WO2009045832A2 - Method for producing liquefied natural gas - Google Patents
Method for producing liquefied natural gas Download PDFInfo
- Publication number
- WO2009045832A2 WO2009045832A2 PCT/US2008/077627 US2008077627W WO2009045832A2 WO 2009045832 A2 WO2009045832 A2 WO 2009045832A2 US 2008077627 W US2008077627 W US 2008077627W WO 2009045832 A2 WO2009045832 A2 WO 2009045832A2
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- WO
- WIPO (PCT)
- Prior art keywords
- gas
- natural gas
- refrigeration
- cooled
- stream
- Prior art date
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- 239000003949 liquefied natural gas Substances 0.000 title claims description 57
- 238000004519 manufacturing process Methods 0.000 title claims description 20
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 174
- 239000003345 natural gas Substances 0.000 claims abstract description 86
- 238000005057 refrigeration Methods 0.000 claims abstract description 85
- 238000000034 method Methods 0.000 claims abstract description 33
- 239000007789 gas Substances 0.000 claims description 139
- 230000008929 regeneration Effects 0.000 claims description 32
- 238000011069 regeneration method Methods 0.000 claims description 32
- 238000000746 purification Methods 0.000 claims description 27
- 238000001816 cooling Methods 0.000 claims description 16
- 238000010792 warming Methods 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000012071 phase Substances 0.000 description 25
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 23
- 239000007788 liquid Substances 0.000 description 14
- 238000001179 sorption measurement Methods 0.000 description 14
- 229910002092 carbon dioxide Inorganic materials 0.000 description 13
- 239000001569 carbon dioxide Substances 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 239000012530 fluid Substances 0.000 description 5
- 238000007906 compression Methods 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 238000002203 pretreatment Methods 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen(.) Chemical compound [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
Classifications
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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
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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
- F25J1/003—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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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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
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
- F25J1/0202—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 only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0232—Coupling of the liquefaction unit to other units or processes, so-called integrated processes integration within a pressure letdown station of a high pressure pipeline system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—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
- F25J1/0267—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 using flash gas as heat sink
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—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
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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
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
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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
- 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
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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
- 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
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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
- 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
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
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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
- 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
- This invention relates generally to the production of liquefied natural gas and, more particularly, to the production of liquefied natural gas (LNG) using cryogenic expansion and the pretreatment of the natural gas for use in such a process.
- LNG liquefied natural gas
- Natural gas (NG) pressure reduction points are often referred to as let-down stations. Such stations enable the regional distribution of natural gas (typically at pressures of 100 to 600 psia). In general, let-down stations are not designed for the useful recovery of the pressure energy. Processes which serve to let-down natural gas while producing a fraction of the inlet gas as liquefied natural gas are often referred to as expander cycles or expander plants.
- U.S. Patent No. 7,134,296 describes a method for cooling a product gas wherein a working gas undergoes a staged expansion to a first temperature and a subsequent turbo-expansion to a second higher temperature and both expanded gas and the turbo-expanded gas provide cooling to the product gas.
- the turbo-expansion uses at least a portion of the warmed gas expanded in the first stage, the remaining portion being pressure boosted, preferably using the shaft work of turbo-expansion.
- U.S. Patent No. 3,503,220 describes a process for natural gas liquefaction using solely letdown pressure energy, without additional refrigeration/work input. Even though the pressure ratio is relatively high (7/8), the LNG product is only 12% of feed due to very low feed pressure level (189 psia). The feed is split into working gas and liquefaction gas and warm end refrigeration is provided by turbo-expansion of working gas with the work produced being used to boost the pressure of the liquefaction gas. A portion of the refrigeration available at the warm end can be shifted to the cold end.
- U.S. Patent No. 6,131,407 describes a process for liquefying nitrogen, oxygen or argon from an air separation unit using natural gas letdown as a source of refrigeration.
- the feed is split into two portions, one providing refrigeration for the warm end and the other providing refrigeration for the cold end. All feed is dehydrated and the second portion is further treated for carbon dioxide removal.
- Warm end refrigeration is provided by turbo-expansion of the working gas.
- the preferred embodiments show an electric generator brake on the expander. However, the energy from the expander can be used for compression of either nitrogen or natural gas at either higher or lower pressure levels to increase the pressure ratio of the expander and increase the liquefaction capacity of the letdown liquefaction unit.
- Cold end refrigeration is provided by two step cascaded Joule-Thomson expansion.
- U.S. Patent No. 6,694,774 describes a process for liquefying natural gas using natural gas letdown to provide the warm end refrigeration and mixed gas refrigeration (MGR) for cold end refrigeration.
- the feed is split into working gas and liquefaction gas and warm end refrigeration is provided by turbo- expansion of the working gas.
- the energy produced by the expander is used in the MGR compressor.
- U.S. Patent No. 7,228,714 describes a method for producing LNG wherein high pressure LNG is subcooled and then flashed to form flash vapor and LNG product, and the flash vapor is employed in a refrigeration cycle to generate refrigeration for subcooling the LNG.
- this process does not recover pressure energy from the regeneration gas before sending the regeneration gas for carbon dioxide removal.
- a method for producing liquefied natural gas comprising:
- the present invention relates to an optimized cycle for LNG production at letdown stations where the process is divided into two regions: a warm end where a portion of the NG is cooled by using only the pressure letdown energy from the remaining portion, and a cold end where an externally powered turbo-expander cycle is used to sub-cool the NG, in order to minimize the flash gas lost at depressurization and maximize LNG production.
- the ratio between the two portions of the feed is optimized for minimum pre-treatment and minimum unit power requirement (kW/gal LNG produced).
- the optimal arrangement of the warm end cycle varies depending on process conditions.
- One embodiment of the invention is a method for producing liquefied natural gas comprising:
- Another embodiment of the invention is a method for producing liquefied natural gas comprising:
- an optional step of purifying a high pressure natural gas in a first purification system [0028] an optional step of purifying a high pressure natural gas in a first purification system; [0029] compressing and cooling a first portion of a natural gas and expanding such first portion in a first expansion to produce at least a part of the refrigeration required to liquefy the remaining second portion of the natural gas; [0030] heating such first portion to bring it to a temperature above its dew point and turbo-expanding such heated first portion;
- Figure 1 is a schematic representation of one preferred embodiment of the liquefied natural gas production method of this invention.
- Figure 2 is a schematic representation of another preferred embodiment of the liquefied natural gas production method of this invention. Detailed Description
- the present invention relates to an optimized cycle for LNG production at letdown stations where the process is divided into two regions: a warm end where a portion of the NG is cooled by using only the pressure letdown energy from the remaining portion, and a cold end where an externally powered turbo-expander cycle is used to sub-cool the NG, in order to minimize the flash gas lost at depressurization and maximize LNG production.
- the ratio between the two portions of the feed is optimized for minimum pre-treatment and minimum unit power requirement (kW/gal LNG produced).
- the optimal arrangement of the warm end cycle varies depending on process conditions.
- the term "adsorption unit” means a system incorporating at least one vessel, preferably two or more, containing a solid adsorbent such as silicon dioxide or molecular sieves, which preferentially adsorbs at least one constituent from a feed gas.
- the adsorption unit also comprises necessary valving to direct both feed and regeneration gases through the bed(s) at varying time intervals.
- regeneration gas means a fluid that contains substantially less adsorbing contaminant than the feed stream to an adsorption unit.
- Joule-Thomson valve expansion means expansion employing an isenthalpic pressure reduction device which typically may be a throttle valve, orifice or capillary tube.
- turboexpansion means an expansion employing an expansion device which produces shaft work. Such shaft work is produced by the rotation of a shaft induced by the depressurization of a fluid through one or more fluid conduits connected to the shaft, such as a turbine wheel.
- subambient expansion means a Joule- Thomson valve expansion or a turboexpansion which produces a lower pressure stream having a temperature lower than ambient.
- flashing means depressurizing a liquid through an expansion device with the conversion of a portion of the liquid to the vapor phase.
- directly heat exchange means the bringing of two fluids into heat exchange relation without any mixing of the fluids with each other.
- subcooling means cooling a liquid to be at a temperature lower than the saturation temperature of that liquid for the existing pressure.
- a high-pressure natural gas stream is extracted from a high-pressure pipeline.
- a portion of this stream is directed to a first adsorption unit for the removal of water. Warming the exhaust/outlet of a sub-ambient expansion generates at least a portion of the gas required for regeneration of this first adsorption unit.
- additional regeneration gas can be taken from the dehydrated gas exiting this first adsorption unit.
- the stream is then split into a first portion, referred to as working gas, and a second portion referred to as liquefaction gas.
- the liquefaction gas is directed to a second adsorption unit, which serves to remove at least carbon dioxide (and potentially hydrogen sulfide and water).
- At least a portion of the regeneration gas for the second adsorption unit is obtained from subsequent down stream sub-ambient temperature processing.
- the remaining portion of the gas needed for regeneration can be provided by taking a portion of the purified liquefaction gas exiting this second adsorption unit.
- the working gas is used to generate refrigeration for the cooling and condensation of the product from the second unit.
- the working gas is first pressure boosted, cooled to ambient temperature and then further cooled to a temperature lower than ambient.
- the cooled working gas is then turbo-expanded; the work generated can be used to power the booster compressor.
- the resulting stream is then warmed to ambient by indirect heat exchange with the liquefaction gas.
- the liquefaction gas exits the heat exchanger in a high pressure cooled state, and is further cooled and expanded to produce low pressure LNG product.
- high pressure natural gas stream 101 which is at a pressure generally within the range of from 400 to 1500 pounds per square inch absolute (psia) is first dried by passage through treatment system 500, which may be a thermal swing adsorption system.
- treatment system 500 which may be a thermal swing adsorption system.
- the resulting natural gas stream 102 is divided into two portions 103 and 104.
- a first portion 103 referred to as working gas, is first compressed in booster compressor 510 and cooled to ambient temperature in compressor after- cooler 515.
- the working gas is further cooled in heat exchanger 520, emerging therefrom as cooled stream 105.
- Cooled natural gas stream 105 is turbo-expanded in turbo-expander 525 to provide cold gas stream 106, having a temperature above its dew point, generally within the range of -30 to -160 0 F.
- the shaft work produced by turbo- expander 525 is preferably employed to provide at least a portion of the power 141 required to operate booster compressor 510.
- turbo- expanded stream 106 is passed to phase separator 530 and the vapor and liquid fractions are passed in respective streams 107 and 108 to a common pass of heat exchanger 545, and further to heat exchangers 535 and 520.
- the turbo-expanded gas stream is warmed by indirect heat exchange to provide cooling to the process natural gas streams 112, 110 and 109, respectively.
- Resulting warmed turbo-expanded gas stream 115 is withdrawn from heat exchanger 520 and may be recovered in stream 116.
- a small portion from stream 115 is taken in stream 117 as regeneration gas for the water removal system 500.
- the water laden regeneration gas exits pre-purification system 500 as stream 118 and may be recovered in stream 116.
- a second portion 104 referred to as liquefaction gas, is passed to additional purification system 505 for the removal of carbon dioxide to a level generally less than 50 ppm. Hydrogen sulfide is also almost entirely removed in this adsorption unit because it is more strongly adsorbed than carbon dioxide.
- Resulting further cleaned natural gas stream 109 is cooled by passage through heat exchanger 520, emerging therefrom as cooled gas 110.
- a small part of the natural gas stream 109 may be passed through valve 610 as stream 140 and combined with natural gas stream 124 as regeneration gas for the additional purification system 505.
- Cooled gas 110 is further cooled in heat exchanger 535 to a temperature such that all heavy hydrocarbons, if present in the stream, are removed from the gas to levels which will prevent their potential freezing in the cold box.
- Natural gas emerges from heat exchanger 535 as stream 111, which is then passed to the phase separator 540.
- the liquid containing the heavy hydrocarbons is then withdrawn from phase separator 540 in stream 113, passed through valve 550 and, in the embodiment illustrated in Figure 1, passed in stream 114 for combination with stream 108 and further processing as described above.
- Vapor is withdrawn from phase separator 540 in stream 112 and further cooled by passage through heat exchanger 545 against warming Joule-Thomson expanded gas to form at least partially liquefied natural gas in stream 119.
- stream 119 may have only a small portion liquefied or be completely liquefied.
- the natural gas in stream 119 has a pressure generally within the range of 400 to 1500 psia and a temperature generally within the range of -70 to -160°F.
- Stream 120 is then flashed by passage through valve 555 to form two-phase stream 121, having a pressure within the range of 100-600 psia.
- Two-phase stream 121 is passed to the phase separator 560 and the vapor and liquid fractions are passed in respective streams 122 and 123 to a common pass of heat exchanger 545, and further for indirect heat exchange in heat exchangers 535 and 520, exiting heat exchanger 520 as stream 124 at ambient temperature.
- the gas is then sent to the carbon dioxide removal system 505, where it is used as regeneration gas.
- the carbon dioxide laden regeneration gas exits the carbon dioxide removal system 505 as stream 125 and can be recovered in stream 116.
- High pressure cooled natural gas in stream 119 is further cooled to a temperature within the range of -200 to -260 0 F by passage through heat exchanger 565 to form subcooled liquid natural gas stream 126.
- Stream 126 is flashed by passage through valve 570 to form two-phase stream 127, having pressure generally within the range of from 14.7 to 40 psia.
- Two-phase stream 127 which comprises flash vapor and liquefied natural gas, is passed into phase separator 575 from which product liquefied natural gas is withdrawn and recovered in stream 128. Flash vapor is withdrawn from phase separator 575 in stream 129 and combined in stream 130 with refrigeration gas 138 and with flash gas from storage tanks (not shown).
- Stream 130 is sent to heat exchanger 565 for indirect heat exchange with incoming high pressure liquid natural gas stream 119.
- Refrigeration gas 131 which has been warmed to about ambient temperature by passage through heat exchanger 580, is compressed first by passage through compressor 585.
- Resulting compressed refrigeration gas 132 is cooled of the heat of compression by passage through heat exchanger 590 to form stream 133.
- Stream 133 is then further compressed in booster compressor 595, and cooled in the compressor after-cooler 600 to form stream 134, having a pressure within the range of 100-600 psia.
- a portion 135 of stream 134 is removed from the refrigeration gas cycle and preferably recovered as natural gas, most preferably as illustrated in Figure 1, by combination with stream 115 to form stream 116.
- the remaining portion 136 of the compressed refrigeration gas is cooled by passage through heat exchanger 580 to a temperature within the range of -70 to -170 0 F.
- Cooled refrigeration gas is passed in stream 137 from heat exchanger 580 to turbo-expander 605, wherein it is turbo-expanded to a pressure within the range of from 14.7 to 40 psia to generate refrigeration.
- the shaft work produced by turbo-expander 605 is preferably employed to provide at least some of the power 142 to operate compressor 595.
- Resulting refrigeration bearing gas from turbo-expander 605 is passed to stream 138 and warmed in heat exchanger 565 to effect the subcooling of the natural gas in stream 119.
- the cooled refrigeration gas in stream 138 is combined with the flash vapor in stream 129 to form combined stream 130 which is passed to heat exchanger 565 and warmed by indirect heat exchange to effect the subcooling of the liquid natural gas in stream 127.
- the resulting warmed refrigeration gas is passed in stream 139 to heat exchanger 580, emerging therefrom in stream 131 for processing as previously described.
- high pressure natural gas stream 201 which is at a pressure generally within the range of from 400 to 1500 pounds per square inch absolute (psia), is first dried by passage through treatment system 700, which may be a thermal swing adsorption system.
- the resulting dried natural gas stream 202 is divided into two portions 203 and 204.
- a first portion 204 referred to as working gas
- a second portion 203 referred to as liquefaction gas
- the working gas is further cooled in heat exchangers 720, 725 and 730, emerging there from as cooled stream 205.
- Cooled natural gas stream 205 is expanded in a first expansion, such as by passing through Joule-Thomson valve 735, to produce an expanded gas stream 206 at a first temperature, which is typically in the range of -70 to -150 0 F.
- the first expansion may be with or without the production of the shaft work.
- the first expansion is a Joule- Thomson expansion which results in two-phase stream 206.
- Stream 206 is passed to separator 740, wherein it is separated into vapor stream 207 and liquid stream 208. Streams 207 and 208 are then fed to the same pass of heat exchanger 730, exiting as two-phase stream 209, which contains less than 5% liquid.
- Stream 209 is then passed to separator 745, where it is separated into vapor stream 210 and liquid stream 211.
- the vapor stream 210 is further warmed in heat exchanger 725, exiting the heat exchanger as superheated natural gas stream 212.
- Stream 212 is then passed to the turbo-expander 750 wherein it is turbo-expanded to a pressure marginally above letdown pressure.
- the shaft work 248 produced by turbo-expander 750 may be employed to provide at least some of the power to operate compressor 710.
- Temperature of stream 212 is chosen such that the temperature of turbo-expanded stream 213 is close to the temperature of stream 206.
- Stream 213 is fed to phase separator 755 together with liquid stream 211 and with the heavy hydrocarbon condensate 233.
- phase separator 755 The resulting liquid 243 and vapor 244 phases from phase separator 755 are fed to the same passage of heat exchanger 730 wherein it is warmed by indirect heat exchange with liquefaction gas 222, exiting heat exchanger 730 as stream 214. Stream 214 is then further warmed in heat exchangers 725 and 720 by indirect heat exchange with the liquefaction gas 219.
- Working gas exits the cold box at ambient temperature as stream 215 and may be recovered in stream 216. A small portion from stream 215 is taken in stream 217 as regeneration gas for the water removal system 700. The water laden regeneration gas exits the pre-purification system 700 as stream 218 and may be recovered in stream 216.
- liquefaction gas 203 is sent for additional purification to system 705, which may be a thermal swing adsorption system.
- system 705 carbon dioxide is removed to a level generally less than 50 ppm. Hydrogen sulfide is also almost entirely removed in this adsorption unit because it is more strongly adsorbed than carbon dioxide.
- the clean liquefaction gas 219 is then cooled by passage through heat exchangers 720 and 725, emerging therefrom as two phase stream 220. A small part of the clean liquefaction gas 219 may be passed through valve 825 as stream 245 and combined with natural gas stream 227 as regeneration gas for the additional purification system 705.
- Stream 220 is separated in phase separator 760 in a liquid phase 221 containing most heavy hydrocarbons, and vapor stream 222.
- Liquid stream 221 is passed through valve 765 and, in the embodiment illustrated in Figure 2, passed in stream 223 for combination with stream 211 and 213 and further processing as described above.
- Vapor stream 222 is further cooled by passage through heat exchanger 730 against warming expanded natural gas streams (combined 243 and 244 and combined 207 and 208) and exits the heat exchanger as cooled high pressure natural gas stream 224.
- the natural gas in stream 224 has a pressure generally within the range of 400 to 1500 psia and a temperature generally within the range of -70 to -160 0 F.
- Stream 225 is then flashed by passage through valve 770 to form two phase stream 226, having a pressure within the range of 100 to 600 psia.
- Two-phase stream 226 is passed to the phase separator 775 and the vapor 246 and liquid 247 fractions are fed to a common passage of heat exchanger 725, and further sent for indirect heat exchange in heat exchanger 720, exiting heat exchanger 720 as stream 227 at ambient temperature.
- the gas is then sent to the CO 2 removal system 705 where it is used as regeneration gas.
- the CO 2 laden regeneration gas exits the CO 2 removal system 705 as stream 228 and can be recovered in stream 216.
- High pressure natural gas in stream 224 is further sub-cooled to a temperature within the range of -200 to -260 0 F by passage through heat exchanger 780 to form subcooled liquid natural gas stream 229.
- Stream 229 is flashed by passage through valve 785 to form two-phase stream 230 having a pressure generally within the range of 14.7 to 40 psia, but possibly having a pressure greater than 40 psia.
- Two-phase stream 230 which comprises flash vapor and liquefied natural gas, is passed into phase separator 790 from which product liquefied natural gas is withdrawn and recovered in stream 231.
- Flash vapor is withdrawn from phase separator 790 in stream 232 and combined with refrigeration gas in stream 233 to sub-cool the natural gas 224 as will be more fully described below. Flash gas from storage tank (not shown) may also be combined in stream 233.
- Refrigeration gas 234 which has been warmed to about ambient temperature by passage through heat exchanger 795, is compressed first by passage through compressor 800 and resulting compressed refrigeration gas 235 is cooled of the heat of compression by passage through heat exchanger 805 to form stream 236.
- Stream 236 is then further compressed in booster compressor 810, and cooled in the compressor after-cooler 815 to form stream 237 having a pressure within the range of 150 to 500 psia.
- a portion 238 of stream 237 is removed from the refrigeration gas cycle and preferably recovered as natural gas, most preferably as illustrated in Figure 2, by combination with stream 215 to form stream 216.
- the remaining portion 239 of the compressed refrigeration gas is cooled by passage through heat exchanger 795 to a temperature within the range of -70 to -170 0 F.
- Cooled refrigeration gas is passed in stream 240 from heat exchanger 795 to turbo-expander 820 wherein it is turbo-expanded to a pressure within the range of from 14.7 to 40 psia to generate refrigeration.
- the shaft work 249 produced by turbo-expander 820 is preferably employed to provide at least some of the power to operate compressor 810.
- Resulting refrigeration bearing gas from turbo-expander 820 is passed to stream 241 and warmed in heat exchanger 780 to effect the subcooling of the liquid natural gas in stream 224.
- the cooled refrigeration gas in stream 241 is combined with the flash vapor in stream 232 and with the flash vapor from storage tanks (not shown) to form combined stream 233 which is passed to heat exchanger 780 and warmed by indirect heat exchange to effect the sub-cooling of the liquid natural gas.
- the resulting warmed refrigeration gas is passed in stream 242 to heat exchanger 795, emerging therefrom in stream 234 for processing as previously described.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
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Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA2700751A CA2700751C (en) | 2007-09-28 | 2008-09-25 | Method for producing liquefied natural gas |
BRPI0817749A BRPI0817749A8 (en) | 2007-09-28 | 2008-09-25 | method to produce liquefied natural gas |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US11/864,316 US20090084132A1 (en) | 2007-09-28 | 2007-09-28 | Method for producing liquefied natural gas |
US11/864,316 | 2007-09-28 |
Publications (2)
Publication Number | Publication Date |
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WO2009045832A2 true WO2009045832A2 (en) | 2009-04-09 |
WO2009045832A3 WO2009045832A3 (en) | 2014-05-01 |
Family
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/US2008/077627 WO2009045832A2 (en) | 2007-09-28 | 2008-09-25 | Method for producing liquefied natural gas |
Country Status (9)
Country | Link |
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US (2) | US20090084132A1 (en) |
AR (1) | AR068575A1 (en) |
BR (1) | BRPI0817749A8 (en) |
CA (1) | CA2700751C (en) |
CL (1) | CL2008002904A1 (en) |
CO (1) | CO6150051A1 (en) |
PE (1) | PE20090925A1 (en) |
UY (1) | UY31371A1 (en) |
WO (1) | WO2009045832A2 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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CN101967413A (en) * | 2010-06-07 | 2011-02-09 | 杭州福斯达实业集团有限公司 | Method and device for liquefying natural gas via refrigeration of single mixed refrigerant |
Families Citing this family (10)
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US7608935B2 (en) * | 2003-10-22 | 2009-10-27 | Scherzer Paul L | Method and system for generating electricity utilizing naturally occurring gas |
WO2012047548A2 (en) * | 2010-09-28 | 2012-04-12 | Uop Llc | Process for regeneration of adsorbent beds |
CA2798057C (en) * | 2012-12-04 | 2019-11-26 | Mackenzie Millar | A method to produce lng at gas pressure letdown stations in natural gas transmission pipeline systems |
CN103983084A (en) * | 2014-05-03 | 2014-08-13 | 宁波鲍斯能源装备股份有限公司 | Natural gas pressure energy comprehensive utilization complete equipment |
CA2958091C (en) | 2014-08-15 | 2021-05-18 | 1304338 Alberta Ltd. | A method of removing carbon dioxide during liquid natural gas production from natural gas at gas pressure letdown stations |
KR102057023B1 (en) * | 2015-09-02 | 2019-12-18 | 엑손모빌 업스트림 리서치 캄파니 | Swing Adsorption Process and System Using Overhead Stream of Demetrizer as Purge Gas |
EA201890319A1 (en) * | 2015-09-02 | 2018-07-31 | Эксонмобил Апстрим Рисерч Компани | DEVICE AND SYSTEM FOR IMPLEMENTATION OF METHODS OF COMBINED SHORT-CYCLIC ADSORPTION WITH SHEET OF TEMPERATURE AND PRESSURE |
CA2994864C (en) * | 2015-09-02 | 2020-04-28 | Exxonmobil Upstream Research Company | Apparatus and system for swing adsorption processes related thereto |
CN108431184B (en) | 2015-09-16 | 2021-03-30 | 1304342阿尔伯塔有限公司 | Method for preparing natural gas at gas pressure reduction station to produce Liquid Natural Gas (LNG) |
US10281203B2 (en) * | 2016-08-05 | 2019-05-07 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for liquefaction of industrial gas by integration of methanol plant and air separation unit |
Citations (1)
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WO2007021351A1 (en) * | 2005-08-09 | 2007-02-22 | Exxonmobil Upstream Research Company | Natural gas liquefaction process for lng |
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DE2110417A1 (en) * | 1971-03-04 | 1972-09-21 | Linde Ag | Process for liquefying and subcooling natural gas |
US4012212A (en) * | 1975-07-07 | 1977-03-15 | The Lummus Company | Process and apparatus for liquefying natural gas |
DE2820212A1 (en) * | 1978-05-09 | 1979-11-22 | Linde Ag | METHOD FOR LIQUIDATING NATURAL GAS |
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2008
- 2008-09-25 BR BRPI0817749A patent/BRPI0817749A8/en not_active Application Discontinuation
- 2008-09-25 CA CA2700751A patent/CA2700751C/en active Active
- 2008-09-25 WO PCT/US2008/077627 patent/WO2009045832A2/en active Application Filing
- 2008-09-29 AR ARP080104237A patent/AR068575A1/en unknown
- 2008-09-29 PE PE2008001694A patent/PE20090925A1/en active IP Right Grant
- 2008-09-29 CL CL2008002904A patent/CL2008002904A1/en unknown
- 2008-09-29 CO CO08103283A patent/CO6150051A1/en not_active Application Discontinuation
- 2008-09-29 UY UY31371A patent/UY31371A1/en not_active Application Discontinuation
-
2009
- 2009-01-05 US US12/348,437 patent/US20090120127A1/en not_active Abandoned
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2007021351A1 (en) * | 2005-08-09 | 2007-02-22 | Exxonmobil Upstream Research Company | Natural gas liquefaction process for lng |
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CN101967413A (en) * | 2010-06-07 | 2011-02-09 | 杭州福斯达实业集团有限公司 | Method and device for liquefying natural gas via refrigeration of single mixed refrigerant |
Also Published As
Publication number | Publication date |
---|---|
BRPI0817749A8 (en) | 2018-12-11 |
BRPI0817749A2 (en) | 2015-03-24 |
US20090084132A1 (en) | 2009-04-02 |
AR068575A1 (en) | 2009-11-18 |
CA2700751C (en) | 2014-09-16 |
PE20090925A1 (en) | 2009-08-06 |
CO6150051A1 (en) | 2010-04-20 |
CL2008002904A1 (en) | 2009-03-20 |
CA2700751A1 (en) | 2009-04-09 |
US20090120127A1 (en) | 2009-05-14 |
WO2009045832A3 (en) | 2014-05-01 |
UY31371A1 (en) | 2009-04-30 |
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