EP3371535A1 - Systems and methods for lng refrigeration and liquefaction - Google Patents
Systems and methods for lng refrigeration and liquefactionInfo
- Publication number
- EP3371535A1 EP3371535A1 EP16863141.4A EP16863141A EP3371535A1 EP 3371535 A1 EP3371535 A1 EP 3371535A1 EP 16863141 A EP16863141 A EP 16863141A EP 3371535 A1 EP3371535 A1 EP 3371535A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- lng
- working fluid
- refrigerant
- stream
- waste heat
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 238000000034 method Methods 0.000 title claims description 35
- 238000005057 refrigeration Methods 0.000 title abstract description 19
- 239000003507 refrigerant Substances 0.000 claims abstract description 107
- 239000012530 fluid Substances 0.000 claims abstract description 69
- 239000002918 waste heat Substances 0.000 claims abstract description 56
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000003345 natural gas Substances 0.000 claims abstract description 17
- 230000006835 compression Effects 0.000 claims abstract description 16
- 238000007906 compression Methods 0.000 claims abstract description 16
- 239000003949 liquefied natural gas Substances 0.000 claims description 131
- 239000007789 gas Substances 0.000 claims description 33
- 229930195733 hydrocarbon Natural products 0.000 claims description 32
- 150000002430 hydrocarbons Chemical class 0.000 claims description 32
- 239000004215 Carbon black (E152) Substances 0.000 claims description 31
- 238000011084 recovery Methods 0.000 claims description 28
- 239000007788 liquid Substances 0.000 claims description 14
- 239000002737 fuel gas Substances 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 6
- 230000004044 response Effects 0.000 claims description 6
- 239000013589 supplement Substances 0.000 claims description 2
- 230000031070 response to heat Effects 0.000 claims 1
- 230000008016 vaporization Effects 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 230000008569 process Effects 0.000 description 8
- 239000002131 composite material Substances 0.000 description 6
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000003993 interaction Effects 0.000 description 4
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000010248 power generation Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000001282 iso-butane Substances 0.000 description 2
- 235000013847 iso-butane Nutrition 0.000 description 2
- 230000000153 supplemental effect Effects 0.000 description 2
- 229910001868 water Inorganic materials 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 235000013844 butane Nutrition 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000005553 drilling Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000005755 formation reaction Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical class CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000011555 saturated liquid Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0204—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
-
- 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
- F25J1/0235—Heat exchange integration
- F25J1/0242—Waste heat recovery, e.g. from heat of compression
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
- F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
- F25J1/025—Details related to the refrigerant production or treatment, e.g. make-up supply from feed gas itself
-
- 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.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
-
- 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.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0283—Gas turbine as the prime mechanical driver
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/70—Steam turbine, e.g. used in a Rankine cycle
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/80—Hot exhaust gas turbine combustion engine
- F25J2240/82—Hot exhaust gas turbine combustion engine with waste heat recovery, e.g. in a combined cycle, i.e. for generating steam used in a Rankine cycle
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
Definitions
- Hydrocarbon drilling and production systems can include the extraction of natural gas from wellbores in subterranean earthen formations.
- the natural gas can be liquefied.
- the liquefaction process includes condensing the natural gas into a liquid by cooling, or refrigeration.
- the liquefied natural gas (LNG) can then be moved and stored more efficiently.
- the natural gas Prior to condensing, the natural gas can be treated or processed to remove certain components such as water, dust, helium, mercury, acid gases such as hydrogen sulfide and carbon dioxide, heavy hydrocarbons, and other components.
- Liquefaction of LNG requires significant quantities of thermal energy
- typical LNG liquefaction facilities employ internal or external refrigerant sources to liquefy LNG prior to storage and delivery.
- external refrigerant sources include a single mixed refrigerant (SMR) with different compositions of nitrogen, methane, ethane, mixed butanes and iso-pentane components.
- the LNG cryogenic heat exchangers may be configured as plate fin, printed circuit or spiral wound heat exchangers.
- LNG liquefaction also requires a reliable power supply to operate refrigerant compressors and pumps for delivery of liquefied LNG product.
- Some LNG liquefaction facilities use internal refrigerant sources. For example, boil off gas (BOG) generated from the LNG itself can be used as the internal refrigerant source.
- BOG boil off gas
- Figure 1 is an equipment and process flow diagram for an embodiment of a LNG liquefaction plant or system using an external refrigerant in accordance with principles disclosed herein;
- Figure 2 is a diagram showing the composite heat curves between LNG and an external refrigerant as a working fluid using a cold box;
- Figure 3 is a flow chart for an embodiment of a method of LNG liquefaction using an external refrigerant in accordance with principles disclosed herein;
- Figure 4 is an equipment and process flow diagram for another embodiment of a LNG liquefaction plant or system using an internal refrigerant in accordance with principles disclosed herein;
- Figure 5 is a diagram showing the composite heat curves between LNG and an internal refrigerant as a working fluid using a cold box.
- Figure 6 is a flow chart for an embodiment of a method of LNG liquefaction using an internal refrigerant in accordance with principles disclosed herein.
- a LNG liquefaction plant or system includes concurrent power production.
- the LNG liquefaction plant uses waste heat recovered from a refrigeration unit for concurrent power production.
- a hydrocarbon is used as a working fluid in a specially configured organic Rankine cycle (ORC).
- ORC organic Rankine cycle
- the LNG liquefaction plant includes closed cycle power production with an external refrigerant, such as a single mixed refrigerant (SMR), and a light hydrocarbon as a working fluid.
- SMR single mixed refrigerant
- a LNG liquefaction plant or system 100 includes a treatment system 101, a heat exchanger system 125, and a waste heat recovery system 165.
- a natural gas feed conduit 102 is coupled to an acid gas removal unit 104, which in turn is coupled to a conduit 106, a dehydration unit 108, a conduit 110, a heavy hydrocarbon removal unit 1 12, a condensate conduit 1 14, a conduit 116, and a conduit 1 18.
- the conduit 116 is coupled to a debutanizer-depentanizer 120, which also includes conduits 122, 124. It is understood that various combinations and arrangements of treatment units is contemplated beyond the exemplary configuration described above.
- the conduit 1 18 carries a treated gas stream to a cold box, or cryogenic exchanger, 126 of the heat exchanger system 125.
- the cold box 126 is coupled to a conduit 132, a conduit 134, a conduit 138, a conduit 140, and a conduit 148.
- the conduit 138 is coupled to a mixing device 130 which is coupled to a conduit 136 that couples back into the cold box 126.
- Conduits 144, 146 are coupled into the cold box 126 with a separator 128 coupled between the conduits 144, 146.
- the conduit 134 couples to a hydraulic turbine or expander 150.
- the turbine 150 is coupled to a conduit 154 and a storage tank 156, as well as a compressor 152.
- a conduit 142 couples between the compressor 152 and the cold box 126.
- the conduit 148 couples between the storage tank 156 and the cold box 126.
- a conduit 158 is coupled to the storage tank 156.
- the waste heat recovery system 165 is coupled to the heat exchanger system 125.
- the waste heat recovery system 165 includes a waste heat recovery unit 162.
- An air cooler 166 and a pump 170 are coupled to the waste heat recovery unit 162 via a series of conduits 164, 168, 172.
- a high pressure expander 178 is coupled into the waste heat recovery unit 162 via conduits 174, 180.
- the high pressure expander 178 may also be referred to as a turbo-expander.
- the high pressure expander 178 is operationally coupled to a refrigerant compressor 182 by a drive shaft 212.
- the system 100 includes multiple stages of refrigerant compression, and thus the compressor 182 may also be referred to as a first refrigerant compressor.
- a conduit 184 is coupled to the first refrigerant compressor 182 and to a second refrigerant compressor 188, and an air cooler 186 is coupled into the conduit 184.
- a conduit 190 is coupled to the second refrigerant compressor 188 and to a third refrigerant compressor 194, and an air cooler 192 is coupled into the conduit 190.
- a conduit 196 is coupled between the third refrigerant compressor 194 and an air cooler 198.
- a conduit 202 is coupled between the air cooler 198 and the separator 128.
- the second refrigerant compressor 188 is operationally coupled to the third refrigerant compressor 194 by a drive shaft 208, and the third refrigerant compressor 194 is operationally coupled to a compressor driver, or turbine or gas turbine, 200.
- the turbine 200 may also be referred to as an expander or turbo- expander.
- a conduit 206 is coupled to the turbine 200 and couples back into the waste heat recovery unit 162.
- a conduit 160 is coupled between the turbine 200 and the compressor 152.
- a conduit 204 also couples into the turbine 200.
- a natural gas feed stream is directed through the conduit 102.
- the feed rate is 150 MMscfd (from a pipeline or other source) and may be at a pressure of 900 psig and at a temperature of about 95°F, or alternatively about 70°F. It will be understood that various quantitative values are provided herein for illustrative purposes, are approximations of the quantities given, and are exemplary only.
- the feed gas is treated in the acid gas removal unit 104, the dehydration unit 108, and the heavy hydrocarbon removal unit 112 for removal of H 2 S, C0 2 , H 2 0, and C5+, which may be required to meet a LNG product specification and/or to avoid freeze-out in the cold box 126.
- the feed gas is also treated in the debutanizer- depentanizer 120 for the production of iso-butane and iso-pentane which can be used as makeup for the working fluid in the ORC power generation as described hereinbelow.
- a treated gas stream is directed through the conduit 118 and into the cold box 126 of the heat exchanger unit 125.
- the treated gas stream is at a pressure of 870 psig and a temperature of 95°F.
- a refrigerant is directed from the third refrigerant compressor 194 and its discharge stream in the conduit 202 to the separator 128 where the stream is split into a liquid stream in the conduit 146 and a vapor stream in the conduit 144.
- the refrigerant working fluid is a single mixed refrigerant (SMR).
- SMR single mixed refrigerant
- the particular composition of the working fluid is generally determined by the specific composition of the feed gas, the LNG product, and the desired liquefaction cycle pressures. It may also be desirable to vary the working fluid compositions and/or cycle operating pressures as necessary to maximize liquefaction.
- the refrigerant streams 144, 146 are used for liquefaction and sub-cooling of LNG in the cold box 126.
- the liquid stream 146 and the vapor stream 144 are directed to the cold box 126 in their respective exchanger stages to facilitate LNG liquefaction and to thereby produce cooled liquid streams in the conduits 138, 140.
- the cooled liquid streams 138, 140 are directed through the mixing device 130 and expanded. In some embodiments, the cooled liquid streams are expanded to 32 psig.
- the expanded liquid streams are directed to the next heat exchange stage via the conduit 136 back into the cold box 126 and the conduit 132 from the cold box 126 to recycle the stream back to the first refrigerant compressor 182.
- the LNG stream 134 is at a pressure of 850 psig and -245°F from the cold box 126 and is expanded across the hydraulic turbine 150 to produce a LNG product stream in the conduit 154.
- the LNG product stream 154 is brought to nearly atmospheric pressure (>1.0 psig) and further sub-cooled to - 258°F and stored in the storage tank 156 for LNG export in the conduit 158.
- the refrigeration content of the refrigerant or SMR can be used in the LNG facility by using the refrigerant or SMR as a working fluid, wherein the refrigerant or SMR is compressed, cooled, expanded in a mixing device, and sub-cooled in multiple heat exchange stages in the cold box 126 (e.g., heat exchange stages of 144 to 140, 146 to 138, 138/140 to 136, 136 to 132, and 148 to 142).
- the waste heat recovery system 165 includes the ORC wherein the working fluid is, in an exemplary embodiment, a high pressure hydrocarbon liquid in the conduit 172 that is pressurized by the pump 170.
- the high pressure hydrocarbon liquid flows at a rate of 1 ,350 gpm, a temperature of 98°F, and a pressure of 580 psia.
- the high pressure hydrocarbon liquid is vaporized and superheated in the waste heat recovery unit 162 by heat from a turbine exhaust stream in the conduit 206.
- the high pressure hydrocarbon liquid is superheated to about 650°F to form a vapor stream in the conduit 174 exiting the waste heat recovery unit 162.
- the vapor stream is expanded across the high pressure expander 178.
- the vapor stream is expanded to about 12 psig, or about 25 psia.
- the high pressure expander 178 is coupled by the drive shaft 212 to provide operational power to the first refrigerant compressor 182.
- the expanded vapor stream in the conduit 180 is at about 530°F.
- the expanded vapor stream is delivered to the waste heat recovery unit 162 where it is cooled.
- the expanded vapor stream is cooled to about 180°F to form a cooled vapor stream in the conduit 164.
- the cooled vapor stream is then condensed in the air cooler 166 to form a saturated liquid stream in the conduit 168 that can be pumped by the pump 170 to recycle the hydrocarbon working fluid in a closed loop cycle.
- the waste heat recovery system 165 includes a closed loop hydrocarbon working fluid cycle.
- the hydrocarbon working fluid is cooled in the waste heat recovery unit 162 and condensed in the air cooler 166.
- the hydrocarbon working fluid is then pumped into the waste heat recovery stage including the gas turbine exhaust 206.
- the waste heat recovery system 165 is configured to use the gas turbine exhaust 206 to vaporize and superheat the high pressure hydrocarbon working fluid prior to sending it to the expander 178.
- the waste heat recovery working fluid may include other fluids.
- the working fluid may be a hydrocarbon or a non-hydrocarbon, provided the boiling temperature is suitable for condensation at the ambient temperature at the liquefaction site.
- a lighter hydrocarbon such as isobutane may be used.
- a heavier hydrocarbon such as isopentane may be used.
- the working fluid can be changed or adjusted depending on the temperature at the same liquefaction site. For example, a lighter hydrocarbon can be used during winter operation, while the lighter hydrocarbon can be replaced with a heavier hydrocarbon in the summer.
- the change in waste heat recovery working fluid can maximize power output from the waste heat ORC, thereby increasing overall energy efficiency.
- a waste heat working fluid hydrocarbon can be extracted from the feed section of the LNG plant in a fractionation column.
- components of the waste heat recovery working fluid can be extracted from the feed from the heavy hydrocarbon removal unit 1 12.
- a C5+ stream is directed from the heavy hydrocarbon removal unit 112 by the conduit 116 to the debutanizer-depentanizer 120, and then by the conduits 122, 124 to the working fluid stream in the conduit 174 of the waste heat recovery ORC loop.
- the expanded refrigerant stream in the conduit 132 is directed into the first refrigerant compressor 182 for first stage compression.
- the compressed refrigerant stream in the conduit 184 is cooled by the air cooler 186 and directed into the second refrigerant compressor 188 for second stage compression.
- the compressed refrigerant stream in the conduit 190 is cooled by the air cooler 192 and directed into the third refrigerant compressor 194 for third stage compression.
- the compressed refrigerant stream in the conduit 196 is cooled by the air cooler 198 and directed into the conduit 202 and toward the separator 128 for use by the heat exchange system 125.
- the SMR vapor stream from the multi-stage compressor assembly 182, 188, 194 is cooled to ambient temperature by the air coolers 186, 192, 198.
- the gas turbine, or turbo-expander, 200 is used to drive the compressors 188, 194 via the drive shafts 208, 210.
- the conduit 206 carries waste heat in the form of turbine exhaust from the gas turbine 200 to the waste heat recovery unit 162 to provide heat to the closed loop ORC of the waste heat recovery system 165 that in turn drives the high pressure expander 178 and the first refrigerant compressor 182 as described above.
- the turbine exhaust can then exit the waste heat recovery unit 162 via the conduit 176.
- a fuel gas stream in the conduit 160 must be provided.
- the refrigeration content of a LNG boil off gas stream on the conduit 148 from the storage tank 156 is used to optimize the liquefaction of LNG in the cold box 126.
- the stream is carried in the conduit 142 to the compressor 152 where it is compressed and then directed to the gas turbine 200 in the conduit 160 as the fuel gas stream.
- the hydraulic turbine 150 powers the compressor 152.
- supplemental power for the compressor 152 can be provided by an electric motor 214.
- power required for the compressor 152 can be supplied from the power generation of the closed loop ORC.
- the high pressure hydrocarbon vapor stream in the conduit 174 can be coupled to the hydraulic turbine 150 (not shown) for power.
- a refrigeration and liquefaction plant system including concurrent power production.
- the refrigeration content of LNG is also employed as a heat sink in LNG liquefaction.
- vaporized LNG from LNG tanks and ships may be coupled with LNG liquefaction, where a refrigeration source, i.e., the SMR as described above, is compressed, cooled, expanded and recompressed via the twin turbo-expander compressor assembly (e.g., the expanders 178, 200 and the compressors 182, 188, 194) and the cold box 126 in a closed loop cycle.
- Recovered waste heat from the turbo-expander 200 exhaust stream is used to vaporize the hydrocarbon working fluid in the waste heat recovery unit 162.
- the hydrocarbon working fluid is then expanded through the turbo-expander 178, condensed, and recycled back in a closed loop ORC.
- the ORC driven turbo- expander 178 in turn drives the first stage refrigerant compressor 182, thereby increasing energy efficiency. Consequently, in some embodiments, power typically provided from an external power grid can be reduced by the amount of internally produced power. With such a reduction in net power consumption, LNG liquefaction can be achieved while reducing undesirable amounts of waste streams, emissions, and greenhouse gases.
- the systems and processes described herein are implemented in new LNG liquefaction plant systems, while in other embodiments the systems and processes are used to retrofit existing LNG liquefaction plant systems.
- the systems and processes described herein can address or eliminate the need to install emission reduction or control devices, such as a selective catalytic reduction (SCR) device, on the turbine exhaust 206.
- SCR selective catalytic reduction
- a graph 500 shows a composite heat curve 502 for the SMR refrigerant working fluid and a composite heat curve 504 for the LNG, using heat flow (kcal/h) as a function of temperature (°C).
- the systems described above can be used for various methods of liquefying and sub- cooling LNG.
- a method 400 includes providing a natural gas stream 402 and providing a compressed and cooled refrigerant stream 404.
- the method 400 includes using the compressed and cooled refrigerant stream as a working fluid for heat exchange 406, such as, for example, in the multiple stages of heat exchange in and adjacent the cold box or cryogenic exchanger 126.
- the method 400 includes using the refrigerant heat exchange to liquefy the natural gas into LNG 408.
- a gas stream, such as the LNG vapor or boil off gas, is directed from the LNG stream 410 and used for heat exchange 412. Such heat exchange can also be used for the LNG liquefaction step 408.
- the method 400 also includes producing an expanded refrigerant stream in response to the heat exchange 414.
- the method 400 includes compressing the expanded refrigerant stream into a compressed and cooled refrigerant stream 416, which can then feed into the providing the refrigerant stream at step 404.
- waste heat is produced at step 418, such as, for example, the turbine exhaust in the conduit 206.
- the method 400 includes providing waste heat to a waste heat working fluid for waste heat exchange 420, such as, for example, by using the waste heat recovery unit 162.
- the waste heat exchange can then be used to drive compression of the expanded refrigerant stream 422, such as, for example, by sending the waste heat working fluid through the expander 178 to drive the compressor 182.
- Driving compression 422 then feeds back into the refrigerant compression step 416.
- the method 400 includes storing LNG 424. It is noted that the steps above can be performed in varying orders and portions of the method can be performed apart from other portions as desired. For example, using the refrigerant as a working fluid for heat exchange can be performed regardless of using a LNG vapor stream for liquefaction or using waste heat in the system to heat a working fluid and drive compression, and vice versa.
- a LNG liquefaction plant or system includes concurrent power production where the working fluid for the cold box is an internal refrigerant, such as a LNG vapor or boil off gas.
- a LNG liquefaction plant or system 300 includes a treatment system 101, a heat exchanger system 325, and a waste heat recovery system 165.
- the treatment system 101 and waste heat recovery system 165 are similar to the corresponding systems in the LNG liquefaction system 100 described above. Therefore, most details of these systems will not be repeated except as needed to illuminate new or modified portions of the system 300 such as the heat exchanger system 325.
- the heat exchanger system 325 includes a cold box or cryogenic exchanger 302 fed a natural gas stream by a conduit 301.
- the natural gas stream can be treated as described above with reference to the treatment system 101.
- the treated gas stream in the conduit 301 is at a pressure of 1090 psig and a temperature of 85°F.
- the treated gas stream is liquefied and sub-cooled in the cold box 302 to produce a LNG stream in a conduit 334.
- the LNG stream is a pressure of 1085 psig and a temperature of -243 °F.
- the LNG stream is directed to an expander or hydraulic turbine 312 to produce an expanded LNG stream in a conduit 338.
- the LNG stream is expanded to about atmospheric pressure (>1.0 psig), and in further embodiments is sub-cooled to -258°F and stored in a storage tank 350 for LNG export in a conduit 354.
- a compressor discharge stream with compressed and cooled refrigerant flows in a conduit 320 to the cold box 302 for liquefaction and sub-cooling of LNG.
- the refrigerant stream flows through a conduit 322 and is split between conduits 324 and 326.
- the refrigerant stream is split at a ratio of 3 :1 for the conduit 324 as compared to the conduit 326 (324:326).
- a first stream portion in the conduit 324 is directed to an expander 306 which in turn drives a compressor 304.
- the combination of 306, 304 may also be referred to as an expander-compressor or compander.
- the second stream portion in the conduit 326 is directed back through and out of the cold box 302 in a conduit 328 to an expander 308 which drives a compressor 310 (i.e., expander-compressor or compander 308/310). It is noted that, unlike the first stream portion 324, the second stream portion 326 is fed to the cold box 302 to thereby produce the stream 328 which is fed to the expander 308. Consequently, a first expanded stream, or low pressure working fluid vapor, flows from the expander 306 in a conduit 330 and a second expanded stream, or low pressure working fluid vapor, flows from the expander 308 in a conduit 340, both to the cold box 302.
- a first expanded stream, or low pressure working fluid vapor flows from the expander 306 in a conduit 330 and a second expanded stream, or low pressure working fluid vapor, flows from the expander 308 in a conduit 340, both to the cold box 302.
- the first and second expanded streams are at temperatures of about -245 °F, and are used in respective heat exchange stages to facilitate LNG liquefaction in the cold box 302.
- the arrangement described can also be referred to as a twin expander-compressor or twin compander assembly, used for compression of the internal refrigerant or working fluid derived from the LNG. While a two stage compander arrangement is shown, additional stages are also contemplated.
- the refrigeration content of the second expanded stream in the conduit 340 is used for liquefaction in the cold box 302 to thereby produce a second warm LNG vapor or boil off gas stream in a conduit 342 (or, a warm intermediate stage working fluid vapor).
- the LNG vapor stream is then compressed in the compressor 310 to produce a compressed stream in a conduit 344, which is further compressed in the compressor 304 to produce a compressed stream in a conduit 346 that is recycled back to the first stage refrigerant compressor 182.
- Conduits 344, 346 can also include air coolers 316, 318 to further cool the compressed refrigerant streams.
- the refrigeration content of the first expanded stream in the conduit 330 is used for liquefaction in the cold box 302 to thereby produce a first warm LNG vapor or boil off gas stream in a conduit 332 (or, a warm intermediate stage working fluid vapor) that is recycled back to the second stage refrigerant compressor 188.
- the warm LNG vapor or boil off gas stream is the working fluid and provides refrigeration content in the cold box 302 for liquefaction.
- the first expanded stream in the conduit 330 is at a pressure of about 380 psia
- the second expanded stream in the conduit 340 is at a pressure of about 35 psia.
- a LNG vapor or boil off gas stream is directed from the storage tank 350 in a conduit 352, and the LNG vapor stream includes refrigeration content.
- the refrigeration content of the LNG vapor stream 352 can be used to supplement or optimize liquefaction of LNG in the cold box 302, prior to sending it as a fuel gas stream in a conduit 336 to the turbine 200.
- the LNG vapor stream 352 is directed through the cold box 302 and out of the cold box 302 in a conduit 348.
- the conduit 348 directs the LNG vapor stream to a compressor 314 that is coupled to and driven by the LNG expander 312.
- the compressed fuel gas stream is directed in the conduit 336 to the turbine 200 for power.
- supplemental power for the compressor 314 can be provided by an electric motor 356.
- additional power is required for the compressor 314, such power can be supplied from the power generation from the ORC (not shown).
- the refrigeration content of LNG is employed in a LNG plant system by using the LNG as a working fluid in a multi-stage Rankine liquefaction cycle configuration, wherein the LNG vapor or boil off gas is compressed, cooled, expanded in a twin compander configuration and sub-cooled in multiple heat exchange states, wherein each of the exchange stages receives expanded working fluid vapors from respective turbines or turbine stages.
- two Rankine cycles are fluidicly coupled to the LNG liquefaction plant system, including two, three, or more expansion stages.
- the refrigeration content of both the LNG and the internally derived LNG refrigerant working fluid are used for LNG liquefaction in various embodiments described herein.
- a graph 600 shows a composite heat curve 602 for the internal refrigerant working fluid and a composite heat curve 604 for the LNG, using heat flow (kcal/h) as a function of temperature (°C).
- the internal refrigerant working fluid compositions and condensation temperatures are also dependent on the operating pressures. As described herein, multiple stages, e.g., more than two stages, of compression will further narrow the temperature gaps between the internal refrigerant working fluid and LNG, reducing loss work and increasing liquefaction efficiency.
- the method 450 includes expanding a first refrigerant portion 454, using the expanded first refrigerant stream portion as a working fluid for heat exchange 456, producing a first LNG vapor stream in response to the heat exchange 458, and compressing the first LNG vapor stream with a refrigerant compressor, such as, for example, using the stream 332 directed into the second stage refrigerant compressor 188.
- a refrigerant compressor such as, for example, using the stream 332 directed into the second stage refrigerant compressor 188.
- the method 450 also includes using a second refrigerant stream portion as a working fluid for heat exchange 462, expanding the second refrigerant portion 464, using the expanded second refrigerant stream portion as a working fluid for heat exchange 466, producing a second LNG vapor stream in response to the heat exchange 468, compressing the second LNG vapor stream with a LNG vapor compressor (such as, for example, with the compressors 304, 310 that are part of the heat exchanger system 325), and compressing the second LNG vapor stream with a refrigerant compressor (such as, for example, the first stage refrigerant compressor 182).
- a LNG vapor compressor such as, for example, with the compressors 304, 310 that are part of the heat exchanger system 325
- a refrigerant compressor such as, for example, the first stage refrigerant compressor 182
- LNG can be produced at a rate of 1.0 MTA.
Landscapes
- 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)
- Combustion & Propulsion (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Claims
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US201562252247P | 2015-11-06 | 2015-11-06 | |
US201562251808P | 2015-11-06 | 2015-11-06 | |
PCT/US2016/060756 WO2017079711A1 (en) | 2015-11-06 | 2016-11-06 | Systems and methods for lng refrigeration and liquefaction |
Publications (2)
Publication Number | Publication Date |
---|---|
EP3371535A1 true EP3371535A1 (en) | 2018-09-12 |
EP3371535A4 EP3371535A4 (en) | 2019-10-30 |
Family
ID=63077600
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP16863141.4A Withdrawn EP3371535A4 (en) | 2015-11-06 | 2016-11-06 | Systems and methods for lng refrigeration and liquefaction |
Country Status (1)
Country | Link |
---|---|
EP (1) | EP3371535A4 (en) |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2714722B1 (en) * | 1993-12-30 | 1997-11-21 | Inst Francais Du Petrole | Method and apparatus for liquefying a natural gas. |
IL157887A (en) * | 2003-09-11 | 2006-08-01 | Ormat Ind Ltd | Method and apparatus for augmenting the pressure head of gas flowing in a pipeline |
WO2009153143A1 (en) * | 2008-05-29 | 2009-12-23 | Shell Internationale Research Maatschappij B.V. | Method of operating a compressor using concentrated solar power and an apparatus therefor |
WO2010063789A2 (en) * | 2008-12-04 | 2010-06-10 | Shell Internationale Research Maatschappij B.V. | Method of cooling a hydrocarbon stream and an apparatus therefor |
WO2013184068A1 (en) * | 2012-06-06 | 2013-12-12 | Keppel Offshore & Marine Technology Centre Pte Ltd | System and process for natural gas liquefaction |
US20140260251A1 (en) * | 2013-03-13 | 2014-09-18 | Apache Corporation | Combined Heat and Power Technology for Natural Gas Liquefaction Plants |
CN104266454A (en) * | 2014-09-05 | 2015-01-07 | 西安交通大学 | Liquefied natural gas production system with gas-supercritical carbon dioxide united power |
-
2016
- 2016-11-06 EP EP16863141.4A patent/EP3371535A4/en not_active Withdrawn
Also Published As
Publication number | Publication date |
---|---|
EP3371535A4 (en) | 2019-10-30 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US20190204006A1 (en) | Systems and Methods for LNG Refrigeration and Liquefaction | |
JP5139292B2 (en) | Natural gas liquefaction method for LNG | |
JP5006515B2 (en) | Improved drive and compressor system for natural gas liquefaction | |
US10077937B2 (en) | Method to produce LNG | |
EP3368631B1 (en) | Method using hydrogen-neon mixture refrigeration cycle for large-scale hydrogen cooling and liquefaction | |
MX2013014870A (en) | Process for liquefaction of natural gas. | |
WO2009029140A1 (en) | Natural gas liquefaction process | |
JP2019526770A (en) | Process for liquefying natural gas and recovering any liquid from natural gas, comprising two semi-open refrigerant cycles using natural gas and one closed refrigerant cycle using gas refrigerant | |
AU2008203713B2 (en) | Method and apparatus for liquefying a hydrocarbon stream | |
US11815308B2 (en) | Pretreatment and pre-cooling of natural gas by high pressure compression and expansion | |
CN100554837C (en) | Provide cooling to be used for the method for gas liquefaction | |
US20110308276A1 (en) | Method and system for periodic cooling, storing, and heating with multiple regenerators | |
US20180283773A1 (en) | Hydraulic Turbine Between Middle and Cold Bundles of Natural Gas Liquefaction Heat Exchanger | |
CA2941494A1 (en) | Refrigerant supply to a cooling facility | |
US11806639B2 (en) | Pretreatment and pre-cooling of natural gas by high pressure compression and expansion | |
EP3371535A1 (en) | Systems and methods for lng refrigeration and liquefaction | |
US10571187B2 (en) | Temperature controlled method to liquefy gas and a production plant using the method | |
Brennan et al. | Liquefaction and Separation of Gases | |
WO2022099233A1 (en) | Natural gas liquefaction methods and systems featuring feed compression, expansion and recycling | |
JP2023543655A (en) | Integration of heat recovery boiler and high pressure feed gas process for production of liquefied natural gas | |
AU2008294046B2 (en) | Natural gas liquefaction process |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE |
|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE |
|
17P | Request for examination filed |
Effective date: 20180531 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR |
|
AX | Request for extension of the european patent |
Extension state: BA ME |
|
DAV | Request for validation of the european patent (deleted) | ||
DAX | Request for extension of the european patent (deleted) | ||
RIC1 | Information provided on ipc code assigned before grant |
Ipc: F25J 3/02 20060101AFI20190507BHEP Ipc: F25J 1/02 20060101ALI20190507BHEP Ipc: F25J 1/00 20060101ALI20190507BHEP |
|
A4 | Supplementary search report drawn up and despatched |
Effective date: 20191001 |
|
RIC1 | Information provided on ipc code assigned before grant |
Ipc: F25J 1/02 20060101ALI20190925BHEP Ipc: F25J 1/00 20060101ALI20190925BHEP Ipc: F25J 3/02 20060101AFI20190925BHEP |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
|
18D | Application deemed to be withdrawn |
Effective date: 20210601 |