EP1118827A1 - Procédé de liquéfaction partielle d'un fluide contenant des hydrocarbures tel que du gaz naturel - Google Patents
Procédé de liquéfaction partielle d'un fluide contenant des hydrocarbures tel que du gaz naturel Download PDFInfo
- Publication number
- EP1118827A1 EP1118827A1 EP01400050A EP01400050A EP1118827A1 EP 1118827 A1 EP1118827 A1 EP 1118827A1 EP 01400050 A EP01400050 A EP 01400050A EP 01400050 A EP01400050 A EP 01400050A EP 1118827 A1 EP1118827 A1 EP 1118827A1
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- EP
- European Patent Office
- Prior art keywords
- fluid
- refrigeration
- natural gas
- stage
- line
- 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.)
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 238000000034 method Methods 0.000 title claims abstract description 61
- 239000003345 natural gas Substances 0.000 title claims abstract description 39
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 19
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 19
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 7
- 239000012530 fluid Substances 0.000 claims abstract description 87
- 238000005057 refrigeration Methods 0.000 claims abstract description 62
- 239000007789 gas Substances 0.000 claims abstract description 51
- 239000003507 refrigerant Substances 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 43
- 230000005611 electricity Effects 0.000 claims abstract description 8
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 34
- 238000005194 fractionation Methods 0.000 claims description 24
- 239000001294 propane Substances 0.000 claims description 17
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 15
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical class CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 13
- 238000001035 drying Methods 0.000 claims description 11
- 235000013844 butane Nutrition 0.000 claims description 10
- 230000003247 decreasing effect Effects 0.000 claims description 8
- 239000002826 coolant Substances 0.000 claims description 6
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 5
- 239000001273 butane Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 abstract description 54
- 238000001816 cooling Methods 0.000 abstract description 14
- 230000008016 vaporization Effects 0.000 abstract description 9
- 239000008246 gaseous mixture Substances 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract 1
- 238000010586 diagram Methods 0.000 description 15
- 239000003949 liquefied natural gas Substances 0.000 description 14
- 150000001875 compounds Chemical class 0.000 description 9
- 238000009834 vaporization Methods 0.000 description 8
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- 238000010992 reflux Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 4
- 239000005977 Ethylene Substances 0.000 description 4
- 238000007792 addition Methods 0.000 description 4
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 239000012808 vapor phase Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- -1 des pentanes Chemical class 0.000 description 2
- 239000001282 iso-butane Substances 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—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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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- 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
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- 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
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- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
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- 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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- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
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- F25J1/0212—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J1/0219—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
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- 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
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- F25J1/0231—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the working-up of the hydrocarbon feed, e.g. reinjection of heavier hydrocarbons into the liquefied gas
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- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—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.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/62—Ethane or ethylene
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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- 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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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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- 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
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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- 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
Definitions
- the present invention relates to a method and a device for at least partially liquefy a fluid or a gaseous mixture formed at less in part of a mixture of hydrocarbons, for example a natural gas.
- Natural gas is commonly produced at remote sites of use and it is common to liquefy it in order to transport it on long distances for example by LNG carrier or to store it under liquid form.
- natural gas we mean within the meaning of this description, a mixture formed mainly of methane, but which can also contain other hydrocarbons and nitrogen, whatever the state in which it is found (gas, liquid or two-phase).
- Natural gas in departure occurs mainly in the gaseous state, and at such a pressure, that during the liquefaction stage, it can be in different states, for example liquid and gaseous coexisting at a given time.
- the refrigerant mixture used in the second stage in which the second refrigeration stage is carried out is cooled by heat exchange with the ambient cooling medium, water or air, then the first stage in which the first refrigeration stage is carried out.
- the refrigerant mixture is in the form of a two-phase fluid comprising a vapor phase and a liquid phase. Said phases are separated, for example in a separating flask, and sent, for example, into a coiled exchanger, in which the vapor fraction is condensed, while the natural gas is liquefied under pressure, the refrigeration being ensured by vaporization of the fraction coolant mixture liquid.
- the liquid fraction obtained by condensation of the vapor fraction is sub-cooled, expanded and vaporized to ensure the final liquefaction of natural gas, which is sub-cooled before being expanded through a valve or a turbine to produce Liquefied Natural Gas (LNG) sought.
- LNG Liquefied Natural Gas
- the presence of a vapor phase requires a condensation operation on the refrigerant mixture at the second stage which requires a relatively complex and expensive device. It has moreover been described in US Pat. No. 4,195,979 the addition of a step of expansion of natural gas between the two cooling steps. It has also been proposed in the applicant's patent FR 2,743,140 to operate under selected pressure and temperature conditions in order to obtain at the outlet of the first refrigeration stage a fully condensed single-phase refrigerant mixture.
- Another arrangement according to the prior art consists in operating by means of three refrigeration cycles in series, each of which operates with a pure body as a refrigerant.
- a first cycle operating with propane makes it possible to condense ethylene under pressure at a temperature of approximately - 35 ° C.
- the vaporization of ethylene at a pressure close to atmospheric pressure in a second cycle makes it possible to condense methane under pressure at a temperature of approximately - 100 ° C.
- the present invention relates to a process for partial liquefaction of a fluid G or a gaseous mixture formed at least in part of hydrocarbons, such than natural gas GN, and its implementation device.
- the process of present invention at least partially overcomes the aforementioned drawbacks of prior art.
- At least part of the gaseous fraction representing at least 20 percent by weight relative to the weight of the fluid G initially introduced into said process can be used to produce electricity.
- At least part of the gaseous fraction representing at least 20 percent by weight relative to the weight of the fluid G initially introduced into said process can be reinjected into the zone to from which it is recovered and in particular in the case where the fluid G is a natural gas in the well from which it is recovered.
- the first refrigeration step comprises for example several zones heat exchange and refrigeration can be provided in said areas successive heat exchange using the external refrigerant M which is relaxed and vaporized at decreasing pressure levels.
- the fluid G leaves monophasic condensed of the first refrigeration stage.
- the fluid G leaves in dense phase from the first refrigeration stage.
- the external refrigerant M comprises at least one hydrocarbon and preferably at least two hydrocarbons. This or these hydrocarbons are preferably chosen from the group formed by methane, ethane, propane and butanes. According to a particular embodiment of the method of the invention the external refrigerant M comprises methane, ethane, propane and at least one butane
- the second step comprises for example a single exchange zone, in which the liquefied fluid G is sub-cooled.
- the liquefied gas is separated into two parts: one part being sent to storage after expansion, the other party being relaxed and returned to the same exchange zone to produce by vaporization the cold necessary for sub-cooling and possibly when the fluid G entering in said second stage is not completely liquid at the total liquefaction of said fluid G.
- the part of the fluid G used to produce the cold necessary for this second stage is vaporized at different decreasing pressure levels.
- a preferred option for the second step is as follows: at the end of the second step the liquefied gas is expanded to an intermediate pressure, between 0.3 and 1.2 MPa, using either a liquid turbine, or a Joule-Thomson valve.
- the fluid G is completely liquid at the end of this first expansion.
- the fluid G is then separated into two substantially equal parts: a part being sent usually after expansion to cryogenic storage, possibly after a denitrogenation step comprising a partial vaporization, the rest being returned, partly to the intermediate pressure and for the other part at a lower pressure towards step b) to produce by vaporization the cold necessary for sub-cooling, and possibly when the fluid G entering in said second step is not completely liquid to the total liquefaction of said fluid G.
- the operating conditions of the process according to the invention will preferably be chosen so that the quantity of liquefied gas obtained is from approximately 20 to approximately 80% by weight, more preferably from approximately 30% to approximately 70% by weight the amount of gas entering the process.
- the liquefied part of the fluid G circulating in the line (21) (designated above by the terms “The other part") is relaxed and partially vaporized in one stage until storage pressure.
- the liquefied part of the fluid G circulating in the line (18) (hereinafter referred to as "the other party") is relaxed and partially vaporized in two stages until storage pressure.
- the process liquefies about 50 percent (%) by weight of the gas entering, while 50% by weight leaves as of gas at a lower pressure than that at which it is at the inlet.
- the specific power per unit of gas liquefied is around 600 kilojoule per kilo (kJ / kg), which is much lower at the usual specific powers (around 1000 kJ / kg).
- This configuration could be applied when jointly with the liquefaction, we have a central electric powered for example using a natural gas turbine, the compressors used for liquefaction would then be driven by a small part of the electricity produced by the power plant.
- a unit of 300 megawatt (MW) could be associated with a liquefaction of 0.4 million tonnes per year, consuming about 8 MW.
- the method could also be associated with a scheme comprising gas reinjection as specified above.
- FIG. 3 illustrates how (without limitation) the gas pre-cooling (R) can be performed.
- the gas G must be almost completely liquefied at the end of this stage, which requires descending more low than with a propane cycle.
- a refrigerant mixture M is therefore used, mainly comprising ethane and propane, and lower quantity of methane and butanes.
- the gas G enters via line (10) into the pre-refrigeration section (R) of the gas, where it is cooled and liquefied successively in the exchange zones E10, E11, and E12, from which it leaves by lines (11), (12) and (13) respectively. In line (13), the fluid G is almost completely liquefied.
- the refrigerant mixture M is compressed by the compressor K10, from where it leaves via the conduit (100). It is condensed by the condenser C10, from where it exits at the bubble point through the conduit (101) to be partly sent to the exchange zone E10 where it is under cooled. he leaves the exchange zone E10 via the conduit (102) to be partly sent to exchange area E11. Another part of the refrigerant mixture M circulating in the line (102) is sampled and sent by the conduit (131) in valve V10 in which it is expanded and then reintroduced through the conduit (132) in the exchange zone E10 where this refrigerant mixture M is vaporized to produce the cold necessary for this area.
- the refrigerant mixture M leaving the exchange zone E11 is partly sent to the exchange zone E12 via the conduit (103).
- Another part of the refrigerant mixture M circulating in the line (103) is taken and sent through the conduit (121), into the valve V11 in which it is relaxed and then returned to the exchange zone E11 by the conduit (122) where it is vaporized to provide the cold necessary for this area.
- the mixture refrigerant leaves the exchange zone E12 via the conduit (111), it crosses the valve V12 in which it is relaxed, then sent by the line (112) in the exchange zone E12 where it is vaporized, to supply the cold for this zone.
- Valves V10, V11, V12 expand the refrigerant mixture M to decreasing pressures corresponding to vaporization temperatures decreasing in the three exchange zones E10, E11 and E12.
- three exchange zones E10, E11, and E12 the vaporized refrigerant mixture is sent to three different stages of the K10 compressor respectively by the conduits (133), (123) and (113).
- the simplified diagram of FIG. 5 presents a variant making it possible to recover almost all of the C2 + compounds (i.e. compounds having at least two carbon atoms, such as ethane, propane, butanes, etc.) present in liquefied natural gas.
- the gas leaving the compressor K1 through the conduit (25) and intended to be burned in turbines is first refrigerated using the pre-refrigeration section (R), then sent by line 62 at the bottom of the fractionation column T2.
- a small part of the refrigerated and liquefied natural gas leaving of the pre-cooling section (R) by the line (61) is expanded in the valve V61 before being introduced at the head of column T2.
- the methane content of the combustible gas at the top of T2 will be around 90% molar, and the methane content of liquefied natural gas 64% molar.
- the rest of the diagram is identical to what has been described above in connection with the illustration in Figure 2.
- At least part of the gaseous fraction representing at least 10% by weight relative to the weight of the fluid G initially introduced in said process is used to produce electricity.
- At least part of the fraction gaseous representing at least 10% by weight relative to the weight of the fluid G initially introduced in said process is reinjected into the zone from from which it is recovered and in the case where the fluid G is a natural gas in the well from which it is recovered.
- the other liquefied part of the fluid G is expanded and partially vaporized in one or two stages until the pressure of the storage.
- the part of the fluid G used to produce the necessary cold at the second stage is sprayed at different pressure levels decreasing.
- the operating conditions are chosen to so that the quantity of liquefied gas obtained is approximately 20% at approximately 80% by weight of the quantity of gas at the inlet of the process.
- the first refrigeration step comprises several heat exchange zones and refrigeration is provided in said heat exchange zones using the external refrigerant M which is expanded and vaporized at pressure levels decreasing.
- the external refrigerant M comprises at least one hydrocarbon and preferably at least two hydrocarbons.
- the external refrigerant M comprises at least one hydrocarbon chosen from the group formed by methane, ethane, propane and butanes. Even more preferably, the refrigerant external M includes methane, ethane, propane and at least one butane.
- the fluid G exits condensed single-phase from the first stage of refrigeration. More preferably, the fluid G leaves in dense phase of the first stage of refrigeration.
- the fluid G is at a temperature at least below about - 40 ° C.
- the vaporized part of the fluid G in the second step of the process is compressed to a pressure sufficient to allow its reinjection into the area from which it is recovers and in case fluid G is a natural gas in the well from from which we recover it.
- the vaporized part of fluid G in the second step of the process is compressed to a sufficient pressure to allow its use to produce electricity especially in a gas turbine.
- the part of the fluid G compressed to a pressure sufficient for its use in a gas turbine is cooled using the first stage of pre-refrigeration then sent to the bottom of a fractionation column in which also introduces at the head of said column a part of the same fluid G cooled in the first pre-refrigeration step and relaxed.
- the liquefaction method according to the invention may optionally further comprise a drying step and a natural gas fractionation step comprising at least two fractionation columns, said fractionation being carried out immediately after drying, by feeding the first fractionation column with the drying temperature, and using the second exchange zone of the first refrigeration step for the condenser of said column. More preferably, the product leaving the bottom of the first fractionation column is refrigerated in the pre-refrigeration section using the external refrigerant M used in the first pre-refrigeration stage, before being expanded and sent in head of the second fractionation column.
- This gas arrives in the liquefaction unit at a pressure of 5.6 MPa and at a temperature of 40 ° C. We also considered a temperature of 40 ° C for the process side output of the water exchangers.
- the natural gas G is supplied by the conduit (10) to the exchanger E13 in which it is cooled by an intermediate fluid (FI), to a temperature of 19 ° C. then is sent by the conduit (51) to the dryer (S) before entering via the conduit (52) in the fractionation zone (F).
- This fractionation zone usually comprises at least two fractionation columns.
- the intermediate fluid FI is moved by the circulation system Cl, and cooled in the exchange zone E10 of the pre-refrigeration section (R).
- the fractionation F has a first column T11.
- the dry gas is sent to the bottom of column T11 by the line (52). This dry gas enters column T11 at its outlet temperature of the drying section.
- the fraction leaving the top of column T11 is sent through the conduit (58) at a temperature of 12 ° C to the area exchange E11 of the pre-refrigeration section (R) from which it leaves partially condensed at a temperature of - 0.5 ° C before being sent by line (59) to the reflux ball B11.
- the P51 pump is used to return by line 201 the liquid fraction separated in flask B11 and leaving by the line 200 to column T11 and thus ensure reflux into the column.
- the gas leaving balloon B11 through line (53) is purified from too heavy cuts and in particular benzene.
- the gas is sent through the conduit (53) (see Figure 7) to the exchange zone E11 where it will be cooled to - 25 ° C before being sent to the exchange zone E12 via the conduit (12).
- the liquid leaving through the line (81) ( Figure 6) at the bottom of column T11 includes enough compounds C2 and C3 (compounds comprising 2 and 3 atoms respectively carbon) for the coolant mixture additions.
- This liquid mixture circulating in the line (81) is sent to the pre-refrigeration section (R2) from where it leaves cooled by the conduit (82), then it is relaxed through the valve V51 and sent via the conduit (83) at the head of the column T12 (demethanizer).
- This column is reboiled using the reboiler E51 to remove most of the methane from the mixture.
- Gas coming out on top from column T12 by line (54), rich in methane, will be remixed with the rest of the combustible gas leaving the compressor K1 via line (25) (see figure 8).
- the product leaving the bottom of column T12 via line (84) (see Figure 6) is sent, after expansion in the valve V52, by the conduit (85) in column T13.
- This column is reboiled using the exchanger E52. The gas leaving the head of column T13 (FIG.
- the mixture thus refrigerated leaves this pre-refrigeration section (R2) by the line (57) then it is mixed with the refrigerated and liquefied gas circulating in the line (12) before being sent to the exchange area E12.
- the part of refrigerant mixture M entering the pre-refrigeration section (R2) through the line (1001) is cooled, separated and expanded at two pressure levels to produce the cold necessary for cooling the incoming mixture in this section by line (56).
- the different vaporized parts leaving respectively by the lines (1123) and (1133) are returned with the fluids in same pressure, entering respectively by lines (123) and (133) in the compressor K10.
- the pre-refrigeration section (R) (simplified diagram of FIG. 7) uses a mixture of refrigerant M whose composition in molar percent (% mol.) Is as follows: Methane 1.9 Ethane 46.5 Propane 44.0 IsoButane 4.9 N-Butane 2.7
- This mixture leaves the compressor K10 by the line (100) compressed to a pressure of 3.23 MPa.
- Intermediate cooling C11 is required to bring the fluid leaving by line 141 of the second stage of the second stage to 40 ° C. compressor K10 before reintroducing it via line (142) on the third compressor stage K10.
- the mixture circulating in line (100) is cooled to a temperature of 40 ° C by the exchanger C10 from which it leaves fully condensed by line (101).
- a small part of the mixture M is sent by line (1001) to the pre-cooling zone (R2), the rest is sent to heat exchange zone E10. It is sub-cooled successively in the heat exchange zones E10, E11, and E12.
- the refrigerant mixture M leaving the exchange zone E11 is partly sent to the exchange zone E12 via the conduit (103).
- Another part of the refrigerant mixture M circulating in the line (103) is taken and sent through the conduit (121), into the valve V11 in which it is relaxed and then reintroduced into the exchange zone E11 by the conduit (122) where it vaporizes to provide the cold necessary for this area.
- the refrigerant mixture leaves the exchange zone E12 via the conduit (111), it crosses the valve V12 in which it is relaxed, then sent by the line (112) in the exchange zone E12 where it is vaporized, to supply the cold of this zone.
- the part of the mixture entering through the line (122) in the exchanger E11 in which it vaporizes is sent by the line (123) to the compressor K10 at a pressure of 0.655 MPa.
- the part of the mixture entering through the line (112) in the exchanger E12 in which it vaporizes is sent by the line (113) to the 1st stage of the compressor K10 at the pressure of 0.15 MPa.
- Total energy consumption for compressors in this section is 15526 kW.
- the liquefied natural gas circulating in the conduit (13) enters the exchanger cryogenic E1 (see the simplified diagram in Figure 8) where it is sub-cooled and exits through line (14) at a temperature of -142.5 ° C. He is then expanded in the EX1 expansion turbine at a pressure of 0.65 MPa below which is still completely liquid at a temperature of -143.2 ° C and leaves this expansion turbine via line (15). Part of the fluid circulating in line (15) is sent by line (16) at this pressure to the cryogenic exchanger E1 in which it vaporizes.
- the rest of this fluid (referred to above as "the other party") is sent by line (18) in the V100 valve in which it is relaxed and then sent to the balloon B1 at a temperature of -144.9 ° C and a pressure of 0.26 MPa.
- a part of the liquid in balloon B1 is returned by line (19) mixed with the vapor coming from the tank B1 and circulating in the line (18V) in the exchanger cryogenic E1 to be vaporized there.
- the other part of this liquid is sent by line (21) in the exchanger E2 in which it is cooled before being expanded in valve V200 and sent to balloon B2 via line (22) at a pressure of 0.105 MPa and at a temperature of -157.6 ° C.
- Steam from of tank B2 via line (24) is sent back to exchanger E2: the flow of steam at the exit of the E2 exchanger (line 26 figure 8) is 544 kmoles at a temperature of -146.7 ° C.
- the liquefied natural gas leaves via line (23) at the bottom of the cylinder B2 with a flow rate of 4,985 kmole / h or approximately 50 mole percent of the input flow natural gas in the liquefaction unit with a molecular weight of 23.34, or by weight 116.35 tonnes / h.
- the gas vaporized at low pressure leaves the cryogenic exchanger E1 by the conduit (20) at a temperature of -66. ° C. It is sent through this conduit to balloon B3 where the non-vaporized fraction is separated and sent by line (20L) to the balloon B4 by the pump P3. Gas vaporized at higher pressure leaving the cryogenic exchanger E1 is sent to the balloon B4 by the conduit (17).
- the liquid (17L) separated in the tank B4 is pumped by the pump P4 and sent as a mixture with the fluid (13) to the inlet of the exchanger cryogenic E1.
- the vapor phases of balloons B3 and B4 (circulating lines 17V and 20V respectively) are sent to the different compressor stages K1 to be compressed at a pressure of 1.5 MPa. There are 4315 Kmole / h at the outlet of compressor K1 in line (25), at a temperature of 22 ° C.
- Energy consumption for this sub-cooling section low temperature is 3820 kW for the K1 compressor, plus 108 kW for P3 and P4 pumps.
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Abstract
Description
Dans de tels procédés, un mélange de fluides, utilisé comme fluide réfrigérant dans le cycle de réfrigération externe, est vaporisé, comprimé, refroidi en échangeant de la chaleur avec un milieu ambiant tel que de l'eau ou de l'air, condensé, détendu et recyclé.
A l'issue du premier étage, le mélange réfrigérant se présente sous la forme d'un fluide diphasique comportant une phase vapeur et une phase liquide. Lesdites phases sont séparées, par exemple dans un ballon séparateur, et envoyées, par exemple, dans un échangeur bobiné, dans lequel la fraction vapeur est condensée, tandis que le gaz naturel est liquéfié sous pression, la réfrigération étant assurée par vaporisation de la fraction liquide de mélange réfrigérant. La fraction liquide obtenue par condensation de la fraction vapeur est sous-refroidie, détendue et vaporisée pour assurer la liquéfaction finale du gaz naturel, qui est sous-refroidi avant d'être détendu à travers une vanne ou une turbine pour produire le Gaz Naturel Liquéfié (GNL) recherché.
La présence d'une phase vapeur nécessite une opération de condensation sur le mélange réfrigérant au niveau du second étage qui demande un dispositif relativement complexe et coûteux.
Il a par ailleurs été décrit dans le brevet US-4 195 979 l'addition d'une étape de détente du gaz naturel entre les deux étapes de refroidissement.
Il a également été proposé dans le brevet du demandeur FR 2 743 140 d'opérer dans des conditions de pression et de températures choisies pour obtenir à la sortie du premier étage de réfrigération un mélange réfrigérant entièrement monophasique condensé.
Ceci induit des contraintes, qui peuvent être pénalisantes pour l'économie du procédé, notamment du fait que la pression à laquelle le mélange réfrigérant utilisé dans le deuxième étage est comprimé, peut être relativement élevé.
Une autre disposition selon l'art antérieur consiste à opérer au moyen de trois cycles de réfrigération en série, dont chacun opère avec un corps pur comme réfrigérant. Un premier cycle fonctionnant avec du propane permet de condenser de l'éthylène sous pression à une température d'environ - 35 °C. La vaporisation de l'éthylène à une pression proche de la pression atmosphérique dans un deuxième cycle permet de condenser du méthane sous pression à une température d'environ - 100°C. La vaporisation du méthane permet de sous-refroidir le gaz naturel liquéfié (GNL) produit et ainsi de pouvoir le détendre pour pouvoir le stocker et le transporter à une pression proche de la pression atmosphérique. Cette façon d'opérer présente l'inconvénient d'avoir à utiliser de l'éthylène sensiblement pur que l'on doit ensuite vaporiser pour condenser du méthane sensiblement pur qui est lui-même vaporisé pour sous refroidir le GNL. L'utilisation de corps sensiblement pur est pénalisante pour l'économie du procédé et l'emploi de l'éthylène qui est un composé insaturé particulièrement réactif impose des précautions particulières ce qui pénalise également ce procédé.
- dans la première étape a) on refroidit le fluide G essentiellement gazeux à l'aide d'un réfrigérant externe M pour qu'à l'issue de cette première étape il soit au moins partiellement, et de préférence totalement liquide à la pression opératoire, qui sera de préférence d'environ 4 à environ 7 MPa.
- dans la deuxième étape b) on termine si nécessaire la liquéfaction dudit fluide G et on sous refroidit ledit fluide G, à l'aide d'une partie du même fluide G, ladite partie étant ainsi détendue et vaporisée de manière à produire le froid nécessaire pour récupérer l'autre partie dudit fluide G totalement liquide.
Les conditions opératoires du procédé selon l'invention seront de préférence choisie de manière à ce que la quantité de gaz liquéfié obtenu soit d'environ 20 à environ 80 % en poids, de manière plus préférée d'environ 30 % à environ 70 % poids de la quantité de gaz à l'entrée du procédé.
- Les figures 1 et 2 montrent les deux options du schéma de principe de l'unité suivant l'invention, la figure 2 figurant une option préférée.
- La figure 3 montre une possibilité pour réaliser la première étape de réfrigération
- La figure 4 montre une réalisation du procédé intégrant le fractionnement du gaz
- La figure 5 montre une variante du procédé permettant d'augmenter la récupération en composés C2+ dans la partie liquéfiée du fluide G.
- Les figures 6 à 8 seront décrites ci-après.
- par le conduit (54) du gaz combustible
- par le conduit (55), des condensats stabilisés contenant des pentanes, la totalité de l'hexane, du benzène et éventuellement des composés plus lourds,
- par le conduit (71) une coupe contenant principalement de l'éthane et par le conduit (74) une coupe contenant principalement du propane. Ces deux coupes sont utilisées comme appoint pour compenser les fuites du mélange réfrigérant M.
- par le conduit (53) on récupère le gaz à liquéfier purifié des composés lourds qui est renvoyé à la section de pré-réfrigération (R)
- par le conduit (56) un mélange, contenant principalement de l'éthane, du
propane et des butanes, est envoyé à la section de pré-réfrigération (R2)
pour être ultérieurement re-mélangé au gaz à liquéfier sortant de la
section de pré-réfrigération (R).
Le gaz purifié provenant de la section de fractionnement F est refroidi et liquéfié dans la section de pré-réfrigération (R), il sort de cette section par le conduit (13) et est mélangé avec le fluide réfrigéré sortant de la section de pré-réfrigération (R2) par le conduit (57). Le mélange est envoyé dans la zone d'échange E1 où il est sous-refroidi. Le reste du schéma est identique à ce qui a été décrit ci-devant en liaison avec l'illustration de la figure 2.
- une fraction liquide après détente,
- une fraction gazeuse représentant au moins 10 % poids par rapport au poids du fluide G introduit initialement dans ledit procédé,
- et comportant au moins deux étapes de réfrigération au cours
desquelles :
- dans la première étape a) on refroidit le fluide G essentiellement gazeux à l'aide d'un réfrigérant externe M pour qu'à l'issue de cette première étape il soit au moins partiellement liquide à la pression opératoire et
- dans la deuxième étape b) on termine si nécessaire la liquéfaction dudit fluide G et on sous refroidit ledit fluide G, à l'aide d'une partie du même fluide G, ladite partie étant ainsi détendue et vaporisée de manière à produire le froid nécessaire pour récupérer l'autre partie dudit fluide G totalement liquide.
De préférence, le réfrigérant externe M comprend au moins un hydrocarbure et de préférence au moins deux hydrocarbures.
De manière plus préférée, le produit sortant en fond de la première colonne de fractionnement est réfrigéré dans la section de pré-réfrigération en se servant du réfrigérant externe M utilisé dans la première étape de pré-réfrigération, avant d'être détendu et envoyé en tête de la deuxième colonne de fractionnement.
Azote | 0,1 |
Méthane | 76,5 |
Éthane | 12,7 |
Propane | 7,8 |
IsoButane | 1,2 |
N-Butane | 1,0 |
IsoPentane | 0,25 |
N-Pentane | 0,15 |
C6+ | 0,3 |
Le gaz naturel G est alimenté par le conduit (10) à l'échangeur E13 dans lequel il est refroidi par un fluide intermédiaire (FI), jusqu'à une température de 19 °C puis est envoyé par le conduit (51) au sécheur (S) avant d'entrer par le conduit (52) dans la zone de fractionnement (F). Cette zone de fractionnement comporte habituellement au moins deux colonnes de fractionnement. Le fluide intermédiaire FI est mû par le système de circulation Cl, et refroidi dans la zone d'échange E10 de la section de pré-réfrigération (R).
Méthane | 1.9 |
Éthane | 46.5 |
Propane | 44.0 |
IsoButane | 4.9 |
N-Butane | 2.7 |
- 99 Kmoles/h de gaz combustible (sortant par le conduit 54 (figures 6 et 7)) en tête de la colonne T12 (figure 6) à une température de - 14°C, et à une pression de 3 MPa,
- 49 Kmoles/h (sortant par le conduit 55) de C5+ stabilisés en fond de la colonne T14 (figures 6 et 7)), et
- 9852 Kmoles/h sont envoyés vers l'échangeur E1 par le conduit (13) (le débit de liquide circulant dans le conduit 13 est égal à la somme des débits de fluides circulant dans les-conduits 12 et 57) sous forme totalement condensée à une température de -64.5 °C et à une pression de 5,58 MPa.
Claims (17)
- Procédé de liquéfaction partielle d'un fluide G formé au moins en partie d'hydrocarbures, produisant simultanément :une fraction liquide après détente,une fraction gazeuse représentant au moins 10 % poids par rapport au poids du fluide G introduit initialement dans ledit procédé,dans la première étape a) on refroidit le fluide G essentiellement gazeux à l'aide d'un réfrigérant externe M pour qu'à l'issue de cette première étape il soit au moins partiellement liquide à la pression opératoire etdans la deuxième étape b) on termine si nécessaire la liquéfaction dudit fluide G et on sous refroidit ledit fluide G, à l'aide d'une partie du même fluide G, ladite partie étant ainsi détendue et vaporisée de manière à produire le froid nécessaire pour récupérer l'autre partie dudit fluide G totalement liquide.
- Procédé de liquéfaction partielle selon la revendication 1 dans lequel le fluide G est un gaz naturel et au moins une partie de la fraction gazeuse est réinjectée dans le puits à partir duquel on récupère ledit gaz naturel.
- Procédé de liquéfaction du fluide G selon l'une des revendications 1 ou 2 dans lequel l'autre partie liquéfiée du fluide G est détendue et partiellement vaporisée en un ou deux étages jusqu'à la pression du stockage.
- Procédé de liquéfaction selon l'une des revendications 1 à 3 dans lequel la partie du fluide G utilisée pour produire le froid nécessaire à cette deuxième étape est vaporisée à différents niveaux de pression décroissants.
- Procédé de liquéfaction selon l'une des revendications 1 à 4 dans lequel les conditions opératoires sont choisies de manière à ce que la quantité de gaz liquéfié obtenu soit d'environ 20 % à environ 80 % en poids de la quantité de gaz à l'entrée du procédé.
- Procédé de liquéfaction selon l'une des revendications 1 à 5 dans lequel la première étape de réfrigération comporte plusieurs zones d'échange de chaleur et dans lequel on assure la réfrigération dans lesdites zones d'échange de chaleur à l'aide du réfrigérant externe M qui est détendu et vaporisé à des niveaux de pression décroissants.
- Procédé de liquéfaction selon l'une des revendications 1 à 6, dans lequel le réfrigérant externe M comprend au moins un hydrocarbure et de préférence au moins deux hydrocarbures.
- Procédé de liquéfaction selon la revendication 7 dans lequel le réfrigérant externe M comprend au moins un hydrocarbure choisi dans le groupe formé par le méthane, l'éthane, le propane et les butanes.
- Procédé de liquéfaction selon la revendication 7 ou 8 dans lequel le réfrigérant externe M comprend du méthane, de l'éthane, du propane et au moins un butane.
- Procédé de liquéfaction selon l'une des revendications 1 à 9 dans lequel le fluide G sort monophasique condensé du premier étage de réfrigération.
- Procédé de liquéfaction selon l'une des revendications 1 à 9 dans lequel le fluide G sort en phase dense du premier étage de réfrigération.
- Procédé de liquéfaction d'un gaz naturel selon l'une des revendications 1 à 11 dans lequel la sortie du premier étage de réfrigération, le fluide G se trouve à une température au moins inférieure à environ - 40°C.
- Procédé de liquéfaction d'un gaz naturel selon l'une des revendications 1 à 12 dans lequel la partie vaporisée du fluide G dans la deuxième étape du procédé est comprimée à une pression suffisante, pour permettre sa réinjection dans la zone à partir duquel on le récupère et dans le cas où le fluide G est un gaz naturel dans le puits à partir duquel on le récupère.
- Procédé de liquéfaction d'un gaz naturel selon l'une des revendications 1 à 13 dans lequel la partie vaporisée du fluide G dans la deuxième étape du procédé est comprimée à une pression suffisante, pour permettre son utilisation pour produire de l'électricité notamment dans une turbine à gaz.
- Procédé de liquéfaction d'un gaz naturel selon la revendication 14 dans lequel la partie du fluide G comprimée à une pression suffisante pour son utilisation dans une turbine à gaz est refroidie à l'aide de la première étape de pré-réfrigération puis envoyée en fond d'une colonne de fractionnement dans laquelle on introduit également en tête de ladite colonne une partie du même fluide G refroidie dans la première étape de pré-réfrigération et détendue.
- Procédé de liquéfaction d'un gaz naturel selon l'une des revendications 1 à 15 caractérisé en ce qu'il comporte en outre une étape de séchage et une étape de fractionnement du gaz naturel comportant au moins deux colonnes de fractionnement ledit fractionnement étant effectué immédiatement après le séchage, en alimentant la première colonne de fractionnement à la température du séchage, et en utilisant la deuxième zone d'échange de la première étape de réfrigération pour le condenseur de ladite colonne.
- Procédé de liquéfaction d'un gaz naturel selon la revendication 16 dans lequel le produit sortant en fond de la première colonne de fractionnement est réfrigéré dans la section de pré-réfrigération en se servant du réfrigérant externe M utilisé dans la première étape de pré-réfrigération, avant d'être détendu et envoyé en tête de la deuxième colonne de fractionnement.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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FR0000737A FR2803851B1 (fr) | 2000-01-19 | 2000-01-19 | Procede de liquefaction partielle d'un fluide contenant des hydrocarbures tel que du gaz naturel |
FR0000737 | 2000-01-19 |
Publications (2)
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EP1118827A1 true EP1118827A1 (fr) | 2001-07-25 |
EP1118827B1 EP1118827B1 (fr) | 2004-10-20 |
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US (1) | US6449982B1 (fr) |
EP (1) | EP1118827B1 (fr) |
JP (1) | JP4898006B2 (fr) |
DE (1) | DE60106499D1 (fr) |
ES (1) | ES2232571T3 (fr) |
FR (1) | FR2803851B1 (fr) |
Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
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FR2841330A1 (fr) * | 2002-06-21 | 2003-12-26 | Inst Francais Du Petrole | Liquefaction de gaz naturel avec recyclage de gaz naturel |
CN103968640A (zh) * | 2014-05-15 | 2014-08-06 | 碧海舟(北京)石油化工设备有限公司 | 一种利用天然气压差发电冷能的空气分离系统 |
CN105758113A (zh) * | 2016-03-04 | 2016-07-13 | 浙江大学常州工业技术研究院 | 一种波动入口换热系统及其方法 |
US9441877B2 (en) | 2010-03-17 | 2016-09-13 | Chart Inc. | Integrated pre-cooled mixed refrigerant system and method |
CN103968640B (zh) * | 2014-05-15 | 2016-11-30 | 碧海舟(北京)节能环保装备有限公司 | 一种利用天然气压差发电冷能的空气分离系统 |
US10480851B2 (en) | 2013-03-15 | 2019-11-19 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
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Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3690114A (en) * | 1969-11-17 | 1972-09-12 | Judson S Swearingen | Refrigeration process for use in liquefication of gases |
US4195979A (en) * | 1978-05-12 | 1980-04-01 | Phillips Petroleum Company | Liquefaction of high pressure gas |
EP0599443A1 (fr) * | 1992-11-20 | 1994-06-01 | Chiyoda Corporation | Procédé de liquéfaction de gaz naturel |
US5826444A (en) * | 1995-12-28 | 1998-10-27 | Institut Francais Du Petrole | Process and device for liquefying a gaseous mixture such as a natural gas in two steps |
WO2000057118A1 (fr) * | 1999-03-23 | 2000-09-28 | Robert Wissolik | Systeme de liquefaction par depressurisation pour gazoduc industriel |
-
2000
- 2000-01-19 FR FR0000737A patent/FR2803851B1/fr not_active Expired - Lifetime
-
2001
- 2001-01-10 DE DE60106499T patent/DE60106499D1/de not_active Expired - Lifetime
- 2001-01-10 EP EP01400050A patent/EP1118827B1/fr not_active Expired - Lifetime
- 2001-01-10 ES ES01400050T patent/ES2232571T3/es not_active Expired - Lifetime
- 2001-01-19 JP JP2001011715A patent/JP4898006B2/ja not_active Expired - Lifetime
- 2001-01-19 US US09/764,438 patent/US6449982B1/en not_active Expired - Lifetime
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3690114A (en) * | 1969-11-17 | 1972-09-12 | Judson S Swearingen | Refrigeration process for use in liquefication of gases |
US4195979A (en) * | 1978-05-12 | 1980-04-01 | Phillips Petroleum Company | Liquefaction of high pressure gas |
EP0599443A1 (fr) * | 1992-11-20 | 1994-06-01 | Chiyoda Corporation | Procédé de liquéfaction de gaz naturel |
US5826444A (en) * | 1995-12-28 | 1998-10-27 | Institut Francais Du Petrole | Process and device for liquefying a gaseous mixture such as a natural gas in two steps |
WO2000057118A1 (fr) * | 1999-03-23 | 2000-09-28 | Robert Wissolik | Systeme de liquefaction par depressurisation pour gazoduc industriel |
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US6763680B2 (en) | 2002-06-21 | 2004-07-20 | Institut Francais Du Petrole | Liquefaction of natural gas with natural gas recycling |
AU2003204772B2 (en) * | 2002-06-21 | 2009-02-19 | Institut Francais Du Petrole | Liquefaction of natural gas with natural gas recycling |
FR2841330A1 (fr) * | 2002-06-21 | 2003-12-26 | Inst Francais Du Petrole | Liquefaction de gaz naturel avec recyclage de gaz naturel |
US10502483B2 (en) | 2010-03-17 | 2019-12-10 | Chart Energy & Chemicals, Inc. | Integrated pre-cooled mixed refrigerant system and method |
US9441877B2 (en) | 2010-03-17 | 2016-09-13 | Chart Inc. | Integrated pre-cooled mixed refrigerant system and method |
US11428463B2 (en) | 2013-03-15 | 2022-08-30 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
US11408673B2 (en) | 2013-03-15 | 2022-08-09 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
US10480851B2 (en) | 2013-03-15 | 2019-11-19 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
CN103968640B (zh) * | 2014-05-15 | 2016-11-30 | 碧海舟(北京)节能环保装备有限公司 | 一种利用天然气压差发电冷能的空气分离系统 |
CN103968640A (zh) * | 2014-05-15 | 2014-08-06 | 碧海舟(北京)石油化工设备有限公司 | 一种利用天然气压差发电冷能的空气分离系统 |
US10663221B2 (en) | 2015-07-08 | 2020-05-26 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
US11408676B2 (en) | 2015-07-08 | 2022-08-09 | Chart Energy & Chemicals, Inc. | Mixed refrigerant system and method |
CN105758113A (zh) * | 2016-03-04 | 2016-07-13 | 浙江大学常州工业技术研究院 | 一种波动入口换热系统及其方法 |
Also Published As
Publication number | Publication date |
---|---|
US6449982B1 (en) | 2002-09-17 |
ES2232571T3 (es) | 2005-06-01 |
FR2803851B1 (fr) | 2006-09-29 |
JP2001226685A (ja) | 2001-08-21 |
JP4898006B2 (ja) | 2012-03-14 |
FR2803851A1 (fr) | 2001-07-20 |
DE60106499D1 (de) | 2004-11-25 |
EP1118827B1 (fr) | 2004-10-20 |
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