US3407052A - Natural gas liquefaction with controlled b.t.u. content - Google Patents

Natural gas liquefaction with controlled b.t.u. content Download PDF

Info

Publication number
US3407052A
US3407052A US57306866A US3407052A US 3407052 A US3407052 A US 3407052A US 57306866 A US57306866 A US 57306866A US 3407052 A US3407052 A US 3407052A
Authority
US
United States
Prior art keywords
exchanger
gas
pressure
refrigerant
vessel
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
Inventor
Charles O Huntress
Jr Russell C Proctor
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Conch International Methane Ltd
Original Assignee
Conch International Methane Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Conch International Methane Ltd filed Critical Conch International Methane Ltd
Priority to US57306866 priority Critical patent/US3407052A/en
Priority to SE1096467A priority patent/SE329182B/xx
Priority to DE19671551617 priority patent/DE1551617A1/en
Priority to GB3625267A priority patent/GB1141219A/en
Priority to CH1127567A priority patent/CH525430A/en
Priority to FR117820A priority patent/FR1534279A/en
Priority to ES344074A priority patent/ES344074A1/en
Priority to BE702669D priority patent/BE702669A/xx
Priority to NO169365A priority patent/NO120941B/no
Priority to NL6711190A priority patent/NL6711190A/xx
Priority to AT752767A priority patent/AT275486B/en
Application granted granted Critical
Publication of US3407052A publication Critical patent/US3407052A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/06—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by mixing with gases
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return 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
    • 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
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
    • 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
    • F25J1/0203—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0204—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR 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
    • F25J1/0232—Coupling of the liquefaction unit to other units or processes, so-called integrated processes integration within a pressure letdown station of a high pressure pipeline system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—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
    • F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
    • F25J1/0255—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature controlling the composition of the feed or liquefied gas, e.g. to achieve a particular heating value of natural gas
    • 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
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/035—High pressure (>10 bar)
    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/036—Very high pressure (>80 bar)
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/02—Mixing or blending of fluids to yield a certain product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • a minor portion of the liquefied natural gas is fiashed to produce a heavier fraction of liquefied hydrocarbons which arevremoved under calorimeter control, vre'gasified, 'and added to the distribution-system at a'rate to maintain the B.t.u. va-lue ofthe gaseous stream supplied to the distribution at the desired value.
  • Refrigerant from exchanger 6 is also taken in line 34 and heat-exchanged with the" cold heavier fraction in drum 27, by means of coil 36, and then returned to heat exchanger 7 through valve 37 and line 40, under control of temperature controller 38 which is in turnV controlled by a thermocouple (not shown) located in the kettle portion of the drum 27', but can be overridden by a signal in line 39 from the liquid level controller 41 associated with exchanger '7, in order to ensure that the liquid level 'in 7 remains at the desired value.
  • the LNG emerging from exchanger 10 in line 2e at about 17.7 p.s.i.a. and 254 F. is reduced to substantially atmospheric pressure in reduction valve 51v and fed to LNG storage tank 52, which may be any suitable large-scale storage facility such as an in-ground storage tank.
  • LNG storage tank 52 which may be any suitable large-scale storage facility such as an in-ground storage tank.
  • the boil-off gas from tank 52 at approximately 15 pounds pressure and 260 F. is compressed by means of any suitable compressor 53 to 18p.s.i.a. and 258 F., and is supplied in line'54 to join the gasin line 47, for subsequent further compression by boil-off compressor 48 to 80 p.s.i.a., at which pressure it is supplied to thedistribution line 33, as previously described.
  • the refrigerant -vapors in lines 15, 16 and 17 are fed to successive stages of a multistage centrifugal compressor 18, which is another advantage of the presentsystem.
  • centrifugal cornt pressors for liquefaction rates as large as those envisaged in a typical system for which the invention would be used (5.0 MM s.c.f.d.) because of their low inlet volume.
  • a refrigerant such as Freon 13 B-l
  • exchanger l8 has a vapor pressureof 2.7 p.s.i.a., and with this low suction pressure the use of a centrifugal compressor is feasible due to the high inlet a.c.f.m. (actual cubic feet per minute).
  • the arrangement of injecting the other feed streams at the inner stages increases the a.c.f.m.
  • the compressed refrigerant emerges in line 54 at approximately 325 p.s.i.a., and is cooled, preferably by water cooler 56 to 100 F., after which it is supplied to surge tank 9, from which it is withdrawn on line 8 as previously described.
  • the above system in addition to being highly efficient with respect to power requirements, thus enables the use of a single compressor, with consequent reduction in cost.
  • the heat exchangers for a liquefaction plant ranging in size up to 5.0l MM s.c.f.d. can be incorporated in a unitized ⁇ construction of exchangers stacked one above ⁇ the other, all .within a cold box structure and skid mounted for convenient transportation. It is thus apparent thatl the above-described system is economical in cost as well as eflicient in operation.
  • the removal of heavies ,while the gas is at high pressure and prior to subcooling has the further advantage of minimizing'the possibility of riming problems which these heavies could cause in the subsequent exchangers 21, 10 which are used for subcooling the gas stream.
  • the external refrigeration system can be easily derimed when necessary Vby passing warm feed gas through the exchangers 5, 6 and 7, and collecting the deriming product in the B.t.u. heavies vessel 27; alternatively, methanol can be injected into the feed gas stream yfor rime removal and collection in' the same vessel, thus minimizing the time neededv for the liquefaction unit to be out of service or bypassed.
  • a process for supplying natural gas containing different hydrocarbon constituents as an outlet gas stream from a n-atural gas liquefaction process to a distribution system at a desired B.t.u. value comprising the following steps:
  • a process for supplying natural gas containing different hydrocarbon constituents to a distribution system at a desired B.t.u. value comprising the following steps:
  • step (b) gasifying the heavier hydrocarbon fractionl, said combined stream of first stream, vapor from storage and heavier fraction forming an outlet gas which is passed in heat exchange'with said natural gas stream to supply the auto refrigeration of step (b), said heavier hydrocarbon fraction being added at a rate to maintain the B.t.u. value of the outlet gas at a desired value,

Abstract

1,141,219. Cold separation of gas mixtures. CONCH INTERNATIONAL METHANE Ltd. 8 Aug., 1967 [17 Aug., 1966], No. 36252/67. Heading F4P. Natural hydrocarbon gas is supplied to a distribution system at a controlled B.T.U. value by liquefying a feed stream 2 at a pressure higher than the distribution pressure in indirect heat exchangers 5, 6, 7 cooled by an external refrigerant, diverting through a line 23 a minor portion of the high pressure L.N.G. leaving exchanger 7, expanding it at a valve 24 into a vessel 27 to produce flash gas and liquid heavy hydrocarbons, expanding at valves 42, 46, 51 the remainder of the L.N.G. into a storage vessel 52 maintained at about atmospheric pressure expanding at a valve 31 the hydrocarbon liquid withdrawn from vessel 27 and adding it to boil-off gas withdrawn by a pump 53 from vessel 52 at a rate controlled by a calorimeter 34a and passing the mixture so formed through a line 47a and a compressor 48 to an outlet line 33 leading to the distribution system. L.N.G. leaving expansion valve 42 is joined by flash gas from chamber 27 and is further cooled in an exchanger 21 traversed by a reverse flow of said boil-off gas and heavy hydrocarbon liquid and also by a reverse flow of a minor portion of L.N.G. withdrawn from the outlet line of exchanger 21 and expanded at a valve 43. The main body of L.N.G. is still further cooled in an exchanger 10 traversed by a reverse flow of a minor portion of L.N.G. leaving expansion valve 46. The two reverse flows of expanded L.N.G. are warmed in exchangers 5, 6, 7 and are fed to the outlet line 33. The external refrigerant for cooling exchanger 5, 6, 7 is circulated in a closed cycle comprising a surge tank 9, expansion valves 11, 21, 22 in series and a three stage compressor to which refrigerant vapour leaving exchangers 5, 6, 7 is fed and which delivers to the tank 9. A portion of liquid refrigerant is withdrawn from exchanger 6 and is used to heat a coil 36 in flash vessel 27; the so-cooled refrigerant being returned to exchanger 7.

Description

CONTENT Oct. 22, 1968 c. o. HUNTREss ETAL NATURAL GAS LIQUEFACTION WITH CONTROLLED BJ; .u.
Filed Aug. 17. 1966 United States Patent* "ice ABSTRACT on THEV nl scllosUn y 'A process for maintaininga gaseous stream supplied to Aa distribution system ata-desired B.tfu. value'in which a high pressure natural gas stream is liquefied while being maintained at high pressure'. A major portion of the liquefied natural gas is-l reduced in pressurefand stored or passed back inheat exchange'. with the natural gas being vliquefied thereafter passingl to-*the distribution system. A minor portion of the liquefied natural gas is fiashed to produce a heavier fraction of liquefied hydrocarbons which arevremoved under calorimeter control, vre'gasified, 'and added to the distribution-system at a'rate to maintain the B.t.u. va-lue ofthe gaseous stream supplied to the distribution at the desired value.
Thisinventionrelates generally to the same problem as is dealt with in the copending application of Bodle and Young, Ser. No. 282,727, now Patent No. 3,285,719, as-
signed to the assignee of the: present invention, over which it has the advantages chieflyV ofincreased ope-rating efficiency and f lower capital investment'. I3his .lis made possible by theuse of asingle external refrigerant inthe placeof .twof or more, 'external `refrigerants,'cornmonly employed, and by the process ofuseparating'out the 'heavier hydrocarbon constituentsfrornthe feedvigas after it has beenl converted to aliquid, and whilek itlris `still iat high pressure, relying mainlypupon a reductionin pressure of theA liquefied vgas to produce thel` required separation. *Y
if i t Descriptionof the invention A The specific lnature of the invention aswell as other objects ,and` advantages thereof will clearly appear from a ,description of a preferred embodiment as shown in the accompanying dra-wing in'which the single' guljeV is a highly 'simplified schematic fiow` chart showingl the principle of the invention.
Referring to theV drawing,'the feed .gas lis typically supplied in a main `feed gas line v2'at a fai'rlyjhigh pressure,
in line 8 from storage tank 9 tothe interior-ofheat ex- 3,407,052 l k'lhifatentedv Qct. 2`2., 1 968 back in lines 15, 1 6 and 17 respectively to refrigerant compressor 18, the vapor from` exchanger 7being passed through exchangers 6 andS, andthat from exchanger' being passed through exchanger 5','-for furtherinterchange of heat energy in order to' improve the 'efiiciencyf The pressure and temperature reductions'in exchangers 6V and 7 are 'successively' achieved; by proper settings of the reduction valves 21"and122 as is well-known. inthe art.
The mainvteed'gasin lin'e"2"emerges'from heatiex hchanger 7 still'at substantially itsinitial pressure of'635 pounds, but is now at a temperature of 125 FA minor proportion of this" gas is takenpff in line 23, and'is reduced in pressure at-valve'24, under control Vof level control 26, to produce in heavies lfiash drum 27 vflash-gases consisting ofthe lighter components,"which'aretreturried ini-line'v 28,jand also a he'avierfraction of' liquid hydrocarbons remaining in the'bottom 'portion of-the drum,
-which remain in the drum at a pressure of 620` pounds and a"tc'mperatu'reof 92` F.; and are withdrawn-in line 29, -and' supplied through valve 31 and lines 32Jand 547e: to the outlet line 33 of the distribution system, under control of calorimeter 34a, in an amount sufficient to make up the required B.t.u. content.
Refrigerant from exchanger 6 is also taken in line 34 and heat-exchanged with the" cold heavier fraction in drum 27, by means of coil 36, and then returned to heat exchanger 7 through valve 37 and line 40, under control of temperature controller 38 which is in turnV controlled by a thermocouple (not shown) located in the kettle portion of the drum 27', but can be overridden by a signal in line 39 from the liquid level controller 41 associated with exchanger '7, in order to ensure that the liquid level 'in 7 remains at the desired value.
from 635 pounds down to approximately 615 pounds,
and is 'still further cooled in exchanger 20 by auto-refrigeration, for which purposes a snmall amount of the gas is taken off line 2d through pressure-reduction valve '43, and returned at 80 pounds pressure and a temperature of 208 F. through line44, which is subsequently extended through the heat exchangers S, 6 and 7 in order to utilize the remaining refrigeration potential of the gas in this line, -finally emerging from exchanger 5 at 44a,
still at 8O pounds pressure and a temperature of approximately 15 F., where it is fed to line 33 of the distribution system as output. The feed gas continues in line 2d at a temperature of 200 F. into exchanger 10, Where again a minor portion of the gas is taken through all of the above-described exchangers in series to provide further refrigeration effect, finally emerging in' line 47a as low pressure flash gas, at 17.7-p.s.i.a. and 35 F., and is thereafter compressed by boil-off compressor 4S to y pounds pressure and fed to line 33 for distribution.
The LNG emerging from exchanger 10 in line 2e at about 17.7 p.s.i.a. and 254 F. is reduced to substantially atmospheric pressure in reduction valve 51v and fed to LNG storage tank 52, which may be any suitable large-scale storage facility such as an in-ground storage tank. The boil-off gas from tank 52 at approximately 15 pounds pressure and 260 F. is compressed by means of any suitable compressor 53 to 18p.s.i.a. and 258 F., and is supplied in line'54 to join the gasin line 47, for subsequent further compression by boil-off compressor 48 to 80 p.s.i.a., at which pressure it is supplied to thedistribution line 33, as previously described.
The refrigerant -vapors in lines 15, 16 and 17 are fed to successive stages of a multistage centrifugal compressor 18, which is another advantage of the presentsystem.
In the past, it has been difficult to utilize centrifugal cornt pressors for liquefaction rates as large as those envisaged in a typical system for which the invention would be used (5.0 MM s.c.f.d.) because of their low inlet volume. However, using a refrigerant such as Freon 13 B-l, exchanger l8 has a vapor pressureof 2.7 p.s.i.a., and with this low suction pressure the use of a centrifugal compressor is feasible due to the high inlet a.c.f.m. (actual cubic feet per minute). The arrangement of injecting the other feed streams at the inner stages increases the a.c.f.m. to each stage, which is desirable in the use of centrifugal compressors in this type of service. The compressed refrigerant emerges in line 54 at approximately 325 p.s.i.a., and is cooled, preferably by water cooler 56 to 100 F., after which it is supplied to surge tank 9, from which it is withdrawn on line 8 as previously described.
It will be noted that the above system, in addition to being highly efficient with respect to power requirements, thus enables the use of a single compressor, with consequent reduction in cost. Furthermore, the heat exchangers, for a liquefaction plant ranging in size up to 5.0l MM s.c.f.d. can be incorporated in a unitized` construction of exchangers stacked one above `the other, all .within a cold box structure and skid mounted for convenient transportation. It is thus apparent thatl the above-described system is economical in cost as well as eflicient in operation. The removal of heavies ,while the gas is at high pressure and prior to subcooling has the further advantage of minimizing'the possibility of riming problems which these heavies could cause in the subsequent exchangers 21, 10 which are used for subcooling the gas stream. Furthermore, the external refrigeration system can be easily derimed when necessary Vby passing warm feed gas through the exchangers 5, 6 and 7, and collecting the deriming product in the B.t.u. heavies vessel 27; alternatively, methanol can be injected into the feed gas stream yfor rime removal and collection in' the same vessel, thus minimizing the time neededv for the liquefaction unit to be out of service or bypassed. It will be apparent that the above simplified design lends itself to shop fabrication resulting in reduced field-costaud direction. When the LNG stored in the tank 52 is needed to supplement the normal supply provided to the consumer distribution system, e.g., during periods of peak demand, it is pumped out of storage and regasified in any known manner, and supplied to the distribution line without any further B.t.u. treatment being required, as it has the proper B.t.u. content by virtue of the above-described process.
It will be apparent that the embodiments shown are only exemplary and that various modifications can be made in construction and arrangement within the scope of the invention as defined in the appended claims.
We claim:
1. A process for supplying natural gas containing different hydrocarbon constituents as an outlet gas stream from a n-atural gas liquefaction process to a distribution system at a desired B.t.u. value, comprising the following steps:
(a) supplying a main stream of natural gas at superatmospheric pressure well above the normal pressure of the distribution system,
(b) liquefying said main stream of natural gas at high pressure to produce liquefied natural gas at high pressure,
(c) reducing the pressure of a major portion of said liquefied natural gas to a low storage pressure and storing it at said low pressure,
(d) removing a minor proportion of said liquefied natural gas at high pressure and reducing its pressure to produce flash gases and a heavier fraction of liquefied hydrocarbons, removing the heavier fraction from the separator exclusive of the flashed gases under calorimeter control, and
(e) regasifying said heavier fraction and adding it to the distribution system -at a rate to maintain the -,B.t.u..value of the outlet gas stream at a desired value.
2. A process according to claim 1, including the step of returning the flash gases from step (d) of claim 1 to the main stream.
3. A process for supplying natural gas containing different hydrocarbon constituents as an outlet gas stream from a natural gas liquefaction process to a distribution system at a desired B.t.u. value comprising l,
(a) supplying a main stream of natural gas at superatmospheric pressure well above the normal pressure of the distribution system, A
(b) liquefying the main stream of supply gas at superatmospheric pressure by heat exchange with a single external refrigerant and by auto-refrigerative heat exchange with returning flashed gasesv derived from the supply gas,
(c) reducing the pressure of the thus liquefied natural gas in stages to a low storage pressure, and storing the liquefied natural gas at said low pressure,
(d) supplying boil-off gas from said storage, together with flashed gas from the pressure reduction stages to said distribution system,
(e) prior to a pressure reduction stage, taking off, from the main stream of liquefied gas, a minor portion of liquefied gas and reducing its pressure to produce flash gases and a heavier fraction of liquid hydrocarbons, removing the heavier fraction from the separator exclusive of the flashed gases under calorimeter control, and
(f) regasifying said heavier fraction and adding it to the distribution system at -a rate' to maintain the B.t.u. value of the outlet gas stream at adesired value.
4. A process as claimed in claim 3, and the further step of retu'rnin'g the flash gases from said minor proportion of`liquefied natural g'as to the main stream.
5. A process as claimed in claim 3, said superatmospheric pressure being in the order of 635 p.s.i.a., and the single refrigerant being capable of cooling the feed gas at said pressure from F. to 125 F.
6. A process as claimed in claim 3, wherein the heat exchanger with a single refrigerant is performed in three successive stages of refrigeration.
7. A process as claimed in claim 6, wherein the autorefrigeration is performed in two successive stages following the external refrigeration, by withdrawing a small proportion of liquefied natural gas from the main stream at each of said two stages, reducing the pressure of said withdrawing liquefied natural gas, and passing it in heat exchange relationship with the main stream in all of the preceding stages.
8. A process for supplying natural gas containing different hydrocarbon constituents to a distribution system at a desired B.t.u. value, comprising the following steps:
(a) supplying a main stream of natural gas at superatmospheric pressure well above the normal pressure of the distribution system, v
(b) liquefying said main stream of natural gas at high pressure in three stages of cooling by heat exchange with Freon and by auto-refrigerative heat exchange with returning flashed gases derived from the natural gas to produce liquid natural gas at high pressure, said Freon being at a successively lower temperature and pressure in each successive cooling stage,
(c) removing a minor portion of said liquid natural gas at high pressure and reducing its pressure to produce flash gases and a heavier fraction of liquefied hydrocarbons, while another portion of the liquid natural gas is further cooled, then expanded and divided into a first and secondV stream of liquid natural gas,
(d) passing said second stream to storage at low pressure,
gasifying the heavier hydrocarbon fractionl, said combined stream of first stream, vapor from storage and heavier fraction forming an outlet gas which is passed in heat exchange'with said natural gas stream to supply the auto refrigeration of step (b), said heavier hydrocarbon fraction being added at a rate to maintain the B.t.u. value of the outlet gas at a desired value,
(g) passing a stream of refrigerant Freon vapor from each stage of cooling, after the arst, through the preceding stages of cooling in heat exchange relationship therewith without significant change in pressure, each said stream being at the pressure of its respective stage,
(h) compressing said respective refrigerant vapor streams of different pressures by single multistage 20 centrifugal compression, to an initial operating stream of natural gas.
References Cited UNITED STATES PATENTS 2,198,098 4/ 1940 Vaughan. 2,557,171 6/1951 Bodle et al 62-39 XR 2,940,271 6/ 1960 Jackson 62-23 XR 2,960,837 11/1960 Swenson et al. 3,020,723 2/ 1962 De Lury 62-40 XR 3,194,025 7/ 1965 Grossmann 62-40 XR 3,271,965 9/ 1966 Maher et al. 62,-23 3,285,719 11/1966 Bodle et al. 3,315,477 4/1967 Carr 62-23 NORMAN YUDKOFF, Primary Examiner.
V. W. PRETKA, Assistant Examiner.
US57306866 1966-08-17 1966-08-17 Natural gas liquefaction with controlled b.t.u. content Expired - Lifetime US3407052A (en)

Priority Applications (11)

Application Number Priority Date Filing Date Title
US57306866 US3407052A (en) 1966-08-17 1966-08-17 Natural gas liquefaction with controlled b.t.u. content
SE1096467A SE329182B (en) 1966-08-17 1967-07-28
DE19671551617 DE1551617A1 (en) 1966-08-17 1967-08-04 Natural gas liquefaction with controlled BTU content
GB3625267A GB1141219A (en) 1966-08-17 1967-08-08 Supplying natural hydrocarbon gas at a desired calorific value
CH1127567A CH525430A (en) 1966-08-17 1967-08-10 Process for storing a mixture containing different normally gaseous hydrocarbons and providing such a mixture having a desired calorific value
FR117820A FR1534279A (en) 1966-08-17 1967-08-11 Process for supplying a distribution installation with natural gas containing different hydrocarbon constituents at a desired calorific value
ES344074A ES344074A1 (en) 1966-08-17 1967-08-12 Natural gas liquefaction with controlled b.t.u. content
BE702669D BE702669A (en) 1966-08-17 1967-08-14
NO169365A NO120941B (en) 1966-08-17 1967-08-14
NL6711190A NL6711190A (en) 1966-08-17 1967-08-15
AT752767A AT275486B (en) 1966-08-17 1967-08-16 Natural gas liquefaction with controlled calorific value

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US57306866 US3407052A (en) 1966-08-17 1966-08-17 Natural gas liquefaction with controlled b.t.u. content

Publications (1)

Publication Number Publication Date
US3407052A true US3407052A (en) 1968-10-22

Family

ID=24290507

Family Applications (1)

Application Number Title Priority Date Filing Date
US57306866 Expired - Lifetime US3407052A (en) 1966-08-17 1966-08-17 Natural gas liquefaction with controlled b.t.u. content

Country Status (10)

Country Link
US (1) US3407052A (en)
AT (1) AT275486B (en)
BE (1) BE702669A (en)
CH (1) CH525430A (en)
DE (1) DE1551617A1 (en)
ES (1) ES344074A1 (en)
GB (1) GB1141219A (en)
NL (1) NL6711190A (en)
NO (1) NO120941B (en)
SE (1) SE329182B (en)

Cited By (51)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3494751A (en) * 1966-02-05 1970-02-10 Messer Griesheim Gmbh Process for the fractionation of natural gas
US3527585A (en) * 1967-12-01 1970-09-08 Exxon Research Engineering Co Method and apparatus for the control of the heating value of natural gas
US3658499A (en) * 1970-10-28 1972-04-25 Chicago Bridge & Iron Co Method of diluting liquefied gases
US3747359A (en) * 1969-08-01 1973-07-24 Linde Ag Gas liquefaction by a fractionally condensed refrigerant
US3857251A (en) * 1971-12-27 1974-12-31 Technigaz Lng storage tank vapor recovery by nitrogen cycle refrigeration with refrigeration make-up provided by separation of same vapor
US3901673A (en) * 1972-12-15 1975-08-26 Phillips Petroleum Co Recovery of natural gas liquids by partial condensation
US3914949A (en) * 1971-02-19 1975-10-28 Chicago Bridge & Iron Co Method and apparatus for liquefying gases
US4828591A (en) * 1988-08-08 1989-05-09 Mobil Oil Corporation Method and apparatus for the liquefaction of natural gas
US5359856A (en) * 1993-10-07 1994-11-01 Liquid Carbonic Corporation Process for purifying liquid natural gas
US5669238A (en) * 1996-03-26 1997-09-23 Phillips Petroleum Company Heat exchanger controls for low temperature fluids
WO1997036139A1 (en) * 1996-03-26 1997-10-02 Phillips Petroleum Company Aromatics and/or heavies removal from a methane-based feed by condensation and stripping
US20050126220A1 (en) * 2003-12-15 2005-06-16 Ward Patrick B. Systems and methods for vaporization of liquefied natural gas
US20060086139A1 (en) * 2004-10-25 2006-04-27 Conocophillips Company LNG system employing stacked vertical heat exchangers to provide liquid reflux stream
US20060086140A1 (en) * 2004-10-25 2006-04-27 Conocophillips Company Vertical heat exchanger configuration for LNG facility
US20060144080A1 (en) * 2004-09-22 2006-07-06 Heath Rodney T Vapor process system
US20060213223A1 (en) * 2001-05-04 2006-09-28 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
US20060218939A1 (en) * 2001-05-04 2006-10-05 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
US20070017250A1 (en) * 2001-05-04 2007-01-25 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
US20070107465A1 (en) * 2001-05-04 2007-05-17 Battelle Energy Alliance, Llc Apparatus for the liquefaction of gas and methods relating to same
US20070186770A1 (en) * 2004-09-22 2007-08-16 Heath Rodney T Natural Gas Vapor Recovery Process System
US20080087041A1 (en) * 2004-09-14 2008-04-17 Denton Robert D Method of Extracting Ethane from Liquefied Natural Gas
US20080190352A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship and operation thereof
US20080295527A1 (en) * 2007-05-31 2008-12-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship with nitrogen generator and method of operating the same
US20090071634A1 (en) * 2007-09-13 2009-03-19 Battelle Energy Alliance, Llc Heat exchanger and associated methods
US20090199759A1 (en) * 2008-02-11 2009-08-13 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US20090217701A1 (en) * 2005-08-09 2009-09-03 Moses Minta Natural Gas Liquefaction Process for Ling
US20090223246A1 (en) * 2008-03-06 2009-09-10 Heath Rodney T Liquid Hydrocarbon Slug Containing Vapor Recovery System
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
US20100040989A1 (en) * 2008-03-06 2010-02-18 Heath Rodney T Combustor Control
US20100107684A1 (en) * 2007-05-03 2010-05-06 Moses Minta Natural Gas Liquefaction Process
US20100122542A1 (en) * 2008-11-17 2010-05-20 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and apparatus for adjusting heating value of natural gas
US20110036543A1 (en) * 2009-01-30 2011-02-17 Conocophillips Company Method and System for Deriming Cryogenic Heat Exchangers
US7905722B1 (en) 2002-02-08 2011-03-15 Heath Rodney T Control of an adjustable secondary air controller for a burner
US20110094263A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams
US20110094261A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Natural gas liquefaction core modules, plants including same and related methods
US20110197925A1 (en) * 2010-01-27 2011-08-18 Conocophillips Company Method and apparatus for deriming cryogenic equipment
US8555672B2 (en) 2009-10-22 2013-10-15 Battelle Energy Alliance, Llc Complete liquefaction methods and apparatus
US20140230458A1 (en) * 2013-02-19 2014-08-21 Hyundai Heavy Industries Co., Ltd. System for supplying liquefied natural gas fuel
US8864887B2 (en) 2010-09-30 2014-10-21 Rodney T. Heath High efficiency slug containing vapor recovery
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
US9291409B1 (en) 2013-03-15 2016-03-22 Rodney T. Heath Compressor inter-stage temperature control
US20160290563A1 (en) * 2015-04-02 2016-10-06 David A. Diggins System and Method for Unloading Compressed Natural Gas
US9527786B1 (en) 2013-03-15 2016-12-27 Rodney T. Heath Compressor equipped emissions free dehydrator
US20170038139A1 (en) * 2015-08-06 2017-02-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of liquefied natural gas
US9574713B2 (en) 2007-09-13 2017-02-21 Battelle Energy Alliance, Llc Vaporization chambers and associated methods
US9932989B1 (en) 2013-10-24 2018-04-03 Rodney T. Heath Produced liquids compressor cooler
US10052565B2 (en) 2012-05-10 2018-08-21 Rodney T. Heath Treater combination unit
US10655911B2 (en) 2012-06-20 2020-05-19 Battelle Energy Alliance, Llc Natural gas liquefaction employing independent refrigerant path

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2198098A (en) * 1939-02-06 1940-04-23 Tide Water Associated Oil Comp High pressure gas process
US2557171A (en) * 1946-11-12 1951-06-19 Pritchard & Co J F Method of treating natural gas
US2940271A (en) * 1959-03-24 1960-06-14 Fluor Corp Low temperature fractionation of natural gas components
US2960837A (en) * 1958-07-16 1960-11-22 Conch Int Methane Ltd Liquefying natural gas with low pressure refrigerants
US3020723A (en) * 1957-11-25 1962-02-13 Conch Int Methane Ltd Method and apparatus for liquefaction of natural gas
US3194025A (en) * 1963-01-14 1965-07-13 Phillips Petroleum Co Gas liquefactions by multiple expansion refrigeration
US3271965A (en) * 1963-01-08 1966-09-13 Chicago Bridge & Iron Co Methane liquefaction process
US3285719A (en) * 1963-05-23 1966-11-15 Ofw xx
US3315477A (en) * 1964-07-15 1967-04-25 Conch Int Methane Ltd Cascade cycle for liquefaction of natural gas

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2198098A (en) * 1939-02-06 1940-04-23 Tide Water Associated Oil Comp High pressure gas process
US2557171A (en) * 1946-11-12 1951-06-19 Pritchard & Co J F Method of treating natural gas
US3020723A (en) * 1957-11-25 1962-02-13 Conch Int Methane Ltd Method and apparatus for liquefaction of natural gas
US2960837A (en) * 1958-07-16 1960-11-22 Conch Int Methane Ltd Liquefying natural gas with low pressure refrigerants
US2940271A (en) * 1959-03-24 1960-06-14 Fluor Corp Low temperature fractionation of natural gas components
US3271965A (en) * 1963-01-08 1966-09-13 Chicago Bridge & Iron Co Methane liquefaction process
US3194025A (en) * 1963-01-14 1965-07-13 Phillips Petroleum Co Gas liquefactions by multiple expansion refrigeration
US3285719A (en) * 1963-05-23 1966-11-15 Ofw xx
US3315477A (en) * 1964-07-15 1967-04-25 Conch Int Methane Ltd Cascade cycle for liquefaction of natural gas

Cited By (92)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3494751A (en) * 1966-02-05 1970-02-10 Messer Griesheim Gmbh Process for the fractionation of natural gas
US3527585A (en) * 1967-12-01 1970-09-08 Exxon Research Engineering Co Method and apparatus for the control of the heating value of natural gas
US3747359A (en) * 1969-08-01 1973-07-24 Linde Ag Gas liquefaction by a fractionally condensed refrigerant
US3658499A (en) * 1970-10-28 1972-04-25 Chicago Bridge & Iron Co Method of diluting liquefied gases
US3914949A (en) * 1971-02-19 1975-10-28 Chicago Bridge & Iron Co Method and apparatus for liquefying gases
US3857251A (en) * 1971-12-27 1974-12-31 Technigaz Lng storage tank vapor recovery by nitrogen cycle refrigeration with refrigeration make-up provided by separation of same vapor
US3901673A (en) * 1972-12-15 1975-08-26 Phillips Petroleum Co Recovery of natural gas liquids by partial condensation
US4828591A (en) * 1988-08-08 1989-05-09 Mobil Oil Corporation Method and apparatus for the liquefaction of natural gas
US5359856A (en) * 1993-10-07 1994-11-01 Liquid Carbonic Corporation Process for purifying liquid natural gas
WO1995010010A1 (en) * 1993-10-07 1995-04-13 Liquid Carbonic Corporation Process for purifying liquid natural gas
US5669238A (en) * 1996-03-26 1997-09-23 Phillips Petroleum Company Heat exchanger controls for low temperature fluids
WO1997036139A1 (en) * 1996-03-26 1997-10-02 Phillips Petroleum Company Aromatics and/or heavies removal from a methane-based feed by condensation and stripping
EA000800B1 (en) * 1996-03-26 2000-04-24 Филлипс Петролеум Компани Method for removal aromatic and/or higher-molecular hydrocarbons from a methane-based gas stream by condensation and stripping and associated apparatus therefor
US20060218939A1 (en) * 2001-05-04 2006-10-05 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
US7637122B2 (en) 2001-05-04 2009-12-29 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
US7594414B2 (en) * 2001-05-04 2009-09-29 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
US20100186446A1 (en) * 2001-05-04 2010-07-29 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
US20060213223A1 (en) * 2001-05-04 2006-09-28 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
US7591150B2 (en) * 2001-05-04 2009-09-22 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
US20070017250A1 (en) * 2001-05-04 2007-01-25 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
US20070107465A1 (en) * 2001-05-04 2007-05-17 Battelle Energy Alliance, Llc Apparatus for the liquefaction of gas and methods relating to same
US7905722B1 (en) 2002-02-08 2011-03-15 Heath Rodney T Control of an adjustable secondary air controller for a burner
US20050126220A1 (en) * 2003-12-15 2005-06-16 Ward Patrick B. Systems and methods for vaporization of liquefied natural gas
US7299655B2 (en) 2003-12-15 2007-11-27 Bp Corporation North America Inc. Systems and methods for vaporization of liquefied natural gas
US20080087041A1 (en) * 2004-09-14 2008-04-17 Denton Robert D Method of Extracting Ethane from Liquefied Natural Gas
US8156758B2 (en) 2004-09-14 2012-04-17 Exxonmobil Upstream Research Company Method of extracting ethane from liquefied natural gas
US20070186770A1 (en) * 2004-09-22 2007-08-16 Heath Rodney T Natural Gas Vapor Recovery Process System
US20060144080A1 (en) * 2004-09-22 2006-07-06 Heath Rodney T Vapor process system
US9353315B2 (en) * 2004-09-22 2016-05-31 Rodney T. Heath Vapor process system
US20080022716A1 (en) * 2004-10-25 2008-01-31 Conocophillips Company Lng system employing stacked vertical heat exchangers to provide liquid reflux stream
US8424340B2 (en) 2004-10-25 2013-04-23 Conocophillips Company LNG system employing stacked vertical heat exchangers to provide liquid reflux stream
US20060086139A1 (en) * 2004-10-25 2006-04-27 Conocophillips Company LNG system employing stacked vertical heat exchangers to provide liquid reflux stream
AU2005299930B2 (en) * 2004-10-25 2011-02-03 Conocophillips Company Vertical heat exchanger configuration for LNG facility
US7310971B2 (en) 2004-10-25 2007-12-25 Conocophillips Company LNG system employing optimized heat exchangers to provide liquid reflux stream
US7266976B2 (en) * 2004-10-25 2007-09-11 Conocophillips Company Vertical heat exchanger configuration for LNG facility
WO2006047097A3 (en) * 2004-10-25 2007-02-08 Conoco Phillips Company Vertical heat exchanger configuration for lng facility
US20060086140A1 (en) * 2004-10-25 2006-04-27 Conocophillips Company Vertical heat exchanger configuration for LNG facility
US20090217701A1 (en) * 2005-08-09 2009-09-03 Moses Minta Natural Gas Liquefaction Process for Ling
US20080190118A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and unloading of lng from the tank
US8028724B2 (en) 2007-02-12 2011-10-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and unloading of LNG from the tank
US10508769B2 (en) 2007-02-12 2019-12-17 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US8820096B2 (en) 2007-02-12 2014-09-02 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US20090211262A1 (en) * 2007-02-12 2009-08-27 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship having lng circulating device
US20080190352A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship and operation thereof
US11168837B2 (en) 2007-02-12 2021-11-09 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US10352499B2 (en) 2007-02-12 2019-07-16 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US8943841B2 (en) 2007-02-12 2015-02-03 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank ship having LNG circulating device
US20080190117A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and operation of the same
US20090266086A1 (en) * 2007-04-30 2009-10-29 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Floating marine structure having lng circulating device
US8616021B2 (en) 2007-05-03 2013-12-31 Exxonmobil Upstream Research Company Natural gas liquefaction process
US20100107684A1 (en) * 2007-05-03 2010-05-06 Moses Minta Natural Gas Liquefaction Process
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
US9254448B2 (en) 2007-09-13 2016-02-09 Battelle Energy Alliance, Llc Sublimation systems and associated methods
US20090071634A1 (en) * 2007-09-13 2009-03-19 Battelle Energy Alliance, Llc Heat exchanger and associated methods
US9574713B2 (en) 2007-09-13 2017-02-21 Battelle Energy Alliance, Llc Vaporization chambers and associated methods
US9217603B2 (en) 2007-09-13 2015-12-22 Battelle Energy Alliance, Llc Heat exchanger and related methods
US8061413B2 (en) 2007-09-13 2011-11-22 Battelle Energy Alliance, Llc Heat exchangers comprising at least one porous member positioned within a casing
US8544295B2 (en) 2007-09-13 2013-10-01 Battelle Energy Alliance, Llc Methods of conveying fluids and methods of sublimating solid particles
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
US20100012015A1 (en) * 2008-02-11 2010-01-21 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US7644676B2 (en) 2008-02-11 2010-01-12 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US7841288B2 (en) 2008-02-11 2010-11-30 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US20090199759A1 (en) * 2008-02-11 2009-08-13 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US20100040989A1 (en) * 2008-03-06 2010-02-18 Heath Rodney T Combustor Control
US20090223246A1 (en) * 2008-03-06 2009-09-10 Heath Rodney T Liquid Hydrocarbon Slug Containing Vapor Recovery System
US8529215B2 (en) 2008-03-06 2013-09-10 Rodney T. Heath Liquid hydrocarbon slug containing vapor recovery system
US8840703B1 (en) 2008-03-06 2014-09-23 Rodney T. Heath Liquid hydrocarbon slug containing vapor recovery system
US8900343B1 (en) 2008-03-06 2014-12-02 Rodney T. Heath Liquid hydrocarbon slug containing vapor recovery system
US9086188B2 (en) 2008-04-10 2015-07-21 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and system for reducing heating value of natural gas
US20090259081A1 (en) * 2008-04-10 2009-10-15 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and system for reducing heating value of natural gas
US8381544B2 (en) * 2008-07-18 2013-02-26 Kellogg Brown & Root Llc Method for liquefaction of natural gas
US20100011663A1 (en) * 2008-07-18 2010-01-21 Kellogg Brown & Root Llc Method for Liquefaction of Natural Gas
US20100122542A1 (en) * 2008-11-17 2010-05-20 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and apparatus for adjusting heating value of natural gas
US8257508B2 (en) * 2009-01-30 2012-09-04 Conocophillips Company Method and system for deriming cryogenic heat exchangers
US20110036543A1 (en) * 2009-01-30 2011-02-17 Conocophillips Company Method and System for Deriming Cryogenic Heat Exchangers
US8899074B2 (en) 2009-10-22 2014-12-02 Battelle Energy Alliance, Llc Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams
US20110094261A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Natural gas liquefaction core modules, plants including same and related methods
US20110094263A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams
US8555672B2 (en) 2009-10-22 2013-10-15 Battelle Energy Alliance, Llc Complete liquefaction methods and apparatus
US8257509B2 (en) * 2010-01-27 2012-09-04 Conocophillips Company Method and apparatus for deriming cryogenic equipment
US20110197925A1 (en) * 2010-01-27 2011-08-18 Conocophillips Company Method and apparatus for deriming cryogenic equipment
US8864887B2 (en) 2010-09-30 2014-10-21 Rodney T. Heath High efficiency slug containing vapor recovery
US10052565B2 (en) 2012-05-10 2018-08-21 Rodney T. Heath Treater combination unit
US10655911B2 (en) 2012-06-20 2020-05-19 Battelle Energy Alliance, Llc Natural gas liquefaction employing independent refrigerant path
US20140230458A1 (en) * 2013-02-19 2014-08-21 Hyundai Heavy Industries Co., Ltd. System for supplying liquefied natural gas fuel
US9291409B1 (en) 2013-03-15 2016-03-22 Rodney T. Heath Compressor inter-stage temperature control
US9527786B1 (en) 2013-03-15 2016-12-27 Rodney T. Heath Compressor equipped emissions free dehydrator
US9932989B1 (en) 2013-10-24 2018-04-03 Rodney T. Heath Produced liquids compressor cooler
US9784411B2 (en) * 2015-04-02 2017-10-10 David A. Diggins System and method for unloading compressed natural gas
US20160290563A1 (en) * 2015-04-02 2016-10-06 David A. Diggins System and Method for Unloading Compressed Natural Gas
US20170038138A1 (en) * 2015-08-06 2017-02-09 L'air Liquide, Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude Apparatus for the production of liquefied natural gas
US20170038139A1 (en) * 2015-08-06 2017-02-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the production of liquefied natural gas

Also Published As

Publication number Publication date
CH525430A (en) 1972-07-15
ES344074A1 (en) 1968-09-16
DE1551617A1 (en) 1970-03-19
AT275486B (en) 1969-10-27
NO120941B (en) 1970-12-28
SE329182B (en) 1970-10-05
BE702669A (en) 1968-01-15
GB1141219A (en) 1969-01-29
NL6711190A (en) 1968-02-19

Similar Documents

Publication Publication Date Title
US3407052A (en) Natural gas liquefaction with controlled b.t.u. content
US3347055A (en) Method for recuperating refrigeration
JP3868998B2 (en) Liquefaction process
US9528758B2 (en) Method and system for regulation of cooling capacity of a cooling system based on a gas expansion process
US3095274A (en) Hydrogen liquefaction and conversion systems
CN101097112B (en) Method for air feeding in low temperature separation process
US3218816A (en) Process for cooling a gas mixture to a low temperature
US6131407A (en) Natural gas letdown liquefaction system
CN100400994C (en) Self-refrigerated LNG process
US5657643A (en) Closed loop single mixed refrigerant process
CN1102213C (en) Reliquefaction of boil-off from pressure LNG
US3323315A (en) Gas liquefaction employing an evaporating and gas expansion refrigerant cycles
US3932154A (en) Refrigerant apparatus and process using multicomponent refrigerant
JPH0587558B2 (en)
US3440828A (en) Liquefaction of natural gas employing cascade refrigeration
US3377811A (en) Liquefaction process employing expanded feed as refrigerant
JPH0545050A (en) Method for liquefying permanent gas using cryogenic cold of liquefied natural gas
NL6504188A (en)
JP2001056177A (en) Air separation unit
US4874413A (en) Process and installation for supplying nitrogen to an apparatus
JPH06241647A (en) Hydrogen liquefying equipment and slush hydrogen producing equipment
JPH10206010A (en) Method of separating air and device
AU681954B2 (en) Liquefaction process
JPH10206009A (en) Air separator
CN1187877A (en) Energy saving process