EP2347205A2 - Procédé de séparation d'azote - Google Patents

Procédé de séparation d'azote

Info

Publication number
EP2347205A2
EP2347205A2 EP09748255A EP09748255A EP2347205A2 EP 2347205 A2 EP2347205 A2 EP 2347205A2 EP 09748255 A EP09748255 A EP 09748255A EP 09748255 A EP09748255 A EP 09748255A EP 2347205 A2 EP2347205 A2 EP 2347205A2
Authority
EP
European Patent Office
Prior art keywords
fraction
nitrogen
column
methane
rich
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP09748255A
Other languages
German (de)
English (en)
Other versions
EP2347205B1 (fr
Inventor
Heinz Bauer
Rainer Sapper
Martin Gwinner
Georg Schopfer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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 Linde GmbH filed Critical Linde GmbH
Priority to PL09748255T priority Critical patent/PL2347205T3/pl
Publication of EP2347205A2 publication Critical patent/EP2347205A2/fr
Application granted granted Critical
Publication of EP2347205B1 publication Critical patent/EP2347205B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

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
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0257—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 nitrogen
    • 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
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure 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
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2270/42—Quasi-closed internal or closed external nitrogen 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements

Definitions

  • the invention relates to a process for separating a nitrogen-rich fraction from a feed fraction containing essentially nitrogen and hydrocarbons, wherein the feed fraction is fractionally separated into a nitrogen-rich and a methane-rich fraction and wherein the methane-rich fraction for the purpose of cooling is evaporated and superheated at the highest possible pressure against the cooled feed fraction.
  • the feed fraction essentially containing nitrogen and hydrocarbons, which may have been subjected to a pretreatment, such as sulfur removal, carbon dioxide removal, drying, etc., fed to a heat exchanger E1 and in this against process streams, to which in the following even closer will be received, cooled and partially condensed.
  • a pretreatment such as sulfur removal, carbon dioxide removal, drying, etc.
  • the partially condensed feed fraction is fed to a pre-separation column T1.
  • This pre-separation column T1 together with the low-pressure column T2, forms a double column T1 / T2.
  • a hydrocarbon-rich liquid fraction is withdrawn via line 2, undercooled in the heat exchanger E2 against process streams, which will be discussed in more detail below, and then fed via line 2 'and expansion valve a to the low-pressure column T2 in the upper region ,
  • a liquid nitrogen-rich fraction is withdrawn from the upper region of the pre-separation column T1.
  • a partial stream of this fraction is added via line 3 'as reflux to the pre-separation column T1.
  • the withdrawn via line 3 Nitrogen-rich fraction is supercooled in the heat exchanger E2 and fed via line 3 "and expansion valve b of the low pressure column T2 above the feed point of the above-described methane-rich fraction.
  • a methane-rich liquid fraction which in addition to methane includes the higher hydrocarbons contained in the feed fraction withdrawn. Their nitrogen content is typically less than 5% by volume.
  • the methane-rich fraction is pumped by the pump P to the highest possible pressure - this is usually between 5 and 15 bar - pumped.
  • the methane-rich liquid fraction is heated and optionally partially evaporated. Via line 5 1 , it is then fed to the heat exchanger E1 and completely evaporated in this against the cooled feed fraction and superheated before it is withdrawn via line 5 "from the process.
  • NRUs Nelculation Unit
  • Nitrogen separation from nitrogen / hydrocarbon mixtures is always carried out when an increased nitrogen content prevents the intended use of the nitrogen / hydrocarbon mixture.
  • a nitrogen content of more than 5 mol% exceeds typical specifications of natural gas pipelines in which the nitrogen / hydrocarbon mixture is transported.
  • Even gas turbines can only be operated up to a certain nitrogen content in the fuel gas.
  • NRUs are typically built similar to an air fractionator with a double column, such as described.
  • a central processing unit Generic methods usually come out without the use of external cold or cold-performing turbines. Therefore, a complex heat integration is necessary.
  • the condenser / reboiler E3 the T1 thermally coupled with T2. The withdrawn via line 5 from the low pressure column T2
  • Bottom product is further evaporated at a high pressure - usually 5 to 15 bar, which is generated by means of the pump P - after heating in the heat exchanger E2 in the heat exchanger E1 and superheated.
  • the highest possible discharge pressure of the vaporized and superheated methane-rich fraction (line 5 ") at the plant boundary is a quality feature of the process concept.
  • Heat exchanger E1 instead. The exact location of the dew point of this fraction is necessary for successful heat integration.
  • the object of the present invention is to provide a generic method for separating a nitrogen-rich fraction from a feed fraction containing essentially nitrogen and hydrocarbons, which avoids the disadvantages described above.
  • a generic method for separating a nitrogen-rich fraction from a feed fraction containing essentially nitrogen and hydrocarbons is proposed, which is characterized in that the still liquid or partially vaporized methane-rich fraction fed to a circulation tank, only in the Circulating container accumulating liquid content of the methane-rich fraction at least partially evaporated, fed again to the circulation tank and the fully vaporized overhead product of the circulation tank is overheated.
  • the temperature profile of the heat exchanger E1 is geometrically fixed.
  • the evaporation of the methane-rich fraction takes place in a controlled manner in the lower part of the heat exchanger E1, while in the upper part of the heat exchanger E1 the overheating of the now pure gas flow is ensured.
  • a helium-rich fraction and in the low pressure column preferably in the head region of Low-pressure column, is relaxed,
  • a partial stream of the nitrogen-rich fraction is compressed at least to the pressure of the pre-separation column and / or the low-pressure column and fed to the pre-separation column and / or the low-pressure column as reflux stream, a partial stream of the nitrogen-rich fraction withdrawn from the head region of the pre-separation column and being supplied to the low-pressure column is vaporized under pressure,
  • the methane content of the rectified nitrogen-rich fraction is less than 1% by volume
  • the nitrogen content of the rectified methane-rich fraction is less than 5% by volume.
  • the still liquid or not completely evaporated methane-rich fraction which is withdrawn via line 5 "from the heat exchanger E2 is not fed directly to the heat exchanger E1 in the procedure shown in FIG
  • only the liquid fraction of the methane-rich fraction which is supplied via line 6 to the heat exchanger E1 in the circulation tank D is partially evaporated in the heat exchanger E1 and then recirculated to the circulation tank D via line 6 ' via line 7 at the top of the circulating tank D withdrawn, fully evaporated methane-rich overhead product is then overheated in the heat exchanger E1 before it is withdrawn from the process via line T.
  • the process control of the methane-rich fraction within the heat exchanger E1 is inventively defined by the fact that the path is divided into an evaporation section and an overheating section.
  • the Evaporation of the methane-rich fraction now takes place exclusively in the section of the heat exchanger E1, which is connected via line 6 to the bottom of the circulating tank D.
  • FIG. 3 differs from the embodiment shown in FIG. 2 in that in the upper region of the pre-separation column T1, preferably below the condenser E3 of the pre-separation column T1, a helium-rich fraction 8 is withdrawn and by means of the valve c in the low-pressure column T2, preferably in the head region of the low-pressure column T2, is relaxed.
  • the process has the advantage that the inert gas helium can be discharged and the effects of operational fluctuations or changes in the helium fraction in the feed fraction are attenuated by the backwash in the low pressure column T2 and not directly to nitrogen-rich ( Product) lead fraction with an increased methane content.
  • FIG. 3 shows an embodiment of the method according to the invention, which is characterized in that at least temporarily a partial stream of the nitrogen-rich fraction which is fed via line 9 to a single- or multi-stage compressor C is at least at the pressure of the pre-separation column T1 and / or the low-pressure column T2 is compressed.
  • the compressed partial flow of the nitrogen-rich fraction is passed via the lines 9 'and 9 "through the heat exchangers E1 and E2 and cooled in this and optionally partially or completely condensed.
  • the compressed partial flow of the nitrogen-rich fraction of the pre-separation column T1 and / or the low-pressure column T2 as reflux or via line 13 directly via line 4 at the top of the low-pressure column T2 withdrawn nitrogen-rich fraction are fed.
  • the operating range of the double column T1 / T2 can be substantially extended in the direction of a low nitrogen content with respect to the nitrogen content in the feed fraction.
  • the compressed partial flow of the nitrogen-rich fraction can thus be used partially or completely for cooling in the heat exchanger E2, without the rectification in the columns T1 and / or T2 being directly influenced.
  • FIG. 4 The embodiment of the process according to the invention shown in FIG. 4 is characterized in that via line 14 a partial stream of the nitrogen-rich liquid fraction withdrawn via line 3 from the top region of pre-separation column T1 and fed to low-pressure column T2 is fed to and warmed in heat exchanger E2 optionally partially evaporated. Via line 14 ', this partial stream is then fed to the heat exchanger E1 and in this preferably completely evaporated before this substream is withdrawn via line 14 "from the process as a further nitrogen-rich (product) fraction.
  • This embodiment of the method according to the invention is particularly advantageous if via line 14 "a partial amount of the separated nitrogen-rich (product) fraction is required under elevated pressure, for example for the supply of inert gas to the system or the process.

Landscapes

  • 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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé pour séparer une fraction riche en azote d'une fraction de charge contenant sensiblement de l'azote et des hydrocarbures. Selon le procédé de l'invention, la fraction de charge est séparée par rectification en une fraction riche en azote et une fraction riche en méthane qui, en vue d'une réfrigération, est évaporée à une pression la plus élevée possible au contact de la fraction de charge à refroidir, puis surchauffée. Selon l'invention, la fraction riche en méthane (5') encore liquide ou partiellement évaporée, est acheminée à un contenant de circulation (D). Seule la partie liquide de la fraction riche en méthane (5') qui s'accumule dans le contenant de circulation (D) s'évapore complètement en circulation naturelle, et le produit de tête (7) du contenant de circulation (D) est surchauffé (E1).
EP09748255.8A 2008-11-06 2009-11-03 Procédé de séparation d'azote Active EP2347205B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL09748255T PL2347205T3 (pl) 2008-11-06 2009-11-03 Sposób oddzielania azotu

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102008056191A DE102008056191A1 (de) 2008-11-06 2008-11-06 Verfahren zum Abtrennen von Stickstoff
PCT/EP2009/007878 WO2010051970A2 (fr) 2008-11-06 2009-11-03 Procédé de séparation d'azote

Publications (2)

Publication Number Publication Date
EP2347205A2 true EP2347205A2 (fr) 2011-07-27
EP2347205B1 EP2347205B1 (fr) 2016-07-20

Family

ID=42096379

Family Applications (1)

Application Number Title Priority Date Filing Date
EP09748255.8A Active EP2347205B1 (fr) 2008-11-06 2009-11-03 Procédé de séparation d'azote

Country Status (8)

Country Link
US (1) US20110209499A1 (fr)
EP (1) EP2347205B1 (fr)
AU (1) AU2009313086B2 (fr)
DE (1) DE102008056191A1 (fr)
MX (1) MX2011004351A (fr)
PL (1) PL2347205T3 (fr)
RU (1) RU2537326C2 (fr)
WO (1) WO2010051970A2 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105806040A (zh) * 2016-04-28 2016-07-27 北京中科瑞奥能源科技股份有限公司 利用炭黑尾气制液化天然气的系统与方法

Family Cites Families (12)

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Publication number Priority date Publication date Assignee Title
US3874184A (en) * 1973-05-24 1975-04-01 Phillips Petroleum Co Removing nitrogen from and subsequently liquefying natural gas stream
US4415345A (en) * 1982-03-26 1983-11-15 Union Carbide Corporation Process to separate nitrogen from natural gas
US4455158A (en) * 1983-03-21 1984-06-19 Air Products And Chemicals, Inc. Nitrogen rejection process incorporating a serpentine heat exchanger
US4715874A (en) * 1986-09-08 1987-12-29 Erickson Donald C Retrofittable argon recovery improvement to air separation
FR2682964B1 (fr) * 1991-10-23 1994-08-05 Elf Aquitaine Procede de deazotation d'un melange liquefie d'hydrocarbures consistant principalement en methane.
GB2297825A (en) * 1995-02-03 1996-08-14 Air Prod & Chem Process to remove nitrogen from natural gas
US5901578A (en) * 1998-05-18 1999-05-11 Praxair Technology, Inc. Cryogenic rectification system with integral product boiler
DE10215125A1 (de) * 2002-04-05 2003-10-16 Linde Ag Verfahren zum Abtrennen von Stickstoff aus einer Stickstoff-enthaltenden Kohlenwasserstoff-reichen Fraktion
GB0216537D0 (en) * 2002-07-16 2002-08-28 Boc Group Plc Nitrogen rejection method and apparatus
US6978638B2 (en) * 2003-05-22 2005-12-27 Air Products And Chemicals, Inc. Nitrogen rejection from condensed natural gas
GB2455462B (en) * 2009-03-25 2010-01-06 Costain Oil Gas & Process Ltd Process and apparatus for separation of hydrocarbons and nitrogen
US8042357B2 (en) * 2009-04-23 2011-10-25 Praxair Technology, Inc. Hydrogen liquefaction method and liquefier

Non-Patent Citations (1)

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Title
See references of WO2010051970A2 *

Also Published As

Publication number Publication date
WO2010051970A3 (fr) 2012-08-30
EP2347205B1 (fr) 2016-07-20
MX2011004351A (es) 2011-05-23
US20110209499A1 (en) 2011-09-01
RU2537326C2 (ru) 2015-01-10
AU2009313086A9 (en) 2015-12-03
DE102008056191A1 (de) 2010-05-12
AU2009313086A1 (en) 2010-05-14
RU2011122643A (ru) 2012-12-20
PL2347205T3 (pl) 2017-08-31
AU2009313086B2 (en) 2015-12-03
WO2010051970A2 (fr) 2010-05-14

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