US3323315A - Gas liquefaction employing an evaporating and gas expansion refrigerant cycles - Google Patents

Gas liquefaction employing an evaporating and gas expansion refrigerant cycles Download PDF

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US3323315A
US3323315A US382775A US38277564A US3323315A US 3323315 A US3323315 A US 3323315A US 382775 A US382775 A US 382775A US 38277564 A US38277564 A US 38277564A US 3323315 A US3323315 A US 3323315A
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gas
refrigerant
methane
line
feed
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US382775A
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Jackson O Carr
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Conch International Methane Ltd
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Conch International Methane Ltd
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Priority to US382775A priority Critical patent/US3323315A/en
Priority to GB19329/65A priority patent/GB1056013A/en
Priority to FR23006A priority patent/FR1441864A/fr
Priority to NL6509010A priority patent/NL6509010A/xx
Priority to OA52115A priority patent/OA01772A/xx
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    • 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
    • F25J1/0208—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 in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a 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
    • F25J1/0032—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
    • F25J1/0047—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
    • F25J1/008—Hydrocarbons
    • F25J1/0087—Propane; Propylene
    • 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
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • 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

  • This invention relates to an improved method and apparatus for the liquefaction of gas, particularly natural gas, and has for its principal object considerably simplifying the equipment and ease of operation and lowering the cost in comparison with known methods.
  • Cascade refrigeration techniques for liquefying natural or other gases on a large scale are well known, for example as shown in U.S. Patent No. 3,020,723 to De Lury et al.
  • Known systems in order to operate at reasonable eiciencies, require a yrelatively large number of cascade stages, generally using several different refrigerants having successfully lower boiling temperatures, in order to achieve the desired efficiency.
  • the present invention achieves a high degree of eiciency by first cooling the natural gas under high pressure with a vapor compression refrigeration cycle in which the natural gas is heat exchanged against an evaporating liquid (e.g., propane) and then, at the same high pressure, is heat exchanged against cold gas in a gas expansion cycle with no liquefaction of the refrigerant gas.
  • an evaporating liquid e.g., propane
  • the gas in the gas expansion cycle is itself cooled against evaporating liquid in the vapor compression cycle to efficiently utilize the refrigeration potential thereof;
  • another feature of the invention is that the refrigerant gas in the gas expansion cycle is the same type of gas as is being liqueed, typically methane, and that ash methane from the pressure let down of the liquefied main stream is put directly into the gas expansion cycle, preferably at more than one stage.
  • Another feature is that the expansion in the gas expansion cycle takes place in' two stages, and the cold gas is put into heat exchange with the main stream between these two expansion stages, as well as after the second stage.
  • a further advantage of the system is that it can handle gas with a relatively high content of impurities of higher volatility than the main constituent, e.g., nitrogen, without special precautions being taken to remove such impurities,
  • FIG. l is a flow chart of a typical embodiment of the invention.
  • the incoming natural gas in line 1 is initially at a pressure of about 750 p.s.i.a. and a tem- ICC perature of about F.
  • the natural gas is initially subjected to two successive stages of heat exchange in a propane cycle, in heat exchangers 2 and 3.
  • the propane from storage tank 4 at 130 p.s.i.a. is let down sufficiently to cool the feed gas in line 1 down to 29 F.
  • Throttle 2a is used with a conventional level-control device 2b to control the liquid level in heat exchanger 3, and similar control means are provided for heat exchangers 3, 13 and 21.
  • the vapor which is flashed off upon expansion in the heat exchanger is conducted in line 6 to line 7, and thence to propane compressor 8 which raises its pressure to 130 p.s.i.a., and after cooling down 70 F. in a heat sink 9, it is returned to the storage tank 4, from which it is taken in line 1.1 to heat exchanger 2.
  • Some of this propane is also diverted in line 12 to heat exchanger 13, where it is used to cool refrigerating gas in the gas expansion cycle as will be explained later.
  • Liquid propane from heat exchanger 2 is also taken in line 14 for use in heat exchanger 3, in which the feed gas is further cooled to minus 20 F. without reduction in pressure.
  • Flash vapor from heat exchanger 3 is taken in line 16 at minus 25 F., and in line 17 at 22 p.s.i.a. to propane compressor 18, in which it is compressed and delivered .to line 19 in a condition similar to the propane in line 7, which it joins as input to propane compressor 8.
  • Propane from heat exchanger 13 is similarly passed through a second heat exchanger 21 to further re-cool refrigerant gas in line 27a which was previously cooled in heat exchanger 13.
  • the ⁇ feed vgas emerges from heat exchanger 24 at a temperature of minus 238 F., and still at high pressure. It will be noted that the temperature of the feed gas was reduced, after passing heat exchanger 22 Ito minus 105 F.; the feed gas is condensed into liquid form in heat exchanger 23.
  • the liquid feed gas emerging rfrom heat exchanger 24 is now throttled down at 26, under control of pressure control device 26a, into flash tank 28, where its pressure is reduced to slightly above atmospheric.
  • the resulting vaporization of some of the feed gas lowers the temperature of the liquid gas in 28 to minus 258 F., at which temperature it is taken in line 29, raised in pressure by compressor 35 to approximately 30 p.s.i.a., and throttled in throttle 50 down into nal storage .tank 31 at -15 p.s.i.a.
  • the liquid methane in final storage tank 31 is at minus 258 F. and l5 p.s.i.a.
  • the methane stream is cooled by heat sinks 42, 43, 44 and 46, which may be water coolers.
  • Part of the output from compressor stage 39 is diverted in line 40 at 331 p.s.i.a. and 70 F. for use as plant fuel, or any other purpose. At the operating conditions indicated, this output may amount to approximately of the input feed gas.
  • the rest of the output ⁇ from compressor 39 is further rcompressed in the final stage compressor 41 and delivered to line 27a at 1020 p.s.i.a., and a final temperature (after passing through heat sink 46) of 70 F.
  • This stream is then precooled in heat exchangers 13 Vand 21 as previously described, by heat exchange with propane from the propane cycle.
  • methane in line 27b is at minus 20 F. and 1,000 p.s.i.a.; this gas is now expanded in methane expander 47 (with the production of some useful work) to a temperature of minus 180 F., and then is passed in line 27C into heat exchanger 23, in conjunction with a separate gas feed stream to be later described. It assists in cooling the feed stream in line 1 from a temperature of minus 105 F. to a temperature of yminus 161 F., as Shown in the ow chart.
  • the methane in line 27d after passing through heat exchanger 23, is at a temperature of minus 120 F.
  • the gas expansion cooling cycle flows in an essentially closed circuit including the methane compressors, methane expanders, and heat exchangers 22, 23 and 24, with flash vapor from the feed gas added in lines 30 and 34, and a corresponding amount of methane gas removed in line 40.
  • a typical liquefaction plant using the invention may have an input flow of over 500,000 pounds per hour, a final storage capacity of 600,000 barrels for receiving liquefied gas at the rate of over 400,000 pounds per hour, and a plant fuel output on line 47 ⁇ of nearly 50,000 pounds per hour.
  • the present invention is directed toward improving both of these factors.
  • Method of liquefying a gas comprising (a) supplying the gas in a main feed stream at high pressure exceeding 300 p.s.i.a. and substantially ambient temperature,
  • Method as claimed in claim 2 including the steps of (a) expanding said second refrigerant in step (e) of claim 1 in two stages,
  • step (c) of claim 3 is performed in several heat exchange steps in series, while the heat exchange of step (b) of claim 3 is performed in conjunction with only one of said series steps.
  • Method of liquefying a gas comprising (a) supplying the gas in a main feed stream at high pressure and substantially ambient temperature,
  • Method as claimed in claim 6, including the steps of (a) expanding said second refrigerant in two stage-s,
  • Method of liquefying a gas comprising (a) supplying the gas in a main feed stream at high pressure and substantially ambient temperature,
  • step (d) cooling the feed gas by heat exchange with a throttled separate evaporating refrigerant from one of the paths while maintaining the feed gas at its high presseries, While the heat exchange of step (g) is performed sure, in conjunction with only one of said series steps.
  • step (e) further cooling the feed gas to below its critical temperature and said high pressure by heat exchange References Cted With a second refrigerant in a recirculating gas eX- 5 UNITED STATES PATENTS pansion cycle wherein said second refrigerant is com- 2 696 088 12/1954 Twomey 62 40 X pressed as a gas, cooled to substantially ambient tem- 2960837 11/1960 Swenson eg'a 62 40 X perature as a gas, expanded to a low temperature as a 2996891 8/1961 Tung gas, and heat exchanged with the feed gas, 3020723V 2/1962 De Lury et aL 62 40 X (f) expanding said second refrigerant
  • step (h) of claim 8 is performed in several heat exchange steps in V- W PRETKA, ASSISIHUI Exllmmeh

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US382775A 1964-07-15 1964-07-15 Gas liquefaction employing an evaporating and gas expansion refrigerant cycles Expired - Lifetime US3323315A (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
US382775A US3323315A (en) 1964-07-15 1964-07-15 Gas liquefaction employing an evaporating and gas expansion refrigerant cycles
GB19329/65A GB1056013A (en) 1964-07-15 1965-05-07 Gas liquefaction with vapour compression and gas expansion cycles
FR23006A FR1441864A (fr) 1964-07-15 1965-06-30 Liquéfaction de gaz avec cycles de compression de vapeur et de détente de gaz
NL6509010A NL6509010A (enrdf_load_stackoverflow) 1964-07-15 1965-07-13
OA52115A OA01772A (fr) 1964-07-15 1965-07-15 Liquéfaction de gaz avec cycles de compression de vapeur et détente de gaz.

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US382775A US3323315A (en) 1964-07-15 1964-07-15 Gas liquefaction employing an evaporating and gas expansion refrigerant cycles

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US3323315A true US3323315A (en) 1967-06-06

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US382775A Expired - Lifetime US3323315A (en) 1964-07-15 1964-07-15 Gas liquefaction employing an evaporating and gas expansion refrigerant cycles

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US (1) US3323315A (enrdf_load_stackoverflow)
FR (1) FR1441864A (enrdf_load_stackoverflow)
GB (1) GB1056013A (enrdf_load_stackoverflow)
NL (1) NL6509010A (enrdf_load_stackoverflow)
OA (1) OA01772A (enrdf_load_stackoverflow)

Cited By (26)

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JPS4910325B1 (enrdf_load_stackoverflow) * 1968-09-18 1974-03-09
US4322182A (en) * 1979-01-15 1982-03-30 Ostgaard John T Apparatus and method for under-water jacking of piles
US6105390A (en) * 1997-12-16 2000-08-22 Bechtel Bwxt Idaho, Llc Apparatus and process for the refrigeration, liquefaction and separation of gases with varying levels of purity
WO2000077466A1 (en) * 1999-06-15 2000-12-21 Exxonmobil Oil Corporation Process and system for liquefying natural gas
US20030089125A1 (en) * 2000-03-15 2003-05-15 Fredheim Arne Olay Natural gas liquefaction process
US6886362B2 (en) 2001-05-04 2005-05-03 Bechtel Bwxt Idaho Llc Apparatus for the liquefaction of natural 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
US20060218939A1 (en) * 2001-05-04 2006-10-05 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural 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
US7219512B1 (en) 2001-05-04 2007-05-22 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
US20070137246A1 (en) * 2001-05-04 2007-06-21 Battelle Energy Alliance, Llc Systems and methods for delivering hydrogen and separation of hydrogen from a carrier medium
US20090071634A1 (en) * 2007-09-13 2009-03-19 Battelle Energy Alliance, Llc Heat exchanger and associated methods
US20090217701A1 (en) * 2005-08-09 2009-09-03 Moses Minta Natural Gas Liquefaction Process for Ling
US20090260392A1 (en) * 2008-04-17 2009-10-22 Linde Aktiengesellschaft Method of liquefying a hydrocarbon-rich fraction
US7637122B2 (en) 2001-05-04 2009-12-29 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
US20100107684A1 (en) * 2007-05-03 2010-05-06 Moses Minta Natural Gas Liquefaction Process
US20100186445A1 (en) * 2007-08-24 2010-07-29 Moses Minta Natural Gas Liquefaction Process
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
US20110094262A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Complete liquefaction methods and apparatus
EP2796819A3 (en) * 2013-04-24 2015-12-16 GNC Galileo S.A. Method and apparatus for the liquefaction of natural gas
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
EP3647395A4 (en) * 2017-11-24 2020-07-29 LG Chem, Ltd. METHOD FOR EVAPORATING LIQUID PROPANE AND EVAPORATING DEVICE THEREFOR

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FR2891900B1 (fr) 2005-10-10 2008-01-04 Technip France Sa Procede de traitement d'un courant de gnl obtenu par refroidissement au moyen d'un premier cycle de refrigeration et installation associee.

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US7594414B2 (en) 2001-05-04 2009-09-29 Battelle Energy Alliance, Llc Apparatus for the liquefaction of natural gas and methods relating to same
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US8616021B2 (en) 2007-05-03 2013-12-31 Exxonmobil Upstream Research Company Natural gas liquefaction process
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US9140490B2 (en) 2007-08-24 2015-09-22 Exxonmobil Upstream Research Company Natural gas liquefaction processes with feed gas refrigerant cooling loops
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US9574713B2 (en) 2007-09-13 2017-02-21 Battelle Energy Alliance, Llc Vaporization chambers and associated methods
US9254448B2 (en) 2007-09-13 2016-02-09 Battelle Energy Alliance, Llc Sublimation systems and associated methods
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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
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US10655911B2 (en) 2012-06-20 2020-05-19 Battelle Energy Alliance, Llc Natural gas liquefaction employing independent refrigerant path
EP2796819A3 (en) * 2013-04-24 2015-12-16 GNC Galileo S.A. Method and apparatus for the liquefaction of natural gas
EP3647395A4 (en) * 2017-11-24 2020-07-29 LG Chem, Ltd. METHOD FOR EVAPORATING LIQUID PROPANE AND EVAPORATING DEVICE THEREFOR
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Also Published As

Publication number Publication date
FR1441864A (fr) 1966-06-10
OA01772A (fr) 1970-01-14
GB1056013A (en) 1967-01-25
NL6509010A (enrdf_load_stackoverflow) 1966-01-17

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