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US2900796A - Method of liquefying natural gas - Google Patents

Method of liquefying natural gas Download PDF

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US2900796A
US2900796A US450256A US45025654A US2900796A US 2900796 A US2900796 A US 2900796A US 450256 A US450256 A US 450256A US 45025654 A US45025654 A US 45025654A US 2900796 A US2900796 A US 2900796A
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gas
nitrogen
dry gas
liquid
dry
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US450256A
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Willard L Morrison
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Constock Liquid Methane Corp
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Constock Liquid Methane Corp
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0042—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by liquid expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0232—Coupling of the liquefaction unit to other units or processes, so-called integrated processes integration within a pressure letdown station of a high pressure pipeline system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
    • F25J1/0282—Steam turbine as the prime mechanical driver
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler

Definitions

  • Morfisonu My invention relates to animproved method of liquefying natural gas.
  • One object of my invention is to provide means for controlling the concentration of nitrogen, other non-condensibles and inerts, in a liquefying system for natural gas wherein the gas circulates ina closed system, expands and does external work with resultant cooling and liquefaction of a part of the gas and recirculation of the uncondensed portions.
  • Another object of my invention is continuously to withdraw from such a system after expansion of the gas and withdrawal from the system of the liquefied portion of the gas such quantity of nitrogen and non-condensibles and inerts as will at least compensate for the amount brought into the system by the raw gas for liquefaction.
  • My invention is especially useful in connection withuse preferably in part at least to be burned to furnish part of the power to operate the liquefaction system.
  • the remainder of the gas is further compressed for recycling through the system with fresh gas supplied in such quantity as to compensate for the gas leaving the system in liquid and gaseous phase.
  • the resulting dry gas will pass through a plurality of compression stages, some of the dry compressed gas, usually at less than the final compression pressure, will be discharged from an interrmediate compression stage at a pressure suitable for use as a fuel, to provide all or part of the power to operate nitrogen, other gases and inerts not condensible at the temperatures and pressures of liquefaction of the methane.
  • the methane When the methane is liquefied, while it may contain some of the above impurities in solution, the quantity w1ll be less than that in the gas, therefore, after separation of n the liquid from the dry gas, the remaining dry gas will be relatively richer in such impurities than rs the raw gas.
  • the proportions of such impurities may vary with the gassupplied to the system.
  • the relative proportions of the impurities left in the dry gas after separation out of the liquid and in solution the liquid may vary.
  • the amount of gas in gaseous phase discharged from the system must be controlled so that it will take out with it substantially the same quantity of the impurities as came into the system with the raw gas.
  • the dry gas discharged from the system will be richer-in these impurities than the raw gas, and it is only necessary to control the discharge of such smaller quantity of richer gas to maintain substantial equality between the impurities entering the system and those leaving it.
  • nitrogen as a generic term to include not only nitrogen itself, but any other substances which are inert or do not condense at thecondensation or liquefaction temperature of the gas being liquefied.
  • the natural gas issuing from the well l0 is cleaned to remove some higher hydrocarbons, carbon dioxide and moisture and contains about 1.5 mol percent (about 2.6 percent by weight) nitrogen and that about 21 percent of the gas fed to the expansion means 12 is condensed and removed from the system as a condensate consisting mostly of liquid methane.
  • the condensatev will contain about .2 mol percent of nitrogen dissolved ⁇ therein and such amounts ofnitrogen will be removed with the condensate from the system. If the feed to the expansion turbine is calculated to contain about 3.8-4.0 mol percent nitrogen, the concentration of nitrogen remaining in the dry gas separated from the wet exhaust will contain about 5 mol percent of nitrogen.
  • the amount of dry gas bled from the system will vary inversely in proportion to the concentration of nitrogen permissible in the feed to the expansion turbine and directly with the concentration of nitrogen in the gas from the Well.
  • An economical balance can be readily established depending upon the conditions existing at the liquefaction plant and the demand for gaseous material for use as a fuel or the like in operation of the equipment or for other purposes.
  • the amount of nitrogen contained in the dry gas bled from the system for nitrogen control will be insucient to interfere with the burning characteristics thereof for such use as a fuel.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Description

- 25, 1959 w. l.. MORRISON METHOD oF LIQUEFYING NATURAL GAS Filed Aug. 16. 1954 N gem nmmm:
Virl
mvENToR, Wiliam! L. Morfisonu My invention relates to animproved method of liquefying natural gas.
One object of my invention is to provide means for controlling the concentration of nitrogen, other non-condensibles and inerts, in a liquefying system for natural gas wherein the gas circulates ina closed system, expands and does external work with resultant cooling and liquefaction of a part of the gas and recirculation of the uncondensed portions.
Another object of my invention is continuously to withdraw from such a system after expansion of the gas and withdrawal from the system of the liquefied portion of the gas such quantity of nitrogen and non-condensibles and inerts as will at least compensate for the amount brought into the system by the raw gas for liquefaction.
These and other objects and advantages of this invention will hereinafter appear and for purposes of illustration, but not of limitation, an embodiment of the invention is shown in the accompanying drawing in which the one gure is a flow diagram illustrating the concepts of this invention.
My invention 'is especially useful in connection withuse preferably in part at least to be burned to furnish part of the power to operate the liquefaction system. The remainder of the gas is further compressed for recycling through the system with fresh gas supplied in such quantity as to compensate for the gas leaving the system in liquid and gaseous phase.v
Preferably after the gas has expanded and done work, and the gas in the liquid phase has been separated out and discharged from the system, the resulting dry gas will pass through a plurality of compression stages, some of the dry compressed gas, usually at less than the final compression pressure, will be discharged from an interrmediate compression stage at a pressure suitable for use as a fuel, to provide all or part of the power to operate nitrogen, other gases and inerts not condensible at the temperatures and pressures of liquefaction of the methane. When the methane is liquefied, while it may contain some of the above impurities in solution, the quantity w1ll be less than that in the gas, therefore, after separation of n the liquid from the dry gas, the remaining dry gas will be relatively richer in such impurities than rs the raw gas.
,l News@ Patented aug. as', teas This condition, if allowed to continue, would ultimately result 'in recycling an unsatisfactory and uneeonomical gas too rich in such impurities. t
The proportions of such impurities may vary with the gassupplied to the system. The relative proportions of the impurities left in the dry gas after separation out of the liquid and in solution the liquid may vary. There- Ifore, the amount of gas in gaseous phase discharged from the system must be controlled so that it will take out with it substantially the same quantity of the impurities as came into the system with the raw gas. The dry gas discharged from the system will be richer-in these impurities than the raw gas, and it is only necessary to control the discharge of such smaller quantity of richer gas to maintain substantial equality between the impurities entering the system and those leaving it. y
A liquefaction system to which my invention is especially well adapted is disclosed in my copending application Serial Number 259,253 filed in the United States Patent Oice November 30, 1951, now -Patent No. 2,705,406. t
In the claims and elsewhere, I have for convenience used the term nitrogen as a generic term to include not only nitrogen itself, but any other substances which are inert or do not condense at thecondensation or liquefaction temperature of the gas being liquefied.
For purposes of illustration but not of limitation, referl ence will be made to a possible set of conditions representative of the practice of this invention.
It may be assumed, for this purpose, that the natural gas issuing from the well l0 is cleaned to remove some higher hydrocarbons, carbon dioxide and moisture and contains about 1.5 mol percent (about 2.6 percent by weight) nitrogen and that about 21 percent of the gas fed to the expansion means 12 is condensed and removed from the system as a condensate consisting mostly of liquid methane. At
minus 260 F. at atmospheric pressure, the condensatev will contain about .2 mol percent of nitrogen dissolved` therein and such amounts ofnitrogen will be removed with the condensate from the system. If the feed to the expansion turbine is calculated to contain about 3.8-4.0 mol percent nitrogen, the concentration of nitrogen remaining in the dry gas separated from the wet exhaust will contain about 5 mol percent of nitrogen.
To take out enough nitrogen from the dry gas to compensate for the amount introduced into the system by the fresh gas from the well, containing only about 1.5 mol percent of nitrogen, less the amount extracted from the system with the condensate, containing about .2 mol percent nitrogen, bleeding ott as little as 9 percent by weight ofthe dry gas from the recycle system will be sullicient.
It will be understood that the amount of dry gas bled from the system will vary inversely in proportion to the concentration of nitrogen permissible in the feed to the expansion turbine and directly with the concentration of nitrogen in the gas from the Well. An economical balance can be readily established depending upon the conditions existing at the liquefaction plant and the demand for gaseous material for use as a fuel or the like in operation of the equipment or for other purposes.
' The amount of nitrogen contained in the dry gas bled from the system for nitrogen control will be insucient to interfere with the burning characteristics thereof for such use as a fuel.
I claim:
1 The method of controlling and limiting the nitrogen concentration in a recycling system, which liquees a combustible gas, which may contain nitrogen, by causing the gas to expand and do external work with resultant liquefaction of part of the gas, separating the liquid from the p 2,900,796 Il l y 'l `l 3 charging some of it from the system, compressing the remaining dry gas and recycling it through the system, together with fresh gas added in such quantity as to compensate for the liquefied and dry gasdischarged from the system.
2. The method of controlling and limiting the nitrogen concentration in a recycling system, which liquees a combustible gas, which may contain nitrogen, by causing the gas to expand and do external work with resultant liquefaction of part of the gas, separating the liquid from the unliquefied dry gas and discharging the liquid from the system, compressing the dry gas discharging part of the compressed dry gas from the system and recycling the remainder of the dry gas through the system with fresh gas added in such quantity as to compensate for the liqueed and dry gas discharged from the system.
3. The method of controlling and limiting the nitrogen concentration in a recycling system, which liqueties a combustible gas, which may contain nitrogen, hy causing the gas to expand and do external work with resultant liquefaction of part of the gas, separating the liquid from the unliqueed dry gas and discharging the liquid from the system, compressing the dry gas to a pressure above that at which separation from the liquid took place and discharging some of it from the system using such discharged dry gas as a fuel to provide at least some of the power to operate the system, compressing the remaining dry gas and recycling it through the system, together with fresh 4 gas added in such quantity as to compensate for the liqueed and dry gas discharged from the system.
4. The method of controlling and limiting the nitrogen concentration in a recycling system, which liquetes a combustible gas, which may contain nitrogen, by causing the gas to expand and do external work with resultant liquefaction of part of the gas, separating the liquid from the unliqueed dry gas and discharging the liquid from the system, compressing the dry gas, discharging part f the compressed dry gas from the system,y using such discharged dry gas as a fuel to provide atleast some of the power to operate the system and recycling the remainder of the dry gas through the system with fresh gas added in such quantity as to compensate for the liquefied and dry gas discharged from the system.
References'Cited in the file of this patent UNITED STATES PATENTS France Nov. 22, 1948

Claims (1)

1. THE METHOD OF CONTROLLING AND LIMITED THE NITROGEN CONCENTRATION IN A RECYCLING SYSTEM, WHICH LIQUEFIES A COMBUSTIBLE GAS, WHICH MAY CONTAIN NITROGEN, BY CAUSING THE GAS TO EXPAND AND TO DO EXTERNAL WORK WITH RESULTANT LIQUEFRACTION OF PART OF THE GAS, SEPARATING THE LIQUID FROM THE UNLIQUEFIED DRY GAS AND DISCHARGING THE LIQUID FROM THE SYSTEM, COMPRESSING DRY GAS TO A PRESSURE ABOVE THAT AT WHICH SEPARATION FROM THE LIQUID TOOK PLACE AND DISCHARGING SOME OF IT FROM THE SYSTEM, COMPRESSING THE REMAINING DRY GAS AND RECYCLING IT THROUGH THE SYSTEM, TO GETHER WITH FRESH GAS ADDED IN SUCH QUANTITY AS TO COMPENSATE FOR THE LIQUEFIED AND DRY GAS DISCHARGED FROM THE SYSTEM.
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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3020723A (en) * 1957-11-25 1962-02-13 Conch Int Methane Ltd Method and apparatus for liquefaction of natural gas
US3095293A (en) * 1960-11-30 1963-06-25 Phillips Petroleum Co Production and recovery of ethylene
US3210950A (en) * 1960-09-26 1965-10-12 Air Prod & Chem Separation of gaseous mixtures
DE1268161B (en) * 1963-02-23 1968-05-16 Linde Ag Process for the liquefaction of natural gas
US3735600A (en) * 1970-05-11 1973-05-29 Gulf Research Development Co Apparatus and process for liquefaction of natural gases
US4179897A (en) * 1975-08-25 1979-12-25 Air Products & Chemicals, Inc. Isentropic expansion of gases via a pelton wheel
US4419114A (en) * 1982-04-19 1983-12-06 Sappsucker, Inc. System and method for converting wellhead gas to liquefied petroleum gases (LPG)
US4462813A (en) * 1982-04-19 1984-07-31 Sappsucker, Inc. System and method for converting wellhead gas to liquefied petroleum gases (LPG)
US5473900A (en) * 1994-04-29 1995-12-12 Phillips Petroleum Company Method and apparatus for liquefaction of natural gas
US6105391A (en) * 1997-12-22 2000-08-22 Institut Francais Du Petrole Process for liquefying a gas, notably a natural gas or air, comprising a medium pressure drain and application
US20140083132A1 (en) * 2011-06-15 2014-03-27 Gasconsult Limited Process for liquefaction of natural gas
US20140165587A1 (en) * 2012-12-14 2014-06-19 Electro-Motive Diesel, Inc. System for converting gaseous fuel into liquid fuel

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1935749A (en) * 1927-01-25 1933-11-21 Schlumbohm Peter Vacuum refrigerating machine
US2355167A (en) * 1940-10-26 1944-08-08 Kellogg M W Co Process for the recovery of hydrocarbons
FR945298A (en) * 1946-06-07 1949-04-29 Escher Wyss & Cie Const Mec Installation for delivering fuel gas by a compressor
US2500129A (en) * 1944-08-29 1950-03-07 Clark Bros Co Inc Liquefaction system
US2557171A (en) * 1946-11-12 1951-06-19 Pritchard & Co J F Method of treating natural gas
US2601599A (en) * 1948-11-26 1952-06-24 Shell Dev Method of recovering liquefiable hydrocarbons from gases
US2696088A (en) * 1949-08-04 1954-12-07 Lee S Twomey Manipulation of nitrogen-contaminated natural gases
US2716332A (en) * 1950-04-20 1955-08-30 Koppers Co Inc Systems for separating nitrogen from natural gas

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1935749A (en) * 1927-01-25 1933-11-21 Schlumbohm Peter Vacuum refrigerating machine
US2355167A (en) * 1940-10-26 1944-08-08 Kellogg M W Co Process for the recovery of hydrocarbons
US2500129A (en) * 1944-08-29 1950-03-07 Clark Bros Co Inc Liquefaction system
FR945298A (en) * 1946-06-07 1949-04-29 Escher Wyss & Cie Const Mec Installation for delivering fuel gas by a compressor
US2557171A (en) * 1946-11-12 1951-06-19 Pritchard & Co J F Method of treating natural gas
US2601599A (en) * 1948-11-26 1952-06-24 Shell Dev Method of recovering liquefiable hydrocarbons from gases
US2696088A (en) * 1949-08-04 1954-12-07 Lee S Twomey Manipulation of nitrogen-contaminated natural gases
US2716332A (en) * 1950-04-20 1955-08-30 Koppers Co Inc Systems for separating nitrogen from natural gas

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3020723A (en) * 1957-11-25 1962-02-13 Conch Int Methane Ltd Method and apparatus for liquefaction of natural gas
US3210950A (en) * 1960-09-26 1965-10-12 Air Prod & Chem Separation of gaseous mixtures
US3095293A (en) * 1960-11-30 1963-06-25 Phillips Petroleum Co Production and recovery of ethylene
DE1268161B (en) * 1963-02-23 1968-05-16 Linde Ag Process for the liquefaction of natural gas
US3735600A (en) * 1970-05-11 1973-05-29 Gulf Research Development Co Apparatus and process for liquefaction of natural gases
US4179897A (en) * 1975-08-25 1979-12-25 Air Products & Chemicals, Inc. Isentropic expansion of gases via a pelton wheel
US4419114A (en) * 1982-04-19 1983-12-06 Sappsucker, Inc. System and method for converting wellhead gas to liquefied petroleum gases (LPG)
US4462813A (en) * 1982-04-19 1984-07-31 Sappsucker, Inc. System and method for converting wellhead gas to liquefied petroleum gases (LPG)
US5473900A (en) * 1994-04-29 1995-12-12 Phillips Petroleum Company Method and apparatus for liquefaction of natural gas
US6105391A (en) * 1997-12-22 2000-08-22 Institut Francais Du Petrole Process for liquefying a gas, notably a natural gas or air, comprising a medium pressure drain and application
US20140083132A1 (en) * 2011-06-15 2014-03-27 Gasconsult Limited Process for liquefaction of natural gas
US20140165587A1 (en) * 2012-12-14 2014-06-19 Electro-Motive Diesel, Inc. System for converting gaseous fuel into liquid fuel
US9309810B2 (en) * 2012-12-14 2016-04-12 Electro-Motive Diesel, Inc. System for converting gaseous fuel into liquid fuel

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