WO2015017293A2 - System and integrated process for liquid natural gas production - Google Patents
System and integrated process for liquid natural gas production Download PDFInfo
- Publication number
- WO2015017293A2 WO2015017293A2 PCT/US2014/048339 US2014048339W WO2015017293A2 WO 2015017293 A2 WO2015017293 A2 WO 2015017293A2 US 2014048339 W US2014048339 W US 2014048339W WO 2015017293 A2 WO2015017293 A2 WO 2015017293A2
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- WIPO (PCT)
- Prior art keywords
- stream
- natural gas
- solid
- ice
- comprised substantially
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- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 131
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims description 41
- 230000008569 process Effects 0.000 title description 20
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 233
- 239000003345 natural gas Substances 0.000 claims abstract description 88
- 239000007787 solid Substances 0.000 claims abstract description 75
- 239000002002 slurry Substances 0.000 claims abstract description 47
- 238000001816 cooling Methods 0.000 claims abstract description 36
- 239000000203 mixture Substances 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 18
- 230000006835 compression Effects 0.000 claims description 36
- 238000007906 compression Methods 0.000 claims description 36
- 238000005057 refrigeration Methods 0.000 claims description 18
- 238000004891 communication Methods 0.000 claims description 13
- 239000012530 fluid Substances 0.000 claims description 10
- 230000005484 gravity Effects 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
- 230000003134 recirculating effect Effects 0.000 claims 1
- 239000012071 phase Substances 0.000 description 70
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 53
- 229910002092 carbon dioxide Inorganic materials 0.000 description 52
- 239000007789 gas Substances 0.000 description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 34
- 239000007788 liquid Substances 0.000 description 11
- 239000012535 impurity Substances 0.000 description 8
- 239000011248 coating agent Substances 0.000 description 5
- 238000000576 coating method Methods 0.000 description 5
- 238000011144 upstream manufacturing Methods 0.000 description 5
- 230000006870 function Effects 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000003607 modifier Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 230000003068 static effect Effects 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
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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"
- F25J1/0042—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 liquid expansion with extraction of work
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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
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0087—Propane; Propylene
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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
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0208—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
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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
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
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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
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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
- F25J2205/10—Processes or apparatus using other separation and/or other processing means using combined expansion and separation, e.g. in a vortex tube, "Ranque tube" or a "cyclonic fluid separator", i.e. combination of an isentropic nozzle and a cyclonic separator; Centrifugal separation
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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
- F25J2205/20—Processes or apparatus using other separation and/or other processing means using solidification of components
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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
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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
- F25J2205/84—Processes or apparatus using other separation and/or other processing means using filter
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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
- F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
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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
- F25J2220/68—Separating water or hydrates
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/30—Dynamic liquid or hydraulic expansion with extraction of work, e.g. single phase or two-phase turbine
Definitions
- the present disclosure relates to a system and process for liquid natural gas
- liquid natural gas production More particularly, the present disclosure relates to a system and process for liquid natural gas production that integrates natural gas cleanup and refrigeration steps in a single process.
- One aspect of the present disclosure resides in a system for producing liquid natural gas (LNG) from a natural gas stream, comprising: a moisture removal device, a compressor, a heat exchanger, a multi-phase turbo expander, a separator, and at least one additional separator.
- the moisture removal device and the compressor remove moisture from and compress the natural gas stream and generate a low moisture compressed natural gas stream.
- the heat exchanger cools the low moisture compressed natural gas stream and generates a cooled compressed discharge stream.
- the multi-phase turbo expander expands the cooled compressed discharge stream and generates an expanded exhaust stream comprised of a mixture of a vapor comprised substantially of CH 4 and a liquid natural gas /ice/solid CO 2 slurry.
- the separator separates the expanded exhaust stream and generates a vapor stream comprised substantially of CH 4 and a liquid natural gas/ice/solid CO 2 slurry stream.
- the at least one additional separator separates the liquid natural gas/ice/solid CO 2 slurry stream and generates a liquid natural gas output stream and an output stream comprised substantially of ice/solid CO 2 .
- a system for producing liquid natural gas (LNG) from a natural gas stream comprising: at least one compression stage, at least one cooling stage and at least one expansion stage.
- the at least one compression stage and the at least one cooling stage are configured to compress and cool a natural gas stream and generate a cooled compressed discharge stream.
- the at least one expansion stage configured to expand cooled compressed discharge stream and generate an expanded exhaust stream.
- the at least one expansion stage comprising at least one multi-phase turbo expander in fluid communication with the cooling stage and the compression stage.
- the multi-phase turbo expander comprising: a housing; at least one rotating component disposed within the housing; at least one inlet disposed in the housing, wherein the inlet is configured to receive the cooled compressed discharge stream; and at least one outlet disposed in the housing, wherein the outlet is configured to discharge an expanded exhaust stream comprising a mixture of a vapor comprised substantially of CH 4 and a liquid natural gas /ice/solid CO 2 slurry.
- Yet another aspect of the disclosure resides in a method for producing liquid natural gas (LNG) from a natural gas stream, comprising: providing an input natural gas stream; removing moisture, compressing and cooling the natural gas stream and generating a cooled compressed discharge stream; expanding the cooled compressed discharge stream in a multiphase turbo expander and generating an expanded exhaust stream comprising a mixture of a vapor comprised substantially of CH 4 and a liquid natural gas /ice/solid CO 2 slurry; separating the expanded exhaust stream in at least one separator and generating a vapor stream comprised substantially of CH 4 and a liquid natural gas/ice/solid CO 2 slurry stream; and separating the liquid natural gas/ice/solid CO 2 slurry stream in at least one additional separator and generating an output stream comprised substantially of ice/solid CO 2 and a liquid natural gas (LNG) output stream.
- LNG liquid natural gas
- FIG. 1 is a block diagram of a system for liquid natural gas production, in accordance with one or more embodiments shown or described herein;
- FIG. 2 is a block diagram of a system for liquid natural gas production, in accordance with one or more embodiments shown or described herein;
- FIG. 3 is a schematic of a multi-phase turbo expander for solid, liquid and gas separation, in accordance with one or more embodiments shown or described herein;
- FIG. 4 is a schematic of a cross-sectional view of a multi-phase turbo expander for solid, liquid and gas separation,, in accordance with one or more embodiments shown or described herein;
- FIG. 5 is a flow chart representing steps involved in an exemplary process for the production of liquid natural gas, in accordance with one or more embodiments shown or described herein;
- FIG. 6 is a comparative plot of liquid natural gas yield as a function of compression, in accordance with one or more embodiments shown or described herein.
- embodiments of the present disclosure provide systems and processes suitable for the production of liquid natural gas.
- embodiments of the present disclosure comprise systems including one or more integrated multi-phase turbo expanders and refrigeration means capable of operation with multi-phase flows (gas, liquids and solids).
- the system includes cooling a gas stream to form liquid natural gas and natural gas impurities, including CO 2 gas, solid CO 2 and/or liquid CO 2 .
- Embodiments of the present disclosure further include methods suitable for liquid natural gas production using the integrated multi-phase turbo expander and refrigeration means.
- the term “the” include plural referents unless the context clearly dictates otherwise.
- the term “or” is not meant to be exclusive and refers to at least one of the referenced components being present and includes instances in which a combination of the referenced components may be present, unless the context clearly dictates otherwise.
- the suffix "(s)” is usually intended to include both the singular and the plural of the term that it modifies, thereby including one or more of that term (e.g., "the jets” may include one or more jets, unless otherwise specified).
- the terms “may” and “may be” indicate a possibility of an occurrence within a set of circumstances; a possession of a specified property, characteristic or function; and/or qualify another verb by expressing one or more of an ability, capability, or possibility associated with the qualified verb. Accordingly, usage of "may” and “may be” indicates that a modified term is apparently appropriate, capable, or suitable for an indicated capacity, function, or usage, while taking into account that in some circumstances the modified term may sometimes not be appropriate, capable, or suitable. For example, in some
- FIG. 1 illustrates an exemplary liquid natural gas
- the LNG production system 10 includes at least one cooling stage 200 configured to receive a natural gas stream 16.
- the system 10 further includes at least one compression stage 100 in fluid communication with the one or more cooling stage 200.
- the combination of the at least one compression stage 100 and the at least one cooling stage 200 is configured to compress and partially cool the natural gas stream 16 prior to expansion and further cooling of a low moisture compressed natural gas stream 21 in an expansion stage 300.
- a separation stage 400 in fluid communication with a multi-phase turbo expander (described presently) in the expansion stage 400 provides separation of a cold CH 4 vapor and a LNG/ice/solid CO 2 slurry, and further separation of the slurry into LNG and solid CO 2 components.
- the LNG production system 10 includes a bulk moisture removal device 12, in fluid communication with a natural gas inlet 14, and through which a natural gas (NG) stream 16 is fed.
- the moisture removal device 12 provides for preliminary moisture removal from the NG stream 16, to generate a low moisture NG stream 20 at an output of the moisture removal device 12.
- the moisture removal device 18 may be configured as a molecular sieves bed. Other sorbent and solvent based systems known in the art may be also utilized.
- the at least one cooling stage 200 includes one or more heat exchangers
- a heat exchanger typically operating at temperatures below -100° C is utilized, requiring moisture in an input NG stream to be reduced to ⁇ 0.5 ppm.
- the temperature of the NG stream 16 within in the heat exchanger is typically -40° C or slightly higher, requiring moisture in the input NG stream 16 to be reduced to ⁇ 180 ppm.
- the compression stage 100 of the LNG production system 10 includes a first compressor 22, disposed between the moisture removals means 12 and one or more heat exchangers 24. More specifically, the first compressor 22 is disposed downstream of the moisture removal device 12, and upstream of the one or more heat exchangers 24. The first compressor 22 provides for the compression of the low moisture NG stream 20 to discharge a compressed NG stream 28. More particularly, in an embodiment the first compressor 22 discharges a low moisture compressed NG stream 21 at a pressure sufficient to provide for the reduction of the temperature in a final stage of cooling.
- the LNG production system may provide for moisture removal from the NG stream 16, subsequent to compression in the first compressor 22.
- the compression stage 100 of the LNG production system includes a first compressor 22 disposed upstream of the moisture removals means 12 and the one or more heat exchangers 24.
- the moisture removal device 12 is disposed downstream of the first compressor 22, and upstream of the one or more heat exchangers 24.
- the first compressor 22 provides for the compression of the NG stream 16 to discharge the compressed NG stream 28. Subsequent removal of moisture from the compressed NG stream 28 discharges the low moisture NG stream 20, and more particularly the low moisture compressed gas stream 21.
- the first compressor 22 comprises a multi-stage compressor 26 with inter stage cooling and provides compression of the low moisture NG stream 20.
- the first compressor 22 may comprise a plurality of compressors (not shown) having one or more air coolers disposed therebetween. The first compressor 22 generates the compressed NG air stream 28 at an outlet of the first compressor 22. NG cooling after the last compression stage of the multi-stage compressor 26 is achieved by an air cooler 29.
- the cooling stage 200 includes the one or more heat exchangers 24 (of which only one is illustrated) configured to remove heat from the low moisture compressed NG stream 21.
- the heat exchanger 24 is disposed downstream from the compression stage 100, and more particularly the first compressor 22.
- the low moisture compressed NG stream 21 is pre-cooled in the one or more heat exchangers 24 to approximately -40° C by cold methane vapor and configured to discharge a cooled compressed discharge stream 32.
- this cooling stage 200 may include a plurality of heat exchangers. It should be noted that in FIGs. 1 and 2, the single heat exchanger 24 is shown as an exemplary embodiment only and the actual number of heat exchangers and their individual configuration may vary depending on the end result desired. In some embodiments, the one or more heat exchangers 24 may be cooled using a cooling medium.
- the one or more heat exchangers 24 may be cooled using cooling air, cooling water, or both.
- the cooling stage 200 may further include one or more intercoolers (not shown) to cool the low moisture compressed NG stream 21 without substantially affecting the pressure.
- the LNG production system 10, and more particularly the expansion stage 300 further includes a multi-phase turbo expander 30 configured to receive the cooled compressed discharge stream 32 from the heat exchanger 24 and generate an expanded exhaust stream 34.
- the at least one cooling stage 200 is in fluid communication with the at least one expansion stage 300 including the multi-phase turbo expander 30, as described herein.
- the first compressor 22 and the multi-phase turbo expander 30 are typically mechanically coupled, such as through a common shaft 36.
- the multiphase turbo expander 30 may be mechanically coupled with compressor 46.
- the temperature of the natural gas stream, and more particularly the cooled compressed discharge stream 32, is decreased during the expansion process primarily as a result of work extraction in the multiphase turbo expander 30 with additional temperature reductions occurring through local depression of the static temperature in high velocity flow and the Joule-Thompson effect during throttling.
- energy recovered in the multi-phase turbo expander 30 is used to partially offset energy requirements for the compression stage 100.
- the expansion process further cools the cooled compressed discharge stream 32 of natural gas generating the expanded exhaust stream 34 comprising a mixture of a vapor stream comprised substantially of CH 4 and a LNG/ice/solid CO 2 slurry.
- the moisture content in the NG stream 16, and more particularly the low moisture compressed NG stream 21, can be adjusted prior to expansion in the multi-phase turbo expander 30 to optimize the LNG output and CO 2 particle sizes using the bulk moisture removal system, and more particularly the moisture removal device 12, at the beginning of the process.
- at least part of solid CO2 and ice are separated from the NG stream 16 and removed from the multi-phase turbo expander 30 by forcing the swirl movement of the stream.
- the LNG production system 10 further includes the at least one separation stage
- the vapor stream 40 comprised substantially of CH 4 is separated from the LNG/ice/C0 2 slurry in the separator 38 and is recirculated in the LNG production system 10, as indicated by the arrows, to pre-cool the low moisture NG stream 20 prior to compression and expansion in the first compressor 22 and multi-phase turbo expander 30, respectively.
- the system 10 further includes a recirculation stage 500 configured to circulate at least a portion of the vapor stream 40 comprised substantially of CH 4 to the low moisture NG stream 20, and more particularly to the low moisture NG stream 20 upstream of the compression stage 100, and the compressor 22 in a recirculation path 501, as best illustrated in FIG. 1.
- the recirculation stage 500 is configured to circulate at least a portion of the vapor stream 40 comprised substantially of CH 4 to the compressed NG stream 28, and more particularly to the compressed NG stream 28 downstream of the compression stage 100, and the compressor 22 in a recirculation path 501, as best illustrated in FIG. 2.
- the recuperation of cold CH 4 vapor stream 40 may result in additional cooling of the gas stream 16.
- the vapor stream 40 is compressed in a second compressor 44.
- the second compressor 44 is one of mechanically or electrically driven by a drive source 46 to provide for compression of the CH 4 vapor stream 40 and generate a compressed vapor stream 48.
- the LNG/ice/solid CO 2 slurry stream 42 is separated in a liquid/solid separator 50 to form a liquid natural gas (LNG) output stream 52 and an output stream 54 comprised substantially of ice/solid CO2.
- the liquid/solid separator 50 is one of a gravity separator, a cyclone, a sintered metal filter or any type of filter configured to separate the solid contaminants from the LNG.
- FIG. 2 illustrated is an alternate embodiment of the LNG production system of the present disclosure. More particularly, illustrated is a LNG production system 60 including an integrated external refrigeration system. It should be understood that like elements have like numbers throughout the embodiments.
- the LNG production system 60 includes a first compressor 22, in fluid communication with a natural gas inlet 14, and through which a natural gas (NG) stream 16 is fed.
- the first compressor 22 may comprise a multi-stage compressor 26 with inter stage cooling and provides compression of a NG stream 16.
- the first compressor 22 may comprise a plurality of compressors (not shown) having one or more air coolers disposed therebetween.
- the first compressor 22 generates a compressed NG air stream 28 at an outlet of the first compressor 22.
- the LNG production system 60 further includes a moisture removal device 12, disposed between the first compressor 22 and a heat exchanger 24.
- a heat exchanger 24 is disposed downstream of the moisture removal device 12 and in fluid communication therewith.
- the moisture removal device 12 is disposed downstream of the first compressor 22, and upstream of the heat exchanger 24.
- the heat exchanger 24 is utilized to remove heat from the low moisture compressed NG stream 21.
- the heat exchanger 24 is configured to discharge a cooled compressed discharge stream 32.
- the LNG production system 60 further includes a multi-phase turbo expander 30 configured to receive the cooled compressed discharge stream 32 from the heat exchanger 24 and generate an expanded exhaust stream 34.
- the first compressor 22 and the multi-phase turbo expander 30 are typically mechanically coupled, such as through a common shaft 36.
- the expansion process further cools the cooled compressed discharge stream 32 of natural gas generating the expanded exhaust stream 34 comprising a mixture of a vapor stream comprised substantially of CH 4 and a LNG/ice/solid CO 2 slurry .
- the LNG production system 60 further includes a separator 38, configured to receive the expanded exhaust stream 34 comprised of a mixture of a vapor stream comprised substantially of CH 4 and a LNG/ice/solid CO 2 slurry and separate the components into a vapor stream 40 comprised substantially of CH 4 and a LNG/ice/CC slurry stream 42.
- the cold vapor CH 4 is separated from the LNG/ice/CC ⁇ slurry in the separator 38 and is recirculated in the LNG production system 60, as indicated by the arrows, to pre-cool the compressed NG stream 28 prior to removal of moisture, cooling and expansion in the moisture removal device 12, the heat exchanger 24 and the multi-phase turbo expander 30, respectively.
- the vapor stream 40 is compressed in a second compressor 44 to generate a compressed vapor stream 48 comprised substantially of CH 4 .
- the LNG/ice/solid CO 2 slurry stream 42 is separated in a liquid/solid separator 50 to form a liquid natural gas (LNG) output stream 52 and an output stream 54 comprised of substantially ice/solid C02.
- LNG liquid natural gas
- the embodiment illustrated in FIG. 2 further includes an external refrigeration system 62 configured to generate a cold vapor stream 64.
- the external refrigeration system 62 is configured in fluidic communication with the heat exchanger 24. During operation, the external refrigeration system 62 provides pre-cooling in the heat exchanger 24 to approximately -40° C prior to expansion in the multi-phase turbo expander 30. The cold vapor stream 64 provides further cooling of the discharge stream 32 of up to -60° C. As previously indicated, although the external refrigeration system 62 is not required, use of such additional refrigeration means provides additional energy to the heat exchanger 24 and further cooling of the low moisture compressed NG stream 21.
- the external refrigeration system 62 is configured as a propane refrigeration system.
- a multi-phase turbo expander for expanding the cooled compressed discharge stream 32 generated by the heat exchanger 42 is presented. Expansion of the cooled compressed discharge stream 32 generates the expanded exhaust stream 34 comprising the mixture of cold CH 4 vapor and the LNG/ice/solid CO 2 slurry.
- multiphase turbo expander refers to a radial, axial, or mixed flow turbo-machine through which a gas or gas mixture is expanded to produce work and additional output components.
- FIG. 4 illustrates in a cross-sectional view, an embodiment of the multi-phase turbo expander 70, in accordance with an embodiment of the disclosure.
- the multi-phase turbo expander 70 includes a housing 72.
- the multi-phase turbo expander 70 further includes at least one rotating component or a rotor 74 configured to extract work from a flow stream.
- the multi-phase turbo expander 70 further includes at least one stationary component 76.
- the stationary component 76 may include a stator or a nozzle.
- the nozzle is equipped with vanes that force swirl stream movement.
- the multi-phase turbo expander 70 further includes one or more seals 78, in some embodiments.
- the multi-phase turbo expander 70 further includes one or more blades 80/82.
- the multi-phase turbo expander 70 further includes one or more stationary blades 80 and one or more rotor blades 82, as indicated in FIG. 4.
- the multi-phase turbo expander 70 further includes at least one inlet 84 disposed in the housing 72.
- the inlet 84 is configured to receive a gas stream 86, in some embodiments.
- the gas stream 86 is generally similar to the cooled compressed discharge stream 32 of FIGs. 1 and 2 exiting the heat exchanger 24, subsequent to compression in a compressor, such as the first compressor 22 of FIGs. 1 and 2 and cooling in the heat exchanger 24.
- the multi-phase turbo expander 70 further includes at least one outlet 88 disposed in the housing 72.
- the outlet 88 is configured to discharge an expanded exhaust stream 90, in some embodiments.
- the expanded exhaust stream 90 is generally similar to the expanded exhaust stream 34 of FIGs.
- the gas stream 86 includes carbon dioxide and having a specific moisture content.
- the gas stream 86 further includes one more of nitrogen, heavy hydrocarbons, or water vapor.
- the gas stream 86 further includes impurities, example of which include, but are not limited to, hydrogen sulfide.
- the gas stream 86 is substantially free of the impurities.
- the gas stream 86 includes nitrogen and carbon dioxide.
- the amount of impurities in the gas stream 86 is less than about 50 mole percent. In some embodiments, the amount of impurities in the gas stream 86 is less than about 20 mole percent. In some embodiments, the amount of impurities in the gas stream 86 is in a range from about 10 mole percent to about 20 mole percent. In some embodiments, the amount of impurities in the gas stream 86 is less than about 5 mole percent.
- the gas stream 86 expands in the multi-phase turbo expander 70 and as the work is extracted from the expanding gas stream, the gas stream 86 is cooled inside the multi-phase turbo expander 70. Cooling the gas stream 86 in the multi-phase turbo expander 70 results in formation of a CH 4 vapor, LNG, and one or both of solid CO 2 and liquid CO 2 in the multi-phase turbo expander 70. More specifically, the multi-phase turbo expander 70 is configured to cool the gas stream 86 such that the gas stream 86 primarily forms a vapor stream comprised substantially of CH 4 and a liquid natural gas/ice/solid CO 2 slurry stream, generally similar to streams 40 and 42 of FIGs. 1 and 2.
- the term “primarily forms” as used herein means that the amount of solid CO 2 formed in the multi-phase turbo expander is less than about 5 mass percent. In an embodiment, the term “primarily forms” as used herein means that the amount of LNG formed in the multi-phase turbo expander is less than about 45 mass percent. In an embodiment, the term “primarily forms” as used herein means that the amount of CH 4 vapor formed in the multi-phase turbo expander is less than about 50 mass percent.
- a flow field within the multi-phase turbo expander 70 may be utilized to aid in separation of the LNG/ice/ solid CO 2 slurry and the CH 4 vapor. This may be accomplished by incorporating one or more separation channels (not shown) into the multi-phase turbo expander housing 72 and additional outlets.
- the separation channels may be designed such that the liquid or solid particles enter due to centrifugal force and may be precluded from re-entering the multi-phase turbo expander flow path by a deflector.
- Example configurations for the inclusion of certain aspects of the multi-phase turbo expander 70, such as multiple outlets, separation channels, and the like, are described in commonly assigned, U.S. Publication No. 2013/0125580, D. Hofer, "Expander and Method of C0 2 Separation", which is incorporated by reference herein in its entirety.
- At least one component of the multi-phase turbo expander is selected from the multi-phase turbo expander
- the 70 further includes a coating configured to preclude adhesion of solid CO 2 to a surface of the multi-phase turbo expander component.
- one or more of the housing 72, the rotating component 74, or the stationary component 76 may include a coating configured to preclude adhesion of solid CO 2 to a surface of the multi-phase turbo expander component.
- the rotating component 74 in the multi-phase turbo expander 70 includes a coating 92.
- the coating 92 is configured to preclude adhesion of solid CO 2 to a surface 94 of the rotating component 74.
- the coating 92 includes a non-stick material capable of precluding adhesion of solid CO 2 to the surface 94 of the rotating component 74.
- the multi-phase turbo expander 70 further includes at least one heated component.
- the heated component is configured to preclude adhesion of solid CO 2 to a surface of the multi-phase turbo expander component.
- one or more of the housing 72, the rotating component 74, or the stationary component 76 may include a heated component to preclude adhesion of solid CO 2 to a surface of the multi-phase turbo expander component.
- a stationary component 76 in the multi-phase turbo expander 70 is heated to preclude adhesion of solid CO2 to a surface 96 of the stationary component 76.
- one or more of the stationary blades 80 may be heated by using electrical heating elements.
- the blade 80 may include heated elements (not shown) disposed in one or more holes formed in the blade 80.
- one or more components of the multi-phase turbo expander 70 may be heated by circulating air or gas.
- the blade 80 in some embodiments may further include gas flow channels (not shown), such as, for example, Z-shaped channels.
- the gas flow channels may have any suitable shape, such as, for example, U-shape, E-shape, and the like.
- example configurations for the inclusion of certain aspects of the multiphase turbo expander 70 including the use of electrical heating elements, circulating air or gas to heat the blades, gas flow channels, and the like, are described in commonly assigned, U.S.
- the multi-phase turbo expander configuration in accordance with some embodiments of the disclosure may advantageously allow for separation of a CH 4 vapor stream and a liquid natural gas/ice/solid CO 2 slurry stream from the gas stream within the multi-phase turbo expander itself, thus precluding the need for an additional separator, such as separator 38 of FIGs. 1 and 2.
- the multi-phase turbo expander 70 further includes the at least one outlet 88 configured to discharge the expanded exhaust stream 90 comprised of the CH 4 vapor, and the LNG/ice/solid CO2 slurry.
- the at least one outlet 88 is disposed downstream of the rotating component 74.
- the expanded exhaust stream 90 may include one or more non-condensable components.
- the expanded exhaust stream 90 may include one or more liquid components.
- the expanded exhaust stream 90 may include one or more solid components.
- the expanded exhaust stream 90 may be further configured to be in fluid communication with one or both of a liquid-gas and a solid-gas separator, such as separators 38 and 50 disclosed in FIGs. 1 and 2.
- the multi-phase turbo expander 70 for generating LNG from a gas stream 86 may include a single-stage multi-phase turbo expander, as illustrated in FIGs 3 and 4.
- the multi-phase turbo expander 70 for generating LNG from a gas stream 86 may include a multi-stage multi-phase turbo expander 70, as described in commonly assigned, U.S. Publication No. 2013/0125580, D. Hofer, "Expander and Method of CO 2 Separation", incorporated by reference herein in its entirety.
- a method 600 for generating LNG from a gas stream includes processing an input gas stream in a cooling stage, compression stage, expansion stage and separation stage. More specifically, the method includes the input of a gas stream, and more particularly a natural gas stream, in a step 602. The method further includes compressing the input gas stream in a compression stage, in a step 604. The compressed gas stream is next expanded, in a step 606, in a multi-phase turbo expander in an expansion stage. The expansion stage produces energy and an expanded exhaust stream comprised of a mixture of cold CH 4 vapor and a LNG/ice/solid CO 2 slurry.
- the expanded exhaust stream is separated in a separator into components, and more specifically, into an output cold CH 4 vapor stream and a LNG/ice/CC ⁇ slurry stream.
- the CH 4 vapor stream is recirculated, in a step 610, to the input gas stream, to pre-cool the gas stream prior to compression and expansion.
- the LNG/ice/solid CO 2 slurry stream is further separated in a separator to discharge, in a step 612, a liquid natural gas stream and a solid CO 2 stream.
- graph 700 illustrates compression ratios (plotted in axis 702) with energy requirements per gallon of LNG output stream (plotted in axis 704) of a novel liquid natural gas (LNG) production system, in accordance with an embodiment described herein.
- the energy requirements per gallon of LNG output stream (shown by plotted points/line 706), illustrates as the compression ration increases, the energy requirement decreases until it reaches a steady level, near 706, at compression ratios above approximately 30 psi.
- illustrated in FIG. 6 is that normalized by the amount of LNG produced, process energy requirements decrease as the compression ratio increases and then level off at approximately 0.8 kWh/gallon at compression ratio of ⁇ 30.
- a novel method and system for the production of liquid natural gas that integrates natural gas (NG) cleanup and refrigeration steps to produce the LNG in one process step by utilizing a multi-phase turbo expander.
- the method and system include the multi-phase turbo expander capable of operation with multi-phase flows (gas, liquids, and solids) and wherein a mixture of a cold CH 4 vapor and a LNG/ice/solid CO 2 slurry are discharged.
- the resulting system and method provide lower equipment cost, smaller footprint, increased LNG production and lower overall cost than conventional LNG production processes.
Abstract
Description
Claims
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JP2016531782A JP2016532846A (en) | 2013-07-31 | 2014-07-28 | System and embedded process for liquefied natural gas production |
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JP2009542881A (en) * | 2006-07-13 | 2009-12-03 | シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ | Method and apparatus for liquefying hydrocarbon streams |
CN201348420Y (en) * | 2008-10-21 | 2009-11-18 | 杭州杭氧股份有限公司 | Device capable of producing liquid nitrogen by utilizing cold energy of liquefied natural gas |
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MY155298A (en) * | 2008-12-22 | 2015-09-30 | Twister Bv | Method of removing carbon dioxide from a fluid stream and separation assembly |
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US20120006055A1 (en) * | 2009-01-08 | 2012-01-12 | Helmar Van Santen | Process and apparatus for separating a gaseous product from a feed stream comprising contaminants |
EP2255864A1 (en) * | 2009-05-26 | 2010-12-01 | Shell Internationale Research Maatschappij B.V. | Process for removing gaseous contaminants from a feed stream |
EP2255863A1 (en) * | 2009-05-26 | 2010-12-01 | Shell Internationale Research Maatschappij B.V. | Process for removing gaseous contaminants from a liquid phase containing feed stream |
JP5643491B2 (en) * | 2009-07-24 | 2014-12-17 | 大陽日酸株式会社 | Air liquefaction separation method and apparatus |
US20130125580A1 (en) * | 2011-11-22 | 2013-05-23 | General Electric Company | Expander and method for co2 separation |
EP2789956A1 (en) * | 2013-04-11 | 2014-10-15 | Shell Internationale Research Maatschappij B.V. | Method of liquefying a contaminated hydrocarbon-containing gas stream |
-
2013
- 2013-07-31 US US13/955,223 patent/US20150033792A1/en not_active Abandoned
-
2014
- 2014-07-28 KR KR1020167005348A patent/KR20160038030A/en not_active Application Discontinuation
- 2014-07-28 CA CA2919120A patent/CA2919120A1/en not_active Abandoned
- 2014-07-28 CN CN201480043001.2A patent/CN105408713B/en not_active Expired - Fee Related
- 2014-07-28 MX MX2016001461A patent/MX2016001461A/en unknown
- 2014-07-28 JP JP2016531782A patent/JP2016532846A/en active Pending
- 2014-07-28 EP EP14750129.0A patent/EP3027987A2/en not_active Withdrawn
- 2014-07-28 AU AU2014296514A patent/AU2014296514B2/en not_active Ceased
- 2014-07-28 WO PCT/US2014/048339 patent/WO2015017293A2/en active Application Filing
- 2014-07-28 MY MYPI2015704730A patent/MY174100A/en unknown
-
2019
- 2019-07-03 JP JP2019124539A patent/JP2020003203A/en active Pending
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107300294A (en) * | 2017-08-04 | 2017-10-27 | 中国华能集团清洁能源技术研究院有限公司 | A kind of co 2 liquefaction device and method of flue gas carbon trapping system |
CN112303769A (en) * | 2020-11-16 | 2021-02-02 | 安瑞科(蚌埠)压缩机有限公司 | LNG cold energy recycling and storing device |
Also Published As
Publication number | Publication date |
---|---|
JP2020003203A (en) | 2020-01-09 |
AU2014296514A1 (en) | 2016-02-18 |
EP3027987A2 (en) | 2016-06-08 |
CA2919120A1 (en) | 2015-02-05 |
KR20160038030A (en) | 2016-04-06 |
MX2016001461A (en) | 2016-06-02 |
MY174100A (en) | 2020-03-10 |
CN105408713B (en) | 2018-06-26 |
US20150033792A1 (en) | 2015-02-05 |
JP2016532846A (en) | 2016-10-20 |
AU2014296514B2 (en) | 2018-07-19 |
WO2015017293A3 (en) | 2015-08-27 |
CN105408713A (en) | 2016-03-16 |
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