EP1639062A2 - Procede et installation de production simultanee d un gaz na turel apte a etre liquefie et d une coupe de liquides du gaz naturel. - Google Patents
Procede et installation de production simultanee d un gaz na turel apte a etre liquefie et d une coupe de liquides du gaz naturel.Info
- Publication number
- EP1639062A2 EP1639062A2 EP04767210A EP04767210A EP1639062A2 EP 1639062 A2 EP1639062 A2 EP 1639062A2 EP 04767210 A EP04767210 A EP 04767210A EP 04767210 A EP04767210 A EP 04767210A EP 1639062 A2 EP1639062 A2 EP 1639062A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- natural gas
- column
- purified
- treated
- liquefied
- 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.)
- Granted
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 320
- 239000003345 natural gas Substances 0.000 title claims abstract description 133
- 238000000034 method Methods 0.000 title claims abstract description 25
- 239000007788 liquid Substances 0.000 title claims description 28
- 238000004519 manufacturing process Methods 0.000 title claims description 12
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 47
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 43
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 36
- 238000004821 distillation Methods 0.000 claims abstract description 29
- 239000007789 gas Substances 0.000 claims description 30
- 238000011084 recovery Methods 0.000 claims description 20
- 238000009434 installation Methods 0.000 claims description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 12
- -1 C 5 hydrocarbons Chemical class 0.000 claims description 10
- 239000004215 Carbon black (E152) Substances 0.000 claims description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 230000006835 compression Effects 0.000 claims description 5
- 238000007906 compression Methods 0.000 claims description 5
- 238000010992 reflux Methods 0.000 claims description 5
- 238000002203 pretreatment Methods 0.000 claims description 4
- 238000005380 natural gas recovery Methods 0.000 abstract 1
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 22
- 239000003507 refrigerant Substances 0.000 description 17
- 239000001294 propane Substances 0.000 description 11
- 239000000203 mixture Substances 0.000 description 9
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 8
- 238000000605 extraction Methods 0.000 description 8
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 8
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 7
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 6
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 5
- 239000001282 iso-butane Substances 0.000 description 4
- 235000013847 iso-butane Nutrition 0.000 description 4
- 229940035415 isobutane Drugs 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 239000012808 vapor phase Substances 0.000 description 4
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- XTFIVUDBNACUBN-UHFFFAOYSA-N 1,3,5-trinitro-1,3,5-triazinane Chemical compound [O-][N+](=O)N1CN([N+]([O-])=O)CN([N+]([O-])=O)C1 XTFIVUDBNACUBN-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003780 insertion Methods 0.000 description 1
- 230000037431 insertion Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—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
- F25J1/0055—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 originating from an incorporated cascade
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0057—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 after expansion of the liquid refrigerant stream with extraction of work
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—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
- F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
- F25J1/0215—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
- F25J1/0216—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle using a C3 pre-cooling cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- 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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- 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
- F25J1/0237—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
- F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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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
- F25J3/0204—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
- F25J3/0209—Natural gas or substitute natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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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- 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
- 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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- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/02—Mixing or blending of fluids to yield a certain product
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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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
- F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
-
- 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
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
-
- 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
- F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
-
- 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
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
-
- 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
- F25J2280/00—Control of the process or apparatus
- F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
Definitions
- the present invention relates to a process for the simultaneous production of a natural gas that can be liquefied and to a section of a natural gas that can be liquefied.
- natural gas liquids (NGLs) from a starting natural gas comprising nitrogen, methane, C 2 to C 5 hydrocarbons, and heavy hydrocarbons in Ce "1" , of the type comprising the following steps :
- step (b) cooling the pre-treated natural gas from step (a) to a temperature close to its dew point; (c) the cooled pre-treated natural gas from step (b) is expanded and the expanded natural gas is introduced into an NGL recovery unit comprising at least one main distillation column, so as to produce one part, at the top of the column, a purified natural gas and secondly, said cut of NGL; and (d) forming said natural gas capable of being liquefied from the purified natural gas from step (c).
- the process of the present invention is applicable to production facilities, from a natural gas extracted from the subsoil, of liquefied natural gas (which will be referred to as "LNG”) as the main product and a cut.
- LNG liquefied natural gas
- NNL natural gas liquids
- NGL is understood to mean C 2 + to C 3 + hydrocarbons that can be extracted from natural gas.
- these NGLs may include ethane, propane, butane, and Cs + hydrocarbons.
- LNG produced after extraction of NGLs has a reduced heating value compared to LNG produced without extraction of NGLs.
- Known natural gas liquefaction plants comprise successively a liquefied gas production unit, a liquefaction unit itself and an LNG denitrogenation unit.
- the unit for producing a gas capable of being liquefied necessarily comprises means for removing heavy hydrocarbons C 6 + which can crystallize during liquefaction.
- Such a process has a thermodynamic efficiency optimized for the production of a natural gas at ambient temperature and for the extraction of NGL.
- this process does not give much satisfaction in the case where the natural gas obtained must be liquefied. Indeed, the energy expenditure required for the liquefaction of the natural gas obtained is relatively high.
- the main purpose of the invention is to overcome this disadvantage, that is to say to have a simultaneous production process of LNG and a cut of NGL, more economical and more flexible than existing processes.
- the object of the invention is a process of the aforementioned type, characterized in that step (a) comprises the following sub-steps:
- step (d) comprises the following sub-steps: (d1) purified natural gas extracted from the head of said main column is compressed at a liquefaction pressure in at least a first compressor;
- step (d2) the purified compressed natural gas resulting from step (d1) is cooled by heat exchange with said purified natural gas extracted from the head of the main column, in a first heat exchanger, for producing the natural gas suitable for liquefying;
- step (b) comprises the following substep:
- step (b1) the pre-treated natural gas from step (a) is cooled by exchanging heat with the purified natural gas extracted from the second main column in a second heat exchanger;
- step (c) comprises the following sub-steps:
- step (d) introducing cooled pre-treated natural gas from step (b) into a separator flask to provide a liquid stream and a gas stream; (c2) the gas stream from (d) is expanded in a turbine coupled to the first compressor;
- step (c3) introducing the stream from step (c2) into the main column at an intermediate N3 level;
- step (c4) the liquid stream resulting from step (d) is expanded and this expanded liquid stream is introduced into the main column at a level N2 lower than the level N3;
- step (d1) the purified compressed natural gas is compressed at the outlet of the first compressor into a second compressor fed by
- the liquefied natural gas further comprises a portion of the pre-treated natural gas directly from step (a);
- the method comprises a start-up phase wherein the natural gas which can be liquefied consists predominantly or completely by the gas natural pretreated directly from step (a) said natural gas which can be liquefied is relatively enriched C 2 to C 5 hydrocarbons, and the process comprises a subsequent production step in which the portion of pre-treated natural gas directly from step (a) in the liquefied natural gas is adjusted as a function of the desired C 2 to C 5 hydrocarbon content in the liquefied natural gas; and
- the invention further relates to a plant for the simultaneous production of a liquefied natural gas and a section of natural gas liquids (NGLs) from a starting natural gas comprising nitrogen, methane, C 2 to C 5 hydrocarbons, and C 4 heavy hydrocarbons of the type comprising:
- an NGL recovery unit comprising means for expanding the cooled pre-treated natural gas and comprising at least one main distillation column which produces, on the one hand, at the top of the column, a purified natural gas and on the other hand, said cut of NGL;
- the pre-treatment unit comprises: (a) means for cooling the starting natural gas to a temperature close to its dew point;
- the installation according to the invention may include any of the following characteristics, taken in isolation or all combinations "possible:
- the means for forming natural gas that can be liquefied include:
- (d1) compression means purified natural gas extracted from the head of the main column at a liquefaction pressure, comprising at least a first compressor;
- the cooling means of the pre-treated natural gas comprise a second heat exchanger which puts the gas in heat exchange relationship with said purified natural gas extracted from the main column;
- the LNG recovery unit includes:
- (c3) means for introducing the gas stream expanded in the main column to an intermediate level N3;
- (c4) means for expanding said liquid stream and means for introducing the expanded liquid stream into the main column at a level N2 less than N3;
- the means for compressing the purified natural gas extracted from the head of the main column further comprises a second compressor driven by an external energy source and intended to increase the pressure of the compressed purified natural gas to the pressure of liquefaction;
- the means for forming the purified natural gas comprise means for selectively introducing an adjustable portion of the pretreated natural gas directly from the pre-treatment unit into a line of natural gas capable of being liquefied.
- the plant shown in the Figure relates to the simultaneous production, from a source 11 of decarbonated, desulphurized and dry starting natural gas, of LNG 13 as the main product and a section of NGL 15 as a by-product.
- This installation comprises a C 6 + heavy hydrocarbon removal unit 17, a NGL recovery unit 19, and a liquefaction unit 21.
- the heavy hydrocarbon removal unit 17 successively comprises, downstream of the source 11, first, second and third refrigerants 25, 27, 29, and a first distillation column, or auxiliary distillation column 31 equipped with a head condenser.
- This condenser comprises, between the head of the first column 31 and a first separator tank 33, a fourth refrigerant 35 on the one hand, and a reflux pump 37 on the other hand.
- the NGL recovery unit 19 comprises first, second, and third heat exchangers 41, 43, 45, a second separator tank 47, a second distillation column, or main distillation column 49, a first turbine 51 coupled to a first compressor 53, a second compressor 55 driven by an external power source 56, a fifth refrigerant 57 and a pump 59 for extracting NGLs.
- Unit 21 for liquefying natural gas comprises fourth and fifth heat exchangers 65, 67 cooled by a refrigerating cycle 69.
- This cycle 69 comprises a compressor 73 with three stages 73A, 73B,
- first and second intermediate refrigerants 75A and 75B and an outlet refrigerant 75C four refrigerants 77A-77D in series, a third separator tank 79 and first and second hydraulic turbines 81 and 83.
- the initial molar composition of the decarbonated, desulfurized and dry starting natural gas stream 101 comprises 3.90% nitrogen, 87.03% methane, 5.50% ethane, 2.00% propane, 0.34% iso butane, 0.54% n-butane, 0.18% iso pentane, 0.15% n-pentane, 0.31% C 6 , 0.03 hydrocarbons % C 7 hydrocarbons and 0.02% C 8 hydrocarbons.
- This gas 101 is successively cooled in the first, second and third refrigerants 25, 27, 29 to form the cooled starting natural gas 103.
- This gas 103 is then introduced into the distillation column 31.
- This column 31 produces at the bottom a cup 105 heavy hydrocarbons at C 6 + .
- This cup 105 is expanded in an expansion valve 106 to produce a relaxed heavy hydrocarbon stream 107, which is introduced into the second distillation column 49 at a lower N1 level.
- the first column 31 produces a stream 109 of pretreated gas at the head.
- This stream 109 is cooled and partially condensed in the fourth refrigerant 35, and then introduced into the first separator tank 33, where separation takes place between a gas phase constituting the pre-treated natural gas 111 and a liquid phase constituting a liquid. of reflux 112, which is refluxed in the purification column by the reflux pump 37.
- the molar composition of the pretreated gas stream 111 comprises
- the pre-treated natural gas stream 111 is then split into a feed stream 113 of the LNG recovery unit 19 and a feed stream of the gas liquefaction unit 21.
- the distribution between these two currents is chosen by the control of two respective control valves 114 and 116.
- the stream 113 introduced into the recovery unit 19 is cooled in the second heat exchanger 43 to give a two-phase flow 117 of cooled pre-treated natural gas.
- This stream 117 is introduced into the second separator tank 47, which produces a vapor stream 119 and a liquid stream 121.
- the liquid stream 121 is expanded in an expansion valve 123 and then introduced into the column 49 at a level N2 higher than the N1 level.
- the vapor stream 119 is separated into a majority fraction 125 and a minor fraction 127.
- the major fraction 125 is expanded in the turbine 51. to give a relaxed main fraction 129, which is introduced at a level N3 greater than the level N2 in the column 49.
- the minor fraction 127 is cooled in the third heat exchanger 45, expanded in an expansion valve 131 and then introduced at an upper N4 level of the distillation column 49.
- the N4 level is higher than the N3 level.
- Column 49 is also equipped with an intermediate reboiler
- a reboiler stream 143 is extracted from this column at a level N1a less than N2 and greater than N1. This current is heated in the second heat exchanger 43 and reintroduced into the second column 49 at a level N1 b between the level N1a and the level N1.
- the NGL section 15 is withdrawn from the bottom of the distillation column 49 by the pump 59.
- a bottom reboiler 145 is mounted on the column 49 to adjust the molar ratio of the C1 hydrocarbons to the C hydrocarbons. ⁇ from the LGN 15 cut. This ratio is preferably less than 0.02.
- this cut of NGL comprises 0.3688% of methane
- the recovery rate of ethane is greater than 30%.
- the propane recovery rate is greater than 80% and is preferably greater than 90%.
- the recovery rate of hydrocarbons ⁇ C 4 + is greater than 90% and preferentially greater than 95%.
- a stream 151 of purified natural gas is extracted at the top of the column 49. This stream 151 is heated successively in the heat exchanger 45, in the heat exchanger 43 and then in the heat exchanger 41. note that no external cold source is required for the operation of the LNG recovery unit 19.
- the heated gas stream 153 from the exchanger 41 is then compressed successively in the first compressor 51 and then in the second compressor 55 to produce a gas stream 155 at the liquefaction pressure.
- This stream 155 is cooled in the fifth refrigerant 57 and then in the first heat exchanger 41 to give a stream 157 of purified cooled gas.
- the stream 157 is mixed with the feed stream 115 of the gas liquefaction unit, extracted from the C 6 + heavy hydrocarbon removal unit 17.
- This stream 157 and this stream 115 have substantially equal temperatures and pressures and form the stream 161 of natural gas capable of being liquefied.
- the molar composition of this liquefied natural gas stream 161 comprises 4.1221% nitrogen, 91.9686% methane, 3.7118% ethane, 0.1858% propane, 0.0063% and the like. % iso butane, 0.0051% n-butane and 0.0003% C 5 + hydrocarbons.
- the stream 161 of natural gas that can be liquefied is then successively cooled in the fourth and fifth heat exchangers 65, 67 to produce the LNG stream 13.
- This LNG stream 13 then undergoes denitrogenation in a unit 165.
- the refrigeration in the fourth and fifth heat exchangers 65, 67 is provided by a flow 201 of refrigerant mixture.
- This stream 201 partially liquefied in the fourth refrigerant 77D, is introduced into the separator tank 71 and separated into a vapor phase 201 and a liquid phase 203.
- the vapor phase 203 is liquefied in the heat exchanger 65 to provide a liquid stream which is then subcooled in the fifth heat exchanger 67 to provide a subcooled liquid stream 207.
- This subcooled liquid flow 207 is expanded in the first hydraulic turbine 81, then in an expansion valve 208, to give a first refrigeration flow 209.
- This flow 209 vaporizes in the heat exchanger 67 and allows the liquid to be liquefied. gas 161.
- the liquid phase 205 is sub-cooled in the exchanger 65 to give a subcooled flow which, in turn, is expanded in the second hydraulic turbine 83 and then in an expansion valve 210, to give a second refrigerant stream 211
- the streams 209 and 211 are mixed to give a combined stream 213 which is vaporized in the exchanger 65. This vaporization cools the stream 161 and condenses the vapor phase 203 of the refrigerant mixture stream 201.
- the mixture stream 213 is then compressed in the compressor 77, whose characteristics are given in the table below, to obtain a compressed mixture stream 215.
- This stream of compressed mixture 215 is then successively cooled in the four refrigerants in series 81 to form the stream 201.
- the first, second, third and fourth refrigerants 25, 27, 29, 35 for cooling the starting natural gas on the one hand, and the four refrigerants 77A to 77D for cooling the mixing flow 201 on the other hand, use the same propane refrigeration cycle (not shown).
- This cycle comprises the following four vaporization stages: 6.7 ° C. and 7.92 bars, 0 ° C. and 4.76 bars, -20 ° C. and 2.44 bars, -36 ° C. and 1.30 bars.
- the pressure of the distillation column 31 is preferably between 45 and 65 bar.
- the pressure in the second column is greater than 35 bars.
- the purified gas stream 157 and the feed stream of the gas liquefying unit 115 are produced at a pressure greater than 55 bar.
- This method thus makes it possible to achieve energy savings as shown in the table below, where the powers consumed in a reference installation without an auxiliary column 31 and in an installation according to the invention are compared. More specifically, in years of the reference installation, the starting natural gas stream 101 is directly fed into the LNG extraction unit 19 and the refrigerants 25, 27, 29 and 35 which use the propane cycle serve also to pre-cool the gas flow at the liquefaction pressure 155, unlike the installation according to the invention where the exchanger 41 is used to perform this pre-cooling.
- the installation according to the invention makes it possible simultaneously to produce LNG 13 and a cut of LGN 15 with a saving of 2285 kW compared to the reference installation. Furthermore, when starting the installation according to the invention, the entire stream of pre-treated natural gas 111 leaving the unit 17 for removing heavy hydrocarbons is directed directly to the liquefaction unit -21 by The feedstock 115.
- the produced LNG then has a relatively high calorific power.
- the NGL recovery unit 19 is then started gradually, without affecting the productivity of the liquefaction unit 21.
- the heating value of the LNG produced is then adjusted by the relative flow rates of the feed streams 113 of the recovery unit. of LNG and 115 of the gas liquefaction unit.
- all the pre-treated natural gas stream 111 leaving the heavy hydrocarbon removal unit 17 is directed directly to the liquefaction unit 21 by the feed stream 115.
- the LNG recovery unit may comprise a third distillation column mounted downstream of the second distillation column and operating at a lower or higher pressure than this second column.
- This third column enriches NGLs in a particular component such as propane.
- An example of such a unit is described in EP-A-0 535 752. Thanks to the invention which has just been described, it is possible to have a facility that simultaneously produces LNG and NGLs economically and flexible with high extraction rates for C 2 -C 5 hydrocarbons. The energy consumption is significantly reduced, surprisingly, by the insertion of an auxiliary distillation column upstream of the LNG recovery unit and the introduction into this unit of the top fraction of this column. .
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PL04767210T PL1639062T3 (pl) | 2003-06-02 | 2004-05-28 | Sposób i instalacja do równoczesnego wytwarzania gazu ziemnego, który może zostać skroplony i frakcji ciekłej gazu |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0306632A FR2855526B1 (fr) | 2003-06-02 | 2003-06-02 | Procede et installation de production simultanee d'un gaz naturel apte a etre liquefie et d'une coupe de liquides du gaz naturel |
PCT/FR2004/001334 WO2004108865A2 (fr) | 2003-06-02 | 2004-05-28 | Procede et installation de production simultanee d'un gaz naturel apte a etre liquefie et d'une coupe de liquides du gaz naturel. |
Publications (2)
Publication Number | Publication Date |
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EP1639062A2 true EP1639062A2 (fr) | 2006-03-29 |
EP1639062B1 EP1639062B1 (fr) | 2007-05-02 |
Family
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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EP04767210A Expired - Lifetime EP1639062B1 (fr) | 2003-06-02 | 2004-05-28 | Procede et installation de production simultanee d un gaz na turel apte a etre liquefie et d une coupe de liquides du gaz naturel. |
Country Status (16)
Country | Link |
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US (1) | US7237407B2 (fr) |
EP (1) | EP1639062B1 (fr) |
JP (1) | JP4669473B2 (fr) |
KR (1) | KR101062153B1 (fr) |
CN (1) | CN100588702C (fr) |
AT (1) | ATE361352T1 (fr) |
CA (1) | CA2527381C (fr) |
CY (1) | CY1106780T1 (fr) |
DE (1) | DE602004006266T2 (fr) |
ES (1) | ES2286670T3 (fr) |
FR (1) | FR2855526B1 (fr) |
MX (1) | MXPA05012952A (fr) |
PL (1) | PL1639062T3 (fr) |
PT (1) | PT1639062E (fr) |
TW (1) | TWI352614B (fr) |
WO (1) | WO2004108865A2 (fr) |
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JP7026490B2 (ja) * | 2017-11-21 | 2022-02-28 | レール・リキード-ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Bog再凝縮装置およびそれを備えるlng貯蔵システム。 |
CN109294647B (zh) * | 2018-09-17 | 2021-08-13 | 广州智光节能有限公司 | 天然气的提纯系统 |
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US3440828A (en) * | 1966-02-11 | 1969-04-29 | Air Prod & Chem | Liquefaction of natural gas employing cascade refrigeration |
US4456461A (en) * | 1982-09-09 | 1984-06-26 | Phillips Petroleum Company | Separation of low boiling constituents from a mixed gas |
FR2681859B1 (fr) * | 1991-09-30 | 1994-02-11 | Technip Cie Fse Etudes Const | Procede de liquefaction de gaz naturel. |
US5325673A (en) | 1993-02-23 | 1994-07-05 | The M. W. Kellogg Company | Natural gas liquefaction pretreatment process |
US5555748A (en) * | 1995-06-07 | 1996-09-17 | Elcor Corporation | Hydrocarbon gas processing |
US6354105B1 (en) * | 1999-12-03 | 2002-03-12 | Ipsi L.L.C. | Split feed compression process for high recovery of ethane and heavier components |
US6401486B1 (en) | 2000-05-18 | 2002-06-11 | Rong-Jwyn Lee | Enhanced NGL recovery utilizing refrigeration and reflux from LNG plants |
FR2817766B1 (fr) * | 2000-12-13 | 2003-08-15 | Technip Cie | Procede et installation de separation d'un melange gazeux contenant du methane par distillation,et gaz obtenus par cette separation |
TW573112B (en) * | 2001-01-31 | 2004-01-21 | Exxonmobil Upstream Res Co | Process of manufacturing pressurized liquid natural gas containing heavy hydrocarbons |
US6526777B1 (en) * | 2001-04-20 | 2003-03-04 | Elcor Corporation | LNG production in cryogenic natural gas processing plants |
US6742358B2 (en) * | 2001-06-08 | 2004-06-01 | Elkcorp | Natural gas liquefaction |
UA76750C2 (uk) * | 2001-06-08 | 2006-09-15 | Елккорп | Спосіб зрідження природного газу (варіанти) |
US6662589B1 (en) | 2003-04-16 | 2003-12-16 | Air Products And Chemicals, Inc. | Integrated high pressure NGL recovery in the production of liquefied natural gas |
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2003
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- 2004-05-28 PT PT04767210T patent/PT1639062E/pt unknown
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- 2004-05-28 JP JP2006508346A patent/JP4669473B2/ja not_active Expired - Lifetime
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- 2004-05-28 DE DE602004006266T patent/DE602004006266T2/de not_active Expired - Lifetime
- 2004-05-28 WO PCT/FR2004/001334 patent/WO2004108865A2/fr active IP Right Grant
- 2004-05-28 MX MXPA05012952A patent/MXPA05012952A/es active IP Right Grant
- 2004-05-28 KR KR1020057022877A patent/KR101062153B1/ko active IP Right Grant
- 2004-05-28 CN CN200480018355A patent/CN100588702C/zh not_active Expired - Lifetime
- 2004-06-01 TW TW093115702A patent/TWI352614B/zh not_active IP Right Cessation
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Also Published As
Publication number | Publication date |
---|---|
TW200503815A (en) | 2005-02-01 |
JP4669473B2 (ja) | 2011-04-13 |
PT1639062E (pt) | 2007-08-09 |
EP1639062B1 (fr) | 2007-05-02 |
CY1106780T1 (el) | 2012-05-23 |
WO2004108865A3 (fr) | 2005-02-17 |
WO2004108865A2 (fr) | 2004-12-16 |
FR2855526B1 (fr) | 2007-01-26 |
KR20060021869A (ko) | 2006-03-08 |
CA2527381A1 (fr) | 2004-12-16 |
CA2527381C (fr) | 2012-03-13 |
ES2286670T3 (es) | 2007-12-01 |
MXPA05012952A (es) | 2006-02-28 |
US20040244415A1 (en) | 2004-12-09 |
JP2007526924A (ja) | 2007-09-20 |
FR2855526A1 (fr) | 2004-12-03 |
CN100588702C (zh) | 2010-02-10 |
DE602004006266D1 (de) | 2007-06-14 |
PL1639062T3 (pl) | 2007-11-30 |
ATE361352T1 (de) | 2007-05-15 |
DE602004006266T2 (de) | 2008-01-10 |
US7237407B2 (en) | 2007-07-03 |
CN1813046A (zh) | 2006-08-02 |
TWI352614B (en) | 2011-11-21 |
KR101062153B1 (ko) | 2011-09-05 |
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