US2952984A - Processing liquefied natural gas - Google Patents

Processing liquefied natural gas Download PDF

Info

Publication number
US2952984A
US2952984A US743732A US74373258A US2952984A US 2952984 A US2952984 A US 2952984A US 743732 A US743732 A US 743732A US 74373258 A US74373258 A US 74373258A US 2952984 A US2952984 A US 2952984A
Authority
US
United States
Prior art keywords
natural gas
vapors
liquefied natural
methane
fractionating zone
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
US743732A
Other languages
English (en)
Inventor
Jr Walton H Marshall
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
Priority to BE579774D priority Critical patent/BE579774A/xx
Priority to NL240371D priority patent/NL240371A/xx
Application filed by Conch International Methane Ltd filed Critical Conch International Methane Ltd
Priority to US743732A priority patent/US2952984A/en
Priority to GB19587/59A priority patent/GB854099A/en
Priority to DEC19159A priority patent/DE1122560B/de
Priority to FR797889A priority patent/FR1228634A/fr
Application granted granted Critical
Publication of US2952984A publication Critical patent/US2952984A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F25J3/0214—Liquefied natural gas
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • 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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream 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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream 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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop

Definitions

  • This invention relates generally to improvements in the art of distributing and processing natural gas, and more particularly, but not by way of limitation, to an improved method of preparing liquefied natural gas for use as a fuel, or partly for use as a fuel and partly for use as raw material in the petrochemical industry.
  • the liquefied natural gas is revaporized and used as a fuel.
  • the natural gas can be revaporized and used directly as a fuel.
  • the gas specifications for existing equipment therein are different from the specifications of the revaporized natural gas, thereby requiring that the rev-aporized natural gas be reformed to a lower heating value and new specific gravity before use.
  • natural gas usually contains a rather wide range of hydrocarbons.
  • methane comprises the major proportion of the natural gas, with the heavier hydrocarbons such as ethane, propane, butane and the like being present in the gas in minor proportions. At least some of these heavier hydrocarbons can be separated before the natural gas is liquefied and transported to the remote localities.
  • These heavier hydrocarbons have two important uses at the remote localities.
  • the heavier hydrocarbons may be conveniently used in the formation of a carrier gas having a lower heating value and new specific gravity, with the carrier gas being subsequently mixed with methane to form the gaseous fuel having the desired heat content and specific gravity specificaitons.
  • the heavier hydrocarbons may be economically used as a raw material in the petrochemical industry in the remote locality.
  • the present invention contemplates a novel method of separating the methane and heavier hydrocarbons in liquefied natural gas, with a simultaneous revaporization of the methane.
  • the revaporization and separation are accomplished in a fractionating zone in such a manner that a portion of the heat in vapors withdrawn from the fractionating zone may be efiiciently utilized in heating the liquefied natural gas fed to the fractionating zone, and the resulting vapors will be extremely rich in methane, i.e., containing a very minor proportion of the heavier hydrocarbons.
  • Condensate formed in said vapors by passage in heat exchange relation with the liquefied natu- 2,952,984 Patented Sept.
  • the present method also contemplates the recovery of work from the separated methane, as well as the utilization of heat from the expanded methane vapors for Warming methane vapors being fed to the work-producing zone, such that the maximum energy of the separated methane may be utilized.
  • the separated heavier hydrocarbons may be used either in forming a carrier gas or as a raw material in the petrochemical industry, as previously indicated.
  • An important object of this invention is to provide an efficient method of separating methane from a liquefied natural gas with a minimum of equipment and cost.
  • Another object of this invention is to simultaneously separate methane fromliquefied natural gas and revapon'ze the methane.
  • a further object of this invention is to provide a novel method of fractionating liquefied natural gas, wherein the overhead from the fractionating zone is utilized to heat the liquefied natural gas being fed to the fractionating zone.
  • a still further object of this invention is to recover power in a process of revaporizing liquefied natural gas.
  • the single figure of the drawing is a flow diagram illustrating a practice of this invention.
  • natural gas ordinarily cornprises a rather wide range of hydrocarbons, and it is desirable that all of the hydrocarbons be liquefied prior to transporting the composition to a remote locality.
  • the liquefied naural gas to be separated and revaporized has the following analysis, although it will be understood that this composition is merely an example and. that the invention may be practiced with a liquefied natural gashaving substantially any composition:
  • reference character 10 designates a line leading from a sourcev (not shown) of the liquefied natural gas, which will ordinarily be a suitable insulated storage tank located in a coastal region where the liquefied natural gas may be received from similar insulated containers mounted aboard a ship used in transporting the gas to the remote locality-
  • the liquefied natural gas is ordinarily stored at. about atmospheric pressure, or slightly above, with a temperature of about 246 F. to 258 F., depending upon the precise composition of the gas.
  • This low pressure and cold liquefied gas is fed to a pump. 12 for pumping the liquefied natural gas through another line 14 to a fractionating tower 16 at increased pressure.
  • the pump 12 provide a substantial increase in the pressure of the liquefied natural gas, with the pressure being raised to about 585 p.s.i.g. to facilitate fractionation and subsequent power recovery, as, will be more fully hereinafter set forth.
  • a pair of heat exchangers 18 and 20 are interposed in the line 14 to. heat the liquefied natural gas being fed to the fractionating tower 16 3 until approximately the bubble point temperature of the liquefied natural gas is reached.
  • the liquefied natural gas being fed to the tower 16 is pressurized and then heated to approximately its bubble point.
  • the fractionating tower 16 may be of any desired con struction which provides a vertically extended fractionating zone.
  • the liquefied natural gas is, fed to the medial portion of the tower 16 and is slightly expanded, as from 585 p.s.i.g. to 535 p.s.i.g. into the tower 16 to facilitate separation of the methane from the heavier hydrocarbons.
  • the liquid accumulating in the lower end portion of the tower 16 is circulated through a re-boilcr 22 for heating the tower to such a temperature that methane enriched vapors will be directed into the upper portion of the tower, and the liquid in the lower portion of the tower will be enriched with the heavier hydrocarbons.
  • the liquid in the lower portion of the tower 16 is heated to a temperature of about 135 F. by the re-boiler 22.
  • the reboiler22 derives its heat from any suitable heating medium, such as a gaseous product from a reforming operation, to maintain the desired temperature of the liquid in the lower portion of the tower 16.
  • the liquid accumulating in the lower portion of the tower 16 is selectively withdrawn through a line 24 to maintain the desired liquid level in the tower.
  • a typical analysis of liquid withdrawn through the line 24 is as follows:
  • This liquid withdrawn through line'24 will, of course, be at the same pressure as the tower 16 and ata temperature of about 135 F. It is preferred that the liquid be passed through a suitable expansion valve 26 for at least partially vaporizing the liquid and reducing the pressure thereof to a pressure suitable for transportation through a pipeline 28 to the point of use. As previously indicated, these heavier hydrocarbons may be conveniently used in forming a carrier gas by a reforming operation or used as a raw material in a petrochemical industry.
  • the methane enriched vapors rising to the upper portion of the fractionating tower 16 are withdrawn through a'line 30 and passed through the heat exchanger 18 interposed in the liquefied natural gas feed line 14.
  • a typical analysis of the vapors withdrawn through the line 30 is as follows:
  • the vapors withdrawn through the line 30 will be at about 535 p.s.i.g. and l18 F.
  • the vapors will be cooled to about l20 F., whereas the liquefied natural gas will be slightly warmed to enhance the subsequent fractionation there of. Cooling of the methane enriched vapors directed through the line 30 condenses a' portion of the vapors. Therefore, the vapors are directed through a line 32 from the heat exchanger 18 into an accumulator 34 which also functions as a separator for collecting the condensates in the lower portion thereof. These condensates are refluxed to the upper portion of the tower 16 through a line 35. The refluxed condensates will'be at about 120 from the heavier hydrocarbons in the tower 16.
  • the refluxed condensates will'be at about 120 from the heavier hydrocarbons in the tower 16.
  • the vapors discharged through the line 36 will be at about 535 p.s.i.g. and about -l20 F. These vapors are passed through a series of heat exchangers 38, 40 and 42 to provide a substantial warming of the vapors. It is preferred that thermethane vapors be warmed by passage through the heat exchangers 38, 40 and 42 to a temperature of about 700 F. whereupon, the gas is expanded through a suitable expander 44 down to aboutp.s.i.g. for the recovery of a substantial amount of work from the revaporized methane.
  • the device 44 may be of any suitable form, such as a turbine, which will form a work-producing zone throughwhich the methane may be expanded to produce work.
  • the expander 44 should produce about 7400 B.H.P.; whereas the pump 12 for increasing :the'pressure of the liquefield natural gas will require only about 790 B.H.P., thereby resulting in a substantial power recovery, from the system.
  • the exhaust from the expander 44 is fed through a line 46 to the heat exchanger 40 to provide heating of the feed to the expander, as previously described.
  • the revaporized methane may be used directly as a fuel, or reformed to a lower heat content and new specific gravity, as previously indicated;
  • the revaporized methane discharging from the heat exchanger 40 will be at about 100 p.s.i.g. and 100 F.
  • the methane vapors passing from the line 36 to the heat exchanger 38 on their way to the expander 44 are initially heated by a heating medium passed through the heat exchanger 38.
  • the heating medium passed through the heat exchanger 38 may be of any suitable form having a temperature higher than the temperature of the methane vapors in the line 36.
  • the heating medium for the heat exchanger 38 may conveniently be a hot fluid from the reforming operation.
  • the heating medium passed through the heat exchanger 38 should have a temperature of about 81 F. This heating medium may then be transferred through a line 48 to the heat exchanger 20 used for heating the liquefied natural gas being fed to the fractionating tower 16.
  • the present invention provides an efiicient method for separating methane from liquefied natural gas by using the minimum of apparatus, and with a minimum of cost. It will be further apparent that the separation of the methane from the heavier hydrocarbon components of a liquefied natural gas stream is accomplished simultaneously with revaporization of the methane, such that the separted components will be in proper form for use as a fuel or for further processing. The method may be performed in such a manner that a substantial amount of work may be recovered from the revaporized methane.
  • the present invention provides a novel method of fractionating liquefield gases, wherein the overhead vapors from the fractionating zone are passed in heat exchange relation with the liquefied gases being fed to the fractionating zone, and wherein the resulting condensates are refluxed to the fractionating zone, to provide an efficient fractionation without the necessity of using a separate reflux condenser and refrigerant.
  • a method as defined in claim 1 characterized further in heating the liquefied natural gas being fed to the fractionating zone to such an extent that said feed is approximately at its bubble point upon entering the fractionating zone.
  • a method as defined in claim 1 characterized further in expanding said methane enriched vapors, after removal of the condensates therefrom, through a workproducing zone.
  • a method as defined in claim 1 characterized further in compressing the liquefied natural gas being fed to the fractionating zone.
  • a method as defined in claim 1 characterized further in compressing the liquefied natural gas being fed to the fractionating zone, and heating the compressed liquefied natural gas to approximately its bubble point temperature.
  • a method as defined in claim 6 characterized further in passing the expanded vapors in heat exchange relation with said vapors between removal of condensates from said vapors and expansion of said vapors.
  • a method as defined in claim 6 characterized further in heating the liquefied natural gas being fed to the fractionating zone to approximately the bubble point temperature thereof.
  • a method as defined in claim 6 characterized further in that the liquefied natural gas being fed to the fractionating zone is raised in pressure to about 585 p.s.i.g and heated to its bubble point temperature before entering the fractionating zone.
  • a method as defined in claim 6 characterized further in heating said vapors to about 700 F. before expansion in said work-producing zone.
  • a method of separating the lower boiling temperature component from a liquefied gas mixture by use of a fractionating tower the improvement which comprises feeding the liquefied gas mixture into the medial portion of the tower, re-boiling the contents of the lower portion of the tower to such a temperature to produce vapors enriched with the lower boiling temperature component in the upper portion of the tower, directly passing said vapors in heat exchange relation with the liquefied gas mixture being fed to the tower, separating condensates from said vapors, and refluxing said condensates back to the upper portion of the tower.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Water Supply & Treatment (AREA)
  • Analytical Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US743732A 1958-06-23 1958-06-23 Processing liquefied natural gas Expired - Lifetime US2952984A (en)

Priority Applications (6)

Application Number Priority Date Filing Date Title
BE579774D BE579774A (de) 1958-06-23
NL240371D NL240371A (de) 1958-06-23
US743732A US2952984A (en) 1958-06-23 1958-06-23 Processing liquefied natural gas
GB19587/59A GB854099A (en) 1958-06-23 1959-06-08 Improved method of processing natural gas
DEC19159A DE1122560B (de) 1958-06-23 1959-06-08 Verfahren zur Zerlegung eines aus Methan und schwerer siedenden Kohlenwasserstoffen bestehenden Naturgases
FR797889A FR1228634A (fr) 1958-06-23 1959-06-18 Procédé de traitement de gaz naturel liquéfié

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US743732A US2952984A (en) 1958-06-23 1958-06-23 Processing liquefied natural gas

Publications (1)

Publication Number Publication Date
US2952984A true US2952984A (en) 1960-09-20

Family

ID=24989951

Family Applications (1)

Application Number Title Priority Date Filing Date
US743732A Expired - Lifetime US2952984A (en) 1958-06-23 1958-06-23 Processing liquefied natural gas

Country Status (6)

Country Link
US (1) US2952984A (de)
BE (1) BE579774A (de)
DE (1) DE1122560B (de)
FR (1) FR1228634A (de)
GB (1) GB854099A (de)
NL (1) NL240371A (de)

Cited By (61)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3362175A (en) * 1964-08-10 1968-01-09 Conch Int Methane Ltd Method of fractionating natural gas feed by preheating feed with fractionator overhead
US3405530A (en) * 1966-09-23 1968-10-15 Exxon Research Engineering Co Regasification and separation of liquefied natural gas
US3433026A (en) * 1966-11-07 1969-03-18 Judson S Swearingen Staged isenthalpic-isentropic expansion of gas from a pressurized liquefied state to a terminal storage state
US3456032A (en) * 1963-10-14 1969-07-15 Lummus Co Utilization of propane recovered from liquefied natural gas
DE1551562A1 (de) * 1966-09-13 1970-05-06 Air Liquide Verfahren zur Herstellung eines methanreichen Fliessmittels aus verfluessigtem Naturgas unter niedrigem Anfangsdruck
US3524897A (en) * 1963-10-14 1970-08-18 Lummus Co Lng refrigerant for fractionator overhead
US3531942A (en) * 1968-02-12 1970-10-06 James K La Fleur Cryogenic separation of fluids associated with a power cycle
US3548024A (en) * 1963-10-14 1970-12-15 Lummus Co Regasification of liquefied natural gas at varying rates with ethylene recovery
US3656312A (en) * 1967-12-15 1972-04-18 Messer Griesheim Gmbh Process for separating a liquid gas mixture containing methane
US3837172A (en) * 1972-06-19 1974-09-24 Synergistic Services Inc Processing liquefied natural gas to deliver methane-enriched gas at high pressure
US3846993A (en) * 1971-02-01 1974-11-12 Phillips Petroleum Co Cryogenic extraction process for natural gas liquids
US4690702A (en) * 1984-09-28 1987-09-01 Compagnie Francaise D'etudes Et De Construction "Technip" Method and apparatus for cryogenic fractionation of a gaseous feed
US5114451A (en) * 1990-03-12 1992-05-19 Elcor Corporation Liquefied natural gas processing
US5600969A (en) * 1995-12-18 1997-02-11 Phillips Petroleum Company Process and apparatus to produce a small scale LNG stream from an existing NGL expander plant demethanizer
US6510706B2 (en) 2000-05-31 2003-01-28 Exxonmobil Upstream Research Company Process for NGL recovery from pressurized liquid natural gas
US20030158458A1 (en) * 2002-02-20 2003-08-21 Eric Prim System and method for recovery of C2+ hydrocarbons contained in liquefied natural gas
US20040079107A1 (en) * 2002-10-23 2004-04-29 Wilkinson John D. Natural gas liquefaction
US20040177646A1 (en) * 2003-03-07 2004-09-16 Elkcorp LNG production in cryogenic natural gas processing plants
US20040187520A1 (en) * 2001-06-08 2004-09-30 Wilkinson John D. Natural gas liquefaction
US20050061029A1 (en) * 2003-09-22 2005-03-24 Narinsky George B. Process and apparatus for LNG enriching in methane
US20050066686A1 (en) * 2003-09-30 2005-03-31 Elkcorp Liquefied natural gas processing
US20050218041A1 (en) * 2004-04-05 2005-10-06 Toyo Engineering Corporation Process and apparatus for separation of hydrocarbons from liquefied natural gas
US20050247078A1 (en) * 2004-05-04 2005-11-10 Elkcorp Natural gas liquefaction
US20060000234A1 (en) * 2004-07-01 2006-01-05 Ortloff Engineers, Ltd. Liquefied natural gas processing
US20060032269A1 (en) * 2003-02-25 2006-02-16 Ortloff Engineers, Ltd. Hydrocarbon gas processing
WO2006031362A1 (en) * 2004-09-14 2006-03-23 Exxonmobil Upstream Research Company Method of extracting ethane from liquefied natural gas
US20060065015A1 (en) * 2004-09-29 2006-03-30 Chevron U.S.A. Inc. Recovering natural gas liquids from LNG using vacuum distillation
US20060131218A1 (en) * 2004-12-17 2006-06-22 Abb Lummus Global Inc. Method for recovery of natural gas liquids for liquefied natural gas
US20060130520A1 (en) * 2004-12-17 2006-06-22 Abb Lummus Global Inc. Method for recovery of natural gas liquids for liquefied natural gas
US20060130521A1 (en) * 2004-12-17 2006-06-22 Abb Lummus Global Inc. Method for recovery of natural gas liquids for liquefied natural gas
WO2006104799A2 (en) * 2005-03-30 2006-10-05 Fluor Technologies Corporation Integrated of lng regasification with refinery and power generation
WO2006125759A1 (en) * 2005-05-23 2006-11-30 Shell Internationale Research Maatschappij B.V. Fischer-tropsch plant
US20070101732A1 (en) * 2003-06-05 2007-05-10 John Mak Power cycle with liquefied natural gas regasification
US20080000265A1 (en) * 2006-06-02 2008-01-03 Ortloff Engineers, Ltd. Liquefied Natural Gas Processing
US20080190136A1 (en) * 2007-02-09 2008-08-14 Ortloff Engineers, Ltd. Hydrocarbon Gas Processing
US20080190352A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship and operation thereof
US20080295527A1 (en) * 2007-05-31 2008-12-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship with nitrogen generator and method of operating the same
US20090056371A1 (en) * 2005-03-22 2009-03-05 Paramasivam Senthil Kumar Method and Apparatus for Deriching a Stream of Liquefied Natural Gas
US20090100862A1 (en) * 2007-10-18 2009-04-23 Ortloff Engineers, Ltd. Hydrocarbon Gas Processing
US20090199591A1 (en) * 2008-02-11 2009-08-13 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Liquefied natural gas with butane and method of storing and processing the same
US20090259081A1 (en) * 2008-04-10 2009-10-15 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and system for reducing heating value of natural gas
US20090266086A1 (en) * 2007-04-30 2009-10-29 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Floating marine structure having lng circulating device
US20100011663A1 (en) * 2008-07-18 2010-01-21 Kellogg Brown & Root Llc Method for Liquefaction of Natural Gas
US20100031700A1 (en) * 2008-08-06 2010-02-11 Ortloff Engineers, Ltd. Liquefied natural gas and hydrocarbon gas processing
US20100122542A1 (en) * 2008-11-17 2010-05-20 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and apparatus for adjusting heating value of natural gas
CN101160498B (zh) * 2004-08-27 2010-10-13 阿梅克帕拉贡公司 一种从lng中提取乙烷和重烃的方法
US20100287982A1 (en) * 2009-05-15 2010-11-18 Ortloff Engineers, Ltd. Liquefied Natural Gas and Hydrocarbon Gas Processing
US20110067443A1 (en) * 2009-09-21 2011-03-24 Ortloff Engineers, Ltd. Hydrocarbon Gas Processing
US20110167868A1 (en) * 2010-01-14 2011-07-14 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US8434325B2 (en) 2009-05-15 2013-05-07 Ortloff Engineers, Ltd. Liquefied natural gas and hydrocarbon gas processing
US8667812B2 (en) 2010-06-03 2014-03-11 Ordoff Engineers, Ltd. Hydrocabon gas processing
US8850849B2 (en) 2008-05-16 2014-10-07 Ortloff Engineers, Ltd. Liquefied natural gas and hydrocarbon gas processing
US9360249B2 (en) 2004-01-16 2016-06-07 Ihi E&C International Corporation Gas conditioning process for the recovery of LPG/NGL (C2+) from LNG
US10533794B2 (en) 2016-08-26 2020-01-14 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US10551118B2 (en) 2016-08-26 2020-02-04 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US10551119B2 (en) 2016-08-26 2020-02-04 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US11274256B2 (en) 2017-11-06 2022-03-15 Toyo Engineering Corporation Apparatus for separation and recovery of hydrocarbons from LNG
US11408678B2 (en) 2017-11-01 2022-08-09 Toyo Engineering Corporation Method and apparatus for separating hydrocarbons
US11428465B2 (en) 2017-06-01 2022-08-30 Uop Llc Hydrocarbon gas processing
US11543180B2 (en) 2017-06-01 2023-01-03 Uop Llc Hydrocarbon gas processing
US11692771B2 (en) 2019-08-28 2023-07-04 Toyo Engineering Corporation Process and apparatus for treating lean LNG

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1465599A (en) * 1918-06-01 1923-08-21 Brey Jan Heinrich Christoph De Process for treating hydrocarbons
US2526996A (en) * 1947-02-21 1950-10-24 Elliott Co Method and apparatus for separating mixed gases
US2583090A (en) * 1950-12-29 1952-01-22 Elliott Co Separation of natural gas mixtures
US2600110A (en) * 1949-01-04 1952-06-10 Phillips Petroleum Co Fractional distillation method
US2666019A (en) * 1950-07-28 1954-01-12 Socony Vacuum Oil Co Inc Method for recovering propane and heavier hydrocarbons

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL83696C (de) * 1953-12-16

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1465599A (en) * 1918-06-01 1923-08-21 Brey Jan Heinrich Christoph De Process for treating hydrocarbons
US2526996A (en) * 1947-02-21 1950-10-24 Elliott Co Method and apparatus for separating mixed gases
US2600110A (en) * 1949-01-04 1952-06-10 Phillips Petroleum Co Fractional distillation method
US2666019A (en) * 1950-07-28 1954-01-12 Socony Vacuum Oil Co Inc Method for recovering propane and heavier hydrocarbons
US2583090A (en) * 1950-12-29 1952-01-22 Elliott Co Separation of natural gas mixtures

Cited By (121)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3456032A (en) * 1963-10-14 1969-07-15 Lummus Co Utilization of propane recovered from liquefied natural gas
US3524897A (en) * 1963-10-14 1970-08-18 Lummus Co Lng refrigerant for fractionator overhead
US3548024A (en) * 1963-10-14 1970-12-15 Lummus Co Regasification of liquefied natural gas at varying rates with ethylene recovery
US3362175A (en) * 1964-08-10 1968-01-09 Conch Int Methane Ltd Method of fractionating natural gas feed by preheating feed with fractionator overhead
DE1551562A1 (de) * 1966-09-13 1970-05-06 Air Liquide Verfahren zur Herstellung eines methanreichen Fliessmittels aus verfluessigtem Naturgas unter niedrigem Anfangsdruck
US3405530A (en) * 1966-09-23 1968-10-15 Exxon Research Engineering Co Regasification and separation of liquefied natural gas
US3433026A (en) * 1966-11-07 1969-03-18 Judson S Swearingen Staged isenthalpic-isentropic expansion of gas from a pressurized liquefied state to a terminal storage state
US3656312A (en) * 1967-12-15 1972-04-18 Messer Griesheim Gmbh Process for separating a liquid gas mixture containing methane
US3531942A (en) * 1968-02-12 1970-10-06 James K La Fleur Cryogenic separation of fluids associated with a power cycle
US3846993A (en) * 1971-02-01 1974-11-12 Phillips Petroleum Co Cryogenic extraction process for natural gas liquids
US3837172A (en) * 1972-06-19 1974-09-24 Synergistic Services Inc Processing liquefied natural gas to deliver methane-enriched gas at high pressure
US4690702A (en) * 1984-09-28 1987-09-01 Compagnie Francaise D'etudes Et De Construction "Technip" Method and apparatus for cryogenic fractionation of a gaseous feed
US5114451A (en) * 1990-03-12 1992-05-19 Elcor Corporation Liquefied natural gas processing
US5600969A (en) * 1995-12-18 1997-02-11 Phillips Petroleum Company Process and apparatus to produce a small scale LNG stream from an existing NGL expander plant demethanizer
US6510706B2 (en) 2000-05-31 2003-01-28 Exxonmobil Upstream Research Company Process for NGL recovery from pressurized liquid natural gas
US20040187520A1 (en) * 2001-06-08 2004-09-30 Wilkinson John D. Natural gas liquefaction
US20050268649A1 (en) * 2001-06-08 2005-12-08 Ortloff Engineers, Ltd. Natural gas liquefaction
US20090293538A1 (en) * 2001-06-08 2009-12-03 Ortloff Engineers, Ltd. Natural gas liquefaction
US7010937B2 (en) 2001-06-08 2006-03-14 Elkcorp Natural gas liquefaction
US7210311B2 (en) 2001-06-08 2007-05-01 Ortloff Engineers, Ltd. Natural gas liquefaction
US7069743B2 (en) * 2002-02-20 2006-07-04 Eric Prim System and method for recovery of C2+ hydrocarbons contained in liquefied natural gas
US20030158458A1 (en) * 2002-02-20 2003-08-21 Eric Prim System and method for recovery of C2+ hydrocarbons contained in liquefied natural gas
US20040079107A1 (en) * 2002-10-23 2004-04-29 Wilkinson John D. Natural gas liquefaction
US6945075B2 (en) 2002-10-23 2005-09-20 Elkcorp Natural gas liquefaction
US7191617B2 (en) 2003-02-25 2007-03-20 Ortloff Engineers, Ltd. Hydrocarbon gas processing
EA008462B1 (ru) * 2003-02-25 2007-06-29 Ортлофф Инджинирс, Лтд. Переработка углеводородного газа
US20060032269A1 (en) * 2003-02-25 2006-02-16 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US6889523B2 (en) 2003-03-07 2005-05-10 Elkcorp LNG production in cryogenic natural gas processing plants
US20040177646A1 (en) * 2003-03-07 2004-09-16 Elkcorp LNG production in cryogenic natural gas processing plants
US20070101732A1 (en) * 2003-06-05 2007-05-10 John Mak Power cycle with liquefied natural gas regasification
US7600396B2 (en) * 2003-06-05 2009-10-13 Fluor Technologies Corporation Power cycle with liquefied natural gas regasification
US20050061029A1 (en) * 2003-09-22 2005-03-24 Narinsky George B. Process and apparatus for LNG enriching in methane
US6986266B2 (en) * 2003-09-22 2006-01-17 Cryogenic Group, Inc. Process and apparatus for LNG enriching in methane
US20050066686A1 (en) * 2003-09-30 2005-03-31 Elkcorp Liquefied natural gas processing
US7155931B2 (en) * 2003-09-30 2007-01-02 Ortloff Engineers, Ltd. Liquefied natural gas processing
CN100406832C (zh) * 2003-09-30 2008-07-30 奥特洛夫工程有限公司 液化天然气的处理
KR101118803B1 (ko) 2003-09-30 2012-03-22 오르트로프 엔지니어스, 리미티드 액화천연가스 가공
WO2005035692A2 (en) * 2003-09-30 2005-04-21 Ortloff Engineers, Ltd Liquefied natural gas processing
WO2005035692A3 (en) * 2003-09-30 2006-09-14 Ortloff Engineers Ltd Liquefied natural gas processing
US9360249B2 (en) 2004-01-16 2016-06-07 Ihi E&C International Corporation Gas conditioning process for the recovery of LPG/NGL (C2+) from LNG
US7310972B2 (en) 2004-04-05 2007-12-25 Toyo Engineering Corporation Process and apparatus for separation of hydrocarbons from liquefied natural gas
US20080022717A1 (en) * 2004-04-05 2008-01-31 Toyo Engineering Corporation Process and apparatus for separation of hydrocarbons from liquefied natural gas
US20050218041A1 (en) * 2004-04-05 2005-10-06 Toyo Engineering Corporation Process and apparatus for separation of hydrocarbons from liquefied natural gas
US7204100B2 (en) 2004-05-04 2007-04-17 Ortloff Engineers, Ltd. Natural gas liquefaction
US20050247078A1 (en) * 2004-05-04 2005-11-10 Elkcorp Natural gas liquefaction
US7216507B2 (en) 2004-07-01 2007-05-15 Ortloff Engineers, Ltd. Liquefied natural gas processing
US20060000234A1 (en) * 2004-07-01 2006-01-05 Ortloff Engineers, Ltd. Liquefied natural gas processing
CN101160498B (zh) * 2004-08-27 2010-10-13 阿梅克帕拉贡公司 一种从lng中提取乙烷和重烃的方法
AU2005285436B2 (en) * 2004-09-14 2010-09-16 Exxonmobil Upstream Research Company Method of extracting ethane from liquefied natural gas
US20080087041A1 (en) * 2004-09-14 2008-04-17 Denton Robert D Method of Extracting Ethane from Liquefied Natural Gas
WO2006031362A1 (en) * 2004-09-14 2006-03-23 Exxonmobil Upstream Research Company 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
CN101027528B (zh) * 2004-09-14 2011-06-15 埃克森美孚上游研究公司 加工液化天然气lng的方法和系统
GB2434435B (en) * 2004-09-29 2008-01-16 Chevron Usa Inc Recovering natural gas liquids from LNG using vacuum distillation
AU2005292419B2 (en) * 2004-09-29 2011-03-17 Chevron U.S.A. Inc. Recovering natural gas liquids from LNG using vacuum distillation
GB2434435A (en) * 2004-09-29 2007-07-25 Chevron Usa Inc Recovering natural gas liquids from LNG using vacuum distillation
US7234323B2 (en) * 2004-09-29 2007-06-26 Chevron U.S.A. Inc. Recovering natural gas liquids from LNG using vacuum distillation
US20060065015A1 (en) * 2004-09-29 2006-03-30 Chevron U.S.A. Inc. Recovering natural gas liquids from LNG using vacuum distillation
WO2006039182A3 (en) * 2004-09-29 2007-03-01 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
US20060130521A1 (en) * 2004-12-17 2006-06-22 Abb Lummus Global Inc. Method for recovery of natural gas liquids for liquefied natural gas
US20060131218A1 (en) * 2004-12-17 2006-06-22 Abb Lummus Global Inc. Method for recovery of natural gas liquids for liquefied natural gas
US20060130520A1 (en) * 2004-12-17 2006-06-22 Abb Lummus Global Inc. Method for recovery of natural gas liquids for liquefied natural gas
US20090056371A1 (en) * 2005-03-22 2009-03-05 Paramasivam Senthil Kumar Method and Apparatus for Deriching a Stream of Liquefied Natural Gas
WO2006104799A2 (en) * 2005-03-30 2006-10-05 Fluor Technologies Corporation Integrated of lng regasification with refinery and power generation
US20080307789A1 (en) * 2005-03-30 2008-12-18 Fluor Technologies Corporation Integration of Lng Regasification with Refinery and Power Generation
US8316665B2 (en) 2005-03-30 2012-11-27 Fluor Technologies Corporation Integration of LNG regasification with refinery and power generation
EA011918B1 (ru) * 2005-03-30 2009-06-30 Флуор Текнолоджиз Корпорейшн Объединенная установка для регазификации сжиженного природного газа и разделения компонентов сопутствующего газа
WO2006104799A3 (en) * 2005-03-30 2006-12-21 Fluor Tech Corp Integrated of lng regasification with refinery and power generation
WO2006125759A1 (en) * 2005-05-23 2006-11-30 Shell Internationale Research Maatschappij B.V. Fischer-tropsch plant
US20080000265A1 (en) * 2006-06-02 2008-01-03 Ortloff Engineers, Ltd. Liquefied Natural Gas Processing
WO2008066570A3 (en) * 2006-06-02 2008-07-31 Ortloff Engineers Ltd Liquefied natural gas processing
WO2008066570A2 (en) * 2006-06-02 2008-06-05 Ortloff Engineers, Ltd Liquefied natural gas processing
US7631516B2 (en) * 2006-06-02 2009-12-15 Ortloff Engineers, Ltd. Liquefied natural gas processing
US20080190136A1 (en) * 2007-02-09 2008-08-14 Ortloff Engineers, Ltd. Hydrocarbon Gas Processing
US8590340B2 (en) 2007-02-09 2013-11-26 Ortoff Engineers, Ltd. Hydrocarbon gas processing
US10352499B2 (en) 2007-02-12 2019-07-16 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US8820096B2 (en) 2007-02-12 2014-09-02 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US8028724B2 (en) 2007-02-12 2011-10-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and unloading of LNG from the tank
US20080190352A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship and operation thereof
US8943841B2 (en) 2007-02-12 2015-02-03 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank ship having LNG circulating device
US20080190117A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and operation of the same
US20090211262A1 (en) * 2007-02-12 2009-08-27 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship having lng circulating device
US10508769B2 (en) 2007-02-12 2019-12-17 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US11168837B2 (en) 2007-02-12 2021-11-09 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US20080190118A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and unloading of lng from the tank
US20090266086A1 (en) * 2007-04-30 2009-10-29 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Floating marine structure having lng circulating device
US20080295527A1 (en) * 2007-05-31 2008-12-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship with nitrogen generator and method of operating the same
US8919148B2 (en) 2007-10-18 2014-12-30 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US20090100862A1 (en) * 2007-10-18 2009-04-23 Ortloff Engineers, Ltd. Hydrocarbon Gas Processing
US20090199591A1 (en) * 2008-02-11 2009-08-13 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Liquefied natural gas with butane and method of storing and processing the same
US20090199759A1 (en) * 2008-02-11 2009-08-13 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US7644676B2 (en) 2008-02-11 2010-01-12 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US7841288B2 (en) 2008-02-11 2010-11-30 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US20100012015A1 (en) * 2008-02-11 2010-01-21 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US20090259081A1 (en) * 2008-04-10 2009-10-15 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and system for reducing heating value of natural gas
US9086188B2 (en) 2008-04-10 2015-07-21 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and system for reducing heating value of natural gas
US8850849B2 (en) 2008-05-16 2014-10-07 Ortloff Engineers, Ltd. Liquefied natural gas and hydrocarbon gas processing
US20100011663A1 (en) * 2008-07-18 2010-01-21 Kellogg Brown & Root Llc Method for Liquefaction of Natural Gas
US8381544B2 (en) 2008-07-18 2013-02-26 Kellogg Brown & Root Llc Method for liquefaction of natural gas
US20100031700A1 (en) * 2008-08-06 2010-02-11 Ortloff Engineers, Ltd. Liquefied natural gas and hydrocarbon gas processing
US20110120183A9 (en) * 2008-08-06 2011-05-26 Ortloff Engineers, Ltd. Liquefied natural gas and hydrocarbon gas processing
US8584488B2 (en) 2008-08-06 2013-11-19 Ortloff Engineers, Ltd. Liquefied natural gas production
US20100122542A1 (en) * 2008-11-17 2010-05-20 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and apparatus for adjusting heating value of natural gas
US20100287982A1 (en) * 2009-05-15 2010-11-18 Ortloff Engineers, Ltd. Liquefied Natural Gas and Hydrocarbon Gas Processing
US8794030B2 (en) 2009-05-15 2014-08-05 Ortloff Engineers, Ltd. Liquefied natural gas and hydrocarbon gas processing
US8434325B2 (en) 2009-05-15 2013-05-07 Ortloff Engineers, Ltd. Liquefied natural gas and hydrocarbon gas processing
US20110067443A1 (en) * 2009-09-21 2011-03-24 Ortloff Engineers, Ltd. Hydrocarbon Gas Processing
US20110067442A1 (en) * 2009-09-21 2011-03-24 Ortloff Engineers, Ltd. Hydrocarbon Gas Processing
US9476639B2 (en) 2009-09-21 2016-10-25 Ortloff Engineers, Ltd. Hydrocarbon gas processing featuring a compressed reflux stream formed by combining a portion of column residue gas with a distillation vapor stream withdrawn from the side of the column
US9021832B2 (en) 2010-01-14 2015-05-05 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US20110167868A1 (en) * 2010-01-14 2011-07-14 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US8667812B2 (en) 2010-06-03 2014-03-11 Ordoff Engineers, Ltd. Hydrocabon gas processing
US10533794B2 (en) 2016-08-26 2020-01-14 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US10551118B2 (en) 2016-08-26 2020-02-04 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US10551119B2 (en) 2016-08-26 2020-02-04 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US11428465B2 (en) 2017-06-01 2022-08-30 Uop Llc Hydrocarbon gas processing
US11543180B2 (en) 2017-06-01 2023-01-03 Uop Llc Hydrocarbon gas processing
US11408678B2 (en) 2017-11-01 2022-08-09 Toyo Engineering Corporation Method and apparatus for separating hydrocarbons
US11274256B2 (en) 2017-11-06 2022-03-15 Toyo Engineering Corporation Apparatus for separation and recovery of hydrocarbons from LNG
US11692771B2 (en) 2019-08-28 2023-07-04 Toyo Engineering Corporation Process and apparatus for treating lean LNG

Also Published As

Publication number Publication date
GB854099A (en) 1960-11-16
FR1228634A (fr) 1960-08-31
NL240371A (de)
BE579774A (de)
DE1122560B (de) 1962-01-25

Similar Documents

Publication Publication Date Title
US2952984A (en) Processing liquefied natural gas
US3292380A (en) Method and equipment for treating hydrocarbon gases for pressure reduction and condensate recovery
US3413817A (en) Liquefaction of natural gas at supercritical pressure employing a single refrigeration cycle
CN101506606B (zh) 用于处理烃物流的方法和设备
US2603310A (en) Method of and apparatus for separating the constituents of hydrocarbon gases
US2577701A (en) Fractionation process
US3846993A (en) Cryogenic extraction process for natural gas liquids
US2960837A (en) Liquefying natural gas with low pressure refrigerants
US3479832A (en) Process for vaporizing liquefied natural gas
US3524897A (en) Lng refrigerant for fractionator overhead
US3393527A (en) Method of fractionating natural gas to remove heavy hydrocarbons therefrom
CN100392052C (zh) 一种用于燃气调峰和轻烃回收的天然气液化方法
CA1098816A (en) Liquefaction of gas
US2812646A (en) Manipulation of nitrogen-contaminated natural gases
CN102272544B (zh) 用于在lng液化设备中脱氮和/或回收氦气的方法
US2535148A (en) Method of storing natural gas
US2475957A (en) Treatment of natural gas
CN88100540A (zh) 从烃气中回收丙烷和重烃的方法
US3119677A (en) Separation of gases
CN107940893A (zh) 采用冷能轻烃回收的lng冷能梯级利用方法
CN110538476A (zh) 一种用于油田伴生气的低温闪蒸轻烃回收系统及方法
CN106256813A (zh) 一种费托合成尾气的分离回收方法
US3162519A (en) Liquefaction of natural gas
US10126049B2 (en) Method and apparatus for removing benzene contaminants from natural gas
US3407613A (en) Enrichment of natural gas in c2+ hydrocarbons