US2952984A - Processing liquefied natural gas - Google Patents
Processing liquefied natural gas Download PDFInfo
- 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
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 Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Combustion & Propulsion (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Separation By Low-Temperature Treatments (AREA)
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
NL240371D NL240371A (no) | 1958-06-23 | ||
BE579774D BE579774A (no) | 1958-06-23 | ||
US743732A US2952984A (en) | 1958-06-23 | 1958-06-23 | Processing liquefied natural gas |
DEC19159A DE1122560B (de) | 1958-06-23 | 1959-06-08 | Verfahren zur Zerlegung eines aus Methan und schwerer siedenden Kohlenwasserstoffen bestehenden Naturgases |
GB19587/59A GB854099A (en) | 1958-06-23 | 1959-06-08 | Improved method of processing natural gas |
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 (no) |
BE (1) | BE579774A (no) |
DE (1) | DE1122560B (no) |
FR (1) | FR1228634A (no) |
GB (1) | GB854099A (no) |
NL (1) | NL240371A (no) |
Cited By (61)
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 |
US20080190118A1 (en) * | 2007-02-12 | 2008-08-14 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Lng tank and unloading of lng from the tank |
US20080190136A1 (en) * | 2007-02-09 | 2008-08-14 | Ortloff Engineers, Ltd. | Hydrocarbon Gas Processing |
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 |
US20090199759A1 (en) * | 2008-02-11 | 2009-08-13 | 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 |
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)
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)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
BE534152A (no) * | 1953-12-16 |
-
0
- BE BE579774D patent/BE579774A/xx unknown
- NL NL240371D patent/NL240371A/xx unknown
-
1958
- 1958-06-23 US US743732A patent/US2952984A/en not_active Expired - Lifetime
-
1959
- 1959-06-08 DE DEC19159A patent/DE1122560B/de active Pending
- 1959-06-08 GB GB19587/59A patent/GB854099A/en not_active Expired
- 1959-06-18 FR FR797889A patent/FR1228634A/fr not_active Expired
Patent Citations (5)
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)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3548024A (en) * | 1963-10-14 | 1970-12-15 | Lummus Co | Regasification of liquefied natural gas at varying rates with ethylene recovery |
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 |
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 |
US20090293538A1 (en) * | 2001-06-08 | 2009-12-03 | Ortloff Engineers, Ltd. | Natural gas liquefaction |
US20050268649A1 (en) * | 2001-06-08 | 2005-12-08 | Ortloff Engineers, Ltd. | Natural gas liquefaction |
US7210311B2 (en) | 2001-06-08 | 2007-05-01 | Ortloff Engineers, Ltd. | Natural gas liquefaction |
US20040187520A1 (en) * | 2001-06-08 | 2004-09-30 | Wilkinson John D. | Natural gas liquefaction |
US7010937B2 (en) | 2001-06-08 | 2006-03-14 | Elkcorp | Natural gas liquefaction |
US20030158458A1 (en) * | 2002-02-20 | 2003-08-21 | Eric Prim | System and method for recovery of C2+ hydrocarbons contained in liquefied natural gas |
US7069743B2 (en) * | 2002-02-20 | 2006-07-04 | Eric Prim | System and method for recovery of C2+ hydrocarbons contained in liquefied natural gas |
US6945075B2 (en) | 2002-10-23 | 2005-09-20 | Elkcorp | Natural gas liquefaction |
US20040079107A1 (en) * | 2002-10-23 | 2004-04-29 | Wilkinson John D. | Natural gas liquefaction |
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 |
US7191617B2 (en) | 2003-02-25 | 2007-03-20 | 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 |
US7600396B2 (en) * | 2003-06-05 | 2009-10-13 | Fluor Technologies Corporation | Power cycle with liquefied natural gas regasification |
US20070101732A1 (en) * | 2003-06-05 | 2007-05-10 | John Mak | Power cycle with liquefied natural gas regasification |
US6986266B2 (en) * | 2003-09-22 | 2006-01-17 | Cryogenic Group, Inc. | Process and apparatus for LNG enriching in methane |
US20050061029A1 (en) * | 2003-09-22 | 2005-03-24 | Narinsky George B. | Process and apparatus for LNG enriching in methane |
WO2005035692A3 (en) * | 2003-09-30 | 2006-09-14 | Ortloff Engineers Ltd | Liquefied natural gas processing |
US7155931B2 (en) * | 2003-09-30 | 2007-01-02 | Ortloff Engineers, Ltd. | Liquefied natural gas processing |
US20050066686A1 (en) * | 2003-09-30 | 2005-03-31 | Elkcorp | 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 |
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 |
US20050218041A1 (en) * | 2004-04-05 | 2005-10-06 | 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 |
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 |
US20060000234A1 (en) * | 2004-07-01 | 2006-01-05 | Ortloff Engineers, Ltd. | Liquefied natural gas processing |
US7216507B2 (en) | 2004-07-01 | 2007-05-15 | 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 |
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 |
WO2006031362A1 (en) * | 2004-09-14 | 2006-03-23 | Exxonmobil Upstream Research Company | Method of extracting ethane from liquefied natural gas |
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 |
GB2434435B (en) * | 2004-09-29 | 2008-01-16 | Chevron Usa 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 |
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 |
WO2006039182A3 (en) * | 2004-09-29 | 2007-03-01 | 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 |
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 |
US8316665B2 (en) | 2005-03-30 | 2012-11-27 | Fluor Technologies Corporation | Integration 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 |
WO2006104799A3 (en) * | 2005-03-30 | 2006-12-21 | Fluor Tech Corp | Integrated 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 |
WO2006125759A1 (en) * | 2005-05-23 | 2006-11-30 | Shell Internationale Research Maatschappij B.V. | Fischer-tropsch plant |
US7631516B2 (en) * | 2006-06-02 | 2009-12-15 | 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 |
US20080000265A1 (en) * | 2006-06-02 | 2008-01-03 | Ortloff Engineers, Ltd. | Liquefied Natural Gas Processing |
US8590340B2 (en) | 2007-02-09 | 2013-11-26 | Ortoff Engineers, Ltd. | Hydrocarbon gas processing |
US20080190136A1 (en) * | 2007-02-09 | 2008-08-14 | Ortloff Engineers, Ltd. | Hydrocarbon Gas Processing |
US20080190118A1 (en) * | 2007-02-12 | 2008-08-14 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Lng tank and unloading of lng from the tank |
US10352499B2 (en) | 2007-02-12 | 2019-07-16 | 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 |
US10508769B2 (en) | 2007-02-12 | 2019-12-17 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | LNG tank and operation of the same |
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 |
US8820096B2 (en) | 2007-02-12 | 2014-09-02 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | LNG tank and operation of the same |
US20080190117A1 (en) * | 2007-02-12 | 2008-08-14 | 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 |
US20090211262A1 (en) * | 2007-02-12 | 2009-08-27 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Lng tank ship having lng circulating device |
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 |
US20090100862A1 (en) * | 2007-10-18 | 2009-04-23 | Ortloff Engineers, Ltd. | Hydrocarbon Gas Processing |
US8919148B2 (en) | 2007-10-18 | 2014-12-30 | 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 |
US7841288B2 (en) | 2008-02-11 | 2010-11-30 | 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 |
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 |
US8584488B2 (en) | 2008-08-06 | 2013-11-19 | Ortloff Engineers, Ltd. | Liquefied natural gas production |
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 |
US20100122542A1 (en) * | 2008-11-17 | 2010-05-20 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Method and apparatus for adjusting heating value of natural gas |
US8434325B2 (en) | 2009-05-15 | 2013-05-07 | Ortloff Engineers, Ltd. | Liquefied natural gas and hydrocarbon gas processing |
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 |
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 |
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 |
US9021832B2 (en) | 2010-01-14 | 2015-05-05 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US8667812B2 (en) | 2010-06-03 | 2014-03-11 | Ordoff Engineers, Ltd. | Hydrocabon gas processing |
US10551119B2 (en) | 2016-08-26 | 2020-02-04 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US10551118B2 (en) | 2016-08-26 | 2020-02-04 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US10533794B2 (en) | 2016-08-26 | 2020-01-14 | 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 |
---|---|
NL240371A (no) | |
BE579774A (no) | |
FR1228634A (fr) | 1960-08-31 |
DE1122560B (de) | 1962-01-25 |
GB854099A (en) | 1960-11-16 |
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 | |
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 | |
US2959020A (en) | Process for the liquefaction and reliquefaction of natural gas | |
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 | |
CN1318543C (zh) | 一种液化天然气的轻烃分离方法 | |
CN106256813A (zh) | 一种费托合成尾气的分离回收方法 | |
CN106866339A (zh) | 一种天然气中回收乙烷联产粗氦的装置及方法 | |
US3162519A (en) | Liquefaction of natural gas |