US20150153101A1 - Method for producing a treated natural gas, a cut rich in c3+ hydrocarbons and optionally an ethane-rich stream, and associated facility - Google Patents

Method for producing a treated natural gas, a cut rich in c3+ hydrocarbons and optionally an ethane-rich stream, and associated facility Download PDF

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Publication number
US20150153101A1
US20150153101A1 US14/412,172 US201314412172A US2015153101A1 US 20150153101 A1 US20150153101 A1 US 20150153101A1 US 201314412172 A US201314412172 A US 201314412172A US 2015153101 A1 US2015153101 A1 US 2015153101A1
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stream
head
natural gas
column
heat exchanger
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Vanessa GAHIER
Fabien Gaël Léo Lacroix
Vincent Patrick Mathieu
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Technip Energies France SAS
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Technip France SAS
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Assigned to TECHNIP FRANCE reassignment TECHNIP FRANCE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: GAHIER, VANESSA, LACROIX, FABIEN GAEL LEO, MATHIEU, VINCENT PATRICK
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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
    • 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
    • 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
    • C10L3/12—Liquefied petroleum 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
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/06—Heat exchange, direct or indirect
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/10—Recycling of a stream within the process or apparatus to reuse elsewhere therein
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/46—Compressors or pumps
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/48—Expanders, e.g. throttles or flash tanks
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/543—Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel
    • 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
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion 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
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • 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
    • F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided

Definitions

  • the present invention relates to a method for simultaneously producing a treated natural gas, a cut rich in C 3 + hydrocarbons, and under at least certain conditions of production, an ethane-rich stream, from an initial natural gas stream containing methane, ethane and C 3 + hydrocarbons, the method comprising the following steps:
  • Such a method is intended for treating a natural gas stream in order to extract at least the C 3 + hydrocarbons therefrom, in order to recover liquids from the natural gas and an adjustable amount of C 2 hydrocarbons.
  • the C 2 and C 3 + hydrocarbons are extracted from the initial natural gas in order to avoid condensation during the transport or/and the handling of the gas. This condensation may lead to the production of liquid plugs in the transport facilities, which is detrimental to production. Further, these hydrocarbons may be marketed with significant merchant value, which contributes to the cost effectiveness of the facilities.
  • Patent U.S. Pat. No. 7,458,232 discloses a solution to this problem, by proposing a method which guarantees optimized extraction of C 3 + hydrocarbons, generally of more than 99%, and which nevertheless attains flexible ethane recoveries comprised, for example, between 2% and 85%, depending on the composition of the load gas.
  • An object of the invention is to obtain a method with which it is possible to obtain in a flexible way ethane extraction rates which may range up to 85%, while notably reducing the energy consumption of the facility.
  • the object of the invention is an insulation of the aforementioned type, characterized in that the method includes the following steps:
  • the method including the sampling in the bottom of the recovery column of at least one bottom reboiling stream, and the establishment of a heat exchange relationship of the bottom reboiling stream with at least one portion of the initial natural gas or/and with the recycling stream, the bottom reboiling being ensured by the calories taken from the initial natural gas stream or/and from the recycling stream.
  • the method according to the invention may comprise one or more of the following features, taken individually or according to all technically possible combinations:
  • the object of the invention is also a facility for simultaneous production of a treated natural gas, of a cut rich in C 3 + hydrocarbons, and under at least certain conditions of production, an ethane-rich stream from an initial natural gas stream containing methane, ethane, and C 3 + hydrocarbons, the facility comprising:
  • the facility according to the invention may comprise one or more of the following features, taken individually or according to all technically possible combinations:
  • FIG. 1 is a functional block diagram of a first facility for applying a first method according to the invention
  • FIG. 2 is a diagram similar to FIG. 1 of a second facility for applying a second method according to the invention
  • FIG. 3 is a diagram similar to FIG. 1 of a third facility for applying a third method according to the invention
  • FIG. 4 is a diagram similar to FIG. 1 of a fourth facility for applying a fourth method according to the invention.
  • FIG. 5 is a diagram similar to FIG. 1 of a fifth facility for applying a fifth method according to the invention.
  • FIG. 6 is a diagram similar to FIG. 1 of a sixth facility, for applying a sixth method according to the invention, the sixth facility resulting from de-bottlenecking of an existing facility.
  • the first facility 11 is intended for simultaneously producing from an initial desulfurized, dry and at least partly decarbonated natural gas stream 13 , a treated natural gas 15 as a main product, a cut 17 of C 3 + hydrocarbons and an ethane-rich stream 19 with adjustable flow rate.
  • the term of “at least partly decarbonated” means that the carbon dioxide content in the initial natural gas stream 13 is advantageously less than or equal to 50 ppm when the treated natural gas 15 has to be liquefied. This content is advantageously less than 3% when the treated natural gas 15 is directly sent to a gas distribution network.
  • the water content is less than 1 ppm, advantageously less than 0.1 ppm.
  • the facility 11 comprises a unit 21 for recovering C 2 + hydrocarbons and a unit 23 for fractionation of C 2 + hydrocarbons.
  • a liquid flow and the conduit which conveys it will be designated by a same reference, the relevant pressures are absolute pressures and the relevant percentages are molar percentages.
  • the unit 21 for recovering C 2 + hydrocarbons successively comprises a first upstream heat exchanger 25 , a first upstream separator flask 27 , a first upstream turbine 29 , coupled with a first compressor 31 , a first head heat exchanger 33 , and a recovery column 35 provided with at least one side reboiling circuit 37 , 39 and with a side reboiling circuit 41 .
  • the column 35 is provided with two side reboiling circuits 37 , 39 .
  • the unit 21 further comprises a second compressor 43 driven by an external energy source and a first cooler 45 placed downstream from the second compressor 43 .
  • the unit 21 also comprises a column bottom pump 47 .
  • the fractionation unit 23 comprises a fractionation column 61 .
  • the column 61 includes at its head, a head condenser 63 and at its foot, a reboiler 65 .
  • the head condenser 63 comprises a second cooler 67 and a first downstream separator flask 69 associated with a reflux pump 71 .
  • An exemplary initial molar composition of the initial desulfurized, dry and at least partly decarbonated natural gas stream 13 is given in the table below.
  • the molar methane fraction in the initial natural gas stream 13 is comprised between 75% and 90%, the molar fraction of C 2 + hydrocarbons is comprised between 5% and 15%, and the molar fraction of C 3 + hydrocarbons is comprised between 1% and 8%.
  • the load flow rate to be treated for example is of the order of 38,000 kmol/h.
  • the initial natural gas stream 13 has a temperature close to room temperature and notably substantially equal to 20° C., and a pressure notably greater than 35 bars.
  • the natural gas stream 13 has a temperature of 20° C. and a pressure of 50 bars absolute.
  • the initial natural gas stream 13 is cooled and at least partly condensed in the first upstream heat exchanger 25 in order to form a cooled initial stream 113 .
  • the cooled initial stream 113 is introduced into the first upstream separator flask 27 in which a separation is performed between a gas phase 115 and a liquid phase 117 .
  • the liquid phase 117 forms, after passing into an expansion valve 119 , an expanded mixed phase 120 which is introduced at a first intermediate level N1 of the recovery column 35 , located in the upper region of the column, above the side reboiling circuits 37 and 39 .
  • intermediate level is meant a location including distillation means above and below this level.
  • the gas fraction 115 is separated into a feed stream 121 and a reflux stream 123 .
  • the molar flow rate of the feed stream 121 is greater than the molar flow rate of the reflux stream 123 .
  • the feed stream 121 is expanded in the turbine 29 down to a pressure close to that of the column 35 in order to obtain an expanded feed stream 125 .
  • the stream 125 is introduced into the recovery column 35 at a second intermediate level N2, located above the first intermediate level N1.
  • the reflux stream 123 is partly or totally condensed in the first head heat exchanger 33 , and is then expanded in an expansion valve 127 in order to form an expanded reflux stream 128 .
  • This stream 128 is introduced into the recovery column 35 at a third intermediate level N3, located above the intermediate level N2.
  • the pressure of the recovery column 35 is for example comprised between 12 and 40 bars.
  • the recovery column 35 produces a head stream 131 which is heated up in the first head heat exchanger 33 by heat exchange with the reflux stream 123 in order to form a partly heated-up head stream 139 .
  • the stream 139 is again heated up in the first upstream heat exchanger 25 by heat exchange with the initial natural gas stream 13 in order to form a heated-up head stream 140 .
  • the heated-up head stream 140 is then compressed in the first compressor 31 , and then in the second compressor 43 , in order to form a compressed head stream 141 .
  • the pressure of the stream 141 is greater than 25 bars, for example equal to 50 bars.
  • the stream 141 is then cooled in the first cooler 45 in order to form the treated natural gas 15 .
  • a recycling stream 152 is sampled in the head stream stemming from the column 35 .
  • the recycling stream 152 is sampled in the compressed heated-up head stream 141 , after its cooling in the first cooler 45 .
  • the ratio of the molar flow rate of the recycling stream 152 , relatively to the molar flow rate of the head stream 131 stemming from the recovery column 35 is comprised between 0% and 25%.
  • the recycling stream 152 is then introduced into the first upstream heat exchanger 25 so as to be cooled therein by heat exchange with at least one portion of the head stream 131 .
  • the stream 152 is placed in a heat exchange relationship with the partly heated-up head stream 139 stemming from the head heat exchanger 33 , in order to form a partly cooled recycling stream 154 .
  • the stream 154 is then introduced into the head heat exchanger 33 , in order to be cooled therein by heat exchange with the head stream 131 , and to form after expansion in a valve 156 , a cooled recycling stream 155 .
  • the cooled recycling stream 155 is introduced into the recovery column 35 at a level N5 located above the level N3, advantageously corresponding to the first stage starting from the top of the column 35 .
  • the treated gas 15 contains in this example 1.36% molar of nitrogen, 96.80% molar of methane and 1.76% molar of C 2 hydrocarbons.
  • the treated gas 15 contains more than 99% molar of the methane contained in the initial natural gas stream 13 and less than 0.1% molar of the C 3 + hydrocarbons contained in the initial natural gas stream.
  • the treated gas 15 contains a molar proportion varying between 2% and 85% of the C 2 hydrocarbons contained in the initial natural gas stream 13 , this proportion being adjustable.
  • the gas 15 thus comprises a content of C 6 + hydrocarbons of less than 1 ppm, a water content of less than 1 ppm, advantageously less than 0.1 ppm and a carbon dioxide content of less than 50 ppm.
  • the treated gas 15 may therefore be directly sent to a liquefaction train in order to produce liquefied natural gas. It may also be directly sent to a gas distribution network.
  • side reboiling streams 161 and 163 are extracted from the column 35 and are reintroduced therein after being heated up in the first upstream heat exchanger 25 , by heat exchange with at least one portion of the initial natural gas stream 13 and at least one portion of the recycling stream 152 .
  • an upper side reboiling stream 163 is sampled at a level N6 located under level N1, for example at the eleventh stage starting from the top of the column 35 , and is then brought as far as the first heat exchanger 25 .
  • the stream 163 is then heated up in the exchanger 25 and then sent back into the column 35 at a level N7 located under the level N6.
  • a lower side reboiling stream 161 is sampled at a level N8 located under the level N7, and is then brought into the heat exchanger 25 .
  • the stream 161 is then heated up in the heat exchanger 25 and is then reintroduced at a level N9 located under the level N8, for example at the fourteenth stage starting from the top of the column 35 .
  • a liquid bottom reboiling stream 165 is extracted in the vicinity of the foot of the column 35 , below the side reboiling streams 161 , 163 .
  • the stream 165 is brought into the first upstream heat exchanger 25 where it is heated up by heat exchange with at least one portion of the initial natural gas stream 13 and at least one portion of the recycling stream 152 .
  • the heated up and partly vaporized bottom reboiling stream is then reintroduced into the column 35 .
  • a bottom stream 171 rich in C 2 + hydrocarbons is extracted from the foot of the recovery column 35 .
  • the bottom stream 171 contains more than 99% molar of C 3 + hydrocarbons contained in the initial natural gas stream 13 . It has a methane content comprised between 9% and 5%.
  • the bottom stream 171 is pumped with the tank bottom pump 47 and introduced at an intermediate level P1 of the fractionation column 61 .
  • the fractionation column 61 operates at a pressure comprised between 20 and 42 bars.
  • the pressure of the fractionation column 61 is greater by at least one bar than the pressure of the recovery column 35 .
  • a foot stream 181 is extracted from the fractionation column 61 in order to form the cut 17 of C 3 + hydrocarbons.
  • the extraction rate of the C 3 + hydrocarbons in the method is greater than 99%. In every case, the propane extraction rate is greater than 99%.
  • the ethane-rich stream 19 is directly drawn off at an intermediate level P2 located in the upper region of the fractionation column 61 .
  • this stream comprises 1.21% of methane, 97.77% of ethane and 1.00% of propane.
  • the molar ethane content in the ethane-rich stream 19 is greater than 95%, notably comprised between 96% and 100%.
  • the number of theoretical plates between the head of the column 61 and the upper level P2 is for example comprised between 1 and 7.
  • the level P2 is above the feed level P1.
  • a second head stream 183 is extracted from the head of the column 61 and is then cooled in the second cooler 67 in order to form a second cooled and at least partly condensed head stream 185 .
  • This second stream 185 is introduced into the second separator flask 69 for producing a liquid fraction 187 and a gas fraction 188 .
  • the totality of the liquid fraction 187 is pumped in the pump 71 in order to form a primary reflux stream 190 before being reintroduced with reflux into the fractionation column 61 at a head level P3 located above the level P2.
  • the totality of the gas fraction 188 forms, after cooling in the head heat exchanger 33 and expansion in a valve 193 , a secondary reflux stream 192 .
  • the gas fraction 188 is cooled by heat exchange with the head stream 131 .
  • the liquid fraction 187 is separated into a liquid primary reflux fraction 189 and a liquid secondary fraction 191 .
  • the secondary liquid fraction 191 when it is present, is then mixed with the gas fraction 188 in order to form after cooling and expansion, the secondary reflux stream 192 .
  • the secondary reflux stream 192 is introduced with reflux at a head level N4 of the recovery column 35 located between the head level N5 and the intermediate level N3.
  • the ethane extraction rate, and subsequently the ethane flow rate produced in the facility 11 is controlled by adjusting the flow rate of the recycling stream 152 , by adjusting the pressure in the recovery column 35 , by means of the compressors 43 and 31 which are of the variable rate type on the one hand, and by finally adjusting the flow rate of the secondary reflux stream 192 circulating through the expansion valve 193 on the other hand.
  • the flow rate of the ethane-rich stream is adjustable, practically without affecting the extraction rate of C 3 + hydrocarbons.
  • the method according to the invention therefore gives the possibility, with simple and inexpensive means, of obtaining a variable and easily adjustable flow rate of an ethane-rich stream 19 extracted from the initial natural gas 13 , by maintaining the extraction rate of propane above 99%. This result is obtained without any significant modification of the facility in which the method is applied.
  • the facility 11 according to the invention moreover does not require the imperative use of multiflow exchangers. It is thus possible to only use exchangers with tubes and a shell.
  • the treated natural gas 15 includes substantially nil contents of C 5 + hydrocarbons, for example less than 1 ppm. Subsequently, if the carbon dioxide content in the treated gas 15 is less than 50 ppm, this gas 15 may be liquefied without any additional treatment or fractionation.
  • the bottom reboiling stream 165 is put into a heat exchange relationship in the first heat exchanger 25 with the recycling stream 152 , with at least one portion of the head stream 131 , with the initial natural gas stream 13 and with the side reboiling streams 161 , 163 .
  • the combined presence of the recycling of a portion of the heated gas and of an integrated bottom reboiling assembly 41 integrated into the first heat exchanger 25 surprisingly generates a larger yield gain than what is observed in the presence of either one of these steps taken individually.
  • the obtained gain is 9.4%
  • the obtained gain is 0.2%.
  • the observed gain by sharing the aforementioned features is therefore notably greater than the sum of the individual gains obtained, demonstrating an unexpected synergistic effect, which does not affect ethane recovery.
  • the treated gas stream stemming from the first compressor 31 may be brought into a compressor 43 with two equivalent power stages, with an intermediate cooler cooling the gas to the same temperature as the cooler 45 .
  • FIG. 2 A second facility 201 according to the invention is illustrated by FIG. 2 .
  • the facility 201 differs from the first facility 11 in that it further includes an auxiliary expansion turbine 203 and an auxiliary compressor 205 coupled with a turbine 203 .
  • the auxiliary compressor 205 is interposed between the first compressor 31 and the second compressor 43 .
  • a second method according to the invention is applied in the second facility 201 .
  • the initial natural gas stream 13 is separated into a first initial stream 207 and a second initial stream 209 .
  • the molar flow rate of the first initial stream 207 is advantageously greater than the molar flow rate of the second initial stream 209 .
  • the first initial stream 207 is introduced into the first heat exchanger 25 so as to be cooled and partly condensed therein and to form the cooled natural gas stream 113 introduced into the first separator flask 27 .
  • the second initial stream 209 is introduced into the auxiliary expansion turbine 203 , so as to be expanded therein down to a pressure close to the operating pressure of the column 35 and to form an auxiliary reflux stream 211 .
  • the auxiliary reflux stream 211 is then introduced into the first head heat exchanger 33 so as to be cooled and partly condensed therein, and then into an expansion valve 213 for forming an expanded auxiliary reflux stream 215 .
  • the stream 215 is then introduced into the recovery column 35 at an upper level N10 located between the level N3 and the level N4.
  • the head stream 217 stemming from the first compressor 31 is introduced, at its outflow from the first compressor 31 , into the auxiliary compressor 205 , so as to be compressed at an intermediate pressure, before joining up with the second compressor 43 .
  • the application of the second method according to the invention produces a result similar to that of the first method, by the synergy observed between the establishment of a heat exchange relationship of the bottom reboiling stream 165 with the initial natural gas stream 13 , taken as a combination with the presence of a recycling stream 152 , put into a heat exchange relationship with at least one portion of the head stream 131 .
  • the consumption of the method for applying the facility 201 leads to a consumed power equal to 37,588 kW, i.e. a gain of 16% as compared with the facility of the state of the art.
  • the auxiliary compressor 205 is mounted downstream from the compressor 43 in order to compress the recycling stream 152 , before introducing it into the first heat exchanger 25 .
  • the facility and the application of the method are moreover similar to the one of FIG. 2 .
  • FIG. 3 A third facility 221 according to the invention is illustrated by FIG. 3 .
  • the facility 221 includes a second upstream separator flask 223 placed downstream from the first separator flask in order to collect the liquid phase 117 stemming from the first separator flask 27 .
  • a third method according to the invention is applied by means of the facility 221 .
  • This third method differs from the first method according to the invention, in that the liquid phase 117 is expanded in a static expansion valve 225 . This expansion is carried out down to a pressure above the operating pressure of the column 35 .
  • the liquid phase is then expanded and introduced into the upstream separator flask 223 .
  • a liquid fraction 227 is recovered at the bottom of the flask 223 and is expanded in a valve 229 in order to form an expanded fraction 231 .
  • the expanded fraction 231 is introduced into the recovery column 35 at level N1.
  • a gas fraction 233 is collected at the head of the second upstream separator flask 223 .
  • This fraction 233 is sent towards the head heat exchanger 33 so as to be cooled therein before being expanded in an expansion valve 135 in order to form an expanded fraction 237 .
  • the expanded fraction 237 is introduced into the recovery column 35 at an intermediate level N11 comprised between the level N2 and the level N3.
  • the method applied by means of a third facility 221 according to the invention leads to a total power consumed by the compressors of 35,960 kW, i.e. a gain of 19.7% relatively to the method of the state of the art.
  • the liquid phase 117 obtained at the foot of the first separator flask 27 is introduced into the first heat exchanger 25 so as to heat it up therein, before being brought into the valve 225 .
  • the mixture is expanded in the valve 225 , before being separated in the second upstream separator flask 223 .
  • FIG. 4 A fourth facility 241 according to the invention is illustrated by FIG. 4 . Unlike the first facility 11 , the stream 171 stemming from the recovery column 35 is passed into the first heat exchanger 25 so as to be heated up therein before being introduced into the fractionation column 61 .
  • the fourth method according to the invention therefore applies heating up of this bottom stream 171 , after its passing into the pump 47 .
  • the total consumption is then of 34,201 kW, which provides a gain of 23.6% as compared with the facility of the state of the art.
  • the gain is moreover 8.6% relatively to the first method according to the invention.
  • FIG. 5 A fifth facility according to the invention 251 is illustrated by FIG. 5 . This facility is intended to apply a fifth method according to the invention.
  • a bypass stream 253 is sampled in the recycling stream 152 , advantageously downstream from the first heat exchanger 25 and upstream from the second heat exchanger 33 , so as to be reintroduced into the stream located downstream from the first dynamic expansion turbine 29 .
  • the bypass stream flow rate 253 is for example equal to 47% of the total molar flow rate of the recycling stream 152 sampled in the treated stream.
  • the fifth method according to the invention is moreover applied similarly to the fourth method according to the invention.
  • bypass stream 253 is mixed with the feed stream 121 before it is introduced into the turbine 29 .
  • the fifth facility 251 further includes a secondary dynamic expansion turbine 255 coupled with a secondary compressor 257 .
  • a secondary recycling stream 258 is then sampled in the recycling stream 152 before its introduction into the first heat exchanger 25 .
  • the secondary recycling stream 258 is introduced into the secondary expansion turbine 255 , in order to form an expanded secondary recycling stream 261 , which is reintroduced into the partly heated-up head stream 139 stemming from the first head heat exchanger 33 .
  • a secondary head stream 263 is sampled in the heated-up head stream 140 stemming from the first heat exchanger 25 so as to be brought as far as the secondary compressor 257 and form a compressed secondary head stream 265 .
  • This stream 265 is then reintroduced into the compressed head stream at an intermediate pressure, stemming from the first compressor 31 upstream from the second compressor 43 .
  • the power gain obtained relatively to the method of the state of the art is then of the order of 15.4%, for a total consumed power of 37,851 kW.
  • FIG. 6 A sixth facility 271 according to the invention is illustrated in FIG. 6 .
  • This facility 271 is intended for de-bottlenecking a facility as illustrated in U.S. Pat. No. 7,458,232 and initially comprising a first upstream heat exchanger 25 , a first separator flask 27 , a recovery column 35 , a first head heat exchanger 33 and a fractionation column 61 provided with a head condenser 63 .
  • the facility 271 further includes a second upstream heat exchanger 273 and a third upstream heat exchanger 275 , intended to be placed in parallel with the first upstream heat exchanger 25 .
  • the facility 271 further includes an auxiliary compressor 277 intended to compress the recycling stream 152 and an auxiliary cooler 279 intended to cool the compressed recycling stream.
  • the sixth facility 271 includes a second head heat exchanger 281 intended to be placed in parallel with the first head heat exchanger 33 , in order to place at least one portion of the head stream 131 in a heat exchange relationship with at least one portion of the recycling stream 152 .
  • a sixth method according to the invention is applied in the sixth facility 271 .
  • the initial natural gas stream 13 is separated into a first initial stream 207 introduced into the first upstream heat exchanger 25 and into a second initial stream 209 introduced into a second upstream heat exchanger 273 .
  • the first initial stream 207 is then cooled in the first upstream heat exchanger 25 in order to form a first cooled initial stream 281 A.
  • the second initial stream 209 is cooled in the second upstream heat exchanger 273 in order to form a second cooled initial stream 283 .
  • the streams 281 A and 283 are mixed so as to form the cooled stream 113 intended to be introduced into the first upstream separator flask 27 .
  • the side reboiling streams 161 , 163 are introduced into the first heat exchanger 25 in order to be heated up therein.
  • the bottom reboiling stream 165 is introduced into the second upstream heat exchanger 273 so as to be heated up therein by heat exchange with the second initial stream 209 .
  • the head stream 131 stemming from the recovery column 35 is first of all separated into a first head stream fraction 285 and a second head stream fraction 287 .
  • the first fraction 285 is introduced into the first head heat exchanger 33 so as to be heated up therein by heat exchange with the reflux stream 123 on the one hand and with the secondary reflux stream 192 on the other hand.
  • the second fraction 287 is introduced into the second head heat exchanger 281 .
  • the ratio of the molar flow rate of the first fraction 285 to the second fraction 287 is for example comprised between 0 and 20.
  • fractions recovered at the outlet of the heat exchangers 33 , 281 are mixed again before being again separated into a first portion 289 of the heated-up head stream and into a second portion 291 of the heated-up head stream.
  • the first portion 289 is introduced into the first upstream heat exchanger 25 so as to be heated up therein by heat exchange with the first initial stream 207 , simultaneously with the side reboiling streams 161 and 163 .
  • the second portion 291 is introduced into the third upstream heat exchanger 275 so as to be heated up therein.
  • the heated-up portions 289 and 291 are then joined together in order to form the heated-up head stream 140 and are then brought to the first compressor 31 .
  • the recycling stream 152 is sampled in the heated head stream 140 upstream from the first compressor 31 .
  • the ratio of the molar flow rate of the recycling stream 152 to the molar flow rate of the head stream 131 stemming from the column 35 is for example comprised between 0% and 25%.
  • the recycling stream 152 is then compressed in the auxiliary compressor 277 , up to a pressure for example greater than 50 bars, and is then cooled in the cooler 279 in order to form a cooled compressed recycling stream 293 .
  • the stream 293 is then successively introduced into the third upstream heat exchanger 275 , and then into the second head heat exchanger 281 so as to be cooled therein, before being expanded in an expansion valve 295 and to form a cooled expanded recycling stream 297 .
  • the stream 297 is then introduced into the recovery column 35 , at the same level as the secondary reflux stream 194 .
  • a portion 207 of the initial natural gas stream 13 , the side reboiling streams 161 , 163 and a portion 289 of the head stream are placed in a heat exchange relationship.
  • a second portion 209 of the initial natural gas stream 13 , and the bottom reboiling stream 165 are placed in a heat exchange relationship.
  • a second portion 291 of the head stream 131 , and the recycling stream 152 are placed in a heat exchange relationship.
  • the facility 271 according to the invention moreover does not require any imperative use of multiflow exchangers. It is thus possible to only use exchangers with tubes and a shell.
  • the reflux stream 123 , a first portion of the head stream 285 , and the secondary reflux stream 192 are placed in a heat exchange relationship in the first head heat exchanger 33 .
  • a second portion 287 of the head stream 131 and the cooled compressed recycling stream 233 are placed in a heat exchange relationship.
  • the facility 271 as illustrated in FIG. 6 gives the possibility of accommodating increases in the feed flow rate from 0% to 15% and more preferentially of at least 10%, by limiting to a minimum the required increase in compression power.
  • the ethane-rich stream 19 is directly sampled in the fractionation column 61 , advantageously at an upper level P2 of the column 61 defined above.
  • the cut of C 3 + hydrocarbons 17 is moreover directly formed by the foot stream 181 of the column 61 .
  • the C 2 + hydrocarbons are extracted from the fractionation column 61 with the foot stream 181 , at the same time as the C 3 + hydrocarbons.
  • the foot stream 181 is then introduced into a downstream fractionation column.
  • the ethane-rich cut 19 like the cut of C 3 + hydrocarbons 17 are then produced in the downstream fractionation column.

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US14/412,172 2012-07-05 2013-07-05 Method for producing a treated natural gas, a cut rich in c3+ hydrocarbons and optionally an ethane-rich stream, and associated facility Abandoned US20150153101A1 (en)

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FR1256488 2012-07-05
FR1256488A FR2992972B1 (fr) 2012-07-05 2012-07-05 Procede de production d'un gaz naturel traite, d'une coupe riche en hydrocarbures en c3+, et eventuellement d'un courant riche en ethane, et installation associee
PCT/EP2013/064238 WO2014006178A1 (fr) 2012-07-05 2013-07-05 Procédé de production d'un gaz naturel traité, d'une coupe riche en hydrocarbures en c3 +, et éventuellement d'un courant riche en éthane, et installation associée

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160327334A1 (en) * 2013-12-26 2016-11-10 Chiyoda Corporation System and method for liquefaction of natural gas
WO2017151147A1 (en) * 2016-03-04 2017-09-08 Pilot Energy Solutions, Llc Flare recovery with carbon capture
WO2017209757A1 (en) * 2016-06-02 2017-12-07 Pilot Energy Solutions, Llc Two column hydrocarbon recovery from carbon dioxide enhanced oil recovery streams
US10352616B2 (en) * 2015-10-29 2019-07-16 Black & Veatch Holding Company Enhanced low temperature separation process
US10852060B2 (en) 2011-04-08 2020-12-01 Pilot Energy Solutions, Llc Single-unit gas separation process having expanded, post-separation vent stream
US20220128299A1 (en) * 2019-08-29 2022-04-28 Exxonmobil Upstream Research Company Liquefaction of Production Gas

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10928128B2 (en) * 2015-05-04 2021-02-23 GE Oil & Gas, Inc. Preparing hydrocarbon streams for storage
MX2020002413A (es) * 2017-09-06 2020-09-17 Linde Eng North America Inc Metodos para proporcionar refrigeracion en plantas de recuperacion de liquidos del gas natural.
FR3088648B1 (fr) * 2018-11-16 2020-12-04 Technip France Procede de traitement d'un flux de gaz d'alimentation et installation associee
CN110185506B (zh) * 2019-05-27 2022-02-08 西南石油大学 一种天然气调压站压力能综合利用系统
CN111253985A (zh) * 2020-03-03 2020-06-09 武汉科技大学 一种用于荒煤气冷却及馏分初步分离的装置及其工艺

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5983664A (en) * 1997-04-09 1999-11-16 Elcor Corporation Hydrocarbon gas processing
US20060144081A1 (en) * 2004-12-22 2006-07-06 Henri Paradowski Method and installation for producing treated natural gas, a C3+ hydrocarbon cut and an ethane rich stream
US20100011810A1 (en) * 2005-07-07 2010-01-21 Fluor Technologies Corporation NGL Recovery Methods and Configurations
US20100263407A1 (en) * 2009-04-21 2010-10-21 Henri Paradowski Method for producing a flow which is rich in methane and a cut which is rich in c2+ hydrocarbons from a flow of feed natural gas and an associated installation
US20130014390A1 (en) * 2011-06-20 2013-01-17 Fluor Technologies Corporation Configurations and methods for retrofitting an ngl recovery plant

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2578637B1 (fr) 1985-03-05 1987-06-26 Technip Cie Procede de fractionnement de charges gazeuses et installation pour l'execution de ce procede
US6116050A (en) * 1998-12-04 2000-09-12 Ipsi Llc Propane recovery methods
US7051553B2 (en) * 2002-05-20 2006-05-30 Floor Technologies Corporation Twin reflux process and configurations for improved natural gas liquids recovery
RU2434671C1 (ru) * 2010-05-11 2011-11-27 Учреждение Российской Академии Наук Институт Сильноточной Электроники Сибирского Отделения Ран (Исэ Со Ран) Способ получения конденсата и осушки природного газа и проточный реактор для его осуществления

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5983664A (en) * 1997-04-09 1999-11-16 Elcor Corporation Hydrocarbon gas processing
US20060144081A1 (en) * 2004-12-22 2006-07-06 Henri Paradowski Method and installation for producing treated natural gas, a C3+ hydrocarbon cut and an ethane rich stream
US20100011810A1 (en) * 2005-07-07 2010-01-21 Fluor Technologies Corporation NGL Recovery Methods and Configurations
US20100263407A1 (en) * 2009-04-21 2010-10-21 Henri Paradowski Method for producing a flow which is rich in methane and a cut which is rich in c2+ hydrocarbons from a flow of feed natural gas and an associated installation
US20130014390A1 (en) * 2011-06-20 2013-01-17 Fluor Technologies Corporation Configurations and methods for retrofitting an ngl recovery plant

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10852060B2 (en) 2011-04-08 2020-12-01 Pilot Energy Solutions, Llc Single-unit gas separation process having expanded, post-separation vent stream
US20160327334A1 (en) * 2013-12-26 2016-11-10 Chiyoda Corporation System and method for liquefaction of natural gas
US10352616B2 (en) * 2015-10-29 2019-07-16 Black & Veatch Holding Company Enhanced low temperature separation process
WO2017151147A1 (en) * 2016-03-04 2017-09-08 Pilot Energy Solutions, Llc Flare recovery with carbon capture
WO2017209757A1 (en) * 2016-06-02 2017-12-07 Pilot Energy Solutions, Llc Two column hydrocarbon recovery from carbon dioxide enhanced oil recovery streams
US10844304B2 (en) 2016-06-02 2020-11-24 Pilot Energy Solutions, Llc Two column hydrocarbon recovery from carbon dioxide enhanced oil recovery streams
US10899987B2 (en) 2016-06-02 2021-01-26 Pilot Energy Solutions, Llc Two column hydrocarbon recovery from carbon dioxide enhanced oil recovery streams
US20220128299A1 (en) * 2019-08-29 2022-04-28 Exxonmobil Upstream Research Company Liquefaction of Production Gas
US11927391B2 (en) * 2019-08-29 2024-03-12 ExxonMobil Technology and Engineering Company Liquefaction of production gas

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EP2870226A1 (fr) 2015-05-13
FR2992972A1 (fr) 2014-01-10
EP2870226B1 (fr) 2017-05-31
AR093223A1 (es) 2015-05-27
FR2992972B1 (fr) 2014-08-15
CA2878125C (fr) 2020-09-22
CA2878125A1 (fr) 2014-01-09
MX2015000147A (es) 2015-04-10
WO2014006178A1 (fr) 2014-01-09
AP2015008259A0 (en) 2015-02-28
RU2015103754A (ru) 2016-08-27

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