WO2017157817A1 - Procédé de séparation d'une fraction riche en éthane du gaz naturel - Google Patents

Procédé de séparation d'une fraction riche en éthane du gaz naturel Download PDF

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Publication number
WO2017157817A1
WO2017157817A1 PCT/EP2017/055770 EP2017055770W WO2017157817A1 WO 2017157817 A1 WO2017157817 A1 WO 2017157817A1 EP 2017055770 W EP2017055770 W EP 2017055770W WO 2017157817 A1 WO2017157817 A1 WO 2017157817A1
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WIPO (PCT)
Prior art keywords
fraction
methane
rectification column
feed
rich gas
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Application number
PCT/EP2017/055770
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English (en)
Inventor
Heinz Bauer
Original Assignee
Linde Aktiengesellschaft
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Filing date
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Publication of WO2017157817A1 publication Critical patent/WO2017157817A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/09—Purification; Separation; Use of additives by fractional condensation
    • 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
    • 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
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2270/08—Internal refrigeration by flash gas recovery 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
    • F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided

Definitions

  • the invention relates to a method for separating a C 2+ rich fraction from a hydrocarbon- rich feed, preferably a natural gas.
  • natural gas mainly consists of hydrocarbons. After methane, ethane usually has the second highest molar concentration.
  • the extraction of technically pure ethane from natural gas is an important technology to supply so-called gas crackers with the feedstock for to provide production of ethylene.
  • the term "technically pure ethane” is to be understood as meaning a fraction high in ethane with an ethane concentration of >95 mol%, preferably >98 mol%.
  • the recovery of a C 2+ fraction from natural gas is usually achieved by a combination of partial condensation and rectification using heat exchanger networks.
  • GSP Gas Subcooled Process
  • Such separation method performs the intersection between methane and lighter components, such as nitrogen, ethane and heavier components, such as propane and higher hydrocarbons.
  • the feed gas is decomposed by a demethanizer into a methane-rich light sales gas (gas high in methane) and a C 2 + rich liquid (liquid C 2+ fraction).
  • the further separation of the C 2+ fraction in fractions of the desired composition takes place in a chain from the distillation columns connected downstream of the demethanizer.
  • the above-mentioned refrigeration system is usually carried out as a closed propane or propylene refrigeration system (hereinafter referred to as a C 3 refrigeration system), in which the refrigerant is condensed under high pressure against its ambient and then evaporated at lower pressure. The evaporation can also take place in several pressure stages, if the refrigerating capacity is required at different temperatures.
  • C 3 refrigerators have the following disadvantages: - the condensation of the refrigerant requires a lot of energy of the control unit at the circulating compressor in the case of strongly fluctuating ambient temperatures (due to seasonal and/or day/night changes) to ensure the respectively optimal condensation pressure. If the final pressure of the refrigeration compressor is too low, the condensation cannot take place and the refrigeration system will not work. If, on the other hand, the final pressure is too high, energy is unnecessarily consumed and operating expenses are increased. If a C 3 refrigeration system is used, for example, at a location with a
  • the optimum final pressure can vary between 5 and 20 bar.
  • the achievable final temperature of a C 3 refrigeration system is limited to -40 ° C, since lower pressure at the compressor suction side can occur at lower evaporation temperatures, which can lead to a safety-related undesirable entry of oxygen from the air.
  • a method for separating a fraction high in C 2+ from a feed high in hydrocarbon is proposed in accordance with claim 1.
  • the refrigerating capacity required for the separation process is not provided by a closed refrigeration system with phase change but instead by an open refrigeration circuit by work-performing expansion exclusively in the gas phase.
  • a hydrocarbon rich feed preferably from natural gas
  • the method comprises:
  • the gas fraction high in methane obtained during C 2 + separation is compressed as a sales gas (to be supplied onwards for storage or consumption) to a pressure which is at least 10 bar, preferably at least 20 bar, above the operating pressure of the rectification column.
  • a sales gas to be supplied onwards for storage or consumption
  • the gas fraction high in methane is compressed to at least 50 bar, preferably more than 60 bar. This means that the pressure of the sales gas is thus clearly above the maximum operating pressure of the rectification column or of the demethanizer, which is approximately 35 bar.
  • the pressure difference between the suction side and the pressure side of the compressor required for the compression of the gas fraction high in methane is utilized according to the invention to operate a work-performing expander in which a partial flow of the previously compressed gas fraction high in methane is expanded.
  • temperatures of -40 ° C can also be reached at the outlet of expander X2 by adjusting the inlet temperature at the expander.
  • the mechanical power of at least one expander (used for the work-performing expansion) may be used to drive at least one generator.
  • the power produced in the generator during normal operation may be fed into one or more of the following: an existing external network, an existing process, a system mains supply.
  • the mechanical power of at least one expander (used for the work-performing expansion) may be used to drive at least one compressor).
  • the rectification column may be operated at a pressure of between 15 and 35 bar.
  • step (h) the methane-rich fraction high may be compressed to a pressure of at least 50 bar. In step (h) the methane-rich fraction high may be compressed to a pressure of at least 60 bar.
  • the feed (to be partially condensed) may have a pressure between 30 and 100 bar.
  • the method may further include liquefying and supercooling the second partial flow of the compressed methane-rich gas fraction against the gaseous methane-rich gas fraction which has been withdrawn from the rectification column.
  • the method may further include feeding the liquefied and supercooled stream to the rectification column as additional reflux.
  • step (e) the partial stream of the gaseous fraction, which is expanded to the pressure of the rectification column, may be expanded in working condition.
  • the upper limit of the operating pressure of the rectification column is predetermined by the required density difference (>250 kg/m 3 , preferably >280 kg/m 3 ) between the liquid phase and the gas phase on the column bottoms of the rectification column.
  • the refrigerant capacity of the expander is reduced, in which at least 60 to 90% of the gaseous fraction is depressurized to the pressure of the rectification column.
  • this can be compensated for without limitation with regards to power and temperature level by the additional expander which serves as a work-performing expansion of the partial flow of the compressed gas fraction high in methane.
  • a partial stream of the sales gas which is not expanded to produce work, can be cooled, liquefied, supercooled and subsequently fed to the rectification column as an additional reflux. This procedure improves the C 2+ yield of the process according to the invention.
  • FIG. 1 shows an embodiment of the invention.
  • the apparatus shown in Figure 1 includes: rectification column (or a demethanizer) T; separator D; a first multi-stream heat exchanger E1 ; a second multi-stream heat exchanger E2; compressors C and C; a generator G, an expansion turbine X1 ; a first expansion valve V1 ; a second expansion valve V2; a third expansion valve V3; a first expander E1 ; a second expander E2; and an aftercooler E4
  • the feed gas 1 is high in hydrocarbon. It is preferably natural gas and which is usually at a pressure of at least 50 bar.
  • the feed gas 1 is partially condensed in the first multi- stream heat exchanger E1 against process streams to be described later.
  • the partially condensed flow is then fed to the separator D via line 1 ', where it is separated into a liquid fraction 4 and a gaseous fraction 3.
  • the liquid fraction of the feed obtained in the partial condensation is fed to the rectification column (or a demethanizer) T via line 4 and expansion valve V2.
  • a fraction of at least 60% to 90% of the gaseous fraction 2 obtained in the partial condensation of the feed 1 is expanded in the expansion turbine X1 to the pressure of the rectification column T and fed via line 2'.
  • mechanical power from the expansion turbine X1 of the gaseous fraction 2 is used for generating current in a generator G.
  • the work-performing expansion X1 of the gaseous fraction 2 can also be used to compress a gas fraction high in methane 8 in a compressor, which is described below.
  • the power produced in the generator during normal operation is fed for use as required.
  • the power may be fed into one or more of the following: an existing external network, an existing process, a system mains supply.
  • the remaining gas phase portion 3 withdrawn from the separator D is completely liquefied in the second heat exchanger E2 against a methane-rich gas fraction 7 (gas fraction high in methane)withdrawn from the rectification column ,T to produce a liquefied portion 3'.
  • the methane-rich gas fraction 7 is heated to form the heated methane-rich gas fraction 8.
  • the liquefied portion is fed to the rectification column T as a reflux via line 3' and expansion valve V1.
  • At least one side stream 6 is also withdrawn from the rectification column T at a suitable point, partially evaporated in the multi-stream heat exchanger E1 , and fed again to the rectification column T below its withdrawal point.
  • the partial evaporation of at least one further side stream can be realized in the multi-flow heat exchanger E1 (not shown in the figure).
  • the rectification column T is usually operated at a pressure of between 15 and 35 bar.
  • a liquid fraction 5 high in C 2+ is withdrawn from the bottom of the rectification column T.
  • a partial stream of this liquid fraction 5 is partially evaporated in the reboiler E3 and fed back to the rectification column T via line 5'.
  • liquid fraction 5 is fed to a further separation stage, and the resulting liquid phase is further processed in the reboiler and fed back to the rectification column (as described above).
  • the maximum operating pressure of the rectification column T is generally approximately 35bar.
  • a partial stream 10 of the compressed gas fraction high in methane which is not required for further use, is fed back.
  • the stream 10 which is fed back is split into a first partial stream 1 1 and a second partial stream 12.
  • the first partial stream 1 1 is cooled in the heat exchanger E1 .
  • the cooled first partial stream is expanded in the expander X2 and fed to be combined with the methane rich fraction 7 which has been withdrawn from the rectification column to form a combined flow 7'.
  • the combined flow T is then fed to the first heat exchanger E1 and against the feed flow 1.
  • the second partial stream 12 of the compressed gas fraction high in methane is cooled, liquefied, supercooled in the heat exchangers E1 and E2 against the gas fraction high in methane 7, 7" It is then fed to the rectification column T via the expansion valve V3 as a further reflux. This causes the C 2 + yield to be increased.
  • the work-sustained expansion of the gaseous fraction 2 in expander X1 can be used to compress the heated gas fraction 8 high in methane. In other words it can be used to drive at least one of the compressors C, C.
  • the supercharging stage compressor C is advantageously designed in such a way that it is driven exclusively by the expander X1 or the power obtained in it. In principle, it is also possible, alternatively or additionally, to operate a post-compressor stage in the same way.
  • the mechanical power from expander X1 is supplied to the generator A.
  • the mechanical power from the expander X2 is additionally supplied to the same generator or is supplied to a second generator.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Water Supply & Treatment (AREA)
  • Mechanical Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

L'invention concerne un procédé de séparation d'une fraction riche en C2+ à partir d'une alimentation riche en hydrocarbures, de préférence à partir de gaz naturel. Le procédé consiste à condenser partiellement l'alimentation dans un premier échangeur de chaleur afin de produire une alimentation condensée ; à séparer l'alimentation condensée en une fraction gazeuse et une fraction liquide dans un séparateur. La fraction gazeuse et la fraction liquide sont séparées de manière rectifiée dans une colonne de rectification, et la fraction gazeuse est divisée en une première fraction gazeuse et une fraction gazeuse restante. Le procédé consiste à dépressuriser la première fraction gazeuse à la pression de la colonne de rectification avant de l'alimenter à la colonne de rectification, et à liquéfier la fraction gazeuse restante contre la fraction gazeuse riche en méthane puis à alimenter la fraction gazeuse liquéfiée à la colonne de rectification en tant que reflux, l'alimentation au premier échangeur de chaleur étant partiellement condensée contre la fraction gazeuse riche en méthane produisant ainsi une fraction gazeuse riche en méthane chauffée. Ensuite, la fraction gazeuse riche en méthane chauffée est comprimée à une pression d'au moins 10 bars au-dessus de la pression de fonctionnement de la colonne de rectification, puis divisée en un premier écoulement partiel et un second écoulement partiel. Le procédé consiste à provoquer l'expansion du premier écoulement partiel de la fraction gazeuse riche en méthane comprimé au moyen d'une réalisation de travail, à introduire l'écoulement expansé afin de rejoindre la fraction gazeuse riche en méthane pour former un écoulement combiné, puis à soumettre l'écoulement combiné à un échange de chaleur avec la fraction d'alimentation.
PCT/EP2017/055770 2016-03-17 2017-03-13 Procédé de séparation d'une fraction riche en éthane du gaz naturel WO2017157817A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016003305.3 2016-03-17
DE102016003305.3A DE102016003305A1 (de) 2016-03-17 2016-03-17 Verfahren zum Abtrennen einer ethanreichen Fraktion aus Erdgas

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WO2017157817A1 true WO2017157817A1 (fr) 2017-09-21

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Cited By (2)

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Publication number Priority date Publication date Assignee Title
EP3771872A1 (fr) * 2019-08-02 2021-02-03 Linde GmbH Procédé et installation de fourniture d'un produit de gaz naturel
CN112781320A (zh) * 2019-11-05 2021-05-11 东洋工程株式会社 用于分离烃的方法和装置

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WO2000034724A1 (fr) * 1998-12-04 2000-06-15 Ipsi, Llc Procedes perfectionnes de recuperation de propane
US20110005273A1 (en) * 2009-07-09 2011-01-13 Gahier Vanessa Method for producing a flow rich in methane and a flow rich in c2+ hydrocarbons, and associated installation
US20130255311A1 (en) * 2010-10-20 2013-10-03 Sandra Armelle Karen Thiebault Simplified method for producing a methane-rich stream and a c2+ hydrocarbon-rich fraction from a feed natural-gas stream, and associated facility
DE102012017486A1 (de) * 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zum Abtrennen von C2+-Kohlenwasserstoffen aus einer Kohlenwasserstoff-reichen Fraktion

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Patent Citations (4)

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Publication number Priority date Publication date Assignee Title
WO2000034724A1 (fr) * 1998-12-04 2000-06-15 Ipsi, Llc Procedes perfectionnes de recuperation de propane
US20110005273A1 (en) * 2009-07-09 2011-01-13 Gahier Vanessa Method for producing a flow rich in methane and a flow rich in c2+ hydrocarbons, and associated installation
US20130255311A1 (en) * 2010-10-20 2013-10-03 Sandra Armelle Karen Thiebault Simplified method for producing a methane-rich stream and a c2+ hydrocarbon-rich fraction from a feed natural-gas stream, and associated facility
DE102012017486A1 (de) * 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zum Abtrennen von C2+-Kohlenwasserstoffen aus einer Kohlenwasserstoff-reichen Fraktion

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3771872A1 (fr) * 2019-08-02 2021-02-03 Linde GmbH Procédé et installation de fourniture d'un produit de gaz naturel
CN112781320A (zh) * 2019-11-05 2021-05-11 东洋工程株式会社 用于分离烃的方法和装置
JP2021076261A (ja) * 2019-11-05 2021-05-20 東洋エンジニアリング株式会社 炭化水素の分離方法及び分離装置
JP7390860B2 (ja) 2019-11-05 2023-12-04 東洋エンジニアリング株式会社 炭化水素の分離方法及び分離装置

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