US20120060553A1 - Natural gas liquefaction - Google Patents

Natural gas liquefaction Download PDF

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Publication number
US20120060553A1
US20120060553A1 US13/226,633 US201113226633A US2012060553A1 US 20120060553 A1 US20120060553 A1 US 20120060553A1 US 201113226633 A US201113226633 A US 201113226633A US 2012060553 A1 US2012060553 A1 US 2012060553A1
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feed fraction
nitrogen
exchange process
heat exchanger
liquefied
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Abandoned
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US13/226,633
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English (en)
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Heinz Bauer
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Linde GmbH
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Linde GmbH
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Publication of US20120060553A1 publication Critical patent/US20120060553A1/en
Abandoned legal-status Critical Current

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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
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/005—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 expansion of a gaseous refrigerant stream with extraction of work
    • 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
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
    • 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
    • F25J1/0221—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 the cold stored in an external cryogenic component in an open refrigeration 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
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
    • F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant

Definitions

  • the invention relates to a method for liquefying a hydrocarbon-rich feed fraction, preferably natural gas, against a nitrogen refrigeration cycle, wherein the feed fraction is cooled against gaseous nitrogen that is to be warmed and the feed fraction is liquefied against liquid nitrogen that is to be vaporized.
  • Hydrocarbon-rich gases in particular natural gases, are liquefied commercially in a capacity range from 10 to 30,000 tons of LNG per day (tpd).
  • tpd tons of LNG per day
  • plants of medium capacity this is taken to mean liquefaction processes having a capacity between 300 and 3000 tpd of LNG—and large capacity—this is taken to mean liquefaction processes having a capacity between 3000 and 30,000 tpd of LNG—those skilled in the art attempt to optimize the operating costs by means of high efficiency.
  • this is taken to mean liquefaction processes having a capacity between 10 and 300 tpd of LNG—low capital costs are in the foreground.
  • brazed aluminum plate heat exchangers are generally used. These appliances, however, are sensitive to high thermal stresses as can arise, for example, by an oversupply of refrigerant and/or large temperature differences between warm and cold process streams. The resultant mechanical stresses can lead to damage to these appliances.
  • a method of the type in question for liquefying a hydrocarbon-rich feed fraction is known from U.S. Pat. No. 5,390,499. This method is suitable, in particular, for plants of small capacity, as explained at the outset.
  • the gas to be liquefied is cooled and liquefied against nitrogen in two separate heat exchangers. In this case the liquid low-boiling nitrogen is completely vaporized in the second heat exchanger and warmed up to a temperature at which relatively heavy crude gas components can be taken off in the liquid state by means of a separator from the gas that is to be liquefied.
  • the point at which the nitrogen vaporizes completely can vary considerably according to load. This can lead to unwanted process conditions which have the abovementioned disadvantages as a consequence.
  • the method according to the invention is suitable for use in plants of large (3000-30,000 tpd of LNG), medium (300-3,000 tpd of LNG), or small (10-300 tpd of LNG) capacities.
  • the most economical capacity range, however, is 10-300 tpd of LNG.
  • the method according to the invention is directed to liquefaction of a hydrocarbon-rich feed fraction, such as natural gas.
  • the hydrocarbon-rich feed fraction can contain 80 to 99 vol. % methane, 0.1 to 10 vol. % ethane, 0 to 5 vol. % propane, 0 to 4 vol. % C4+hydrocarbons, 0 to 10 vol. % nitrogen, 0 to 10 vol. % carbon dioxide, 0 to 1 vol. % hydrogen sulfide, up to trace amounts of other sulfur species, up to trace amounts of helium, and up to trace amounts of hydrogen.
  • FIGURE illustrates an embodiment according to the invention.
  • the hydrocarbon-rich feed fraction that is to be liquefied is fed via line 1 to a heat exchanger E 1 .
  • This is subdivided into three sections or stages a to c. The boundaries between these sections or stages are shown by the two dashed lines.
  • the hydrocarbon-rich feed fraction is cooled against superheated gaseous nitrogen, which is fed via line 9 to the heat exchanger E 1 .
  • the hydrocarbon-rich feed fraction is cooled to the extent that a separation of the heavy components from the feed fraction is possible in a separator D 2 downstream of the heat exchanger E 1 .
  • the cooled feed fraction is fed from the heat exchanger E 1 via line 1 ′ to the separator D 2 .
  • the unwanted heavy components are removed in liquid form and discharged from the process.
  • a rectification column can be used to achieve a more precise separation of relatively heavy components or higher hydrocarbons from the feed fraction.
  • the feed fraction, freed from heavy components is removed and fed to the second section b of the heat exchanger E 1 .
  • the feed fraction that is freed from heavy components is partially liquefied against gaseous nitrogen that is to be superheated 9 .
  • the feed fraction is completely liquefied against nitrogen to be partially vaporized which is fed to the heat exchanger E 1 via the line 8 .
  • the liquefied feed fraction after passage through the heat exchanger E 1 is fed to a storage vessel D 4 via line 3 , in which a control valve V 3 is arranged.
  • the liquefied product (LNG) can be discharged therefrom via line 4 .
  • the control valve V 3 serves for expanding the liquefied feed fraction to the product delivery pressure, which corresponds at least approximately to atmospheric pressure.
  • the boil-off gas formed in the storage vessel D 4 is advantageously removed via line 5 , compressed in the compressor C 3 and fed back to the feed fraction 2 which is freed from heavy components before liquefaction thereof and reliquefied in the heat exchanger E 1 .
  • This process procedure should be selected, in particular, in the case of significant temporary storage of the LNG product in an atmospheric flat-bottom tank D 4 , since the resultant boil-off gas is also processed thereby.
  • the nitrogen required for providing cold is fed to the liquefaction process via line 6 .
  • a buffer tank D 3 is provided which serves for compensating for quantitative fluctuations of the feed fraction that is to be liquefied and/or of the refrigerant nitrogen.
  • a pump P 1 liquid nitrogen is fed in the amount required to a separator D 1 via line 7 .
  • boiling nitrogen is removed and conducted via line 8 through the coldest section c of the heat exchanger E 1 .
  • the nitrogen that is partially vaporized in this case is then fed via line 8 ′ back to the separator D 1 .
  • gaseous nitrogen is taken off via line 9 and fed to the middle section b of the heat exchanger E 1 .
  • the gaseous nitrogen is conducted through the second and first sections of the heat exchanger E 1 in countercurrent flow to the feed fraction 2 that is to be cooled and partially liquefied, and is warmed and superheated in this process.
  • the superheated nitrogen is then removed from the process via the line sections 10 and 11 .
  • the boiling pressure of the gaseous nitrogen that is to be superheated 9 can be controlled.
  • this boiling pressure is adjusted to values between 5 and 30 bara, preferably between 10 and 20 bara.
  • condensation pressure of the feed fraction 2 that is freed from relatively heavy components can be controlled by means of the control valve V 2 .
  • This condensation pressure is preferably adjusted to values between 1 and 15 bara, preferably between 1 and 8 bara.
  • the temperature profile in the third section c of the heat exchanger E 1 can be controlled thereby.
  • the condensation pressure of the feed fraction is established in the section between the control valves V 2 and V 3 , and, by means of the control valve V 4 , the boiling pressure of the nitrogen in the separator D 1 and the third section c of the heat exchanger E 1 is controlled. Owing to the above-described subdivision of the heat-exchange process into a second and third section and with the phase separation in separator D 1 it can then be established exactly in what section of the heat exchanger E 1 a (partial) vaporization or superheating of the nitrogen is taking place.
  • nitrogen boiling pressure (pN 2 ) and the crude gas condensation pressure (pRG) are selected according to the inequality pRG (bara) ⁇ 0.3 pN 2 (bara) ⁇ 1, a thermal overload of the heat exchanger E 1 due to impermissibly high temperature differences can be safely avoided.
  • the associated boiling temperature is ⁇ 179° C.—it is possible to prevent reliably a temperature below the freezing temperature of methane occurring in the heat exchanger E 1 . Operating problems and possible damage due to solids formation are thereby excluded.
  • the superheated nitrogen taken off from the heat exchanger E 1 via line 10 can, alternatively to a removal via line 11 , be at least partially reliquefied.
  • the nitrogen is fed via the line sections 12 and 13 to a compression—shown in the figure by a two-stage compressor unit C 1 /C 2 , wherein a heat exchanger, E 3 or E 4 respectively, is connected downstream of each compressor unit—and then is fed via line 14 to a heat exchanger E 2 .
  • the nitrogen is reliquefied and then fed to separator D 1 via line 15 .
  • Pressure regulation of the compressor C 2 is performed by the control valve V 5 .
  • a substream of the compressed nitrogen stream is removed via line 16 , preferably expanded in a multistage manner—shown by the gas expanders X 1 and X 2 —and then conducted via line 17 through the heat exchanger E 2 in countercurrent flow to the nitrogen stream that is to be liquefied.
  • the shafts of the compressors C 1 and C 2 are preferably coupled to the shafts of the gas expanders X 2 and X 1 .
  • the liquefaction process can proceed by means of “imported” nitrogen—in this case, the superheated nitrogen is taken off from the heat exchanger E 1 via the line sections 10 and 11 —by means of reliquefied nitrogen, or by any desired combination of both modes of operation.
US13/226,633 2010-09-09 2011-09-07 Natural gas liquefaction Abandoned US20120060553A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102010044869A DE102010044869A1 (de) 2010-09-09 2010-09-09 Erdgasverflüssigung
DE102010044869.9 2010-09-09

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US20120060553A1 true US20120060553A1 (en) 2012-03-15

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US (1) US20120060553A1 (de)
CN (1) CN102410702B (de)
AR (1) AR082919A1 (de)
AU (1) AU2011221424B2 (de)
BR (1) BRPI1104609A2 (de)
CH (1) CH703773B1 (de)
DE (1) DE102010044869A1 (de)
NO (1) NO20111212A1 (de)

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20140157824A1 (en) * 2012-12-06 2014-06-12 L'air Liquide Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude Method for improved thermal performing refrigeration cycle
FR3021091A1 (fr) * 2014-05-14 2015-11-20 Ereie Energy Res Innovation Engineering Procede et dispositif de liquefaction du methane
EP2899116A3 (de) * 2014-01-22 2015-11-25 Meyer Werft GmbH & Co. KG Verfahren und Tankvorrichtung zur Rückverflüssigung und Kühlung von Flüssigerdgas in Tanksystemen
US20180038643A1 (en) * 2016-08-05 2018-02-08 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for the integration of liquefied natural gas and syngas production
WO2018157019A1 (en) * 2017-02-24 2018-08-30 Praxair Technology, Inc. Liquid natural gas liquefier utilizing mechanical and liquid nitrogen refrigeration
WO2019101502A1 (en) * 2017-11-21 2019-05-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Bog recondenser and lng supply system provided with same
WO2019101652A1 (en) * 2017-11-21 2019-05-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Bog recondenser and lng storage system provided with same
US10634425B2 (en) * 2016-08-05 2020-04-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Integration of industrial gas site with liquid hydrogen production
US11083994B2 (en) 2019-09-20 2021-08-10 Exxonmobil Upstream Research Company Removal of acid gases from a gas stream, with O2 enrichment for acid gas capture and sequestration
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US11465093B2 (en) 2019-08-19 2022-10-11 Exxonmobil Upstream Research Company Compliant composite heat exchangers
US11703277B2 (en) * 2020-02-06 2023-07-18 Cosmodyne, LLC Systems and methods for natural gas cooling
US11808411B2 (en) 2019-09-24 2023-11-07 ExxonMobil Technology and Engineering Company Cargo stripping features for dual-purpose cryogenic tanks on ships or floating storage units for LNG and liquid nitrogen
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WO2019101652A1 (en) * 2017-11-21 2019-05-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Bog recondenser and lng storage system provided with same
WO2019101502A1 (en) * 2017-11-21 2019-05-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Bog recondenser and lng supply system provided with same
TWI721276B (zh) * 2017-11-21 2021-03-11 法商液態空氣喬治斯克勞帝方法研究開發股份有限公司 蒸發氣體再冷凝裝置及具備其的液化天然氣儲藏系統
US11465093B2 (en) 2019-08-19 2022-10-11 Exxonmobil Upstream Research Company Compliant composite heat exchangers
US11927391B2 (en) 2019-08-29 2024-03-12 ExxonMobil Technology and Engineering Company Liquefaction of production gas
US11083994B2 (en) 2019-09-20 2021-08-10 Exxonmobil Upstream Research Company Removal of acid gases from a gas stream, with O2 enrichment for acid gas capture and sequestration
US11808411B2 (en) 2019-09-24 2023-11-07 ExxonMobil Technology and Engineering Company Cargo stripping features for dual-purpose cryogenic tanks on ships or floating storage units for LNG and liquid nitrogen
US11703277B2 (en) * 2020-02-06 2023-07-18 Cosmodyne, LLC Systems and methods for natural gas cooling
RU2775341C1 (ru) * 2022-02-16 2022-06-29 Публичное акционерное общество криогенного машиностроения (ПАО "Криогенмаш") Способ сжижения природного газа (варианты)

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AR082919A1 (es) 2013-01-16
AU2011221424B2 (en) 2016-03-31
CH703773B1 (de) 2015-02-27
AU2011221424A1 (en) 2012-03-29
CN102410702B (zh) 2016-01-20
CN102410702A (zh) 2012-04-11
BRPI1104609A2 (pt) 2013-04-24

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