obtainable from natural deposits of such gases in the ground or associated with crude oil.
It is increasingly the practice to liquefy natural gas for convenient transport to places where it can be utilized. On arrival, the liquefied natural gas is vaporized and used as a fuel or for other purposes, some of its components being more advantageous for some of the purposes than others. At the same time, the considerable expense of liquefying the natural gas in the first instance can be partly recovered by utilizing the liquefied natural gas as a sink of heat, namely by utilizing the cold inherent in the liquefied natural gas and made available for use in the course of their vaporization.
It has now been found that by vaporizing the liquefied natural gas in two stages not only can its components be separated into different fractions having different properties (namely an easily vaporizable fraction hereafter called lean gas and a heavier more slowly vaporizable fraction hereafter called rich gas), but that the sources of cold constituted by the successive stages of vaporization are themselves of diiferent qualities and can be used advantageously for different purposes.
According to the present invention, therefore, a method of vaporizing liquefied natural gas comprises: heating the liquefied natural gas under constant pressure .to give a lean gas and leave a residual liquid, heat for the vaporization being provided by a first heat exchange medium which is-thereby cooled to give a first source of cold for external duty; and heating the residual liquid under constant pressure to give a rich gas, heat for the vaporization being provided by a second heat exchange medium which is thereby cooled to give a second source of cold for external duty.
In practicing the invention, if it is desired to produce the rich gas at a higher pressure than that at which the liquefied natural gas is available, the pressure on the residual liquid from the first stage of vaporization is preferably increased before the residual liquid is completely vaporized. Increasing the pressure on the residual liquid will also provide a convenient way of adjusting the final temperature of the second heat exchange medium, because the greater the pressure on the residual liquid the higher will be the lowest temperature at which the residual liquid will be completely vaporized.
3,253,418 Patented May 31, 1966 The present invention will now be illustrated by the following example, in which reference is made to the accompanying drawing which is a flow diagram for practicing the invention.
Example A mixture of liquefied gases under a pressure of 14.7 p.s.i.a. and at a temperature of 240 F. consisting of methane, 40 mol percent; and propane, 20 mol percent enters the system at a constant rate via a liquid line 1 and passes into the cold side of a heat exchanger 2. In the cold side of the heat exchanger 2, the mixture of liquefied gases is heated to a temperature of 160 F., half of the mixture being vaporized to give a lean gas mixture consisting of methane, 77.8 mol percent; ethane, 21.8 mol percent; and propane, 0.4 mol percent and leave a residual liquid consisting of methane, 2.2 mol percent; ethane, 58.2 'mol percent; and propane, 39.6 mol percent. The lean gas mixture leaves the heat exchanger 2 via a gas line 3. The heat for producing the part vaporization. of the mixture of liquefied gases is provided by gaseous ethylene under a pressure of 17 p.s.i.a condensing at a temperature of l50 F. in the warm side of the heat exchanger 2. Liquid ethylene leaves the heat exchanger via a liquid line 4 to be used as a refrigerant. Fresh gaseous ethylene enters the warm side of the heat exchanger 2 from a gas line 5.
The residual liquid in the cold side of the heat ex changer 2 is pumped into a liquid line 6 by a pump 7, and then passes via the pump 7 into a further liquid line 8 under a pressure of 26 p.s.i.a The residual liquid then passes into the cold side of a heat exchanger 9 in which it'is heated to a temperature of 50 F. and completely vaporized to give a rich gas mixture. The rich gas mixture passes from the heat exchanger 9 into a gas line 10.
The heat for producing the complete vaporization of the residual liquid in the cold side of the heat exchanger 9 is provided by a gaseous propane under a pressure of 16 p.s.i.a. condensing in the warm side of the heat exchanger 9 at a temperature at 40 F. Liquid propane leaves the heat exchanger 9 via a liquid line 11 to be used as a refrigerant. Fresh gaseous propane enters the warm side of the heat exchanger 9 from a gas line 12.
In the above procedure, the pump 7 is not necessary but if it is omitted the temperature to which the residual liquid is heated in the cold side of the heat exchanger 9 is --75 P. not 50 F. In this case, the gaseous propane in the warm side of the heat exchanger 9 still condenses at a temperature of 40 F. but it is also subcooled to a temperature of about F.
It will be apparent that the embodiments shown are only exemplary and that various modifications can be made in construction and arrangement within the scope of my invention as defined by the appended claims.
I claim:
1. Method of vaporizing liquefied natural gas (LNG) comprising (a) heating the LNG under constant pressure by heat exchange with a first heat exchange medium, at a temperature such as to convert the LNG into two major fractions, one of which is a lean gas and the other a residual liquid gas containing the heavier, more slowly vaporizable constituents of the original LNG,
(b) cooling said first heat exchange medium by said 3 heat exchange to provide a first source of low temperature for external duty,
(0) heating the residual liquid gas from step (a), at constant pressure, by heat exchange with a second heat exchange medium, at a temperature such as to convert said residual liquid gas to a rich gas containing said heavier constituents,
(d) and cooling said second heat exchange medium by the heat exchange of step (c) to provide a second source of low temperature, but at a higher temperature than that produced in step (b), for external duty.
2. A method as claimed in claim 1, comprising increasing the pressure on the residual liquid before it is completely vaporized.
3. A method as claimed inclaim 1, said first heat exchange medium being a gas prior to said heat exchange step and being liquefied during said first heat exchange step.
4. Method as claimed in claim 3, said second heat exchange medium being a gas prior to said second heat exchange step and being liquefied during said second heat exchange step.
5. Method according to claim 4, said first heat exchange medium being ethane.
6. Method according to claim 5, said second heat exchange medium being propane.
7. Method according to claim 6, said LNG being composed of substantial par-ts of methane, ethane and propane; said lean gas being composed of methane and ethane with a negligible percentage of propane: said rich gas being composed of ethane and'propane with a negligible percentage of met-bane.
References Cited by the Examiner UNITED STATES PATENTS 12/1950 Martin et a1. 6252 ROBERT A. OLEARY, Primary Examiner.
LLOYD L. KING, Assistant Examiner.

Claims (1)

1. METHOD OF VAPORIZING LIQUEFIED NATURAL GAS (LNG) COMPRISING (A) HEATING THE LNG UNDER CONSTANT PRESSURE BY HEAT EXCHANGE WITH A FIRST HEAT EXCHANGE MEDIUM, AT A TEMPERATURE SUCH AS TO CONVERT THE LNG INTO TWO MAJOR FRACTIONS, ONE OF WHICH IS A LEAN GAS AND THE OTHER A RESIDUAL LIQUID GAS CONTAINING THE HEAVIER, MORE SLOWLY VAPORIZABLE CONSTITUENTS OF THE ORIGINAL LNG, (B) COOLING SAID FIRST HEAT EXCHANGE MEDIUM BY SAID HEAT EXCHANGE TO PROVIDE A FIRST SOURCE OF LOW TEMPERATURE FOR EXTERNAL DUTY, (C) HEATING THE RESIDUAL LIQUID GAS FROM STEP (A), AT CONSTANT PRESSURE, BY HEAT EXCHANGE WITH A SECOND HEAT EXCHANGE MEDIUM, AT A TEMPERATURE SUCH AS TO CONVERT SAID RESIDUAL LIQUID GAS TO A RICH GAS CONTAINING SAID HEAVIER CONSTITUENTS, (D) AND COOLING SAID SECOND HEAT EXCHANGE MEDIUM BY THE HEAT EXCHANGE OF STEP (C) TO PROVIDE A SECOND SOURCE OF LOW TEMPERATURE, BUT AT A HIGHER TEMPERATURE THAN THAT PRODUCED IN STEP (B), FOR EXTERNAL DUTY.
US412383A 1964-02-11 1964-11-19 Method of processing a mixture of liquefied gases Expired - Lifetime US3253418A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
GB5743/64A GB983977A (en) 1964-02-11 1964-02-11 A method of processing a mixture of liquefied gases

Publications (1)

Publication Number Publication Date
US3253418A true US3253418A (en) 1966-05-31

Family

ID=9801824

Family Applications (1)

Application Number Title Priority Date Filing Date
US412383A Expired - Lifetime US3253418A (en) 1964-02-11 1964-11-19 Method of processing a mixture of liquefied gases

Country Status (3)

Country Link
US (1) US3253418A (en)
ES (1) ES307757A1 (en)
GB (1) GB983977A (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060065014A1 (en) * 2004-09-29 2006-03-30 Chevron U.S.A. Inc. Method for recovering LPG boil off gas using LNG as a heat transfer medium
US20060065015A1 (en) * 2004-09-29 2006-03-30 Chevron U.S.A. Inc. Recovering natural gas liquids from LNG using vacuum distillation
US20080087041A1 (en) * 2004-09-14 2008-04-17 Denton Robert D Method of Extracting Ethane from Liquefied Natural Gas

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2535148A (en) * 1946-04-18 1950-12-26 Pritchard & Co J F Method of storing natural gas
US2964917A (en) * 1956-09-19 1960-12-20 British Oxygen Co Ltd Evaporation of liquefied gases
US3068659A (en) * 1960-08-25 1962-12-18 Conch Int Methane Ltd Heating cold fluids with production of energy

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2535148A (en) * 1946-04-18 1950-12-26 Pritchard & Co J F Method of storing natural gas
US2964917A (en) * 1956-09-19 1960-12-20 British Oxygen Co Ltd Evaporation of liquefied gases
US3068659A (en) * 1960-08-25 1962-12-18 Conch Int Methane Ltd Heating cold fluids with production of energy

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080087041A1 (en) * 2004-09-14 2008-04-17 Denton Robert D Method of Extracting Ethane from Liquefied Natural Gas
US8156758B2 (en) 2004-09-14 2012-04-17 Exxonmobil Upstream Research Company Method of extracting ethane from liquefied natural gas
WO2006039182A3 (en) * 2004-09-29 2007-03-01 Chevron Usa Inc Recovering natural gas liquids from lng using vacuum distillation
US7299643B2 (en) * 2004-09-29 2007-11-27 Chevron U.S.A. Inc. Method for recovering LPG boil off gas using LNG as a heat transfer medium
US20060065014A1 (en) * 2004-09-29 2006-03-30 Chevron U.S.A. Inc. Method for recovering LPG boil off gas using LNG as a heat transfer medium
WO2006039172A3 (en) * 2004-09-29 2007-03-01 Chevron Usa Inc Method for recovering lpg boil off gas using lng as a heat transfer medium
US7234323B2 (en) * 2004-09-29 2007-06-26 Chevron U.S.A. Inc. Recovering natural gas liquids from LNG using vacuum distillation
GB2434434A (en) * 2004-09-29 2007-07-25 Chevron Usa Inc Method for recovering LPG boil offgas using LNG as a heat transfer medium
GB2434435A (en) * 2004-09-29 2007-07-25 Chevron Usa Inc Recovering natural gas liquids from LNG using vacuum distillation
WO2006039182A2 (en) * 2004-09-29 2006-04-13 Chevron U.S.A. Inc. Recovering natural gas liquids from lng using vacuum distillation
GB2434434B (en) * 2004-09-29 2008-01-16 Chevron Usa Inc Method for recovering LPG boil offgas using LNG as a heat transfer medium
GB2434435B (en) * 2004-09-29 2008-01-16 Chevron Usa Inc Recovering natural gas liquids from LNG using vacuum distillation
WO2006039172A2 (en) * 2004-09-29 2006-04-13 Chevron U.S.A. Inc. Method for recovering lpg boil off gas using lng as a heat transfer medium
AU2005292419B2 (en) * 2004-09-29 2011-03-17 Chevron U.S.A. Inc. Recovering natural gas liquids from LNG using vacuum distillation
AU2005292409B2 (en) * 2004-09-29 2011-08-11 Chevron U.S.A. Inc. Method for recovering LPG boil off gas using LNG as a heat transfer medium
US20060065015A1 (en) * 2004-09-29 2006-03-30 Chevron U.S.A. Inc. Recovering natural gas liquids from LNG using vacuum distillation

Also Published As

Publication number Publication date
GB983977A (en) 1965-02-24
ES307757A1 (en) 1965-05-01

Similar Documents

Publication Publication Date Title
US3846993A (en) Cryogenic extraction process for natural gas liquids
US2577701A (en) Fractionation process
US3413817A (en) Liquefaction of natural gas at supercritical pressure employing a single refrigeration cycle
US3596473A (en) Liquefaction process for gas mixtures by means of fractional condensation
RU2702074C2 (en) Method (embodiments) and apparatus (embodiments) for producing nitrogen-depleted lng product
US3702063A (en) Refrigeration cycle for the aliquefaction of natural gas
US3479832A (en) Process for vaporizing liquefied natural gas
US3302416A (en) Means for maintaining the substitutability of lng
US3018634A (en) Method and apparatus for vaporizing liquefied gases and obtaining power
NO132703B (en)
US2475957A (en) Treatment of natural gas
EP0043212B1 (en) Producing power from a cryogenic liquid
US3315477A (en) Cascade cycle for liquefaction of natural gas
US2716332A (en) Systems for separating nitrogen from natural gas
US2089558A (en) Process and apparatus for separating vapors from gaseous mixtures
NO345734B1 (en) Method and device for recovering liquefied natural gas from a gaseous feed stream.
US4586942A (en) Process and plant for the cooling of a fluid and in particular the liquefaction of natural gas
US2970107A (en) Stabilization of oil well fluid
US3261169A (en) Method of processing a mixture of liquefied gases
US3160489A (en) Nitrogen removal from natural gas
US3729944A (en) Separation of gases
US3257813A (en) Liquefaction of gases
US3253418A (en) Method of processing a mixture of liquefied gases
US3181307A (en) Helium separation
US3066492A (en) Process for the liquefaction of a gas