EP1834144B1 - Procede de separation d'une fraction riche en c2+ a partir de gnl - Google Patents

Procede de separation d'une fraction riche en c2+ a partir de gnl Download PDF

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Publication number
EP1834144B1
EP1834144B1 EP05823015.2A EP05823015A EP1834144B1 EP 1834144 B1 EP1834144 B1 EP 1834144B1 EP 05823015 A EP05823015 A EP 05823015A EP 1834144 B1 EP1834144 B1 EP 1834144B1
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Prior art keywords
fraction
separation
rich
rectification
natural gas
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EP05823015.2A
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German (de)
English (en)
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EP1834144A1 (fr
Inventor
Heinz Bauer
Hubert Franke
Rainer Sapper
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Linde GmbH
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Linde GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • 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
    • 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
    • F25J3/0214—Liquefied 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
    • F25J3/0238—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
    • 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
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the 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
    • 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
    • F25J2200/72—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
    • 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
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream

Definitions

  • the invention relates to a method for separating a C 2+ -rich fraction from liquefied natural gas (LNG) according to the preamble of claim 1.
  • LNG liquefied natural gas
  • Generic methods are to be provided, for example, when the calorific value of liquefied natural gas does not correspond to the desired specifications of the pipeline network into which the natural gas is to be fed.
  • a calorific value-lowering component for example nitrogen
  • components which cause an increase in the calorific value are removed from the liquefied natural gas.
  • Object of the present invention is to provide a generic method for separating a C 2+ -rich fraction of liquefied natural gas (LNG), the an increase in the yield of C 2+ -rich fraction while reducing the investment and operating costs of the process, in particular the absence of compression of the methane-rich gas fraction allows.
  • LNG liquefied natural gas
  • the first C 1 -rich gas fraction obtained in the separation of the partially vaporized natural gas is now reliquefied and at least partially fed to the rectification separation as reflux.
  • the cold required for the re-liquefaction of the first C 1 -rich gas fraction can be provided exclusively by the liquid natural gas stream, which is subjected to heating up to at most the boiling point. Since the rectification separation discontinued as reflux C 1 -rich gas fraction has a relatively low ethane content, a back washing of ethane and heavier components from the overhead product of the rectification separations and thus the desired increase in C is effected 2+ yield through it.
  • the process according to the invention therefore makes it possible to realize ethane yields of more than 90% in an economically sensible procedure.
  • This value is in the range of ethane yield, as with the complex process according to US-A 5,114,451 can be achieved, but well above the value in a process according to US-A 3,420,068 ,
  • the partially vaporized natural gas stream is fed via line 2 to a separator D1.
  • a separation of the partially evaporated natural gas stream into a first C 1 -rich gas fraction, which is withdrawn at the top of the separator D1 via line 4, and a first C 2+ -rich liquid fraction.
  • the latter is supplied via line 3, in which a pump P3 is provided to the separation column T and thus the rectification separation.
  • separator D1 can be provided a rectification column, in which the separation of the partially vaporized natural gas 2 is realized.
  • the feed of the partially evaporated natural gas stream 2 would take place in the bottom of the rectification column.
  • the required column reflux can be realized either by means of a withdrawn from the still to be described line 6 stream or from the still to be described line 8 after the heat exchanger E2 and before the valve c withdrawn stream.
  • the separation column T may have bottoms and / or packings.
  • the aforementioned second C 2+ -rich liquid fraction is withdrawn via the line 10, in which a control valve e is provided, from the bottom of the separation column T and discharged from the process as so-called NGL ( N atural G as L iquids) fraction possibly fed to another use.
  • NGL N atural G as L iquids
  • a partial stream of this fraction is partially evaporated in the heat exchanger E3 and fed via line 11 as a reboiler stream of the separation column T.
  • the rectification separation is carried out T at a higher pressure than the separation D1 of the partially evaporated natural gas 2 into a first gas fraction rich in C 1 4, and a first liquid fraction rich in C 2 + 3.
  • the separation or separator D1 preferably a pressure between 15 and 25 bar and in the rectificatory separation T preferably a pressure between 30 and 40 bar realized.
  • a pump P3 is to be provided in line 3.
  • the recovered in the rectification separation T second C 1 -rich gas fraction is withdrawn at the top of the separation column T via line 8 and in the heat exchanger E2 against the natural gas to be heated 1 'at least partially, but preferably completely reliquefied and via line 8', in which a control valve c is arranged, fed to a pump reservoir D2. This is via line section 7, in which also a control valve b is arranged, the one Partial flow of the first recycled liquefied C 1 -rich fraction fed, which is not the separation column T is charged as reflux.
  • the C 2+ -depleted LNG product fraction is pumped to the desired discharge or pipeline pressure by means of the pump P 4 - this is usually pumped between 50 and 150 bar and via line 9, in which also a control valve a is discharged from the process.
  • the second C 2+ -rich liquid fraction is subjected to a (second) rectification C 2 / C 3 separation in the separation column T '.
  • a C 3+ -rich LPG product fraction is withdrawn via line 18, a C 3+ -rich LPG product fraction and possibly fed to further processing or use.
  • a partial stream of this fraction is partially evaporated in the heat exchanger E5 and fed via line 19 as a reboiler stream of the separation column T '.
  • the condensed C 2 / C 3 -rich fraction via line 15 of the pump P 5 is supplied and pumped by this to the desired discharge pressure.
  • a side stream of the pumped fraction is fed via line 16 and control valve f the head of the separation column T 'as reflux, while the main flow of the pumped fraction removed via line 17 from the process and optionally fed to further use or processing.
  • the inventive method for separating a fraction rich in C 2+ of liquefied natural gas it is proposed that the cooling of process streams resulting 2+ -rich liquid fraction from the separation T 'of the second C, calcareous against the first liquid fraction C 2+ and / or against at least one liquid fraction which is withdrawn from the rectification separation below the feed of the first C 2+ -rich liquid fraction.
  • the heat exchanger required for this purpose can be provided for example between the pump P3 and the separation column T.
  • a temperature of about -100 ° C is required.
  • the inventive method for separating a C 2+ -rich fraction from liquefied natural gas (LNG) allows the realization of high Ethanausbeuten while dispensing with expensive compressors.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Claims (9)

  1. Procédé de séparation d'une fraction riche en C2+ à partir de gaz naturel liquéfié (GNL), comprenant les étapes de procédé suivantes :
    a) l'évaporation partielle (E1, E2) du gaz naturel liquéfié (1, 1'),
    b) la séparation (D) du gaz naturel partiellement évaporé (2) en une première fraction de gaz riche en C1 (4) et une première fraction de liquide riche en C2+ (3),
    c) la séparation par rectification (T) de la première fraction de liquide riche en C2+ (3) en une deuxième fraction de gaz riche en C1 (8) et une deuxième fraction de liquide riche en C2+ (10),
    d) la reliquéfaction (E1) de la première fraction de gaz riche en C1 (4) par échange de chaleur avec le gaz naturel liquéfié à évaporer (1), caractérisé en ce que
    e) au moins un courant partiel de la fraction de gaz riche en C1 reliquéfiée (5) est introduit en tant que reflux dans la séparation par rectification (T).
  2. Procédé selon la revendication 1, caractérisé en ce que la séparation par rectification (T) a lieu à une pression plus élevée que la séparation (D1) du gaz naturel partiellement évaporé (2) en une première fraction de gaz riche en C1 (4) et une première fraction de liquide riche en C2+ (3).
  3. Procédé selon la revendication 2, caractérisé en ce que la séparation (D1) du gaz naturel partiellement évaporé (2) en une première fraction de gaz riche en C1 (4) et une première fraction de liquide riche en C2+ (3) a lieu dans une plage de pression comprise entre 15 et 25 bar et la séparation par rectification (T) dans une plage de pression comprise entre 30 et 40 bar.
  4. Procédé selon l'une quelconque des revendications 1 à 3 précédentes, caractérisé en ce que le courant partiel (7) de la fraction de gaz riche en C1 reliquéfiée (5) qui n'est pas introduit dans la séparation par rectification (T) en tant que reflux est réuni avec la deuxième fraction de gaz riche en C1 (8, 8') obtenue dans la séparation par rectification (T).
  5. Procédé selon l'une quelconque des revendications 1 à 4 précédentes, caractérisé en ce que la deuxième fraction de gaz riche en C1 (8) obtenue dans la séparation par rectification (T) est au moins partiellement reliquéfiée (E2), cette reliquéfaction ayant de préférence lieu par échange de chaleur avec le gaz naturel liquéfié à évaporer (1').
  6. Procédé selon l'une quelconque des revendications 1 à 5 précédentes, caractérisé en ce que le refroidissement de courants de procédé qui résultent de la séparation de la deuxième fraction de liquide riche en C2+ (10) a lieu avec la première fraction de liquide riche en C2+ (3) et/ou avec au moins une fraction de liquide (13) qui est soutirée à partir de la séparation par rectification (T) en dessous de l'alimentation de la première fraction de liquide riche en C2+ (3).
  7. Procédé selon l'une quelconque des revendications 1 à 6 précédentes, dans lequel la deuxième fraction de liquide riche en C2+ (10) est soumise à une séparation des C2/C3 par rectification (T'), caractérisé en ce que la condensation de tête de la séparation des C2/C3 (T') a lieu dans un rebouilleur latéral (E4) avec au moins une fraction de liquide (13), qui est soutirée à partir de la séparation par rectification (T) en dessous de l'alimentation de la première fraction de liquide riche en C2+ (3).
  8. Procédé selon l'une quelconque des revendications 1 à 7 précédentes, dans lequel la deuxième fraction de liquide riche en C2+ (10) est soumise à une séparation des C2/C3 par rectification (T'), caractérisé en ce que la fraction de gaz riche en C2/C3 (12) obtenue dans la séparation des C2/C3 par rectification est refroidie par échange de chaleur avec la première fraction de liquide riche en C2+ (3), de préférence à une température de stockage sans pression.
  9. Procédé selon l'une quelconque des revendications 1 à 8 précédentes, caractérisé en ce que la séparation (D1) du gaz naturel partiellement évaporé (2) en une première fraction de gaz riche en C1 (4) et une première fraction de liquide riche en C2+ (3) a lieu dans un séparateur ou une colonne de rectification.
EP05823015.2A 2005-01-03 2005-12-21 Procede de separation d'une fraction riche en c2+ a partir de gnl Active EP1834144B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102005000634A DE102005000634A1 (de) 2005-01-03 2005-01-03 Verfahren zum Abtrennen einer C2+-reichen Fraktion aus LNG
PCT/EP2005/013748 WO2006072390A1 (fr) 2005-01-03 2005-12-21 Procede de separation d'une fraction riche en c2+ a partir de gnl

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Publication Number Publication Date
EP1834144A1 EP1834144A1 (fr) 2007-09-19
EP1834144B1 true EP1834144B1 (fr) 2018-02-28

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US (1) US20090211296A1 (fr)
EP (1) EP1834144B1 (fr)
JP (1) JP2008527287A (fr)
KR (1) KR101236863B1 (fr)
CN (1) CN101095023B (fr)
BR (1) BRPI0518529B1 (fr)
DE (1) DE102005000634A1 (fr)
ES (1) ES2665688T3 (fr)
MX (1) MX2007006584A (fr)
WO (1) WO2006072390A1 (fr)

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7603867B2 (en) * 2006-09-11 2009-10-20 Cryogenic Group, Inc. Process and system to produce multiple distributable products from source, or imported LNG
US8820096B2 (en) 2007-02-12 2014-09-02 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US7644676B2 (en) 2008-02-11 2010-01-12 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
KR20090107805A (ko) 2008-04-10 2009-10-14 대우조선해양 주식회사 천연가스 발열량 저감방법 및 장치
JP5686989B2 (ja) * 2010-05-13 2015-03-18 エア・ウォーター株式会社 自動車用液化天然ガスの製法
DE102012021637A1 (de) * 2012-11-02 2014-05-08 Linde Aktiengesellschaft Verfahren zum Abkühlen einer Kohlenwasserstoff-reichen Fraktion

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006066015A2 (fr) * 2004-12-16 2006-06-22 Fluor Technologies Corporation Conceptions et procedes de regasification de lng et commande de btu
WO2006118583A1 (fr) * 2004-07-01 2006-11-09 Ortloff Engineers, Ltd. Traitement de gaz naturel liquefie

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1501013A (fr) * 1966-09-13 1967-11-10 Air Liquide Procédé de production d'un gaz riche en méthane, sous pression élevée à partirde gaz naturel liquide sous basse pression
US5114451A (en) * 1990-03-12 1992-05-19 Elcor Corporation Liquefied natural gas processing
US6116050A (en) * 1998-12-04 2000-09-12 Ipsi Llc Propane recovery methods
US6742358B2 (en) * 2001-06-08 2004-06-01 Elkcorp Natural gas liquefaction
FR2831656B1 (fr) * 2001-10-31 2004-04-30 Technip Cie Procede et installation de separation d'un gaz contenant du methane et de l'ethane a deux colonnes fonctionnant sous deux pressions differentes
US6941771B2 (en) 2002-04-03 2005-09-13 Howe-Baker Engineers, Ltd. Liquid natural gas processing
US6564579B1 (en) * 2002-05-13 2003-05-20 Black & Veatch Pritchard Inc. Method for vaporizing and recovery of natural gas liquids from liquefied natural gas
US7051553B2 (en) * 2002-05-20 2006-05-30 Floor Technologies Corporation Twin reflux process and configurations for improved natural gas liquids recovery
US6907752B2 (en) * 2003-07-07 2005-06-21 Howe-Baker Engineers, Ltd. Cryogenic liquid natural gas recovery process
US7155931B2 (en) * 2003-09-30 2007-01-02 Ortloff Engineers, Ltd. Liquefied natural gas processing
US7278281B2 (en) * 2003-11-13 2007-10-09 Foster Wheeler Usa Corporation Method and apparatus for reducing C2 and C3 at LNG receiving terminals
MX2007002797A (es) * 2004-09-14 2007-04-23 Exxonmobil Upstream Res Co Metodo para extraer etano del gas natural licuado.
CN101460800B (zh) * 2006-06-02 2012-07-18 奥特洛夫工程有限公司 液化天然气的处理

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006118583A1 (fr) * 2004-07-01 2006-11-09 Ortloff Engineers, Ltd. Traitement de gaz naturel liquefie
WO2006066015A2 (fr) * 2004-12-16 2006-06-22 Fluor Technologies Corporation Conceptions et procedes de regasification de lng et commande de btu

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US20090211296A1 (en) 2009-08-27
CN101095023B (zh) 2010-12-22
DE102005000634A1 (de) 2006-07-13
BRPI0518529A2 (pt) 2008-11-25
JP2008527287A (ja) 2008-07-24
CN101095023A (zh) 2007-12-26
BRPI0518529B1 (pt) 2018-06-26
EP1834144A1 (fr) 2007-09-19
KR101236863B1 (ko) 2013-02-26
WO2006072390A1 (fr) 2006-07-13
ES2665688T3 (es) 2018-04-26
KR20070100760A (ko) 2007-10-11
MX2007006584A (es) 2007-07-13

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