EP1639062B1 - 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. Download PDF

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Publication number
EP1639062B1
EP1639062B1 EP04767210A EP04767210A EP1639062B1 EP 1639062 B1 EP1639062 B1 EP 1639062B1 EP 04767210 A EP04767210 A EP 04767210A EP 04767210 A EP04767210 A EP 04767210A EP 1639062 B1 EP1639062 B1 EP 1639062B1
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EP
European Patent Office
Prior art keywords
natural gas
column
pretreated
stream
liquefiable
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.)
Expired - Lifetime
Application number
EP04767210A
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German (de)
English (en)
French (fr)
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EP1639062A2 (fr
Inventor
Henri Paradowski
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
TotalEnergies SE
Technip Energies France SAS
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Technip France SAS
Total SE
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Priority to PL04767210T priority Critical patent/PL1639062T3/pl
Publication of EP1639062A2 publication Critical patent/EP1639062A2/fr
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Publication of EP1639062B1 publication Critical patent/EP1639062B1/fr
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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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—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
    • 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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    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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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    • 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
    • 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
    • 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
    • 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
    • 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
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    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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    • F25J2270/00—Refrigeration techniques used
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    • 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 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 comprise ethane, propane, butane, and C 5 + 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.
  • 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 methods.
  • 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 unit 17 for removing heavy hydrocarbons 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 three-stage compressor 73A, 73B, 73C, provided with 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 hydrocarbons, 0.03% d 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 section 105 of heavy hydrocarbons 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 reflux liquid. 112, which is refluxed in the purification column by the reflux pump 37.
  • the molar composition of the pretreated gas stream 111 comprises 3.9783% nitrogen, 88.2036% methane, 5.3622% ethane, 1.7550% propane, 0.2488% iso butane, 0.3465% n-butane, 0.0616% iso pentane, 0.0384% n-pentane, 0.0057% C 6 hydrocarbons.
  • 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 115 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 141.
  • a reboiler stream 143 is extracted from this column at a level N1a less than N2 and greater than N1. This stream is warmed in the second heat exchanger 43 and reintroduced into the second column 49 at a level b N1 between the level N1 and the level N1.
  • the section 15 of NGL is extracted 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 hydrocarbons to C 1 relative to the hydrocarbons in question.
  • this cut of NGL comprises 0.3688% of methane, 36.8810% of ethane, 33.8344% of propane, 6.157% of iso-butane, 9.9267% of n-butane, 3, 3354% of iso pentane, 2.7808% of n-pentane, 5.7498% of C 6 hydrocarbons, 0.5564% of C 7 hydrocarbons, 0.3710% of C 8 hydrocarbons.
  • the respective extraction rates of ethane, propane, and C 4 + hydrocarbons are 36.15%, 91.21%, and 99.3%.
  • the recovery rate of ethane is greater than 30%.
  • the recovery rate of propane is greater than 80% and is preferably greater than 90%.
  • the recovery rate of C 4 + hydrocarbons is greater than 90% and is preferably 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 stream 161 of natural gas capable of being liquefied comprises 4.1221% nitrogen, 91.9686% methane, 3.7118% ethane, 0.1858% propane, 0.0063% d iso butane, 0.0051% n-butane and 0.0003% C 5 + hydrocarbons.
  • the flow 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 is then denitrogenized in a unit 165.
  • Refrigeration in the fourth and fifth heat exchangers 65, 67 is provided by a coolant stream 201.
  • 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.
  • Compressor 73A 73B 73C Suction temperature (° C) - 37.44 34 34 Discharge temperature (° C) 67.25 68.70 68.15 Suction pressure (Bar) 3.65 18.30 29.70 Discharge pressure (Bar) 18.70 30.00 47.61 Polytropic yield (%) 82 82 82 Power (KW) 74109 24396 21882
  • 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 bar.
  • 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.
  • the starting natural gas stream 101 is directly fed into the LNG extraction unit 19 and the refrigerants 25, 27, 29 and 35 that use the propane cycle are also used 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.
  • Reference method Process according to the invention Compressor 73 of mixed refrigerant (KW) 119460 120387 Compressor (not shown) of refrigerant propane (KW) 69700 72174 Compressor 55 of treated gas (KW) 20650 14964 Total (KW) 209810 207525
  • 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.
  • 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 115.
  • the LNG produced then has a relatively high calorific value.
  • 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.
  • 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.

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  • Engineering & Computer Science (AREA)
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  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Bakery Products And Manufacturing Methods Therefor (AREA)
EP04767210A 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. Expired - Lifetime EP1639062B1 (fr)

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

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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.

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EP1639062A2 EP1639062A2 (fr) 2006-03-29
EP1639062B1 true EP1639062B1 (fr) 2007-05-02

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CA2527381C (fr) 2012-03-13
WO2004108865A3 (fr) 2005-02-17
CA2527381A1 (fr) 2004-12-16
KR20060021869A (ko) 2006-03-08
US7237407B2 (en) 2007-07-03
FR2855526B1 (fr) 2007-01-26
CN100588702C (zh) 2010-02-10
WO2004108865A2 (fr) 2004-12-16
PT1639062E (pt) 2007-08-09
US20040244415A1 (en) 2004-12-09
DE602004006266D1 (de) 2007-06-14
ATE361352T1 (de) 2007-05-15
PL1639062T3 (pl) 2007-11-30
TW200503815A (en) 2005-02-01
KR101062153B1 (ko) 2011-09-05
FR2855526A1 (fr) 2004-12-03
JP2007526924A (ja) 2007-09-20
DE602004006266T2 (de) 2008-01-10
JP4669473B2 (ja) 2011-04-13
EP1639062A2 (fr) 2006-03-29
CY1106780T1 (el) 2012-05-23
MXPA05012952A (es) 2006-02-28
CN1813046A (zh) 2006-08-02
ES2286670T3 (es) 2007-12-01
TWI352614B (en) 2011-11-21

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