EP1929227B1 - Erdgasverflüssigungsprozess für flüssigerdgas - Google Patents

Erdgasverflüssigungsprozess für flüssigerdgas Download PDF

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Publication number
EP1929227B1
EP1929227B1 EP06760347.2A EP06760347A EP1929227B1 EP 1929227 B1 EP1929227 B1 EP 1929227B1 EP 06760347 A EP06760347 A EP 06760347A EP 1929227 B1 EP1929227 B1 EP 1929227B1
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EP
European Patent Office
Prior art keywords
gas stream
heat exchange
cooled
expanded
refrigerant
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EP06760347.2A
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English (en)
French (fr)
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EP1929227A1 (de
EP1929227A4 (de
Inventor
Moses Minta
Kevin N. Stanley
John B. Stone
Ronald R. Bowen
Linda J. Cote
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ExxonMobil Upstream Research Co
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ExxonMobil Upstream Research Co
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Publication of EP1929227A4 publication Critical patent/EP1929227A4/de
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of 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
    • F25J1/0002—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
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    • 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
    • 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
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    • 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
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    • 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
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    • 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
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    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
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    • F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts of nitrogen
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    • F25J1/0215—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
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    • 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
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    • F25J1/0219—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
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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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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

Definitions

  • Embodiments of the invention relate to a process for liquefaction of natural gas and other methane-rich gas streams, and more particularly to a process for producing liquefied natural gas (LNG).
  • LNG liquefied natural gas
  • LNG liquefied natural gas
  • the refrigerants used may be a mixture of components such as methane, ethane, propane, butane, and nitrogen in multi-component refrigeration cycles.
  • the refrigerants may also be pure substances such as propane, ethylene, or nitrogen in "cascade cycles.” Substantial volumes of these refrigerants with close control of composition are required. Further, such refrigerants may have to be imported and stored imposing logistics requirements.
  • some of the components of the refrigerant may be prepared, typically by a distillation process integrated with the liquefaction process.
  • the use of gas expanders to provide the feed gas cooling thereby eliminating or reducing the logistical problems of refrigerant handling has been of interest to process engineers.
  • the expander system operates on the principle that the feed gas can be allowed to expand through an expansion turbine, thereby performing work and reducing the temperature of the gas.
  • the low temperature gas is then heat exchanged with the feed gas to provide the refrigeration needed.
  • Supplemental refrigeration is typically needed to fully liquefy the feed gas and this may be provided by a refrigerant system.
  • the power obtained from the expansion is usually used to supply part of the main compression power used in the refrigeration cycle.
  • the typical expander cycle for making LNG operates at the feed gas pressure, typically under about 6,895 kPa (1,000 psia).
  • U.S. Patent No. 6,378,330 B1 is directed to liquefying a pressurized gas stream rich in methane, the process including withdrawing and entropically expanding a first fraction of the pressurized feed stream, preferably above 11.000 kPa, to a lower pressure and cooling a second fraction of the pressurized feed stream by indirect heat exchange with the expanded first fraction followed by expanding the second fraction to a lower pressure.
  • 2003/0177785 A1 is directed to cooling and expanding a gas stream to liquefy the gas stream and subsequently withdrawing the liquefied gas stream as a pressurized product with a portion recycled through the heat exchanger to provide cooling which helps keep the cooling and compression of the gas stream in the supercritical region of the phase diagram.
  • FR 2 714 722 is directed to liquefying a natural gas whereby during expansion of the gas stream the gas changes from a dense phase to a liquid phase without undergoing a phase transition.
  • Embodiments of the present invention provide a process for liquefying natural gas and other methane-rich gas streams to produce liquefied natural gas (LNG) and/or other liquefied methane-rich gases.
  • natural gas as used in this specification, including the appended claims, means a gaseous feed stock suitable for manufacturing LNG.
  • the natural gas could comprise gas obtained from a crude oil well (associated gas) or from a gas well (non-associated gas).
  • the composition of natural gas can vary significantly.
  • natural gas is a methane-rich gas containing methane (C 1 ) as a major component.
  • a process for liquefying a gas stream rich in methane comprising providing a gas stream rich in methane at a pressure less than 1,000 psia (6895 kPa); providing a refrigerant at a pressure of less than 1,000 psia (6895 kPa); compressing said refrigerant to a pressure greater than or equal to 1500 psia (10342 kPa) to provide a compressed refrigerant; cooling said compressed refrigerant by indirect heat exchange with a cooling fluid; expanding said compressed refrigerant to further cool said compressed refrigerant, thereby producing an expanded, cooled refrigerant; passing said expanded, cooled refrigerant to a heat exchange area; and passing said gas stream through said heat exchange area to cool at least part of said gas stream by indirect heat exchange with said expanded, cooled refrigerant, thereby forming a cooled gas stream.
  • the providing the refrigerant at a pressure of less than 1,000 psia (6895 kPa) comprises withdrawing a portion of the gas at a pressure of less than 1,000 psia (6895 kPa) for use as the refrigerant.
  • the portion of the gas stream to be used as the refrigerant is withdrawn from the gas stream before the gas stream is passed to the heat exchange area.
  • the process according to the present invention further comprises providing at least a portion of the refrigeration duty for the heat exchange area using a closed loop charged with flash vapor produced in the process for liquefying the gas stream rich in methane. Additional embodiments according to the present invention will be apparent to those skilled in the art.
  • Embodiments of the present invention provide a process for natural gas liquefaction using primarily gas expanders and eliminating the need for external refrigerants. That is the feed gas itself (e.g., natural gas) is used as the refrigerant in all refrigeration cycles. Such refrigeration cycles do not require supplemental cooling using external refrigerants (i.e., refrigerants other than the feed gas itself or gas that is produced at or near the LNG process plant) as typical proposed gas expander cycles do, yet such refrigeration cycles have a higher efficiency.
  • cooling water or air are the only external sources of cooling fluids and are used for compressor inter-stage or after cooling.
  • FIG. 1 illustrates one embodiment of the present invention in which an expander loop 5 (i.e., an expander cycle) and a sub-cooling loop 6 are used.
  • expander loop 5 and sub-cooling loop 6 are shown with double-width lines in FIG. 1 .
  • the terms "loop” and "cycle” are used interchangeably.
  • feed gas stream 10 enters the liquefaction process at a pressure less than 1000 psia, or less than 900 psia (6205 kPa), or less than 800 psia (5516 kPa), or less than 700 psia (4826 kPa), or less than 600 psia (4137 kPa).
  • the pressure of feed gas stream 10 will be about 800 psia (5516 kPa).
  • Feed gas stream 10 generally comprises natural gas that has been treated to remove contaminants using processes and equipment that are well known in the art. Before it is passed to a heat exchanger, a portion of feed gas stream 10 is withdrawn to form side stream 11, thus providing, as will be apparent from the following discussion, a refrigerant at a pressure corresponding to the pressure of feed gas stream 10, namely any of the above pressures, including a pressure of less than 1000 psia (6895 kPa). Thus, in the embodiment shown in FIG. 1 , a portion of the feed gas stream is used as the refrigerant for expander loop 5. Although the embodiment shown in FIG.
  • the present method is any of the other embodiments herein described, wherein the portion of the feed gas stream to be used as the refrigerant is withdrawn from the heat exchange area, expanded, and passed back to the heat exchange area to provide at least part of the refrigeration duty for the heat exchange area.
  • Side stream 11 is passed to compression unit 20 where it is compressed to a pressure greater than or equal to 1500 psia (10342 kPa), thus providing compressed refrigerant stream 12.
  • side stream 11 is compressed to a pressure greater than or equal to 1600 psia (11032 kPa), or greater than or equal to 1700 psia (11721 kPa), or greater than or equal to 1800 psia (12411 kPa), or greater than or equal to 1900 psia (13100 kPa), or greater than or equal to 2000 psia (13790 kPa), or greater than or equal to 2500 psia (17237 kPa), or greater than or equal to 3000 psia (20684 kPa), thus providing compressed refrigerant stream 12.
  • compression unit means any one type or combination of similar or different types of compression equipment, and may include auxiliary equipment, known in the art for compressing a substance or mixture of substances.
  • a “compression unit” may utilize one or more compression stages.
  • Illustrative compressors may include, but are not limited to, positive displacement types, such as reciprocating and rotary compressors for example, and dynamic types, such as centrifugal and axial flow compressors, for example.
  • compressed refrigerant stream 12 is passed to cooler 30 where it is cooled by indirect heat exchange with a suitable cooling fluid to provide a compressed, cooled refrigerant.
  • cooler 30 is of the type that provides water or air as the cooling fluid, although any type of cooler can be used.
  • the temperature of compressed refrigerant stream 12 as it emerges from cooler 30 depends on the ambient conditions and the cooling medium used and is typically from about 35 °F (1.7 °C) to about 105 °F (40.5 °C).
  • Cooled compressed refrigerant stream 12 is then passed to expander 40 where it is expanded and consequently cooled to form expanded refrigerant stream 13.
  • expander 40 is a work-expansion device, such as gas expander producing work that may be extracted and used for compression.
  • Expanded refrigerant stream 13 is passed to heat exchange area 50 to provide at least part of the refrigeration duty for heat exchange area 50.
  • heat exchange area means any one type or combination of similar or different types of equipment known in the art for facilitating heat transfer.
  • a "heat exchange area” may be contained within a single piece of equipment, or it may comprise areas contained in a plurality of equipment pieces. Conversely, multiple heat exchange areas may be contained in a single piece of equipment.
  • feed gas stream 10 is sub-cooled by sub-cooling loop 6 (described below) to produce sub-cooled stream 10a.
  • Sub-cooled stream 10a is then expanded to a lower pressure in expander 70, thereby partially liquefying sub-cooled stream 10a to form a liquid fraction and a remaining vapor fraction.
  • Expander 70 may be any pressure reducing device, including, but not limited to a valve, control valve, Joule Thompson valve, Venturi device, liquid expander, hydraulic turbine, and the like.
  • Partially liquefied sub-cooled stream 10a is passed to surge tank 80 where the liquefied fraction 15 is withdrawn from the process as LNG having a temperature corresponding to the bubble point pressure.
  • flash vapor stream 16 is used as fuel to power the compressor units and/or as a refrigerant in sub-cooling loop 6 as described below. Prior to being used as fuel, all or a portion of flash vapor stream 16 may optionally be passed from surge tank 80 to heat exchange areas 50 and 55 to supplement the cooling provided in such heat exchange areas.
  • a portion of flash vapor 16 is withdrawn through line 17 to fill sub-cooling loop 6.
  • a portion of the feed gas from feed gas stream 10 is withdrawn (in the form of flash gas from flash gas stream 16 ) for use as the refrigerant in sub-cooling loop 6.
  • make-up gas i.e., additional flash vapor from line 17
  • expanded stream 18 is discharged from expander 41 and drawn through heat exchange areas 55 and 50.
  • Expanded flash vapor stream 18 (the sub-cooling refrigerant stream) is then returned to compression unit 90 where it is re-compressed to a higher pressure and warmed.
  • the re-compressed sub-cooling refrigerant stream is cooled in cooler 31, which can be of the same type as cooler 30, although any type of cooler may be used.
  • the re-compressed sub-cooling refrigerant stream is passed to heat exchange area 50 where it is further cooled by indirect heat exchange with expanded refrigerant stream 13, sub-cooling refrigerant stream 18, and, optionally, flash vapor stream 16.
  • the present method is any of the other embodiments disclosed herein further comprising providing cooling using a closed loop (e.g., sub-cooling loop 6 ) charged with flash vapor resulting from the LNG production (e.g., flash vapor 16 ).
  • feed gas stream 10 passes from one heat exchange area to another, the temperature of feed gas stream 10 will be reduced until ultimately a sub-cooled stream is produced.
  • mass flow rate of feed gas stream 10 will be reduced.
  • Other modifications, such as compression, may also be made to feed gas stream 10. While each such modification to feed gas stream 10 could be considered to produce a new and different stream, for clarity and ease of illustration, the feed gas stream will be referred to as feed gas stream 10 unless otherwise indicated, with the understanding that passage through heat exchange areas, the taking of side streams, and other modifications will produce temperature, pressure, and/or flow rate changes to feed gas stream 10.
  • FIG. 2 illustrates an unclaimed embodiment of the present invention that is similar to the embodiment shown in FIG. 1 , except that expander loop 5 has been replaced with expander loop 7.
  • Expander loop 7 is shown with double-width lines in FIG. 2 for clarity. Expander loop 7 utilizes substantially the same equipment as expander loop 5 (for example, compressor 20, cooler 30, and expander 40, all of which have been described above).
  • the gaseous refrigerant in expander loop 7 however, is de-coupled from the feed gas and may therefore have a different composition than the feed gas. That is, expander loop 7 is essentially a closed loop and is not connected to feed gas stream 10.
  • the refrigerant for expander loop 7 is therefore not necessarily the feed gas, although it may be.
  • Expander loop 7 may be charged with any suitable refrigerant gas that is produced at or near the LNG process plant in which expander loop 7 is utilized.
  • the refrigerant gas used to charge expander loop 7 could be a feed gas, such as natural gas, that has only been partially treated to remove contaminants.
  • expander loop 7 is a high pressure gas loop.
  • Stream 12a exits compression unit 20 at a pressure greater than or equal to about 1500 psia (10342 kPa), or greater than or equal to about 1600 psia (11032 kPa), or greater than or equal to about 1700 psia (11721 kPa), or greater than or equal to about 1800 psia (12411 kPa), or greater than or equal to about 1900 psia (13100 kPa), or greater than or equal to about 2000 psia (13790 kPa), or greater than or equal to about 2500 psia (17237 kPa), or greater than or equal to about 3000 psia (20684 kPa).
  • the temperature of compressed refrigerant stream 12a as it emerges from cooler 30 depends on the ambient conditions and the cooling medium used and is typically about from about 35 °F (1.7 °C) to about 105 °F (40.5 °C). Cooled compressed refrigerant stream 12a is then passed to expander 40 where it is expanded and further cooled to form expanded refrigerant stream 13a. Expanded refrigerant stream 13a is passed to heat exchange area 50 to provide at least part of the refrigeration duty for heat exchange area 50, where feed gas stream 10 is at least partially cooled by indirect heat exchange with expanded refrigerant stream 13a. Upon exiting heat exchange area 50, expanded refrigerant stream 13a is returned to compression unit 20 for re-compression.
  • expander loops 5 and 7 may be used interchangeably. For example, in an embodiment utilizing expander loop 5, expander loop 7 may be substituted for expander loop 5.
  • FIG. 3 shows another embodiment for producing LNG in accordance with the process of the invention.
  • the process illustrated in FIG. 3 utilizes a plurality of work expansion cycles to provide supplemental cooling for the feed gas and other streams.
  • the use of such work expansion cycles results in overall improved efficiency for the liquefaction process.
  • feed gas stream 10 again enters the liquefaction process at the pressures described above.
  • side stream 11 is fed to expander loop 5 in the manner previously described, but it will be apparent in an unclaimed aspect of the invention that closed expander loop 7 could be utilized in the place of expander loop 5, in which case side stream 11 would not be necessary.
  • Expander loop 5 operates in the same manner as described above for the embodiment shown in FIG. 1 , except that expanded refrigerant stream 13 is passed through heat exchange area 56, described in detail below, to provide at least a part of the refrigeration duty for heat exchange area 56.
  • feed gas stream 10 is passed to heat exchange area 56 where it is cooled, at least in part, by indirect heat exchange with expanded refrigerant stream 13 and other streams described below.
  • feed gas stream 10 is passed through heat exchange areas 57 and 58 where it is further cooled by indirect heat exchange with additional streams described below.
  • first and second work expansion cycles are utilized for improved efficiency as follows: before feed gas stream 10 enters heat exchange area 57, side stream 11b is taken from feed gas stream 10. After feed gas stream 10 exits heat exchange area 57, but before it enters heat exchange area 58, side stream 11c is taken from feed gas stream 10.
  • side streams 11b and 11c are taken from feed gas stream 10 at different stages of feed gas stream cooling. That is, each side stream is withdrawn from the feed gas stream at a different point on the cooling curve of the feed gas such that each successively withdrawn side stream has a lower initial temperature than the previously withdrawn side stream.
  • expanded streams 13b and 13c are passed to compression units 61 and 62, respectively, where they are re-compressed and combined to form stream 14a.
  • Stream 14a is cooled by cooler 32 prior to being re-combined with feed gas stream 10.
  • Cooler 32 can be the same type of cooler or cooler types as coolers 30 and 31.
  • Expanders 42 and 43 are work expansion devices of the type well know to those of skill in the art. Illustrative, non-limiting examples of suitable work expansion devices include liquid expanders and hydraulic turbines.
  • the feed gas stream is further cooled using a plurality of work expansion devices. It will be apparent to those of ordinary skill in the art that additional work expansion cycles can be added to the embodiment illustrated in FIG.
  • each of the work expansion devices expands a portion of the feed gas stream and thereby cools such portion, wherein each of the portions of the feed gas stream expanded in the work expansion devices is withdrawn from the feed gas stream at a different stage of feed gas stream cooling (i.e., at a different feed gas stream temperature).
  • the work expansion devices are utilized by withdrawing one or more side streams from the feed gas stream; passing said one or more side streams to one or more work expansion devices; expanding said one of more side streams to expand and cool said one or more side streams, thereby forming one or more expanded, cooled side streams; passing said one or more expanded, cooled side streams to at least one heat exchange area; passing said gas stream through said at least one heat exchange area; and at least partially cooling said gas stream by indirect heat exchange with said one or more expanded, cooled side streams.
  • feed gas stream 10 after being cooled in heat exchange areas 56, 57, and 58, is then passed to heat exchange area 59 where it is further cooled to produce sub-cooled stream 10a.
  • the principal function of heat exchange area 59 is to sub-cool feed gas stream 10.
  • Sub-cooled stream 10a is then expanded to a lower pressure in expander 85, thereby partially liquefying sub-cooled stream 10a to form a liquid fraction and a remaining vapor fraction.
  • Expander 85 may be any pressure reducing device, including, but not limited to a valve, control valve, Joule Thompson valve, Venturi device, liquid expander, hydraulic turbine, and the like.
  • Partially liquefied sub-cooled stream 10a is passed to surge tank 80 where the liquefied fraction 15 is withdrawn from the process as LNG having a temperature corresponding to the bubble point pressure.
  • the remaining vapor fraction (flash vapor) stream 16 is used as fuel to power the compressor units and/or as a refrigerant in sub-cooling loop 8 in a manner substantially the same as previously described for sub-cooling loop 6.
  • sub-cooling loop 8 is similar to sub-cooling loop 6, except that sub-cooling loop 8 supplies cooling to four heat exchange areas (heat exchange areas 56, 57, 58, and 59 ).
  • FIG. 4 illustrates yet another embodiment of the present invention.
  • the embodiment shown in FIG. 4 is substantially the same as the embodiment shown in FIG. 3 , except that compression unit 25 and expander 35 have been added.
  • Expander 35 may be any type of liquid expander or hydraulic turbine. Expander 35 is placed between heat exchange areas 58 and 59 such that feed gas stream 10 flows from heat exchange area 58 into expander 35 where it is expanded, and consequently cooled to produce expanded feed gas stream 10b. Stream 10b then is passed to heat exchange area 59 where it is sub-cooled to produce sub-cooled stream 10c.
  • the overall cooling load on sub-cooling loop 8 is advantageously reduced.
  • the present method is any of the other embodiments disclosed herein further comprising expanding at least a portion of the cooled feed gas stream to produce a cooled, expanded feed gas stream (e.g., stream 10b ); and further cooling the cooled, expanded feed gas stream by indirect heat exchange with a closed loop (e.g., sub-cooling loop 6 or 8 ) charged with flash vapor resulting from the LNG production (e.g., flash vapor 16 ).
  • a closed loop e.g., sub-cooling loop 6 or 8
  • compression unit 25 is utilized to increase the pressure of feed gas stream 10 prior to entry into the liquefaction process.
  • feed gas stream 10 is passed to compression unit 25 where it is compressed to a pressure above the feed gas supply pressure or, in one or more unclaimed embodiments, to a pressure greater than about 1200 psia (8274 kPa).
  • feed gas stream 10 is compressed to a pressure greater than or equal to about 1300 psia (8963 kPa), or greater than or equal to about 1400 psia (9653 kPa), or greater than or equal to about 1500 psia (10342 kPa), or greater than or equal to about 1600 psia (11032 kPa), or greater than or equal to about 1700 psia (11721 kPa), or greater than or equal to about 1800 psia (12411 kPa), or greater than or equal to about 1900 psia (13100 kPa), or greater than or equal to about 2000 psia (13790 kPa), or greater than or equal to about 2500 psia (17237 kPa), or greater than or equal to about 3000 psia (20684 kPa).
  • feed gas stream 10 is passed to cooler 33 where it is cooled prior to being passed to heat exchange area 56. It will be appreciated that to the extent compression unit 25 is used to compress feed gas stream 10 (and, hence, side stream 11 ) to a lower pressure than that desired for compressed refrigerant stream 12, compression unit 20 may be used to boost the pressure.
  • feed gas stream 10 as described above provides three benefits. First, by increasing the pressure of the feed gas stream, the pressures of side streams 11b and 11c are also increased, with the result that the cooling performance of work expansion devices 42 and 43 is enhanced. Second, the heat transfer coefficient in the heat exchange areas is improved. Thus, in one or more embodiments, the process for producing LNG described herein is carried out according to any of the other embodiments described herein wherein the feed gas is compressed to the pressures described above prior to entry into a heat exchange area.
  • the present method comprises providing supplemental cooling for the feed gas stream from a plurality of work expansion devices, each of the work expansion devices expanding a portion of the feed gas stream and thereby cooling the portion to form one or more expanded, cooled side streams, wherein each of the portions of the feed gas stream expanded in the work expansion devices is withdrawn from the feed gas stream at a different stage of feed gas stream cooling (i.e., at a different feed gas stream temperature); and cooling said feed gas stream by indirect heat exchange with said one or more expanded, cooled side streams.
  • each of the above-described portions of feed gas has a pressure, prior to expansion, greater than about 1200 psia (8274 kPa), or greater than or equal to about 1300 psia (8963 kPa), or greater than or equal to about 1400 psia (9653 kPa), or greater than or equal to about 1500 psia (10342 kPa), or greater than or equal to about 1600 psia (11032 kPa), or greater than or equal to about 1700 psia (11721 kPa), or greater than or equal to about 1800 psia (12411 kPa), or greater than or equal to about 1900 psia (13100 kPa), or greater than or equal to about 2000 psia (13790 kPa), or greater than or equal to about 2500 psia (17237 kPa), or greater than or equal to about 3000 psia (206
  • the present method is any of the other embodiments described herein further comprising compressing the feed gas stream to any of the pressures described above to produce a pressurized feed gas stream; feeding the pressurized feed gas stream to a work expansion device, or to a plurality of work expansion devices; expanding the compressed feed gas stream through the work expansion device, or through a plurality of work expansion devices, to provide supplemental cooling for the feed gas stream.
  • a third benefit obtained by compression the feed gas stream as described above is that the cooling capacity of expander 35 is improved, with the result that expander 35 is able to even further reduce the cooling load on sub-cooling loop 8.
  • compression unit 25 and/or expander 35 could also be advantageously added to other embodiments described herein to provide similar reductions in the cooling load on the sub-cooling loops utilized in those embodiments or other improvements in cooling, and that compression unit 25 and expander 35 may be used independently of each other in any embodiment herein.
  • the cooling capacity of expander 35 (or the work expansion devices 42 and 43 ) will be improved, even without compression of the feed stream, to the extent the feed stream is supplied at a pressure above the bubble point pressure of the LNG.
  • FIG. 5 is a schematic flow diagram of a fifth embodiment for producing LNG in accordance with the process of this invention that is similar to the embodiment shown in FIG. 4 , but utilizes yet another expansion step to provide sub-cooling.
  • sub-cooling loop 8 is not present in the embodiment shown in FIG. 5 .
  • side stream 11d is taken from stream 10b and passed to expansion device 105 where it is expanded and consequently cooled to form expanded stream 13d.
  • Expansion device 105 is a work-producing expander, many types of which are readily available. Illustrative, non-limiting examples of such devices include liquid expanders and hydraulic turbines.
  • Expanded stream 13d is passed through heat exchange areas 59, 58, 57, and 56 to provide at least part of the refrigeration duty for those heat exchange areas.
  • stream 10b is also cooled by indirect heat exchange with expanded stream 13d, as well as by the flash vapor stream 16.
  • the inventive process further comprises expanding at least a portion of the cooled gas stream (feed gas stream 10 ) in expander 35 before the final heat exchange step (for example, prior to heat exchange area 59 ) to produce an expanded, cooled gas stream (for example, stream 10b ); passing a portion of said expanded, cooled gas stream to a work-producing expander; further expanding said expanded, cooled gas stream in said work-producing expander; and passing the stream emerging from said work-producing expander (for example, stream 13d ) to a heat exchange area to further cool said expanded, cooled gas stream by indirect heat exchange in said heat exchange area.
  • expanded stream 13d is passed to compression unit 95 where it is re-compressed and combined with the streams emerging from compression units 61 and 62 to form part of stream 14a, which is cooled and then re-cycled to feed stream 10 as before.
  • FIG. 6 A further embodiment shown in FIG. 6 is similar to the embodiment shown in FIG.1 and described above, except that sub-cooling loop 6 has been modified such that after exiting heat exchange area 50, the re-compressed and cooled sub-cooling refrigerant stream is further cooled in heat exchange area 55 prior to being expanded through expander 41.
  • This embodiment is favorable where a cooling fluid is used that does not present much condensation after expander 41.
  • FIG. 7 depicts another embodiment in which sub-cooling loop 6a uses a portion of feed gas 10.
  • the portion of feed gas 10 is re-pressurized in compressor 25 and cooled in cooler 33 from 201, in the same fashion as in FIG. 4 .
  • FIG. 8 is another embodiment similar to FIG. 7 showing an alternative arrangement for the sub-cooling loop 6.
  • an additional compressor (not shown) may be used to prevent condensation in the sub-cooling loop or to ensure adequate line pressures.
  • FIG. 9 depicts an embodiment for use with certain feed gas 10 compositions and/or pressures.
  • an expansion valve 82 or other expander e.g., a Joules-Thompson valve
  • FIG. 10 represents another embodiment showing the integration of a nitrogen rejection stage using distillation column 81 or equivalent device, for the case where nitrogen rejection is needed, based on feed gas 10 composition. This may be needed to meet the nitrogen specification of product LNG for transmission and end use.
  • FIG. 11 represents another embodiment showing the integration of a nitrogen rejection unit, where the flash vapor from the nitrogen rejection unit is used as refrigerant for the sub-cooling loop.
  • the resulting refrigerant is therefore rich in nitrogen.
  • the volume of flash vapor stream 16 is controlled to match the fuel requirements of the compression units and other equipment.
  • the temperature at state point 207 can be controlled to produce more or less flash vapor (stream 16 ) depending on the fuel requirements. Higher temperatures at state point 207 will result in the production of more flash vapor (and hence more available fuel), and vice-versa.
  • the temperature may be adjusted such that the flash vapor flow rate is higher than the fuel requirement, in which case the excess flow above the fuel flow requirement may be recycled after compression and cooling.

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Claims (20)

  1. Verfahren zum Verflüssigen eines Gasstroms (10), der reich an Methan ist, bei dem
    der Gasstrom mit einem Druck von weniger als 1000 psia (6895 kPa) bereitgestellt wird,
    ein Kühlmittel mit einem Druck von weniger als 1000 psia (6895 kPa) bereitgestellt wird, indem ein Anteil (11) des Gasstroms mit einem Druck von weniger als 1000 psia (6895 kPa) zur Verwendung als das Kühlmittel abgezogen wird,
    das Kühlmittel auf einen Druck von mehr als oder gleich 1500 psia (10342 kPa) komprimiert wird, um ein komprimiertes Kühlmittel (12) bereitzustellen,
    das komprimierte Kühlmittel durch indirekten Wärmetausch mit einem Kühlfluid gekühlt wird,
    das komprimierte Kühlmittel expandiert wird, um das komprimierte Kühlmittel weiter zu kühlen, wodurch ein expandiertes gekühltes Kühlmittel (13) produziert wird,
    das expandierte gekühlte Kühlmittel in einen Wärmetauschbereich (50, 56) geleitet wird, und
    der Gasstrom durch den Wärmetauschbereich geleitet wird, um mindestens einen Anteil des Gasstroms durch indirekten Wärmetausch mit dem expandierten gekühlten Kühlmittel zu kühlen, wodurch ein gekühlter Gasstrom (10a) gebildet wird.
  2. Verfahren nach Anspruch 1, bei dem der Anteil des Gasstroms abgezogen wird, bevor der Gasstrom in den Wärmetauschbereich geleitet wird.
  3. Verfahren nach Anspruch 1, bei dem der Anteil des Gasstroms aus dem Wärmetauschbereich abgezogen wird.
  4. Verfahren nach Anspruch 1, das ferner Bereitstellen mindestens eines Anteils der Kühllast für den Wärmetauschbereich unter Verwendung einer geschlossenen Schleife (6, 8) umfasst, die mit einem Flash-Dampf (16) beschickt worden ist, der in dem Verfahren zum Verflüssigen eines Gasstroms, der reich an Methan ist, produziert worden ist.
  5. Verfahren nach Anspruch 4, bei dem ferner
    mindestens ein Anteil des gekühlten Gasstroms expandiert wird, um einen expandierten gekühlten Gasstrom zu produzieren, und der expandierte, gekühlte Gasstrom durch indirekten Wärmetausch mit der geschlossenen Schleife, die mit dem Flash-Dampf beschickt worden ist, weiter gekühlt wird.
  6. Verfahren nach Anspruch 1, bei dem ferner
    mindestens ein Anteil des gekühlten Gasstroms expandiert wird, um einen expandierten gekühlten Gasstrom zu produzieren, und der expandierte gekühlte Gasstrom durch indirekten Wärmetausch in einem oder mehreren zusätzlichen Wärmetauschbereichen weiter gekühlt wird.
  7. Verfahren nach Anspruch 1, bei dem ferner
    der Gasstrom unter Verwendung einer Vielzahl von Arbeitsexpansionsvorrichtungen (42, 43) gekühlt wird, wobei jede der Arbeitsexpansionsvorrichtungen einen Anteil des Einsatzmaterialgasstroms expandiert und dadurch den Anteil kühlt, um einen oder mehrere expandierte gekühlte Nebenströme (13b, 13c) zu bilden, wobei jeder der Anteile des Einsatzmaterialgasstroms, der in den Arbeitsexpansionsvorrichtungen expandiert worden ist, aus dem Einsatzmaterialgasstrom in einer anderen Stufe des Kühlens des Einsatzmaterialgasstroms abgezogen wird, und
    der Einsatzmaterialgasstrom durch indirekten Wärmetausch mit dem einen oder den mehreren expandierten, gekühlten Nebenströmen gekühlt wird.
  8. Verfahren nach Anspruch 1, bei dem ferner
    ein oder mehrere Anteile des Gasstroms (11b, 11c) abgezogen werden,
    jeder von dem einen oder den mehreren Anteilen des Gasstroms zu einer oder mehreren Arbeitsexpansionsvorrichtungen (42, 43) geleitet wird und jeder von dem einen oder den mehreren Anteilen des Gasstroms expandiert wird, um den einen oder die mehreren Anteile zu expandieren und zu kühlen, wodurch ein oder mehrere expandierte gekühlte Nebenströme (13b, 13c) gebildet werden,
    der eine oder die mehreren expandierten gekühlten Nebenströme zu mindestens einem Wärmetauschbereich (57, 58) geleitet wird bzw. werden,
    der Gasstrom durch den mindestens einen Wärmetauschbereich geleitet wird, und
    der Gasstrom durch indirekten Wärmetausch mit dem einen oder den mehreren expandierten, gekühlten Nebenströmen mindestens teilweise gekühlt wird.
  9. Verfahren nach Anspruch 1, das ferner eine Expansionsstufe des gekühlten Gasstroms vor einem letzten Wärmetauschschritt und vor der Expansion umfasst, um LNG zu produzieren.
  10. Verfahren nach Anspruch 1, bei dem ferner
    mindestens ein Anteil des gekühlten Gasstroms vor einem letzten Wärmetauschschritt expandiert wird, um einen expandierten gekühlten Gasstrom zu produzieren,
    ein Anteil des expandierten gekühlten Gasstroms zu einem Arbeit produzierenden Expander geleitet wird und der Anteil des expandierten gekühlten Gasstroms in dem Arbeit produzierenden Expander weiter expandiert wird, und
    der aus dem Arbeit produzierenden Expander kommende Strom zu einem Wärmetauschbereich geleitet wird, um den Rest des expandierten gekühlten Gasstroms durch indirekten Wärmetausch in dem Wärmetauschbereich weiter zu kühlen.
  11. Verfahren nach Anspruch 1, bei dem das Kühlmittel auf einen Druck von mehr als oder gleich 3000 psia (20684 kPa) komprimiert wird, um ein komprimiertes Kühlmittel bereitzustellen.
  12. Verfahren nach Anspruch 1, bei dem der Wärmetauschbereich mehrere Wärmetauschkammern umfasst.
  13. Verfahren nach Anspruch 1, das ferner
    einen Unterkühlungswärmetauschbereich (55, 59), der den Gasstrom empfängt und durch Expansion eines zweiten Kühlmittels gekühlt wird, um einen unterkühlten Gasstrom bereitzustellen,
    gefolgt von einer letzten Expansion des unterkühlten Gasstroms und Gewinnung von LNG umfasst.
  14. Verfahren nach Anspruch 13, bei dem das zweite Kühlmittel in dem Unterkühlungswärmetauschbereich vor der Expansion des zweiten Kühlmittels unterkühlt wird.
  15. Verfahren nach Anspruch 14, bei dem der Gasstrom, der reich an Methan ist, vor dem Leiten durch den Wärmetauschbereich erneut mit Druck beaufschlagt wird, der gekühlte Gasstrom expandiert wird, und ein Anteil des expandierten gekühlten Gasstroms weiter expandiert und als das zweite Kühlmittel in dem Unterkühlungswärmetauschbereich verwendet wird.
  16. Verfahren nach Anspruch 14, bei dem ein Anteil des unterkühlten Gasstroms expandiert wird und ein Anteil davon das zweite Kühlmittel ist.
  17. Verfahren nach Anspruch 16, bei dem der Anteil des unterkühlten Gasstroms in zwei Teilströme aufgeteilt wird, wobei einer der Teilströme weiter expandiert wird, und beide Teilströme das zweite Kühlmittel umfassen.
  18. Verfahren nach Anspruch 1, das ferner Aussondern von Stickstoff mit LNG-Gewinnung umfasst.
  19. Verfahren nach Anspruch 1, bei dem der Gasstrom mit einem Druck von weniger als 900 psia (6205 kPa) bereitgestellt wird.
  20. Verfahren nach Anspruch 1, bei dem das Kühlmittel auf einen Druck von mehr als oder gleich 2000 psia (13790 kPa) komprimiert wird.
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Families Citing this family (93)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2452908C2 (ru) * 2006-09-22 2012-06-10 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Способ и устройство для получения охлажденного потока углеводородов
WO2008136884A1 (en) * 2007-05-03 2008-11-13 Exxonmobil Upstream Research Company Natural gas liquefaction process
US9003828B2 (en) * 2007-07-09 2015-04-14 Lng Technology Pty Ltd Method and system for production of liquid natural gas
NZ582507A (en) * 2007-07-09 2012-08-31 Lng Technology Pty Ltd A method and system for production of liquid natural gas
WO2009007435A2 (en) 2007-07-12 2009-01-15 Shell Internationale Research Maatschappij B.V. Method and apparatus for cooling a hydrocarbon stream
EP2165139A2 (de) * 2007-07-12 2010-03-24 Shell Internationale Research Maatschappij B.V. Verfahren und vorrichtung zum verflüssigen eines gasförmigen kohlenwasserstoffstroms
CA2695348A1 (en) * 2007-08-24 2009-03-05 Exxonmobil Upstream Research Company Natural gas liquefaction process
US9217603B2 (en) 2007-09-13 2015-12-22 Battelle Energy Alliance, Llc Heat exchanger and related methods
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
US20090084132A1 (en) * 2007-09-28 2009-04-02 Ramona Manuela Dragomir Method for producing liquefied natural gas
US8020406B2 (en) 2007-11-05 2011-09-20 David Vandor Method and system for the small-scale production of liquified natural gas (LNG) from low-pressure gas
US9243842B2 (en) 2008-02-15 2016-01-26 Black & Veatch Corporation Combined synthesis gas separation and LNG production method and system
WO2009135069A1 (en) * 2008-04-30 2009-11-05 Altarock Energy, Inc. Method and cooling system for electric submersible pumps/motors for use in geothermal wells
AU2009249761B2 (en) 2008-05-20 2012-10-04 Shell Internationale Research Maatschappij B.V. Method of cooling and liquefying a hydrocarbon stream, an apparatus therefor, and a floating structure, caisson or off-shore platform comprising such an apparatus
NO331740B1 (no) * 2008-08-29 2012-03-12 Hamworthy Gas Systems As Fremgangsmate og system for optimalisert LNG produksjon
NO331154B1 (no) * 2008-11-04 2011-10-24 Hamworthy Gas Systems As System for kombinert syklusmekanisk drift i kryogene kondensasjonsprosesser.
FR2938903B1 (fr) * 2008-11-25 2013-02-08 Technip France Procede de production d'un courant de gaz naturel liquefie sous-refroidi a partir d'un courant de charge de gaz naturel et installation associee
WO2010090865A2 (en) * 2009-01-21 2010-08-12 Conocophillips Company Method for utilization of lean boil-off gas stream as a refrigerant source
GB2469077A (en) 2009-03-31 2010-10-06 Dps Bristol Process for the offshore liquefaction of a natural gas feed
US8397535B2 (en) * 2009-06-16 2013-03-19 Praxair Technology, Inc. Method and apparatus for pressurized product production
ES2355467B1 (es) * 2009-09-11 2012-02-03 Repsol Ypf, S.A. Proceso y sistema para obtener gas natural licuado.
US20130145794A1 (en) * 2010-03-05 2013-06-13 Chad C. Rasmussen "flexible liquefied natural gas plant"
US9441877B2 (en) 2010-03-17 2016-09-13 Chart Inc. Integrated pre-cooled mixed refrigerant system and method
US20120067079A1 (en) * 2010-03-25 2012-03-22 Sethna Rustam H Nitrogen rejection and liquifier system for liquified natural gas production
US10113127B2 (en) 2010-04-16 2018-10-30 Black & Veatch Holding Company Process for separating nitrogen from a natural gas stream with nitrogen stripping in the production of liquefied natural gas
AU2011283126C1 (en) * 2010-07-30 2017-09-14 Exxonmobil Upstream Research Company Systems and methods for using multiple cryogenic hydraulic turbines
US10030908B2 (en) * 2010-08-16 2018-07-24 Korea Gas Corporation Natural gas liquefaction process
KR101037226B1 (ko) * 2010-10-26 2011-05-25 한국가스공사연구개발원 천연가스 액화공정
WO2012075266A2 (en) * 2010-12-01 2012-06-07 Black & Veatch Corporation Ngl recovery from natural gas using a mixed refrigerant
GB2486036B (en) * 2011-06-15 2012-11-07 Anthony Dwight Maunder Process for liquefaction of natural gas
US20130111948A1 (en) * 2011-11-04 2013-05-09 Air Products And Chemicals, Inc. Purification of Carbon Dioxide
US10139157B2 (en) 2012-02-22 2018-11-27 Black & Veatch Holding Company NGL recovery from natural gas using a mixed refrigerant
US9863696B2 (en) * 2012-06-06 2018-01-09 Keppel Offshore & Marine Technology Centre Pte Ltd System and process for natural gas liquefaction
US10655911B2 (en) * 2012-06-20 2020-05-19 Battelle Energy Alliance, Llc Natural gas liquefaction employing independent refrigerant path
GB2503731A (en) * 2012-07-06 2014-01-08 Highview Entpr Ltd Cryogenic energy storage and liquefaction process
KR101386543B1 (ko) * 2012-10-24 2014-04-18 대우조선해양 주식회사 선박의 증발가스 처리 시스템
CA2894176C (en) * 2013-01-24 2017-06-06 Exxonmobil Upstream Research Company Liquefied natural gas production
US11408673B2 (en) 2013-03-15 2022-08-09 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
CA3140415A1 (en) 2013-03-15 2014-09-18 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
US11428463B2 (en) 2013-03-15 2022-08-30 Chart Energy & Chemicals, Inc. Mixed refrigerant system and method
KR101640768B1 (ko) 2013-06-26 2016-07-29 대우조선해양 주식회사 선박의 제조방법
WO2014210409A1 (en) 2013-06-28 2014-12-31 Exxonmobil Upstream Research Company Systems and methods of utilizing axial flow expanders
EP3014077B1 (de) 2013-06-28 2018-01-17 Mitsubishi Heavy Industries Compressor Corporation Axialströmungsexpander
US10563913B2 (en) 2013-11-15 2020-02-18 Black & Veatch Holding Company Systems and methods for hydrocarbon refrigeration with a mixed refrigerant cycle
US20150211788A1 (en) * 2014-01-28 2015-07-30 Starrotor Corporation Modified Claude Process for Producing Liquefied Gas
US9574822B2 (en) 2014-03-17 2017-02-21 Black & Veatch Corporation Liquefied natural gas facility employing an optimized mixed refrigerant system
US9945604B2 (en) 2014-04-24 2018-04-17 Air Products And Chemicals, Inc. Integrated nitrogen removal in the production of liquefied natural gas using refrigerated heat pump
DE102014005936A1 (de) * 2014-04-24 2015-10-29 Linde Aktiengesellschaft Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion
US20150308737A1 (en) * 2014-04-24 2015-10-29 Air Products And Chemicals, Inc. Integrated Nitrogen Removal in the Production of Liquefied Natural Gas Using Intermediate Feed Gas Separation
US9816754B2 (en) 2014-04-24 2017-11-14 Air Products And Chemicals, Inc. Integrated nitrogen removal in the production of liquefied natural gas using dedicated reinjection circuit
NO20141176A1 (no) * 2014-09-30 2016-03-31 Global Lng Services As Fremgangsmåte og anlegg for fremstilling av LNG
JP6415329B2 (ja) * 2015-01-09 2018-10-31 三菱重工エンジニアリング株式会社 ガス液化装置及びガス液化方法
AR105277A1 (es) 2015-07-08 2017-09-20 Chart Energy & Chemicals Inc Sistema y método de refrigeración mixta
TWI641789B (zh) 2015-07-10 2018-11-21 艾克頌美孚上游研究公司 使用液化天然氣製造液化氮氣之系統與方法
TWI606221B (zh) 2015-07-15 2017-11-21 艾克頌美孚上游研究公司 一倂移除溫室氣體之液化天然氣的生產系統和方法
TWI608206B (zh) * 2015-07-15 2017-12-11 艾克頌美孚上游研究公司 藉由預冷卻天然氣供給流以增加效率的液化天然氣（ｌｎｇ）生產系統
AU2016372709B2 (en) 2015-12-14 2019-09-12 Exxonmobil Upstream Research Company Method and system for separating nitrogen from liquefied natural gas using liquefied nitrogen
KR102116718B1 (ko) 2015-12-14 2020-06-01 엑손모빌 업스트림 리서치 캄파니 액체 질소를 저장하는 lng 운반선에서의 천연 가스 액화 방법
WO2017121751A1 (en) * 2016-01-12 2017-07-20 Global Lng Services As Method and plant for liquefaction of pre-processed natural gas
GB201601878D0 (en) 2016-02-02 2016-03-16 Highview Entpr Ltd Improvements in power recovery
FR3048074B1 (fr) * 2016-02-18 2019-06-07 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Methode pour eviter l'evaporation instantanee de gaz naturel liquefie en cours de transport.
FR3053771B1 (fr) * 2016-07-06 2019-07-19 Saipem S.P.A. Procede de liquefaction de gaz naturel et de recuperation d'eventuels liquides du gaz naturel comprenant deux cycles refrigerant semi-ouverts au gaz naturel et un cycle refrigerant ferme au gaz refrigerant
AU2018218196B2 (en) * 2017-02-13 2021-04-08 Exxonmobil Upstream Research Company Pre-cooling of natural gas by high pressure compression and expansion
SG11201906786YA (en) 2017-02-24 2019-09-27 Exxonmobil Upstream Res Co Method of purging a dual purpose lng/lin storage tank
CA3056865A1 (en) * 2017-03-31 2018-10-04 Exxonmobil Upstream Research Company Hydraulic turbine between middle and cold bundles of natural gas liquefaction heat exchanger
CA3076605C (en) 2017-09-29 2022-06-28 Exxonmobil Upstream Research Company Natural gas liquefaction by a high pressure expansion process
JP7003236B2 (ja) * 2017-09-29 2022-01-20 エクソンモービル アップストリーム リサーチ カンパニー 高圧膨張プロセスによる天然ガス液化
CA3079890C (en) 2017-10-25 2022-07-26 Exxonmobil Upstream Research Company Natural gas liquefaction by a high pressure expansion process using multiple turboexpander compressors
RU2684232C1 (ru) * 2018-02-12 2019-04-05 Акционерное общество "НИПИгазпереработка" (АО "НИПИГАЗ") Установка и способ сжижения природного газа
JP7150063B2 (ja) * 2018-06-07 2022-10-07 エクソンモービル アップストリーム リサーチ カンパニー 高圧圧縮および膨張による天然ガスの前処理および前冷却
AU2019322808B2 (en) 2018-08-14 2022-10-13 ExxonMobil Technology and Engineering Company Conserving mixed refrigerant in natural gas liquefaction facilities
AU2019326291B9 (en) 2018-08-22 2023-04-13 ExxonMobil Technology and Engineering Company Managing make-up gas composition variation for a high pressure expander process
US11635252B2 (en) * 2018-08-22 2023-04-25 ExxonMobil Technology and Engineering Company Primary loop start-up method for a high pressure expander process
WO2020040953A2 (en) 2018-08-22 2020-02-27 Exxonmobil Upstream Research Company Heat exchanger configuration for a high pressure expander process and a method of natural gas liquefaction using the same
WO2020106394A1 (en) 2018-11-20 2020-05-28 Exxonmobil Upstream Research Company Poly refrigerated integrated cycle operation using solid-tolerant heat exchangers
WO2020106397A1 (en) 2018-11-20 2020-05-28 Exxonmobil Upstream Research Company Methods and apparatus for improving multi-plate scraped heat exchangers
EP3918261A1 (de) 2019-01-30 2021-12-08 Exxonmobil Upstream Research Company (EMHC-N1-4A-607) Verfahren zur entfernung von feuchtigkeit aus lng-kältemittel
US11668524B2 (en) 2019-01-30 2023-06-06 Exxonmobil Upstream Research Company Methods for removal of moisture from LNG refrigerant
US11465093B2 (en) 2019-08-19 2022-10-11 Exxonmobil Upstream Research Company Compliant composite heat exchangers
US20210063083A1 (en) 2019-08-29 2021-03-04 Exxonmobil Upstream Research Company Liquefaction of Production Gas
US12050054B2 (en) 2019-09-19 2024-07-30 ExxonMobil Technology and Engineering Company Pretreatment, pre-cooling, and condensate recovery of natural gas by high pressure compression and expansion
EP4031822A1 (de) 2019-09-19 2022-07-27 Exxonmobil Upstream Research Company (EMHC-N1-4A-607) Vorbehandlung und vorkühlung von erdgas durch hochdruckkompression und -expansion
WO2021055021A1 (en) 2019-09-19 2021-03-25 Exxonmobil Upstream Research Company Pretreatment and pre-cooling of natural gas by high pressure compression and expansion
WO2021055074A1 (en) 2019-09-20 2021-03-25 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
EP4133226A1 (de) * 2020-04-08 2023-02-15 Cryostar SAS Verflüssigungs- und unterkühlsystem und -verfahren
WO2022099233A1 (en) * 2020-11-03 2022-05-12 Exxonmobil Upstream Research Company Natural gas liquefaction methods and systems featuring feed compression, expansion and recycling
US20230115492A1 (en) * 2021-10-13 2023-04-13 Henry Edward Howard System and method to produce liquefied natural gas
US20230113326A1 (en) * 2021-10-13 2023-04-13 Henry Edward Howard System and method to produce liquefied natural gas
US20230129424A1 (en) * 2021-10-21 2023-04-27 Henry Edward Howard System and method to produce liquefied natural gas
US20230159185A1 (en) * 2021-11-19 2023-05-25 General Electric Company Sub-coolers for refueling onboard cryogenic fuel tanks and methods for operating the same

Family Cites Families (54)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3162519A (en) * 1958-06-30 1964-12-22 Conch Int Methane Ltd Liquefaction of natural gas
US3323315A (en) * 1964-07-15 1967-06-06 Conch Int Methane Ltd Gas liquefaction employing an evaporating and gas expansion refrigerant cycles
DE1626325B1 (de) * 1964-11-03 1969-10-23 Linde Ag Verfahren und Einrichtung zum Verfluessigen von tiefsiedenden Gasen
DE1501730A1 (de) * 1966-05-27 1969-10-30 Linde Ag Verfahren und Vorrichtung zum Verfluessigen von Erdgas
US3407052A (en) * 1966-08-17 1968-10-22 Conch Int Methane Ltd Natural gas liquefaction with controlled b.t.u. content
GB1096697A (en) * 1966-09-27 1967-12-29 Int Research & Dev Co Ltd Process for liquefying natural gas
US3735600A (en) * 1970-05-11 1973-05-29 Gulf Research Development Co Apparatus and process for liquefaction of natural gases
DE2110417A1 (de) * 1971-03-04 1972-09-21 Linde Ag Verfahren zum Verfluessigen und Unterkuehlen von Erdgas
US4140223A (en) * 1977-08-24 1979-02-20 Rau Arthur G Tiered rotatable spice-cans storage unit
JPS6060463A (ja) * 1983-09-14 1985-04-08 株式会社日立製作所 液化ガス発生装置
US4740223A (en) * 1986-11-03 1988-04-26 The Boc Group, Inc. Gas liquefaction method and apparatus
US4846862A (en) * 1988-09-06 1989-07-11 Air Products And Chemicals, Inc. Reliquefaction of boil-off from liquefied natural gas
US5036671A (en) * 1990-02-06 1991-08-06 Liquid Air Engineering Company Method of liquefying natural gas
JPH06159928A (ja) * 1992-11-20 1994-06-07 Chiyoda Corp 天然ガス液化方法
FR2714722B1 (fr) * 1993-12-30 1997-11-21 Inst Francais Du Petrole Procédé et appareil de liquéfaction d'un gaz naturel.
FR2714720B3 (fr) * 1993-12-30 1996-05-03 Inst Francais Du Petrole Procédé et appareil de liquéfaction d'un gaz naturel.
AUPM485694A0 (en) * 1994-04-05 1994-04-28 Bhp Petroleum Pty. Ltd. Liquefaction process
MY113626A (en) * 1995-10-05 2002-04-30 Bhp Petroleum Pty Ltd Liquefaction apparatus
US5669234A (en) * 1996-07-16 1997-09-23 Phillips Petroleum Company Efficiency improvement of open-cycle cascaded refrigeration process
US5755114A (en) * 1997-01-06 1998-05-26 Abb Randall Corporation Use of a turboexpander cycle in liquefied natural gas process
JPH10204455A (ja) * 1997-01-27 1998-08-04 Chiyoda Corp 天然ガス液化方法
US5836173A (en) * 1997-05-01 1998-11-17 Praxair Technology, Inc. System for producing cryogenic liquid
DZ2535A1 (fr) * 1997-06-20 2003-01-08 Exxon Production Research Co Procédé perfectionné pour la liquéfaction de gaz naturel.
US5931021A (en) * 1997-06-24 1999-08-03 Shnaid; Isaac Straightforward method and once-through apparatus for gas liquefaction
TW366409B (en) * 1997-07-01 1999-08-11 Exxon Production Research Co Process for liquefying a natural gas stream containing at least one freezable component
US5992175A (en) * 1997-12-08 1999-11-30 Ipsi Llc Enhanced NGL recovery processes
US6446465B1 (en) * 1997-12-11 2002-09-10 Bhp Petroleum Pty, Ltd. Liquefaction process and apparatus
FR2772896B1 (fr) * 1997-12-22 2000-01-28 Inst Francais Du Petrole Procede de liquefaction d'un gaz notamment un gaz naturel ou air comportant une purge a moyenne pression et son application
US6006545A (en) * 1998-08-14 1999-12-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Liquefier process
US6269656B1 (en) * 1998-09-18 2001-08-07 Richard P. Johnston Method and apparatus for producing liquified natural gas
US6085545A (en) * 1998-09-18 2000-07-11 Johnston; Richard P. Liquid natural gas system with an integrated engine, compressor and expander assembly
TW421704B (en) * 1998-11-18 2001-02-11 Shell Internattonale Res Mij B Plant for liquefying natural gas
MY117548A (en) * 1998-12-18 2004-07-31 Exxon Production Research Co Dual multi-component refrigeration cycles for liquefaction of natural gas
US6070429A (en) * 1999-03-30 2000-06-06 Phillips Petroleum Company Nitrogen rejection system for liquified natural gas
US6306531B1 (en) * 1999-07-06 2001-10-23 General Motors Corporation Combustor air flow control method for fuel cell apparatus
US6308531B1 (en) * 1999-10-12 2001-10-30 Air Products And Chemicals, Inc. Hybrid cycle for the production of liquefied natural gas
US6354105B1 (en) * 1999-12-03 2002-03-12 Ipsi L.L.C. Split feed compression process for high recovery of ethane and heavier components
MY122625A (en) * 1999-12-17 2006-04-29 Exxonmobil Upstream Res Co Process for making pressurized liquefied natural gas from pressured natural gas using expansion cooling
US6220053B1 (en) * 2000-01-10 2001-04-24 Praxair Technology, Inc. Cryogenic industrial gas liquefaction system
US6484533B1 (en) * 2000-11-02 2002-11-26 Air Products And Chemicals, Inc. Method and apparatus for the production of a liquid cryogen
US6412302B1 (en) * 2001-03-06 2002-07-02 Abb Lummus Global, Inc. - Randall Division LNG production using dual independent expander refrigeration cycles
US6581409B2 (en) * 2001-05-04 2003-06-24 Bechtel Bwxt Idaho, Llc Apparatus for the liquefaction of natural gas and methods related to same
GB0120272D0 (en) * 2001-08-21 2001-10-10 Gasconsult Ltd Improved process for liquefaction of natural gases
US6564578B1 (en) * 2002-01-18 2003-05-20 Bp Corporation North America Inc. Self-refrigerated LNG process
US6751985B2 (en) * 2002-03-20 2004-06-22 Exxonmobil Upstream Research Company Process for producing a pressurized liquefied gas product by cooling and expansion of a gas stream in the supercritical state
FR2841330B1 (fr) * 2002-06-21 2005-01-28 Inst Francais Du Petrole Liquefaction de gaz naturel avec recyclage de gaz naturel
US6622519B1 (en) * 2002-08-15 2003-09-23 Velocys, Inc. Process for cooling a product in a heat exchanger employing microchannels for the flow of refrigerant and product
US6694774B1 (en) * 2003-02-04 2004-02-24 Praxair Technology, Inc. Gas liquefaction method using natural gas and mixed gas refrigeration
US6889523B2 (en) * 2003-03-07 2005-05-10 Elkcorp LNG production in cryogenic natural gas processing plants
US6742357B1 (en) * 2003-03-18 2004-06-01 Air Products And Chemicals, Inc. Integrated multiple-loop refrigeration process for gas liquefaction
US6722157B1 (en) * 2003-03-20 2004-04-20 Conocophillips Company Non-volatile natural gas liquefaction system
US7204100B2 (en) * 2004-05-04 2007-04-17 Ortloff Engineers, Ltd. Natural gas liquefaction
EP1792130B1 (de) * 2004-08-06 2017-04-05 BP Corporation North America Inc. Erdgasverflüssigungsverfahren
US7228714B2 (en) * 2004-10-28 2007-06-12 Praxair Technology, Inc. Natural gas liquefaction system

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

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EP1929227A1 (de) 2008-06-11
RU2406949C2 (ru) 2010-12-20
CA2618576C (en) 2014-05-27
EP1929227A4 (de) 2017-05-17
WO2007021351A1 (en) 2007-02-22
AU2006280426A1 (en) 2007-02-22
AU2006280426B2 (en) 2010-09-02
JP5139292B2 (ja) 2013-02-06
CA2618576A1 (en) 2007-02-22
RU2008108998A (ru) 2009-09-20
JP2009504838A (ja) 2009-02-05
NO20081190L (no) 2008-05-07
US20090217701A1 (en) 2009-09-03

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