WO2008022998A2 - Procédé et appareil permettant de traiter un courant d'hydrocarbures - Google Patents

Procédé et appareil permettant de traiter un courant d'hydrocarbures Download PDF

Info

Publication number
WO2008022998A2
WO2008022998A2 PCT/EP2007/058648 EP2007058648W WO2008022998A2 WO 2008022998 A2 WO2008022998 A2 WO 2008022998A2 EP 2007058648 W EP2007058648 W EP 2007058648W WO 2008022998 A2 WO2008022998 A2 WO 2008022998A2
Authority
WO
WIPO (PCT)
Prior art keywords
stream
gas
liquid separator
feeding point
liquid
Prior art date
Application number
PCT/EP2007/058648
Other languages
English (en)
Other versions
WO2008022998A3 (fr
Inventor
Eduard Coenraad Bras
Jill Hui Chiun Chieng
Akash Damodar Wani
Original Assignee
Shell Internationale Research Maatschappij B.V.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shell Internationale Research Maatschappij B.V. filed Critical Shell Internationale Research Maatschappij B.V.
Priority to US12/438,032 priority Critical patent/US20100162753A1/en
Priority to CN2007800310082A priority patent/CN101506606B/zh
Priority to JP2009525048A priority patent/JP2010501657A/ja
Priority to EP07788495A priority patent/EP2054685A2/fr
Publication of WO2008022998A2 publication Critical patent/WO2008022998A2/fr
Publication of WO2008022998A3 publication Critical patent/WO2008022998A3/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • 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
    • F25J3/0233—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
    • 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
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

Definitions

  • the present invention relates to a method and/or apparatus of treating a hydrocarbon stream such as a natural gas stream.
  • a problem of the known method is that it is rather complicated thereby resulting in high capital expenses (CAPEX), but at the same time it does not obtain a satisfactory recovery of in particular ethane. Also the amount of fuel gas produced is not optimal, because the focus of US 2005/0268649 Al is mainly on the liquefaction of natural gas rather than on the production of 'residual streams' and recovery of ethane therefrom.
  • the present invention provides a method of treating a hydrocarbon stream such as a natural gas stream, in a plant, the method at least comprising the steps of:
  • step (c) expanding the liquid stream obtained in step (b) and feeding it into a second gas/liquid separator at a first feeding point;
  • step (g) removing from the bottom of the second gas/liquid separator a liquid stream; wherein the liquefied natural gas stream as fed in step (e) is obtained from a source of liquefied natural gas from a separate plant.
  • Fig. 1 schematically shows a process scheme in accordance with the present invention.
  • Embodiments of the present invention relate to the treatment of a natural gas stream, and may involve recovery of at least some of the ethane, propane, butanes and higher hydrocarbons such as pentane from the natural gas.
  • the recovery of hydrocarbons may be done for several purposes.
  • One purpose may be the production of hydrocarbon streams consisting primarily of hydrocarbon products heavier than methane such as natural gas liquids (NGLs; usually composed of ethane, propane and butanes), liquefied petroleum gas (LPG; usually composed of propane and butane) or condensates (usually composed of butanes and heavier hydrocarbon components).
  • Another purpose may be the adjustment of e.g. the heating value of the hydrocarbon stream to correspond to desired specifications of sales gas.
  • the CAPEX can be significantly lowered. As an example no (partial) reflux of the gaseous overhead stream from the second gas/liquid separator is needed.
  • a further advantage is that more sales gas is produced, in particular if the overhead gas is not subsequently liquefied or refluxed to the second gas/liquid separator (contrary to e.g. US 2005/0268649 Al) .
  • the hydrocarbon feed stream may be any suitable hydrocarbon-containing stream to be treated, but is usually a natural gas stream which may be obtained from natural gas or petroleum reservoirs.
  • the natural gas stream may also be obtained from another source, also including a synthetic source such as a Fischer-Tropsch process.
  • the feed stream is comprised substantially of methane.
  • the feed stream comprises at least 60 mole% methane, more preferably at least 80 mole% methane .
  • the feed stream may contain varying amounts of hydrocarbons heavier than methane such as ethane, propane, butanes and pentanes as well as some aromatic hydrocarbons .
  • the feed stream may also contain non-hydrocarbons such as H2O, N2, CO2, H2S and other compounds, and the like.
  • the feed stream containing the natural gas may be pre-treated before feeding it to the first gas/liquid separator.
  • This pre-treatment may comprise removal of undesired components such as CO2 and H2S, or other steps such as pre-cooling, pre-pressurizing or the like. As these steps are well known to the person skilled in the art, they are not further discussed here.
  • the hydrocarbon feed stream contains ⁇ (less than) 1 mole% CO2.
  • the first and second gas/liquid separator may be any suitable means for obtaining at least a gaseous stream and a liquid stream, such as a scrubber, distillation column, etc. If desired, three or more gas/liquid separators may be present.
  • the second gas/liquid separator is a de-methanizer, i.e. the overhead stream of the second gas/liquid separator being methane-enriched and the bottom stream of the second gas/liquid separator being ethane-enriched when compared with the hydrocarbon feed stream.
  • the gaseous and liquid streams may be expanded before feeding them into the second gas/liquid separator.
  • the person skilled in the art will understand that the steps of expanding may be performed in various ways using any expansion device (e.g. using a throttling valve, a flash valve or a common expander) .
  • treated hydrocarbon streams may be further processed, if desired. Also, further intermediate processing steps between the first and second gas/liquid separator may be performed.
  • the invention provides methods and apparatuses wherein a C2+ lean gaseous stream is produced in a plant, whereby a liquefied natural gas (LNG) stream is employed that is obtained from a source of liquefied natural gas from a separate plant .
  • LNG liquefied natural gas
  • the LNG stream may be fed into the second gas/liquid separator.
  • the LNG stream has a temperature below - 100 0 C and is at least partially condensed and comprises more than 60 mole% methane, preferably more than 80 mole% methane.
  • source of liquefied natural gas from a separate plant means that the LNG is produced in a separate plant from the plant in which the C2+ lean gaseous stream is produced.
  • No LNG stream is used that is generated in the hydrocarbon treating plant of the invention, such as any LNG stream produced during the treating itself or downstream of the treating (e.g. downstream of the second gas/liquid separator) .
  • an already existing LNG stream is used that has been produced elsewhere, for example an LNG stream produced in a separate liquefaction plant.
  • the separate source may be a storage tank or a stream from a nearby liquefaction plant.
  • the LNG stream may have been obtained from an offloading LNG carrier vessel.
  • the LNG stream is obtained from a separate plant at an LNG import terminal, such as an LNG storage tank at an LNG import terminal.
  • a gaseous stream is removed from the top of the second gas/liquid separator.
  • the gaseous stream obtained in step (f) is a C2+ lean gaseous stream.
  • C2+ lean is meant a gaseous stream which has a low proportion of hydrocarbons having two or more carbon atoms, including a stream rich in methane, with only a minor proportion of hydrocarbons having two or more carbon atoms.
  • the gaseous stream obtained in step (f) is provided with a composition and/or heating value required for used as a sales gas.
  • the C2+ lean gaseous stream removed from the top of the second gas/liquid separator in step (f) may comprise ⁇ (less than) 10 mole% hydrocarbons having 2 of more carbon atoms, preferably ⁇ 5 mole%, more preferably ⁇ 2 mole% and even more preferably ⁇ 1 mole%.
  • the gaseous stream obtained in step (f) is sent to a gas network and not liquefied to obtain a methane-rich LNG stream. Further it may be that the gaseous stream obtained in step (f) is heat exchanged against the feed stream.
  • a liquid stream is removed from the bottom of the second gas/liquid separator.
  • This liquid stream may be further processed.
  • this liquid stream is subjected to fractionation thereby obtaining two or more products, including ethane .
  • > (more than) 75 mole% of hydrocarbons having 2 or more carbon atoms present in the partially condensed feed stream are recovered in the liquid stream obtained from the second gas/liquid separator, preferably > 80, more preferably > 85, even more preferably > 90, most preferably > 95 mole%.
  • ⁇ (less than or equal to) 25 mole% of the hydrocarbons having 2 or more carbon atoms present in the partially condensed feed stream are transferred to the gaseous stream obtained in step (f), preferably ⁇ 20, more preferably ⁇ 15, even more preferably ⁇ 10, most preferably ⁇ 5 mole%.
  • > (more than) 75 mole% of the ethane present in the partially condensed feed stream is recovered in the liquid stream obtained in step (g), preferably > 80, more preferably > 85, even more preferably > 90, most preferably > 95 mole%.
  • ⁇ (less than or equal to) 25 mole% of the ethane present in the partially condensed feed stream is transferred to the gaseous stream obtained from the second gas/liquid separator in step (f), preferably ⁇ 20, more preferably ⁇ 15, even more preferably ⁇ 10, most preferably ⁇ 5 mole%.
  • the pressure in the second gas/liquid separator is from 15 to 40 bar, preferably from 20 to 30 bar. Examples include from 23 to 27 bar and about 25 bar.
  • Figure 1 schematically shows a process scheme (generally indicated with reference no. 1) for the treating of a hydrocarbon feed stream such as natural gas whereby ethane and heavier hydrocarbons are recovered to a certain extent.
  • a hydrocarbon feed stream such as natural gas
  • a partly condensed feed stream 10 containing natural gas is supplied to the inlet 21 of the first gas/liquid separator 2 at a certain inlet pressure and inlet temperature.
  • the inlet pressure to the first gas/liquid separator 2 will be between 10 and 100 bar, preferably above 30 bar and preferably below 90 bar, more preferably below 70 bar.
  • the temperature will usually be between 0 and -80 0 C.
  • it may have been pre- cooled in several ways.
  • the feed stream 10 may have been further pre-treated before it is fed to the first gas/liquid separator 2.
  • H2O, CO2, H2S and hydrocarbon components having the molecular weight of pentane or higher may also at least partially have been removed from the feed stream 10 before entering the first separator 2.

Landscapes

  • Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un procédé de traitement d'un courant d'hydrocarbures dans une usine, le procédé comprenant au moins les étapes consistant à : (a) introduire un courant d'alimentation partiellement condensé (10) dans un premier séparateur gaz/liquide (2); (b) séparer le courant d'alimentation (10) dans le premier séparateur gaz/liquide (2) en un courant gazeux (20) et un courant liquide (30); (c) dilater le courant liquide (30) obtenu à l'étape (b) et l'introduire (40) dans un deuxième séparateur gaz/liquide (3) en un premier point d'alimentation (31); (d) dilater le courant gazeux (20) obtenu à l'étape (b) pour obtenir ainsi un courant au moins partiellement condensé (50), puis l'introduire dans le deuxième séparateur gaz/liquide (3) en un deuxième point d'alimentation (32), le deuxième point d'alimentation (32) se situant à un niveau supérieur à celui du premier point d'alimentation (31); (e) introduire un courant de gaz naturel liquéfié (70, 70b) dans le deuxième séparateur gaz/liquide (3) en un troisième point d'alimentation (33) situé à un niveau supérieur à celui du deuxième point d'alimentation (32); (f) retirer par le sommet du deuxième séparateur gaz/liquide (3) un courant gazeux pauvre en C2+ (60); et (g) retirer par le fond du deuxième séparateur gaz/liquide (3) un courant liquide (80, 80a); dans lequel le courant de gaz naturel liquéfié (70, 70b) tel qu'introduit à l'étape (e) est obtenu à partir d'une source (4) de gaz naturel liquéfié d'une usine distincte.
PCT/EP2007/058648 2006-08-23 2007-08-21 Procédé et appareil permettant de traiter un courant d'hydrocarbures WO2008022998A2 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US12/438,032 US20100162753A1 (en) 2006-08-23 2007-08-21 Method and apparatus for treating a hydrocarbon stream
CN2007800310082A CN101506606B (zh) 2006-08-23 2007-08-21 用于处理烃物流的方法和设备
JP2009525048A JP2010501657A (ja) 2006-08-23 2007-08-21 炭化水素流の処理方法及び処理装置
EP07788495A EP2054685A2 (fr) 2006-08-23 2007-08-21 Procédé et dispositif pour traiter un courant d'hydrocarbures

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP06119358.7 2006-08-23
EP06119358 2006-08-23

Publications (2)

Publication Number Publication Date
WO2008022998A2 true WO2008022998A2 (fr) 2008-02-28
WO2008022998A3 WO2008022998A3 (fr) 2008-11-20

Family

ID=37831502

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2007/058648 WO2008022998A2 (fr) 2006-08-23 2007-08-21 Procédé et appareil permettant de traiter un courant d'hydrocarbures

Country Status (6)

Country Link
US (1) US20100162753A1 (fr)
EP (1) EP2054685A2 (fr)
JP (1) JP2010501657A (fr)
KR (1) KR20090068213A (fr)
CN (1) CN101506606B (fr)
WO (1) WO2008022998A2 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9920985B2 (en) 2011-08-10 2018-03-20 Conocophillips Company Liquefied natural gas plant with ethylene independent heavies recovery system
RU2748142C1 (ru) * 2020-01-09 2021-05-19 Андрей Владиславович Курочкин Установка подготовки попутного нефтяного газа с получением широкой фракции легких углеводородов (варианты)

Families Citing this family (45)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2943683B1 (fr) * 2009-03-25 2012-12-14 Technip France Procede de traitement d'un gaz naturel de charge pour obtenir un gaz naturel traite et une coupe d'hydrocarbures en c5+, et installation associee
RU2615703C2 (ru) * 2015-09-10 2017-04-06 Публичное акционерное общество "НОВАТЭК" Способ комплексной подготовки газоконденсатных залежей с глубоким извлечением углеводородов с3+ и установка для его осуществления
RU2625846C2 (ru) * 2015-10-21 2017-07-19 Андрей Владиславович Курочкин Способ безотходной подготовки скважинной продукции
RU2608392C1 (ru) * 2015-10-21 2017-01-18 Андрей Владиславович Курочкин Способ промысловой деэтанизации скважинной продукции
RU2609170C1 (ru) * 2015-10-21 2017-01-30 Андрей Владиславович Курочкин Способ подготовки скважинной продукции
RU2622948C1 (ru) * 2016-09-13 2017-06-21 Федеральное государственное бюджетное образовательное учреждение высшего образования "Воронежский институт Государственной противопожарной службы Министерства Российской Федерации по делам гражданской обороны, чрезвычайным ситуациям и ликвидации последствий стихийных бедствий" (ФГБОУ ВО Воронежский Способ конденсации паров нефтепродуктов
RU2622925C1 (ru) * 2016-10-11 2017-06-21 Андрей Владиславович Курочкин Установка трехпродуктовой подготовки сернистого природного газа
RU2624652C1 (ru) * 2016-10-11 2017-07-05 Андрей Владиславович Курочкин Трехпродуктовая установка комплексной подготовки газа
RU2624710C1 (ru) * 2016-10-11 2017-07-05 Андрей Владиславович Курочкин Установка комплексной подготовки газа
RU2622926C1 (ru) * 2016-10-19 2017-06-21 Андрей Владиславович Курочкин Установка низкотемпературной сепарации (варианты)
RU2624654C1 (ru) * 2016-10-21 2017-07-05 Андрей Владиславович Курочкин Устройство промежуточной сепарации газа (варианты)
RU2622930C1 (ru) * 2016-10-28 2017-06-21 Андрей Владиславович Курочкин Трехпродуктовая установка комплексной подготовки природного газа (варианты)
RU2717669C2 (ru) * 2017-01-17 2020-03-24 Андрей Владиславович Курочкин Трехпродуктовая установка комплексной подготовки газа (варианты)
RU2726325C2 (ru) * 2017-01-17 2020-07-13 Андрей Владиславович Курочкин Блок низкотемпературной сепарации
RU2683091C1 (ru) * 2017-10-27 2019-03-26 Ассоциация инженеров-технологов нефти и газа "Интегрированные технологии" Способ модернизации установки низкотемпературной сепарации газа
RU2668896C1 (ru) * 2018-03-27 2018-10-04 Андрей Владиславович Курочкин Установка для деэтанизации природного газа (варианты)
RU2740201C2 (ru) * 2018-06-27 2021-01-12 Общество с ограниченной ответственностью научно-исследовательский и проектный институт "ПЕГАЗ" Установка деэтанизации природного газа
RU2694337C1 (ru) * 2018-07-02 2019-07-11 Андрей Владиславович Курочкин Установка выделения углеводородов c2+ из природного газа (варианты)
RU2696375C1 (ru) * 2018-08-06 2019-08-01 Андрей Владиславович Курочкин Установка для получения углеводородов c2+ из природного газа (варианты)
RU2694746C1 (ru) * 2018-08-06 2019-07-16 Андрей Владиславович Курочкин Установка получения углеводородов с2+ из природного газа (варианты)
RU2681897C1 (ru) * 2018-08-30 2019-03-13 Андрей Владиславович Курочкин Установка низкотемпературной сепарации с дефлегмацией нтсд для переработки природного газа с выделением углеводородов c2+ (варианты)
RU2694731C1 (ru) * 2018-08-30 2019-07-16 Андрей Владиславович Курочкин Установка низкотемпературной фракционирующей абсорбции нтфа для переработки природного газа с выделением углеводородов c2+ (варианты)
RU2682595C1 (ru) * 2018-08-30 2019-03-19 Андрей Владиславович Курочкин Установка низкотемпературной дефлегмации нтд для переработки природного газа с получением углеводородов c2+ (варианты)
RU2694735C1 (ru) * 2018-08-30 2019-07-16 Андрей Владиславович Курочкин Установка низкотемпературной сепарации с фракционирующей абсорбцией нтсфа для переработки природного газа с выделением углеводородов c2+ (варианты)
RU2736031C2 (ru) * 2018-11-20 2020-11-11 Андрей Владиславович Курочкин Установка комплексной подготовки природного газа с получением сжиженного природного газа
RU2688151C1 (ru) * 2018-11-20 2019-05-20 Андрей Владиславович Курочкин Установка низкотемпературной дефлегмации с сепарацией нтдс для подготовки природного газа с получением сжиженного природного газа и способ ее работы (варианты)
RU2695553C1 (ru) * 2018-11-20 2019-07-24 Андрей Владиславович Курочкин Установка низкотемпературной дефлегмации с сепарацией нтдс для подготовки природного газа с получением этан-бутановой фракции и способ ее работы
RU2688533C1 (ru) * 2018-12-29 2019-05-21 Андрей Владиславович Курочкин Установка нтдр для комплексной подготовки газа и получения спг и способ ее работы
RU2727502C1 (ru) * 2019-01-09 2020-07-22 Андрей Владиславович Курочкин Установка комплексной безотходной подготовки газа по технологии нтдр
RU2699915C1 (ru) * 2019-01-09 2019-09-11 Андрей Владиславович Курочкин Установка нтдр для деэтанизации магистрального газа (варианты)
RU2727503C1 (ru) * 2019-01-09 2020-07-22 Андрей Владиславович Курочкин Установка комплексной безотходной подготовки газа нтдр
RU2689737C1 (ru) * 2019-01-09 2019-05-28 Андрей Владиславович Курочкин Установка нтдр для безотходной комплексной подготовки газа
RU2741026C2 (ru) * 2019-01-09 2021-01-22 Андрей Владиславович Курочкин Установка низкотемпературной ддефлегмации с ректификацией для комплексной подготовки газа и получения сжиженного природного газа
RU2699910C1 (ru) * 2019-01-10 2019-09-11 Андрей Владиславович Курочкин Установка деэтанизации магистрального газа с получением спг (варианты)
RU2727501C1 (ru) * 2019-01-31 2020-07-22 Андрей Владиславович Курочкин Установка нтдр для выделения углеводородов с2+ из магистрального газа (варианты)
RU2699912C1 (ru) * 2019-01-31 2019-09-11 Андрей Владиславович Курочкин Установка нтдр для получения углеводородов с2+ из магистрального газа (варианты)
RU2699913C1 (ru) * 2019-02-01 2019-09-11 Андрей Владиславович Курочкин Установка нтдр для комплексной безотходной промысловой подготовки газа (варианты)
RU2739738C2 (ru) * 2019-04-30 2020-12-28 Андрей Владиславович Курочкин Установка деэтанизации магистрального газа (варианты)
RU2718074C1 (ru) * 2019-11-21 2020-03-30 Андрей Владиславович Курочкин Способ реконструкции установки низкотемпературной сепарации газа
RU2718073C1 (ru) * 2019-11-21 2020-03-30 Андрей Владиславович Курочкин Способ реконструкции установки низкотемпературной сепарации газа с предотвращением образования факельных газов
RU2723654C1 (ru) * 2019-12-30 2020-06-17 Андрей Владиславович Курочкин Установка низкотемпературного фракционирования для деэтанизации магистрального газа (варианты)
RU2741023C1 (ru) * 2020-01-09 2021-01-22 Андрей Владиславович Курочкин Установка подготовки попутного нефтяного газа с получением пропан-бутановой фракции (варианты)
RU2731709C1 (ru) * 2020-01-20 2020-09-08 Андрей Владиславович Курочкин Установка низкотемпературного фракционирования для деэтанизации магистрального газа с выработкой спг
RU2733711C1 (ru) * 2020-05-28 2020-10-06 Андрей Владиславович Курочкин Установка для выделения углеводородов из газовой смеси
RU2733710C1 (ru) * 2020-05-28 2020-10-06 Андрей Владиславович Курочкин Установка выделения углеводородов из газовой смеси (варианты)

Family Cites Families (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL6611036A (fr) * 1966-08-05 1968-02-06
US3846993A (en) * 1971-02-01 1974-11-12 Phillips Petroleum Co Cryogenic extraction process for natural gas liquids
US4629484A (en) * 1983-08-31 1986-12-16 C F Braun & Co. Process for separating hydrogen and methane from an ethylene rich stream
US4698081A (en) * 1986-04-01 1987-10-06 Mcdermott International, Inc. Process for separating hydrocarbon gas constituents utilizing a fractionator
US4854955A (en) * 1988-05-17 1989-08-08 Elcor Corporation Hydrocarbon gas processing
US5108472A (en) * 1990-11-05 1992-04-28 Pride Of The Hills Mfg., Inc. Gas-liquid separator
US5325673A (en) * 1993-02-23 1994-07-05 The M. W. Kellogg Company Natural gas liquefaction pretreatment process
FR2707745B1 (fr) * 1993-07-15 1995-10-06 Technip Cie Procédé autoréfrigéré de fractionnement cryogénique et de purification de gaz et échangeur de chaleur pour la mise en Óoeuvre de ce procédé.
US5673571A (en) * 1996-03-06 1997-10-07 Manley; David B. Deethanizer/depropanizer sequences with thermal and thermo-mechanical coupling and component distribution
AR007346A1 (es) * 1996-06-05 1999-10-27 Shell Int Research Un metodo para separar dioxido de carbono, etano y componentes mas pesados de una corriente de gas natural a alta presion
US5953935A (en) * 1997-11-04 1999-09-21 Mcdermott Engineers & Constructors (Canada) Ltd. Ethane recovery process
US6021647A (en) * 1998-05-22 2000-02-08 Greg E. Ameringer Ethylene processing using components of natural gas processing
US6732881B1 (en) * 1998-10-15 2004-05-11 Mobil Oil Corporation Liquefied gas storage tank
GB9826999D0 (en) * 1998-12-08 1999-02-03 Costain Oil Gas & Process Limi Low temperature separation of hydrocarbon gas
US6453698B2 (en) * 2000-04-13 2002-09-24 Ipsi Llc Flexible reflux process for high NGL recovery
US6367286B1 (en) * 2000-11-01 2002-04-09 Black & Veatch Pritchard, Inc. System and process for liquefying high pressure natural gas
US6742358B2 (en) * 2001-06-08 2004-06-01 Elkcorp Natural gas liquefaction
DE10140585A1 (de) * 2001-08-18 2003-02-27 Linde Ag Verfahren zum Abtrennen einer C2-reichen Fraktion aus einer Kohlenwasserstoffreichen Fraktion mit gleichzeitiger C3+-, C4+- und/oder C5+Gewinnung
US6823692B1 (en) * 2002-02-11 2004-11-30 Abb Lummus Global Inc. Carbon dioxide reduction scheme for NGL processes
MY136353A (en) * 2003-02-10 2008-09-30 Shell Int Research Removing natural gas liquids from a gaseous natural gas stream
FR2855526B1 (fr) * 2003-06-02 2007-01-26 Technip France Procede et installation de production simultanee d'un gaz naturel apte a etre liquefie et d'une coupe de liquides du gaz naturel
US20050048345A1 (en) * 2003-09-03 2005-03-03 Meacham G.B. Kirby Hybrid fuel cell system with internal combustion reforming
US7278281B2 (en) * 2003-11-13 2007-10-09 Foster Wheeler Usa Corporation Method and apparatus for reducing C2 and C3 at LNG receiving terminals
US7159417B2 (en) * 2004-03-18 2007-01-09 Abb Lummus Global, Inc. Hydrocarbon recovery process utilizing enhanced reflux streams
KR101200611B1 (ko) * 2004-07-01 2012-11-12 오르트로프 엔지니어스, 리미티드 액화 천연 가스 처리
CN100478317C (zh) * 2004-07-09 2009-04-15 西南化工研究设计院 煤层气低温分离提浓甲烷工艺
US7165423B2 (en) * 2004-08-27 2007-01-23 Amec Paragon, Inc. Process for extracting ethane and heavier hydrocarbons from LNG
PE20060989A1 (es) * 2004-12-08 2006-11-06 Shell Int Research Metodo y dispositivo para producir una corriente de gas natural liquido
US20060131218A1 (en) * 2004-12-17 2006-06-22 Abb Lummus Global Inc. Method for recovery of natural gas liquids for liquefied natural gas
US7437889B2 (en) * 2006-01-11 2008-10-21 Air Products And Chemicals, Inc. Method and apparatus for producing products from natural gas including helium and liquefied natural gas
WO2007138067A2 (fr) * 2006-05-30 2007-12-06 Shell Internationale Research Maatschappij B.V. Procédé de traitement d'un flux d'hydrocarbure

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9920985B2 (en) 2011-08-10 2018-03-20 Conocophillips Company Liquefied natural gas plant with ethylene independent heavies recovery system
RU2748142C1 (ru) * 2020-01-09 2021-05-19 Андрей Владиславович Курочкин Установка подготовки попутного нефтяного газа с получением широкой фракции легких углеводородов (варианты)

Also Published As

Publication number Publication date
JP2010501657A (ja) 2010-01-21
KR20090068213A (ko) 2009-06-25
CN101506606A (zh) 2009-08-12
EP2054685A2 (fr) 2009-05-06
CN101506606B (zh) 2011-06-08
US20100162753A1 (en) 2010-07-01
WO2008022998A3 (fr) 2008-11-20

Similar Documents

Publication Publication Date Title
WO2008022998A2 (fr) Procédé et appareil permettant de traiter un courant d'hydrocarbures
AU2007310863B2 (en) Method and apparatus for treating a hydrocarbon stream
JP5997798B2 (ja) 等圧開放冷凍天然ガス液回収による窒素除去
US8434326B2 (en) Method and apparatus for liquefying a hydrocarbon stream
AU2007267116B2 (en) Method for treating a hydrocarbon stream
JP5032562B2 (ja) 天然ガス流の液化方法及び装置
EA031162B1 (ru) Способ сжижения загрязненного углеводородсодержащего газового потока
EP1869382A1 (fr) Procede et appareil permettant de liquefier un flux de gaz naturel
JP5210302B2 (ja) 炭化水素流の処理方法及び処理装置
US20100000234A1 (en) Method and apparatus for the vaporization of a liquid hydrocarbon stream
WO2007141227A2 (fr) Procédé et appareil de traitement d'un flux d'hydrocarbure

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 200780031008.2

Country of ref document: CN

WWE Wipo information: entry into national phase

Ref document number: 2007788495

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 12438032

Country of ref document: US

Ref document number: 956/CHENP/2009

Country of ref document: IN

WWE Wipo information: entry into national phase

Ref document number: 2009525048

Country of ref document: JP

NENP Non-entry into the national phase

Ref country code: DE

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 07788495

Country of ref document: EP

Kind code of ref document: A2

WWE Wipo information: entry into national phase

Ref document number: 1020097005801

Country of ref document: KR

NENP Non-entry into the national phase

Ref country code: RU