EP0361557B1 - Procédé de traitement d'un gaz naturel contenant des hydrocarbures et de l'acide sulfhydrique - Google Patents

Procédé de traitement d'un gaz naturel contenant des hydrocarbures et de l'acide sulfhydrique Download PDF

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Publication number
EP0361557B1
EP0361557B1 EP89202108A EP89202108A EP0361557B1 EP 0361557 B1 EP0361557 B1 EP 0361557B1 EP 89202108 A EP89202108 A EP 89202108A EP 89202108 A EP89202108 A EP 89202108A EP 0361557 B1 EP0361557 B1 EP 0361557B1
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EP
European Patent Office
Prior art keywords
natural gas
zone
heat exchange
hydrocarbons
gas
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.)
Expired - Lifetime
Application number
EP89202108A
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German (de)
English (en)
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EP0361557A1 (fr
Inventor
Joachim Dr. Wilhelm
Ulf Jauernik
Manfred Dr. Kriebel
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GEA Group AG
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Metallgesellschaft AG
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Priority to AT89202108T priority Critical patent/ATE67298T1/de
Publication of EP0361557A1 publication Critical patent/EP0361557A1/fr
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Publication of EP0361557B1 publication Critical patent/EP0361557B1/fr
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • 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
    • 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
    • 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
    • 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
    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/921—Chlorine
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/922—Sulfur
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/931—Recovery of hydrogen
    • Y10S62/932—From natural gas

Definitions

  • the invention relates to a process for the treatment of natural gas, which in addition to methane contains hydrocarbons having 2 to 4 carbon atoms per molecule and H2S, for the partial removal of the hydrocarbons and the H2S.
  • the hydrocarbons with 5 and more carbon atoms per molecule can be removed relatively easily by adsorption.
  • the object of the present process is to remove the more difficult to separate C2 to C4 hydrocarbons and at the same time also the H2S, which also damages the reforming catalyst, to a sufficient extent.
  • this is achieved in that the natural gas, which has a pressure of at least 5 bar, is indirectly cooled in a heat exchange zone to temperatures from -30 to -100 ° C and condensate is separated, that the condensate is expanded and passed through the heat exchange zone as a coolant that one cools a washing liquid coming from a regeneration zone in the heat exchange zone to temperatures from -30 to -80 ° C and passes into a washing zone, to which one also supplies the natural gas freed from condensate, that washing liquid loaded with H2S and hydrocarbons from the washing zone through the heat exchange zone and into the regeneration zone, and that the natural gas cleaned in the scrubbing zone is expanded and passed through the heat exchange zone.
  • the cold necessary for the process is achieved by relaxing the condensate and also by relaxing the natural gas coming from the washing zone.
  • a refrigeration system can advantageously be dispensed with. Since the cooling requirement in the washing zone is not high because the necessary amount of washing liquid is kept low, the cold generated by condensation is also sufficient to cool the washing liquid in front of the washing zone sufficiently.
  • the condensate separated from the cooled natural gas is expediently expanded in two stages and the expansion gas formed in the process is passed through the heat exchange zone.
  • the washing liquid used is methanol, acetone or other C1 to C3 oxo hydrocarbons.
  • Natural gas containing hydrocarbons and H2S is introduced in line (1).
  • the solids and also the hydrocarbons having 5 and more carbon atoms per molecule have preferably been separated from this natural gas beforehand.
  • the natural gas in line (1) thus contains in addition to H2S especially C2, C3 and C- hydrocarbons.
  • This natural gas is in a heat exchange zone (2), e.g. a plate heat exchanger, indirectly cooled to temperatures from -30 to -100 ° C and preferably -40 to -90 ° C. This cooling creates condensate, which contains the main part of the hydrocarbons and also a considerable part of the H2S.
  • this mixture is led to a separator (5), from which the condensate is drawn off through line (6).
  • the gas mixture is added to a washing column (8) in line (7).
  • the condensate is partially expanded via the expansion valve (10) and fed to a separation tank (11).
  • the expansion gas is drawn off in line (12) and the condensate is expanded again via the expansion valve (13).
  • the expansion of the condensate in the valves (10) and (13) leads to a considerable drop in temperature.
  • the condensate which is led through the heat exchange zone (2) in the line (14) can effectively serve as a coolant.
  • the exhaust gas resulting from the heating in the heat exchange zone (2) is available in line (15) and, since it is high in calorific value, it can be used as fuel gas.
  • the washing column (8) is fed through the line (20) with a washing liquid at temperatures of -30 to -80 ° C and preferably -60 to -70 ° C. Below is of it assumed that this is methanol, but other washing liquids are also possible per se.
  • the column (8) usually contains trays or packing. In it, the H2S is sufficiently washed out of the natural gas introduced in line (7), and the methanol also absorbs hydrocarbons. Purified natural gas is drawn off in the line (21), it is at least partially expanded in the expansion valve (22) and the temperature is thereby reduced. The natural gas is then passed together with the gas of line (12) through the heat exchange zone (2), where it serves as a coolant, and is available in line (24) as a product for further use.
  • the washing liquid loaded with H2S and hydrocarbons is withdrawn from the column (8) in the line (26), expediently expanded in the expansion valve (27) and the mixture is placed in a separation container (28).
  • An H2S-containing exhaust gas is passed through line (29) to the condensate of line (14) and the washing liquid is passed through line (30) after passing through the heat exchange zone (2) to a regeneration system (31).
  • the load is largely removed from the washing liquid in a manner known per se by stripping or heating and also by a combination of these measures.
  • An exhaust gas is drawn off in line (32) and leads to a further treatment, not shown.
  • Regenerated washing liquid is drawn off in line (20) and returned to the washing column (8) via a pump (not shown).
  • a partial flow of the product gas of the line (24) can be used, which can be obtained via the Line (34) shown in broken lines leads and used as stripping gas.
  • the product gas of line (24) consists mainly of methane and may also contain 2 to 20 vol .-% of C2 hydrocarbons.
  • the content of C3-hydrocarbons is usually below 0.1 vol .-% and the H2S content is at most about 1/10 of the H2S content in the gas line (1). In this purity, it is well suited as a feed gas for catalytic steam reforming to generate a gas mixture containing CO and H2.
  • the natural gas which also contains 400 vol. Ppm H2S, has a pressure of 28 bar and a temperature of 30 ° C. It is cooled to -73 ° C in a plate heat exchanger (2) and thus reaches the separator (5).
  • the separated condensate is expanded to 10 bar in the expansion valve (10) and further expansion to 2 bar in the valve (13).
  • the gas in line (7) which is fed to the washing column (8), still contains about half of the C2-hydrocarbons and H2S, as well as N2 and CO2 and traces of C3-hydrocarbons.
  • the column (8) is given methanol of -70 ° C. in a quantity of 10 m3 / h as washing liquid, a pressure of 28 bar prevailing in the washing column.
  • the washed gas which is practically free of H2S and C3 hydrocarbons and contains only a small amount of C2 hydrocarbons, is passed through the expansion valve (22), the pressure being reduced to 10 bar.
  • the loaded washing liquid drawn off from the washing column in line (26) is let down to 2 bar; the expansion gas released during the expansion is mixed with the gas in line (14).
  • 7,000 Nm 3 / h of exhaust gas are obtained in line (15) with a pressure of 2 bar and a temperature of + 10 ° C.
  • the methanol arrives in line (30) for regeneration (31), where it is largely freed from the load at temperatures of + 10 ° C. by stripping with natural gas from line (34).
  • the methanol is then fed back to the washing column (8) via a pump (not shown).

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

Claims (5)

1. Procédé de traitement de gaz naturel qui contient, à côté de méthane, des hydrocarbures à 2 à 4 atomes de C par molécule et de l'H₂S, en vue de l'élimination partielle des hydrocarbures et de l'H₂S, dans lequel on refroidit indirectement à des températures de  -30 à  -100°C le gaz naturel qui se trouve sous une pression d'au moins 5 bars dans une zone d'éhange de chaleur et on sépare le condensat, on détend le condensat et on l'amène comme agent de refroidissement dans la zone d'échange de chaleur, on refroidit dans la zone d'échange de chaleur à des températures de  -30 à  -80°C un liquide de lavage venant d'une zone de régénération et on l'amène dans une zone de lavage où on amène aussi le gaz naturel débarrassé du condensat, on conduit depuis la zone de lavage le liquide de lavage chargé de H₂S et d'hydrocarbures dans la zone d'échange de chaleur et puis dans la zone de régénération et on détend le gaz naturel qui a été épuré dans la zone de lavage et on l'amène dans la zone d'échange de chaleur.
2. Procédé suivant la revendication 1 caractérisé en ce qu'on conduit le gaz naturel sous une pression d'au moins 10 bars au refroidissement indirect dans la zone d'échange de chaleur.
3. Procédé suivant l'une des revendications 1 ou 2 caractérisé en ce qu'on détend en deux étapes le condensat séparé du gaz naturel refroidi et en ce qu'on conduit le gaz de détente ainsi formé dans la zone d'échange de chaleur.
4. Procédé suivant la revendication 1 ou l'une des suivantes caracterisé en ce qu'on détend partiellement le liquide de lavage chargé sortant de la zone de lavage et on conduit le gaz de détente contenant de l'H₂S ainsi séparé dans la zone d'échange de chaleur.
5. Procédé suivant la revendication 1 ou l'une des suivantes caractérisé en ce qu'on emploie comme liquide de lavage du méthanol, de l'acétone ou d'autres oxohydrocarbures en C₁ à C₃.
EP89202108A 1988-09-02 1989-08-17 Procédé de traitement d'un gaz naturel contenant des hydrocarbures et de l'acide sulfhydrique Expired - Lifetime EP0361557B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT89202108T ATE67298T1 (de) 1988-09-02 1989-08-17 Verfahren zum behandeln eines kohlenwasserstoffe und h2s enthaltenden erdgases.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3829878 1988-09-02
DE3829878A DE3829878A1 (de) 1988-09-02 1988-09-02 Verfahren zum behandeln eines kohlenwasserstoffe und h(pfeil abwaerts)2(pfeil abwaerts)s enthaltenden erdgases

Publications (2)

Publication Number Publication Date
EP0361557A1 EP0361557A1 (fr) 1990-04-04
EP0361557B1 true EP0361557B1 (fr) 1991-09-11

Family

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EP89202108A Expired - Lifetime EP0361557B1 (fr) 1988-09-02 1989-08-17 Procédé de traitement d'un gaz naturel contenant des hydrocarbures et de l'acide sulfhydrique

Country Status (13)

Country Link
US (1) US4934146A (fr)
EP (1) EP0361557B1 (fr)
AR (1) AR246603A1 (fr)
AT (1) ATE67298T1 (fr)
CA (1) CA1320429C (fr)
DE (2) DE3829878A1 (fr)
GR (1) GR3002720T3 (fr)
ID (1) ID893B (fr)
IN (1) IN171560B (fr)
MX (1) MX171737B (fr)
MY (1) MY105042A (fr)
PT (1) PT91618B (fr)
SA (1) SA91110375B1 (fr)

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US5325672A (en) * 1992-12-03 1994-07-05 Uop Process for the purification of gases
US5321952A (en) * 1992-12-03 1994-06-21 Uop Process for the purification of gases
FR2722110B1 (fr) * 1994-07-08 1996-08-30 Inst Francais Du Petrole Procede de desacidification d'un gaz pour production de gaz acides concentres
US5659109A (en) * 1996-06-04 1997-08-19 The M. W. Kellogg Company Method for removing mercaptans from LNG
DE102004036708A1 (de) * 2004-07-29 2006-03-23 Linde Ag Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
US7645322B2 (en) * 2006-09-15 2010-01-12 Ingersoll Rand Energy Systems Corporation System and method for removing water and siloxanes from gas
GB0814556D0 (en) * 2008-08-11 2008-09-17 Edwards Ltd Purification of gas stream
US9528704B2 (en) 2014-02-21 2016-12-27 General Electric Company Combustor cap having non-round outlets for mixing tubes

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IT1190359B (it) * 1985-05-24 1988-02-16 Snam Progetti Procedimento criogenico di rimozione di gas acidi da miscele di gas mediante solvente
US4654062A (en) * 1986-07-11 1987-03-31 Air Products And Chemicals, Inc. Hydrocarbon recovery from carbon dioxide-rich gases
DE3626561A1 (de) * 1986-08-06 1988-02-11 Linde Ag Verfahren zum abtrennen von c(pfeil abwaerts)2(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)- oder von c(pfeil abwaerts)3(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)- kohlenwasserstoffen aus einem gasgemisch

Also Published As

Publication number Publication date
DE58900284D1 (de) 1991-10-17
GR3002720T3 (en) 1993-01-25
MY105042A (en) 1994-07-30
AR246603A1 (es) 1994-08-31
US4934146A (en) 1990-06-19
MX171737B (es) 1993-11-11
SA91110375B1 (ar) 2002-06-01
IN171560B (fr) 1992-11-21
ID893B (id) 1996-09-05
ATE67298T1 (de) 1991-09-15
PT91618A (pt) 1990-03-30
PT91618B (pt) 1995-05-04
DE3829878A1 (de) 1990-03-08
CA1320429C (fr) 1993-07-20
EP0361557A1 (fr) 1990-04-04

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