US3593535A - Liquefaction of natural gas employing multiple-component refrigerants - Google Patents
Liquefaction of natural gas employing multiple-component refrigerants Download PDFInfo
- Publication number
- US3593535A US3593535A US882781A US3593535DA US3593535A US 3593535 A US3593535 A US 3593535A US 882781 A US882781 A US 882781A US 3593535D A US3593535D A US 3593535DA US 3593535 A US3593535 A US 3593535A
- Authority
- US
- United States
- Prior art keywords
- liquid
- heat exchange
- refrigerant
- multicomponent
- fraction
- 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
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 239000003507 refrigerant Substances 0.000 title claims abstract description 77
- 239000003345 natural gas Substances 0.000 title claims abstract description 22
- 230000003247 decreasing effect Effects 0.000 claims abstract description 4
- 230000000750 progressive effect Effects 0.000 claims abstract description 4
- 239000007788 liquid Substances 0.000 claims description 72
- 229930195733 hydrocarbon Natural products 0.000 claims description 17
- 150000002430 hydrocarbons Chemical class 0.000 claims description 17
- 238000009835 boiling Methods 0.000 claims description 14
- 239000012530 fluid Substances 0.000 claims description 9
- 238000005194 fractionation Methods 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 5
- 230000008016 vaporization Effects 0.000 claims description 5
- 239000004215 Carbon black (E152) Substances 0.000 claims description 4
- 238000005507 spraying Methods 0.000 claims description 4
- 241000269627 Amphiuma means Species 0.000 claims description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 239000007921 spray Substances 0.000 description 9
- 238000001816 cooling Methods 0.000 description 6
- 239000003949 liquefied natural gas Substances 0.000 description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 6
- 230000009467 reduction Effects 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000007792 gaseous phase Substances 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/0231—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the working-up of the hydrocarbon feed, e.g. reinjection of heavier hydrocarbons into the liquefied gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0234—Integration with a cryogenic air separation unit
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
- F25J1/0238—Purification or treatment step is integrated within one refrigeration cycle only, i.e. the same or single refrigeration cycle provides feed gas cooling (if present) and overhead gas cooling
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
- F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
- F25J1/025—Details related to the refrigerant production or treatment, e.g. make-up supply from feed gas itself
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0258—Construction and layout of liquefaction equipments, e.g. valves, machines vertical layout of the equipments within in the cold box
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
-
- 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
- F25J3/04—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 for air
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
-
- 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
Definitions
- a system for liquefying a feed stream composed primarily of methane comprising:
- multistage heat exchanger means for passing each of said expanded liquid condensates in countercurrent heat exchange with said feed stream at progressively lower temperature stages for liquefying said feed stream, said multistage heat exchanger means including a final lowest temperature stage, at least said lowest temperature stage comprising a vertically extending coil through which said feed stream is passed upwardly, and means for spraying said lowest temperature liquid condensate downwardly over said coil.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Natural gas is liquefied by heat exchange with a multicomponent refrigerant. The respective refrigerant components in the order of increasing volatility are heat exchanged serially with the natural gas stream at progressive points along zones of decreasing temperature.
Description
United States Patent Inventors Lee S. Gaumer, Jr. [56] References Cited g lgs f E UNITED STATES PATENTS App No 3,205,669 9/1965 Grossman .4 62/23 Fued Dec. 22, 1969 3,315,477 4/1967 Carr 62/23 Patented July 20, 1971 FOREIGN PATENTS Assignee Air Products and Chemicals, Inc. 1,302,989 7/1962 France 62/40 Allentown, Pa. AD 80.294 2/1963 France 62/40 Continuation of application Ser. No. OTHER REFERENCES 722,135, Apr. 17, 1968, now abandoned which is a continuation of application Sen 921605;: a1nmlllifliggseratio; -icgegnce and Technology, Vol. 1 No. 468,008, June 29, 1965, now abandoned. g pp Primary Examiner-Norman Yudltoftj Attaineys- Ronald B Sherer and B. Max Klevit LlQUEF ACTION OF NATURAL GAS EMPLOYING gigglrllfliisfgvhilnlggllflENT REFRIG ERANTS ABSTRACT:
Natural gas is liquefied by heat exchange with a multicom US. Cl 62/23, ponent refrigerant, The respective refrigerant components in 62/40 the order of increasing volatility are heat exchanged serially Int. Cl with the natural gas stream at progressive points along zones Field of Search of decreasing temperature.
58 ABSORBER 90 4 NATURAL H s FUEL GAS FEED 54 E 56 Y 122 I LNG 64 72 STORAGE 70 3 s2 PLANT FUEL 32 4 68 FRACTIONATION 13e- PLANT I40 52 50 K A A NATURAL GASOLINE :T 1 7 5;
AIR SEPARATION 44 E;
PLANT {34 183 i MULTl-COMPONENT 124 REFRIGERANT') LIQUEFACTION OF NATURAL GAS EMPLOYING MULTIPLE-COMPONENT REFRIG ERANTS This application is a continuation of application Ser. No. 722,135, filed Apr. 17, 1968 now abandoned, which is a continuation of application Ser. No. 468,008 filed June 29, i965 now abandoned.
LIQUEFACTION OF NATURAL GAS The present invention relates to the liquefaction of low boiling point gases and, more particularly, to an improved method and apparatus particularly designed for liquefying natural gas with a substantial reduction in the cost of the liquefaction facility as compared to previous liquefaction cycles of the cascade-type wherein the process stream is heat exchanged with different refrigerants circulated in independent closed loops.
The above-indicated object, as well as other objects relating more particularly to specific structural and functional advantages, will become more fully apparent form the following description when taken with the accompanying drawing wherein the sole Figure is a simplified and schematic diagram illustrating the major flow circuits comprising the complete liquefaction facility or plant.
Referring first to the upper left-hand portion of the drawing,
-the natural gas feed is supplied to the liquefaction plant through a pipeline as a two-phase mixture having a major portion in the gaseous phase and a minor portion in the liquid phase. This feed mixture is initially separated in a separator 12 from which the minor portion is withdrawn at the bottom as a liquid and pressurized by a liquid pump 14. The major portion is withdrawn in the gaseous phase from the top of the drum, compressed in compressor 16 and heat exchanged with cooling water in exchanger 18. The two portions of the feed are then joined and expanded into a flash drum 20 wherein a portion of the original gaseous feed is liquified and mixes with that portion of the feed which was initially in the liquid phase. The total liquid comprising most of the heavy hydrocarbons (i.e., heavier than C hydrocarbons) is then hydrocarbons from the bottom of flash drum 20 and supplied through a line 22 to a conventional fractionation plant 23 the general operation of which will be described hereinafter although the particular details of the plant form no part of the present invention. The gaseous fraction of the feed comprising most of the methane, nitrogen and the C to C hydrocarbons is withdrawn from the top of flash drum 20 and passed through one or more conventional absorbers 24 which remove, impurities such as hydrogen sulfide and carbon dioxide. The gaseous feed is then slightly cooled by heat exchange with cooling water in exchanger 26 and passed through line 28 to the lowermost heat exchanger coil 30 located in the bottom of main heat exchanger 32 wherein the stream is sufficiently cooled so that the water and most of the C and C hydrocarbons are condensed and separated out in the first stage 34 of a two-stage separator 36. The major portion of the stream is withdrawn in the gaseous phase through line 38 and is passed through one or more driers 40 wherein the remaining water is removed. After drying, the main stream flows through line 42 to intermediate heat exchange coils 44 wherein the stream is further cooled to form a second liquid fraction which is separated in the second stage 46 of separator 36; this fraction containing most of the C and C hydrocarbons. The major portion of the main stream remains in the gaseous phase and is conducted through lines 50 and 51 to low temperature coil'52 of the mainexchanger 32 wherein the feed stream is totally liquefied. In order to prevent vapor losses during subsequent expansion of the LNG to atmospheric pressure, the pressure of the liquefied natural gas is reduced from 600 to 200 p.s.i.a. by passage through expansion valve 54 prior to passage through exchanger coil 56 wherein the LNG is subcooled. Thus, the provision of valve 54 enables the enthalpy of the LNG to be reduced so that the liquid is not vaporized during the final pressure letdown in passing through expansion valve 58 after which the liquid is maintained at atmospheric pressure in storage tank 59.
From the foregoing description of the main process stream it is apparent that all of the refrigeration required to liquefy and subcool the feed stream (except for the very small amount of refrigeration provided by water'coolers l8 and 26) is provided by main exchanger 32. This exchanger is an integral unit composed of a plurality of cylindrical shell segments 60, 62, 64, and 66 connected by a plurality of frustoconical transition sections 68, 70, and 72. In addition to the feed stream coils previously mentioned, the exchanger includes a plurality of refrigerant coils 74, 76,78, and as well as a plurality of refrigerant spray headers 82,84, 86, 88, and 90.
The above-mentioned refrigerant coils and spray headers, together with a multistage refrigerant separator 92 and a refrigerant compressor 9'4, form the entire refrigeration system which will now be described in detail beginning with compressor inlet line 96 shown in the bottom right-hand comer of the drawing. Line 96 contains a single gaseous refrigerant which is a mixture of a plurality of component gases hereinafter referred to as a multicomponent refrigerant (MCR). For example, a preferred multicomponent refrigerant consists (by volume) of 31 parts methane, 35 parts ethane, 7 parts propane, 14 parts butane, 4 parts pentane, 3 parts hexane, and 6 parts nitrogen. This multicomponent refrigerant is compressed in stage A of compressor 94 and cooled in interstage water cooler 97 so that a portion is condensed and then separated in separator 98. The condensate is withdrawn from the bottom of the separator and pumped directly into the first stage 99 of MCR separator 92. The gaseous fraction ofv the refrigerant is withdrawn from the top of separator 98, compressed in's tage B, cooled in water cooler 100 and joined with the previously mentioned condensate which is supplied to separator 92 at a pressure in the order of 515 p.s.i.a. and at'a' temperature of 100 F.
ln the first stage 99 of MCR separator 92 the liquid fraction rich in C and heavier hydrocarbons is separated and supplied through line 101 and pressure reduction valve 102 to spray header 82 from which it is sprayed downwardly over the lower portions of coil 52 as well as coils 30, 44, and 74 whereby the' liquid refrigerant is vaporized in cooling the fluids injthe coils. Referring back to separator 92, the gaseous fraction is withdrawn from stage 99 through line 103, cooled in coil 74, and returned to the second stage .104 of the separator wherein a second fraction of liquefied refrigerant is separated. This liquid fraction'at a temperature in the order of 17 F. is rich in the C to C hydrocarbons and is supplied through line 106 and pressure reduction valve 107 to spray header 84 which is' positioned above coil 76'and at an intermediate point along coil 52. Thus, this second liquid fraction of the refrigerant is sprayed over coils 52 and 76 whereby the refrigerant is vaporized in cooling the fluids in these coils.
The gaseous fraction in stage 104 is withdrawn through line 108, cooled in coil 76, and returned to the third stage 110 of the separator wherein a third fraction of liquefied refrigerant is separated. Thisliquid fraction at a temperature in the order of minus 7l F. is rich in the'C, to C hydrocarbons and is supplied through line 112 and pressure reduction valve 113 to spray header 86 which is positioned above coil and at a- P point near the upper portion of coil 52. Thus, this fraction of the liquid refrigerant is sprayed over 'coil 78 and the inter= J mediate portion of coil 52 whereby the refrigerant is vaporized in cooling the fluids in these coils.
The gaseous fraction in stage 110 of the separator is hydrocarbons and is supplied through'line ll8-and pressure reduction valve 119 to spray header 88 which ispositioned above coils 52 and 80. Thus, the fourth liquidfraction is vaporized in cooling the feed in the upper end of coil 52 as well as the last remaining fraction of the refrigerant which is supplied to coil 80 through line l20 from stage 116. This last fraction of the refrigerant rich in nitrogen and methane is liquified in passing through coil 80 from which it exits at a temperature in the order of minus 206 F. and is reduced in pressure by passage through expansion valve 122 whereby its temperature drops to minus 259 F. Thereafter, it is supplied to spray header 90 which is positioned above subcooling coil 56 so that the last refrigerant fraction is vaporized in subcooling the feed stream in coil 56 to a temperature in the order of minus 258 F.
From the foregoing description, it is apparent that each of the liquid fractions of the multicomponent refrigerant is vaporized by heat exchange with the feed stream and high pressure refrigerant fractions at a specific temperature level. For example, the temperature levels in the vicinity of the spray headers 82, 84, 86, 88, and 90 may be in the order of 9 F.,
minus 79 F., minus 146 F., minus 222 F., and minus 259 F., respectively. At the same time, the temperatures of the MCR fractions downstream of pressure reduction valves 102, 107, 113, 119, and 122 are in the order of 27 F., minus 66 F., minus 142 F., minus 220 F., and minus 259 F.
After being vaporized in heat exchanger 32, each of the MCR fractions are recombined, withdrawn through line 124 at a pressure in the order of 41 p.s.i.a. and recycled back to compressor 94 along with a small amount of makeup refrigerant which is supplied through line 126. This makeup refrigerant, as well as the original charge of refrigerant, is obtained from the feed stream except for the nitrogen which is supplied from an air separation plant 128 through control valve l29. That is, the liquid fractions in stages 34 and 46 of feed separator 36 are withdrawn through lines 130 and 132, dried in drier 134, and supplied to the previously mentioned fractionation plant 23 through line 136. This plant is conventional in that it consists of a plurality of fractionation columns which separate the natural gas feed from line 136 into the components. Thus, predetermined amounts of ethane, propane, butane, pentane, and hexane are withdrawn through lines 138, 140, 142, 144, and 146 as determined by control valves 148 whilev methane is added to makeup line 126 through branch line 150 and control valve 152. in order to maintain a desired heating value of the LNG, controlled amounts of the C, to C hydrocarbons are withdrawn from the fractionation plant through line 154 and added to main process stream in line 50.
From the foregoing description of the liquefaction plant it will be apparent that significant economies in initial capital investment are possible due to the fact that the utilization of a single refrigerant requires a single compressor as opposed to the utilization of separate refrigerants in cascade wherein each refrigerant requires a separate compressor. In addition, the effective utilization of more than three hydrocarbons plus nitrogen substantially reduces the compression horsepower since closer matching of the cooling curves is possible at each temperature level in the exchanger. Furthermore, substantial functional as well as economic advantages are obtained from the utilization of a one-piece, multitemperature level exchanger as opposed to a plurality of individual exchangers operating over individual temperature ranges which cannot be matched so exactly to the optimum cooling curve of the feed stream. Significant advantages in the cost and ease of fabrication also flow from the combination of utilizing more than three hydrocarbons as an MCR refrigerant in an integral exchanger in that at least the majority if not all of the spray headers may be physically positioned between adjacent MCR coils as opposed to their physical location intermediate the inlet and outlets of the coils. Lastly, the utilization of pressure reducn'on valve 54 reduces the undesired flash losses of the liquefied product while the utilization of interstage phase separator 98 decreases operating horsepower requirements. Of course, it is to be understood that the foregoing description is intended to be illustrative rather than exhaustive of the invention and that the latter is not to be limited other than as expressly set forth in the following claims including all patentable equivalents thereof.
We claim:
1. A method of liquefying and subcooling a natural gas stream comprising the steps of:
a. compressing said natural gas to a first relatively high pressure,
b. flowing said compressed natural gas through a confined passageway of an elongated heat exchange zone, said confined passageway having an inlet and an outlet, reducing the pressure of said compressed natural gas in said confined passageway intermediate said inlet and said outlet,
d. compressing a multicomponent refrigerant having a plurality of components of different normal boiling points,
e. forming a plurality of liquid fractions of said multicomponent refrigerant by successively partially liquefying and fractionating said multicomponent refrigerant in heat exchange with said liquid fractions after expansion thereof,
f. liquefying said natural gas in said confined passageway by successive indirect heat exchange with said liquid fractions after expansion thereof, and
g. subcooling said liquified natural gas in said confined passageway after reducing the pressure thereof to a second lower pressure by indirect heat exchange and vaporization of at least one of said liquid fractions.
2. A method of liquefying and subcooling a methane-rich stream comprising:
a. compressing said methane-rich stream to a first pressure and passing said stream through a first heat exchange zone,
b. expanding said stream to a lower pressure after passage through said first heat exchange zone,
. passing said expanded stream through a second heat exchange zone,
d. compressing a multicomponent refrigerant comprising a plurality of components having different boiling points,
. partially condensing said multicomponent refrigerant to form a first vapor fraction and a first liquid fraction, expanding saidfirst liquid fraction and passing some of said expanded first liquid fraction in countercurrent heat exchange with said multicomponent refrigerant undergoing partial condensation,
f. passing another portion of said expanded first liquid fraction through said first heat exchange zone to condense said methane-rich stream,
g. partially condensing said first vapor fraction to form a second liquid fraction, expanding said second liquid fraction and passing some of said expanded second liquid fraction in countercurrent heat exchange with said first vapor fraction undergoing partial condensation, and
h. passing another portion of said second expanded liquid fraction through said second heat exchange zone to subcool said condensed methane-rich stream.
3. A system for liquefying a methane-rich stream comprising:
a. means forming an elongated, vertically extending heat exchanger having a warm end and a cold end,
b. first fluid passage means extending through said exchanger from said warm end to said cold end,
c. first compressor means for compressing said methanerich stream and passing said stream through said first fluid passage means from said warm end to said cold end,
d. second compressor means for compressing a multicomponent refrigerant comprising a plurality of components having different boiling points,
e. a series of phase separators, each of said separators having an inlet, a liquid fraction outlet and a vapor fraction outlet,
f. passage means connecting said second compressor means to the first separator of said series,
g. a series of refrigerant passage means located in said exchanger and positioned along the vertical length thereof,
h. passage means connecting said vapor fraction outlet of each separator to one of said refrigerant passage means,
. passage means connecting each of said refrigerant passage means to the inlet of the next separator for progressive partial condensation of said multicomponent refrigerant to form a plurality of liquid refrigerant fractions,
. means for spraying each of said liquid refrigerant fractions in countercurrent heat exchange with said first fluid passage means for progressively vaporizing each liquid fraction and liquefying said methane-rich stream, and
k. closed cycle passage means for collecting all of said vaporized liquid fractions at the warm end of said exchanger and returning them to said second compressor means.
4. A system for liquefying a feed stream composed primarily of methane comprising:
a. first compressor means for compressing a multicomponent refrigerant comprising a plurality of components having different boiling points,
b. a plurality of heat exchange means and phase separator means connected in series for progressively condensing and separating said compressed multicomponent refrigerant into a plurality of liquid condensates of decreasing temperatures,
. expansion means for expanding each of said liquid condensates,
d. multistage heat exchanger means for passing each of said expanded liquid condensates in countercurrent heat exchange with said feed stream at progressively lower temperature stages for liquefying said feed stream, said multistage heat exchanger means including a final lowest temperature stage, at least said lowest temperature stage comprising a vertically extending coil through which said feed stream is passed upwardly, and means for spraying said lowest temperature liquid condensate downwardly over said coil.
5. A method of liquefying a compressed natural gas stream comprising the steps of:
a. precooling and partially condensing said compressed natural gas stream to form a first liquid fraction and a first vapor fraction,
b. separating said vapor and liquid fractions,
c. passing said first vapor fraction through a confined passageway of a heat exchange zone from the warm end thereof to the cold end thereof,
d. passing said first liquid fraction through independent fractionation means to fractionate said liquid into a plurality of substantially pure hydrocarbon components,
e. combining selected amounts of each of said plurality of hydrocarbon components to maintain a multicomponent refrigerant of selected composition, maintaining independently of said natural gas stream and said fractionation means a separate source of a nonhydrocarbon component having a boiling point substantially below that of methane, g. introducing selected amounts of said nonhydrocarbon component from said separate source into said multicomponent refrigerant so as to substantially reduce the boiling point of said multicomponent refrigerant, forming a series of multicomponent liquids fractions of said multicomponent refrigerant at progressively lower temperatures by successive partial liquefaction of said multicomponent refrigerant in heat exchange with expanded liquid fractions thereof in closed cycle passage means, the lowest temperature multicomponent liquid fraction so formed being rich in said nonhydrocarbon component having a boiling point substantially below methane,
. introducing said multicomponent liquid fractions, including said lowest temperatureliquid fraction, into said heat exchange zone at a plurality of locations intermediate said warm and cold ends thereof and flowing each of said multicomponent liquid fractions in countercurrent heat exchange with said first vapor fraction in said confined passageway,
. progressively vaporizing each of said multicomponent liquid fractions in countercurrent heat exchange with said first vapor fraction so as to liquefy said first vapor fraction,
k. withdrawing all of said vaporized multicomponent fractions from said heat exchange zone, and
. recombining all of said withdrawn vaporized multicomponent fractions to reconstitute the major portion of said multicomponent refrigerant.
Claims (4)
- 2. A method of liquefying and subcooling a methane-rich stream comprising: a. compressing said methane-rich stream to a first pressure and passing said stream through a first heat exchange zone, b. expanding said stream to a lower pressure after passage through said first heat exchange zone, c. passing said expanded stream through a second heat exchange zone, d. compressing a multicomponent refrigerant comprising a plurality of components having different boiling points, e. partially condensing said multicomponent refrigerant to form a first vapor fraction and a first liquid fraction, expanding said first liqUid fraction and passing some of said expanded first liquid fraction in countercurrent heat exchange with said multicomponent refrigerant undergoing partial condensation, f. passing another portion of said expanded first liquid fraction through said first heat exchange zone to condense said methane-rich stream, g. partially condensing said first vapor fraction to form a second liquid fraction, expanding said second liquid fraction and passing some of said expanded second liquid fraction in countercurrent heat exchange with said first vapor fraction undergoing partial condensation, and h. passing another portion of said second expanded liquid fraction through said second heat exchange zone to subcool said condensed methane-rich stream.
- 3. A system for liquefying a methane-rich stream comprising: a. means forming an elongated, vertically extending heat exchanger having a warm end and a cold end, b. first fluid passage means extending through said exchanger from said warm end to said cold end, c. first compressor means for compressing said methane-rich stream and passing said stream through said first fluid passage means from said warm end to said cold end, d. second compressor means for compressing a multicomponent refrigerant comprising a plurality of components having different boiling points, e. a series of phase separators, each of said separators having an inlet, a liquid fraction outlet and a vapor fraction outlet, f. passage means connecting said second compressor means to the first separator of said series, g. a series of refrigerant passage means located in said exchanger and positioned along the vertical length thereof, h. passage means connecting said vapor fraction outlet of each separator to one of said refrigerant passage means, i. passage means connecting each of said refrigerant passage means to the inlet of the next separator for progressive partial condensation of said multicomponent refrigerant to form a plurality of liquid refrigerant fractions, j. means for spraying each of said liquid refrigerant fractions in countercurrent heat exchange with said first fluid passage means for progressively vaporizing each liquid fraction and liquefying said methane-rich stream, and k. closed cycle passage means for collecting all of said vaporized liquid fractions at the warm end of said exchanger and returning them to said second compressor means.
- 4. A system for liquefying a feed stream composed primarily of methane comprising: a. first compressor means for compressing a multicomponent refrigerant comprising a plurality of components having different boiling points, b. a plurality of heat exchange means and phase separator means connected in series for progressively condensing and separating said compressed multicomponent refrigerant into a plurality of liquid condensates of decreasing temperatures, c. expansion means for expanding each of said liquid condensates, d. multistage heat exchanger means for passing each of said expanded liquid condensates in countercurrent heat exchange with said feed stream at progressively lower temperature stages for liquefying said feed stream, said multistage heat exchanger means including a final lowest temperature stage, at least said lowest temperature stage comprising a vertically extending coil through which said feed stream is passed upwardly, and means for spraying said lowest temperature liquid condensate downwardly over said coil.
- 5. A method of liquefying a compressed natural gas stream comprising the steps of: a. precooling and partially condensing said compressed natural gas stream to form a first liquid fraction and a first vapor fraction, b. separating said vapor and liquid fractions, c. passing said first vapor fraction through a confined passageway of a heat exchange zone from the warm end thereof to the cold end thereof, d. passing said first liquid fraction through independent fraCtionation means to fractionate said liquid into a plurality of substantially pure hydrocarbon components, e. combining selected amounts of each of said plurality of hydrocarbon components to maintain a multicomponent refrigerant of selected composition, f. maintaining independently of said natural gas stream and said fractionation means a separate source of a nonhydrocarbon component having a boiling point substantially below that of methane, g. introducing selected amounts of said nonhydrocarbon component from said separate source into said multicomponent refrigerant so as to substantially reduce the boiling point of said multicomponent refrigerant, h. forming a series of multicomponent liquids fractions of said multicomponent refrigerant at progressively lower temperatures by successive partial liquefaction of said multicomponent refrigerant in heat exchange with expanded liquid fractions thereof in closed cycle passage means, the lowest temperature multicomponent liquid fraction so formed being rich in said nonhydrocarbon component having a boiling point substantially below methane, i. introducing said multicomponent liquid fractions, including said lowest temperature liquid fraction, into said heat exchange zone at a plurality of locations intermediate said warm and cold ends thereof and flowing each of said multicomponent liquid fractions in countercurrent heat exchange with said first vapor fraction in said confined passageway, j. progressively vaporizing each of said multicomponent liquid fractions in countercurrent heat exchange with said first vapor fraction so as to liquefy said first vapor fraction, k. withdrawing all of said vaporized multicomponent fractions from said heat exchange zone, and l. recombining all of said withdrawn vaporized multicomponent fractions to reconstitute the major portion of said multicomponent refrigerant.
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US46800865A | 1965-06-29 | 1965-06-29 | |
US65998867A | 1967-08-11 | 1967-08-11 | |
US72213568A | 1968-04-17 | 1968-04-17 | |
US88278169A | 1969-12-22 | 1969-12-22 | |
US357170A | 1970-01-09 | 1970-01-09 | |
US4962270A | 1970-06-25 | 1970-06-25 |
Publications (1)
Publication Number | Publication Date |
---|---|
US3593535A true US3593535A (en) | 1971-07-20 |
Family
ID=44022995
Family Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US882781A Expired - Lifetime US3593535A (en) | 1965-06-29 | 1969-12-22 | Liquefaction of natural gas employing multiple-component refrigerants |
US49622A Expired - Lifetime US3645106A (en) | 1965-06-29 | 1970-06-25 | Process for liquefying natural gas employing a multicomponent refrigerant for obtaining low temperature cooling |
Family Applications After (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US49622A Expired - Lifetime US3645106A (en) | 1965-06-29 | 1970-06-25 | Process for liquefying natural gas employing a multicomponent refrigerant for obtaining low temperature cooling |
Country Status (4)
Country | Link |
---|---|
US (2) | US3593535A (en) |
FR (1) | FR1557019A (en) |
GB (1) | GB1135871A (en) |
MY (1) | MY7000139A (en) |
Cited By (33)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3742721A (en) * | 1970-01-08 | 1973-07-03 | Technip Cie | Method of regulation of the temperature of the liquefied gas or gaseous mixture in an apparatus for the liquefaction of gaseous fluids |
US3855810A (en) * | 1972-02-11 | 1974-12-24 | Linde Ag | One flow cascade cycle with buffer volume bypass |
US3884044A (en) * | 1970-02-09 | 1975-05-20 | Exxon Research Engineering Co | Mixed refrigerant cycle |
US3884045A (en) * | 1970-02-09 | 1975-05-20 | Exxon Research Engineering Co | Mixed refrigerant cycle |
US3898857A (en) * | 1972-09-22 | 1975-08-12 | Teal Soc | Process for regulating the quantity of cold delivered by a refrigerating installation |
US3932154A (en) * | 1972-06-08 | 1976-01-13 | Chicago Bridge & Iron Company | Refrigerant apparatus and process using multicomponent refrigerant |
US3957473A (en) * | 1970-02-09 | 1976-05-18 | Stark Thomas M | Mixed refrigerant cycle |
US4065278A (en) * | 1976-04-02 | 1977-12-27 | Air Products And Chemicals, Inc. | Process for manufacturing liquefied methane |
USRE29914E (en) * | 1965-03-31 | 1979-02-20 | Compagnie Francaise D'etudes Et De Construction Technip | Method and apparatus for the cooling and low temperature liquefaction of gaseous mixtures |
USRE30140E (en) * | 1961-06-01 | 1979-11-06 | Compagnie Francaise D'etudes Et De Construction Technip | Method for cooling a gaseous mixture to a low temperature |
US4251247A (en) * | 1974-05-31 | 1981-02-17 | Compagnie Francaise D'etudes Et De Construction Technip | Method and apparatus for cooling a gaseous mixture |
US4813987A (en) * | 1987-10-13 | 1989-03-21 | Mobil Oil Corporation | Process for the liquefaction of natural gas |
US4814152A (en) * | 1987-10-13 | 1989-03-21 | Mobil Oil Corporation | Process for removing mercury vapor and chemisorbent composition therefor |
US4813986A (en) * | 1987-10-13 | 1989-03-21 | Mobil Oil Corporation | Process for the low temperature deriming of cryogenic heat exchangers |
US4828591A (en) * | 1988-08-08 | 1989-05-09 | Mobil Oil Corporation | Method and apparatus for the liquefaction of natural gas |
US4859491A (en) * | 1987-10-13 | 1989-08-22 | Mobil Oil Corporation | Process for repairing a cryogenic heat exchanger |
US5950453A (en) * | 1997-06-20 | 1999-09-14 | Exxon Production Research Company | Multi-component refrigeration process for liquefaction of natural gas |
US6250105B1 (en) | 1998-12-18 | 2001-06-26 | Exxonmobil Upstream Research Company | Dual multi-component refrigeration cycles for liquefaction of natural gas |
WO2003019095A1 (en) * | 2001-08-21 | 2003-03-06 | Gasconsult Limited | Method for liquefying methane-rich gas |
WO2003064946A1 (en) * | 2002-01-30 | 2003-08-07 | Exxonmobil Upstream Research Company | Processes and systems for liquefying natural gas |
US20040069015A1 (en) * | 2001-02-26 | 2004-04-15 | Henri Paradowski | Method for ethane recovery, using a refrigeration cycle with a mixture of at least two coolants, gases obtained by said method, and installation therefor |
US20040083756A1 (en) * | 2002-11-01 | 2004-05-06 | Jean-Pierre Tranier | Combined air separation natural gas liquefaction plant |
US20050198998A1 (en) * | 2004-03-09 | 2005-09-15 | Guang-Chung Lee | Refrigeration system |
US20100058802A1 (en) * | 2006-11-01 | 2010-03-11 | Einar Brendeng | Method for liquefaction of gas |
DE102009015411A1 (en) | 2009-03-27 | 2010-10-07 | Marine-Service Gmbh | Method and device for operating a drive machine for a ship for transporting liquefied gas |
US20120247147A1 (en) * | 2011-03-29 | 2012-10-04 | Linde Aktiengesellschaft | Heat exchanger system |
CN103542693A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Ethylene cryogenic separation method for large-sized ethylene device |
US20140075986A1 (en) * | 2012-09-18 | 2014-03-20 | Woodside Energy Technologies Pty Ltd. | Production of ethane for start-up of an lng train |
EP2857782A1 (en) | 2013-10-04 | 2015-04-08 | Shell International Research Maatschappij B.V. | Coil wound heat exchanger and method of cooling a process stream |
US20190186818A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2020225096A1 (en) * | 2019-05-03 | 2020-11-12 | Shell Internationale Research Maatschappij B.V. | Method and system for controlling refrigerant composition in case of gas tube leaks in a heat exchanger |
US11460244B2 (en) * | 2016-06-30 | 2022-10-04 | Baker Hughes Oilfield Operations Llc | System and method for producing liquefied natural gas |
RU2805608C2 (en) * | 2019-05-03 | 2023-10-20 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Method and system for control of refrigerant composition in case of leaks from the gas pipe in the heat exchanger |
Families Citing this family (31)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
USRE30085E (en) * | 1965-03-31 | 1979-08-28 | Compagnie Francaise D'etudes Et De Construction Technip | Method and apparatus for the coding and low temperature liquefaction of gaseous mixtures |
JPS5440512B1 (en) * | 1968-11-04 | 1979-12-04 | ||
US3581511A (en) * | 1969-07-15 | 1971-06-01 | Inst Gas Technology | Liquefaction of natural gas using separated pure components as refrigerants |
FR2085216B2 (en) * | 1970-02-12 | 1973-08-10 | Technip Cie | |
FR2217648B1 (en) * | 1973-02-12 | 1976-05-14 | Inst Francais Du Petrole | |
DE2438443C2 (en) * | 1974-08-09 | 1984-01-26 | Linde Ag, 6200 Wiesbaden | Process for liquefying natural gas |
DE2631134A1 (en) * | 1976-07-10 | 1978-01-19 | Linde Ag | METHOD FOR LIQUIDIFYING AIR OR MAIN COMPONENTS |
JPS6124967A (en) * | 1984-07-13 | 1986-02-03 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
JPS6124968A (en) * | 1984-07-13 | 1986-02-03 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
US4970867A (en) * | 1989-08-21 | 1990-11-20 | Air Products And Chemicals, Inc. | Liquefaction of natural gas using process-loaded expanders |
FR2679635B1 (en) * | 1991-07-26 | 1993-10-15 | Air Liquide | COMPRESSION CIRCUIT FOR A LOW-PRESSURE AND LOW-TEMPERATURE GAS FLUID. |
FR2725503B1 (en) * | 1994-10-05 | 1996-12-27 | Inst Francais Du Petrole | NATURAL GAS LIQUEFACTION PROCESS AND INSTALLATION |
US6347531B1 (en) * | 1999-10-12 | 2002-02-19 | Air Products And Chemicals, Inc. | Single mixed refrigerant gas liquefaction process |
US6347532B1 (en) * | 1999-10-12 | 2002-02-19 | Air Products And Chemicals, Inc. | Gas liquefaction process with partial condensation of mixed refrigerant at intermediate temperatures |
ATE311580T1 (en) * | 2002-05-27 | 2005-12-15 | Air Prod & Chem | HEAT EXCHANGER WITH WOUND COILS |
US20080141711A1 (en) * | 2006-12-18 | 2008-06-19 | Mark Julian Roberts | Hybrid cycle liquefaction of natural gas with propane pre-cooling |
NO329177B1 (en) * | 2007-06-22 | 2010-09-06 | Kanfa Aragon As | Process and system for forming liquid LNG |
US8555672B2 (en) * | 2009-10-22 | 2013-10-15 | Battelle Energy Alliance, Llc | Complete liquefaction methods and apparatus |
US9217603B2 (en) | 2007-09-13 | 2015-12-22 | Battelle Energy Alliance, Llc | Heat exchanger and related methods |
US9254448B2 (en) | 2007-09-13 | 2016-02-09 | Battelle Energy Alliance, Llc | Sublimation systems and associated methods |
US9574713B2 (en) | 2007-09-13 | 2017-02-21 | Battelle Energy Alliance, Llc | Vaporization chambers and associated methods |
US10655911B2 (en) | 2012-06-20 | 2020-05-19 | Battelle Energy Alliance, Llc | Natural gas liquefaction employing independent refrigerant path |
US11428463B2 (en) | 2013-03-15 | 2022-08-30 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
KR102312640B1 (en) | 2013-03-15 | 2021-10-13 | 차트 에너지 앤드 케미칼즈 인코포레이티드 | Mixed refrigerant system and method |
US11408673B2 (en) | 2013-03-15 | 2022-08-09 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
DE102015002443A1 (en) * | 2015-02-26 | 2016-09-01 | Linde Aktiengesellschaft | Process for liquefying natural gas |
AR105277A1 (en) * | 2015-07-08 | 2017-09-20 | Chart Energy & Chemicals Inc | MIXED REFRIGERATION SYSTEM AND METHOD |
EP3162870A1 (en) | 2015-10-27 | 2017-05-03 | Linde Aktiengesellschaft | Low-temperature mixed-refrigerant for hydrogen precooling in large scale |
US20180066888A1 (en) * | 2016-08-29 | 2018-03-08 | Stanislav Sinatov | Method for Electrical Energy Storage with Co-production of Liquefied Methaneous Gas |
US10655913B2 (en) * | 2016-09-12 | 2020-05-19 | Stanislav Sinatov | Method for energy storage with co-production of peaking power and liquefied natural gas |
US10731795B2 (en) * | 2017-08-28 | 2020-08-04 | Stanislav Sinatov | Method for liquid air and gas energy storage |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR1302989A (en) * | 1961-06-01 | 1962-09-07 | Air Liquide | Process for cooling a gas mixture at low temperature |
US3205669A (en) * | 1960-08-15 | 1965-09-14 | Phillips Petroleum Co | Recovery of natural gas liquids, helium concentrate, and pure nitrogen |
US3315477A (en) * | 1964-07-15 | 1967-04-25 | Conch Int Methane Ltd | Cascade cycle for liquefaction of natural gas |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3364685A (en) * | 1965-03-31 | 1968-01-23 | Cie Francaise D Etudes Et De C | Method and apparatus for the cooling and low temperature liquefaction of gaseous mixtures |
-
1966
- 1966-06-28 GB GB28964/66A patent/GB1135871A/en not_active Expired
-
1967
- 1967-10-18 FR FR1557019D patent/FR1557019A/fr not_active Expired
-
1969
- 1969-12-22 US US882781A patent/US3593535A/en not_active Expired - Lifetime
-
1970
- 1970-06-25 US US49622A patent/US3645106A/en not_active Expired - Lifetime
- 1970-12-31 MY MY1970139A patent/MY7000139A/en unknown
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3205669A (en) * | 1960-08-15 | 1965-09-14 | Phillips Petroleum Co | Recovery of natural gas liquids, helium concentrate, and pure nitrogen |
FR1302989A (en) * | 1961-06-01 | 1962-09-07 | Air Liquide | Process for cooling a gas mixture at low temperature |
US3315477A (en) * | 1964-07-15 | 1967-04-25 | Conch Int Methane Ltd | Cascade cycle for liquefaction of natural gas |
Non-Patent Citations (1)
Title |
---|
Progress in Refrigeration Science and Technology, Vol. 1 1960 Permagon Press. pp 34 39 * |
Cited By (84)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
USRE30140E (en) * | 1961-06-01 | 1979-11-06 | Compagnie Francaise D'etudes Et De Construction Technip | Method for cooling a gaseous mixture to a low temperature |
USRE29914E (en) * | 1965-03-31 | 1979-02-20 | Compagnie Francaise D'etudes Et De Construction Technip | Method and apparatus for the cooling and low temperature liquefaction of gaseous mixtures |
US3742721A (en) * | 1970-01-08 | 1973-07-03 | Technip Cie | Method of regulation of the temperature of the liquefied gas or gaseous mixture in an apparatus for the liquefaction of gaseous fluids |
US3884044A (en) * | 1970-02-09 | 1975-05-20 | Exxon Research Engineering Co | Mixed refrigerant cycle |
US3884045A (en) * | 1970-02-09 | 1975-05-20 | Exxon Research Engineering Co | Mixed refrigerant cycle |
US3957473A (en) * | 1970-02-09 | 1976-05-18 | Stark Thomas M | Mixed refrigerant cycle |
US3855810A (en) * | 1972-02-11 | 1974-12-24 | Linde Ag | One flow cascade cycle with buffer volume bypass |
US3932154A (en) * | 1972-06-08 | 1976-01-13 | Chicago Bridge & Iron Company | Refrigerant apparatus and process using multicomponent refrigerant |
US3898857A (en) * | 1972-09-22 | 1975-08-12 | Teal Soc | Process for regulating the quantity of cold delivered by a refrigerating installation |
US4251247A (en) * | 1974-05-31 | 1981-02-17 | Compagnie Francaise D'etudes Et De Construction Technip | Method and apparatus for cooling a gaseous mixture |
US4065278A (en) * | 1976-04-02 | 1977-12-27 | Air Products And Chemicals, Inc. | Process for manufacturing liquefied methane |
US4813987A (en) * | 1987-10-13 | 1989-03-21 | Mobil Oil Corporation | Process for the liquefaction of natural gas |
US4814152A (en) * | 1987-10-13 | 1989-03-21 | Mobil Oil Corporation | Process for removing mercury vapor and chemisorbent composition therefor |
US4813986A (en) * | 1987-10-13 | 1989-03-21 | Mobil Oil Corporation | Process for the low temperature deriming of cryogenic heat exchangers |
US4859491A (en) * | 1987-10-13 | 1989-08-22 | Mobil Oil Corporation | Process for repairing a cryogenic heat exchanger |
US4828591A (en) * | 1988-08-08 | 1989-05-09 | Mobil Oil Corporation | Method and apparatus for the liquefaction of natural gas |
ES2170630A1 (en) * | 1997-06-20 | 2002-08-01 | Exxonmobil Upstream Res Co | Improved multi-component refrigeration process for liquefaction of natural gas |
EP0988497A4 (en) * | 1997-06-20 | 2002-05-15 | Exxonmobil Upstream Res Co | Improved multi-component refrigeration process for liquefaction of natural gas |
US5950453A (en) * | 1997-06-20 | 1999-09-14 | Exxon Production Research Company | Multi-component refrigeration process for liquefaction of natural gas |
EP0988497A1 (en) * | 1997-06-20 | 2000-03-29 | Exxon Production Research Company | Improved multi-component refrigeration process for liquefaction of natural gas |
US6250105B1 (en) | 1998-12-18 | 2001-06-26 | Exxonmobil Upstream Research Company | Dual multi-component refrigeration cycles for liquefaction of natural gas |
US20040069015A1 (en) * | 2001-02-26 | 2004-04-15 | Henri Paradowski | Method for ethane recovery, using a refrigeration cycle with a mixture of at least two coolants, gases obtained by said method, and installation therefor |
US7234321B2 (en) * | 2001-08-21 | 2007-06-26 | Gasconsult Limited | Method for liquefying methane-rich gas |
GB2393504A (en) * | 2001-08-21 | 2004-03-31 | Gasconsult Ltd | Method for liquefying methane-rich gas |
WO2003019095A1 (en) * | 2001-08-21 | 2003-03-06 | Gasconsult Limited | Method for liquefying methane-rich gas |
US20040255616A1 (en) * | 2001-08-21 | 2004-12-23 | Maunder Anthony D. | Method for liquefying methane-rich gas |
GB2393504B (en) * | 2001-08-21 | 2005-05-18 | Gasconsult Ltd | Method for liquefying methane-rich gas |
US6658892B2 (en) | 2002-01-30 | 2003-12-09 | Exxonmobil Upstream Research Company | Processes and systems for liquefying natural gas |
WO2003064946A1 (en) * | 2002-01-30 | 2003-08-07 | Exxonmobil Upstream Research Company | Processes and systems for liquefying natural gas |
US7143606B2 (en) * | 2002-11-01 | 2006-12-05 | L'air Liquide-Societe Anonyme A'directoire Et Conseil De Surveillance Pour L'etide Et L'exploitation Des Procedes Georges Claude | Combined air separation natural gas liquefaction plant |
US20040083756A1 (en) * | 2002-11-01 | 2004-05-06 | Jean-Pierre Tranier | Combined air separation natural gas liquefaction plant |
US7082787B2 (en) | 2004-03-09 | 2006-08-01 | Bp Corporation North America Inc. | Refrigeration system |
US20050198998A1 (en) * | 2004-03-09 | 2005-09-15 | Guang-Chung Lee | Refrigeration system |
US20100058802A1 (en) * | 2006-11-01 | 2010-03-11 | Einar Brendeng | Method for liquefaction of gas |
US8806891B2 (en) | 2006-11-01 | 2014-08-19 | Sinvent As | Method for liquefaction of gas |
DE102009015411A1 (en) | 2009-03-27 | 2010-10-07 | Marine-Service Gmbh | Method and device for operating a drive machine for a ship for transporting liquefied gas |
US20120247147A1 (en) * | 2011-03-29 | 2012-10-04 | Linde Aktiengesellschaft | Heat exchanger system |
US9927170B2 (en) * | 2011-03-29 | 2018-03-27 | Linde Aktiengesellschaft | Heat exchanger system |
CN103542693A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Ethylene cryogenic separation method for large-sized ethylene device |
CN103542693B (en) * | 2012-07-12 | 2016-07-13 | 中国石油天然气股份有限公司 | The ethylene deep cooling separating method of large-scale ethylene plant |
US10060674B2 (en) * | 2012-09-18 | 2018-08-28 | Woodside Energy Technologies Pty Ltd. | Production of ethane for start-up of an LNG train |
US20140075986A1 (en) * | 2012-09-18 | 2014-03-20 | Woodside Energy Technologies Pty Ltd. | Production of ethane for start-up of an lng train |
EP2857782A1 (en) | 2013-10-04 | 2015-04-08 | Shell International Research Maatschappij B.V. | Coil wound heat exchanger and method of cooling a process stream |
US11460244B2 (en) * | 2016-06-30 | 2022-10-04 | Baker Hughes Oilfield Operations Llc | System and method for producing liquefied natural gas |
CN111656114A (en) * | 2017-12-15 | 2020-09-11 | 沙特阿拉伯石油公司 | Process integration for natural gas condensate recovery |
CN111630333B (en) * | 2017-12-15 | 2022-05-31 | 沙特阿拉伯石油公司 | Process integration for natural gas condensate recovery |
WO2019118673A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2019118578A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2019118616A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US20190186823A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
CN111684227A (en) * | 2017-12-15 | 2020-09-18 | 沙特阿拉伯石油公司 | Process integration for natural gas condensate recovery |
WO2019118668A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2019118670A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2019118600A3 (en) * | 2017-12-15 | 2019-08-08 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2019118609A3 (en) * | 2017-12-15 | 2019-08-22 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2019118605A3 (en) * | 2017-12-15 | 2019-08-22 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2019118593A3 (en) * | 2017-12-15 | 2019-08-22 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2019118614A3 (en) * | 2017-12-15 | 2019-08-22 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2019118595A3 (en) * | 2017-12-15 | 2019-08-22 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
CN111630334A (en) * | 2017-12-15 | 2020-09-04 | 沙特阿拉伯石油公司 | Process integration for natural gas condensate recovery |
CN111630333A (en) * | 2017-12-15 | 2020-09-04 | 沙特阿拉伯石油公司 | Process integration for natural gas condensate recovery |
CN111699355A (en) * | 2017-12-15 | 2020-09-22 | 沙特阿拉伯石油公司 | Process integration for natural gas condensate recovery |
WO2019118672A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US20190186824A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
WO2019118608A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11644235B2 (en) * | 2017-12-15 | 2023-05-09 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US10976103B2 (en) | 2017-12-15 | 2021-04-13 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US10989470B2 (en) | 2017-12-15 | 2021-04-27 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11226154B2 (en) * | 2017-12-15 | 2022-01-18 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11231226B2 (en) * | 2017-12-15 | 2022-01-25 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11231227B2 (en) * | 2017-12-15 | 2022-01-25 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11236941B2 (en) * | 2017-12-15 | 2022-02-01 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11248839B2 (en) * | 2017-12-15 | 2022-02-15 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11248840B2 (en) * | 2017-12-15 | 2022-02-15 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11262123B2 (en) * | 2017-12-15 | 2022-03-01 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11268756B2 (en) * | 2017-12-15 | 2022-03-08 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11268755B2 (en) * | 2017-12-15 | 2022-03-08 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11320196B2 (en) | 2017-12-15 | 2022-05-03 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
CN111699354A (en) * | 2017-12-15 | 2020-09-22 | 沙特阿拉伯石油公司 | Process integration for natural gas condensate recovery |
US20190186818A1 (en) * | 2017-12-15 | 2019-06-20 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US11428464B2 (en) | 2017-12-15 | 2022-08-30 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
US20220205713A1 (en) * | 2019-05-03 | 2022-06-30 | Shell Oil Company | Method and system for controlling refrigerant composition in case of gas tube leaks in a heat exchanger |
WO2020225096A1 (en) * | 2019-05-03 | 2020-11-12 | Shell Internationale Research Maatschappij B.V. | Method and system for controlling refrigerant composition in case of gas tube leaks in a heat exchanger |
RU2805608C2 (en) * | 2019-05-03 | 2023-10-20 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Method and system for control of refrigerant composition in case of leaks from the gas pipe in the heat exchanger |
Also Published As
Publication number | Publication date |
---|---|
US3645106A (en) | 1972-02-29 |
GB1135871A (en) | 1968-12-04 |
MY7000139A (en) | 1970-12-31 |
FR1557019A (en) | 1969-02-14 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US3593535A (en) | Liquefaction of natural gas employing multiple-component refrigerants | |
US3763658A (en) | Combined cascade and multicomponent refrigeration system and method | |
RU2752223C2 (en) | Complex system for methane cooling for natural gas liquefaction | |
RU2253809C2 (en) | Mode of liquefaction of natural gas by way of cooling at the expense of expansion | |
US5036671A (en) | Method of liquefying natural gas | |
CA1195230A (en) | Separation of nitrogen from natural gas | |
US4430103A (en) | Cryogenic recovery of LPG from natural gas | |
CN1102213C (en) | Reliquefaction of boil-off from pressure LNG | |
US3780534A (en) | Liquefaction of natural gas with product used as absorber purge | |
JP4741468B2 (en) | Integrated multi-loop cooling method for gas liquefaction | |
US4727723A (en) | Method for sub-cooling a normally gaseous hydrocarbon mixture | |
US4065278A (en) | Process for manufacturing liquefied methane | |
US5737940A (en) | Aromatics and/or heavies removal from a methane-based feed by condensation and stripping | |
US3420068A (en) | Process for the production of a fluid rich in methane from liquefied natural gas under a low initial pressure | |
US5669234A (en) | Efficiency improvement of open-cycle cascaded refrigeration process | |
US7234322B2 (en) | LNG system with warm nitrogen rejection | |
US6016665A (en) | Cascade refrigeration process for liquefaction of natural gas | |
USRE29914E (en) | Method and apparatus for the cooling and low temperature liquefaction of gaseous mixtures | |
RU2215952C2 (en) | Method of separation of pressurized initial multicomponent material flow by distillation | |
CA3029950C (en) | System and method for liquefaction of natural gas | |
US6925837B2 (en) | Enhanced operation of LNG facility equipped with refluxed heavies removal column | |
USRE30140E (en) | Method for cooling a gaseous mixture to a low temperature | |
KR100962627B1 (en) | Integrated multiple-loop refrigeration process for gas liquefaction | |
US3418819A (en) | Liquefaction of natural gas by cascade refrigeration | |
US20030177785A1 (en) | Process for producing a pressurized liquefied gas product by cooling and expansion of a gas stream in the supercritical state |