EP0340465A2 - Procédé de séparation d'hydrocarbures - Google Patents

Procédé de séparation d'hydrocarbures Download PDF

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Publication number
EP0340465A2
EP0340465A2 EP89105944A EP89105944A EP0340465A2 EP 0340465 A2 EP0340465 A2 EP 0340465A2 EP 89105944 A EP89105944 A EP 89105944A EP 89105944 A EP89105944 A EP 89105944A EP 0340465 A2 EP0340465 A2 EP 0340465A2
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EP
European Patent Office
Prior art keywords
residual gas
column
rectification
fraction
fed
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
EP89105944A
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German (de)
English (en)
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EP0340465B1 (fr
EP0340465A3 (en
Inventor
Heinz Dr. Rer. Nat. Dipl.-Phys. Bauer
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Linde GmbH
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Linde GmbH
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Publication of EP0340465A3 publication Critical patent/EP0340465A3/de
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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
    • F25J3/0252—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 hydrogen
    • 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
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • F25J2200/04—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
    • F25J2200/70—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
    • F25J2200/78—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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/12—Refinery or petrochemical off-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
    • 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
    • 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
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/08—Internal refrigeration by flash gas recovery loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration

Definitions

  • the invention relates to a process for the separation of hydrocarbons from a gas stream containing light and heavy hydrocarbons and possibly components which boil lighter than methane, in which the gas stream under increased pressure is cooled, partially condensed and separated into a liquid and a gaseous fraction and in which the liquid fraction is broken down by rectification into a product stream containing essentially high-boiling components and a residual gas stream containing predominantly lower-boiling components, and the gaseous fraction separated off after the partial condensation is fed to a backwash column in which residual gas obtained in the rectification after its partial condensation high-boiling hydrocarbons are washed out of the gaseous fraction and the liquid fraction obtained in the bottom of the backwash column is fed to the rectification.
  • Such processes are primarily used to remove ethane and propane from hydrocarbon gas mixtures, such as natural gas or refinery waste gases. These processes are also suitable for the removal of analog unsaturated hydrocarbons such as ethylene and propylene. Refinery exhaust gases contain such hydrocarbons, which has made their work-up interesting due to increased market prices for C3 / C4 hydrocarbon mixtures.
  • DE-OS 35 11 636 a method of the type mentioned is described, which is used to separate C2+ or C3+ hydrocarbons from a gas mixture.
  • a raw gas stream is partially condensed in countercurrent to process streams to be heated and separated into a liquid and a gaseous fraction.
  • the liquid fraction which consists essentially of the high-boiling hydrocarbon components C2+ or C3+, is passed into a rectification column in which the low-boiling components are removed from this fraction.
  • a residual gas fraction which, after its partial condensation, is passed into a backwash column in order to wash out high-boiling components from the gaseous fraction of the separator.
  • the bottom fraction obtained in the backwash column is also fed into the rectification column.
  • the backwashing serves to increase the yield of the process, since this measure can be used to obtain C2+ or C3+ components that cannot otherwise be obtained both from the gaseous fraction of the separator and from the residual gas from the rectification column.
  • a disadvantage of the above method is that the required process temperature must be generated by means of a refrigeration system, possibly a refrigeration cascade.
  • the cold-relieving expansion of at least part of the residual gas flows is provided.
  • the invention is therefore based on the object of further improving a method of the type mentioned, in particular a costly generation of cold should be avoided while at the same time maintaining high pressures of the residual gas flows.
  • This object is achieved in that the residual gas obtained in the rectification is separated into a gaseous and a liquid fraction after its partial condensation and before it is fed to the backwash column, and the liquid fraction is at least partially expanded to provide cooling, and is warmed against partially condensing residual gas from the rectification column and the residual gas stream of the rectification is mixed again, while the remaining part of the liquid fraction is fed to the backwash column.
  • the renewed admixing of the part of the liquid fraction of the residual gas stream used as the cooling medium to the top product of the rectification column has the effect that the total amount circulating is greater than the actual top product amount. In this way, the cooling capacity of the branched-off part of the condensed residual gas stream can be used to cool further process streams.
  • the backwash column and the rectification column are operated under increased pressure.
  • the pressure of the residual gas which is fed to the backwash column is adjusted to the pressure of the backwash column.
  • the ethane-rich top product of the backwash column contributes significantly to achieving a sufficient level Joule-Thompson effect in the downstream H2 cleaning.
  • the invention provides that, before the cold-venting relaxed fraction is mixed with the residual gas from the rectification, the two streams are equalized and the mixture stream is adjusted to the pressure of the backwash column.
  • the pressures of both streams can be equalized on the one hand by relieving one of the two to the pressure of the other, or, in the opposite case, by increasing the pressure of the one stream.
  • the pressure is then adjusted to the pressure of the backwash column. This is usually done by compressing the mixture flow, since the pressure level of the backwash column is above that of the rectification column.
  • the quantitative ratio of the part of the liquid fraction which has been relaxed in terms of cold performance to the part which is fed to the backwash column is 0.43-2.3: 1.
  • the inventive method is particularly suitable for the combination of different separation steps of H2 and hydrocarbon-containing gas mixtures, which work with high inlet pressures.
  • any combination of two separation steps consisting of C5+, C3+, C2+ and H2 separation, can be operated in a particularly energy-saving and efficient manner.
  • a raw gas stream under increased pressure is introduced via line 1, partially condensed by indirect heat exchange in heat exchanger E1 and separated into a liquid and a gaseous fraction in separator D1.
  • the liquid fraction is drawn off via line 3 and, after heating in heat exchanger E1, expanded into a central region of the rectification column T.
  • the gaseous fraction of the separator is fed via line 2 and after further cooling in heat exchanger E2 into the lower region of the backwash column R, in which further components are obtained by washing out of the gaseous fraction.
  • the liquid fraction obtained is drawn off via lines 7 and 8.
  • the part in line 7 is expanded directly into the upper region of the rectification column T, while the part of the bottom product in line 8 is initially in the heat exchangers E2 and E1 is warmed before it is released into a central area of the rectification column.
  • a product fraction is obtained in the bottom of the rectification column and is withdrawn via line 10. Part of it is branched off via branch line 11, heated in heat exchanger E3 and fed back as a boiling stream into the bottom of the rectification column T.
  • a residual gas stream is obtained which still contains desired heavy components.
  • this current is drawn off partially condensed in the heat exchangers E1 and E2 and separated into a gaseous and a liquid fraction in separator D3.
  • the liquid fraction is fed via line 14 to the upper region of the backwash column R for backwashing.
  • the fraction of line 14 is branched off in a branch-cold manner to reduce the pressure, heated in heat exchangers E2 and E1 against streams of lines 1 to be cooled (raw gas) and 12 (residual gas stream from the rectification column) and after compression in compressors C1 and C2 and renewed heating in the heat exchangers E4 and E5 mixed again with the top residual gas stream of the rectification column T.
  • the residual gas obtained at the top of the backwash column R consisting of low-boiling components, is at least partially condensed in heat exchanger E6 after removal by means of line 4.
  • Separator D2 then separates them into gaseous and liquefied components.
  • the gaseous fractions are withdrawn in line 6, while the liquefied fractions are withdrawn from the system via line 5, together with the gaseous fraction of the separator D3 from line 13.
  • the flows 9 of the heat exchanger E1 are auxiliary circuits for the refrigeration.
  • a raw gas stream under increased pressure is passed via line 1, after cooling and partial condensation by indirect heat exchange in heat exchanger E1, to separator D, where it is separated into a liquid and a gaseous fraction.
  • the liquid fraction is drawn off via line 3, decompressed and, after heating in heat exchanger E1, passed into a central region of the rectification column T.
  • the gaseous fraction of the separator is fed via line 2, after further cooling in heat exchange E2, into the lower region of the backwash column R.
  • the liquid fraction obtained is drawn off from the bottom of the backwash column via lines 5 and 6.
  • the liquid fraction of line 5 is expanded, heated in heat exchanger E2 and fed to a central area of the rectification column T, while the portion in line 6 is expanded directly into an upper area of the rectification column.
  • the liquid fraction obtained in the bottom of the rectification column is removed via line 7. After heating in heat exchanger E3, a part is returned to the bottom of the rectification column as a boiling stream, the rest of the stream is compressed P and released
  • the top product of the rectification column T drawn off by means of line 8, is first warmed up in E1, expanded and mixed with the compressed and heated stream of line 9, after which the mixture is further compressed in line 10 into compressor C2, and heating in the heat exchanger ES takes place .
  • the flow of the line 10 is washed back into the separation chamber column R relaxed.
  • the separation room is arranged in the upper area of the backwash column R and separated from the actual backwash room by a chimney tray.
  • a gaseous fraction is released via line 4 and, after heating, is drawn off in E2 and E1.
  • the liquid fraction accumulating on the chimney floor is drawn off by means of line 9 and partly fed in as a return to the upper area of the backwashing room.
  • the remaining portion, after relaxation and heating in E2 and E1, is compressed by compressor C1, further heated in heat exchanger E4 and mixed with the relaxed top product of the rectification column T.
  • the flows 11 of the heat exchanger E1 are auxiliary circuits for the refrigeration.

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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)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP89105944A 1988-04-28 1989-04-05 Procédé de séparation d'hydrocarbures Expired - Lifetime EP0340465B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3814294 1988-04-28
DE3814294A DE3814294A1 (de) 1988-04-28 1988-04-28 Verfahren zur abtrennung von kohlenwasserstoffen

Publications (3)

Publication Number Publication Date
EP0340465A2 true EP0340465A2 (fr) 1989-11-08
EP0340465A3 EP0340465A3 (en) 1990-03-21
EP0340465B1 EP0340465B1 (fr) 1991-10-16

Family

ID=6353045

Family Applications (1)

Application Number Title Priority Date Filing Date
EP89105944A Expired - Lifetime EP0340465B1 (fr) 1988-04-28 1989-04-05 Procédé de séparation d'hydrocarbures

Country Status (5)

Country Link
US (1) US4966612A (fr)
EP (1) EP0340465B1 (fr)
AU (1) AU613180B2 (fr)
DE (2) DE3814294A1 (fr)
ES (1) ES2027431T3 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0448439A1 (fr) * 1990-03-20 1991-09-25 Institut Français du Pétrole Procédé de fractionnement d'un mélange gazeux renfermant de l'hydrogène, des hydrocarbures aliphatiques légers et des hydrocarbures aromatiques légers
EP0465366A1 (fr) * 1990-07-04 1992-01-08 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de production simultanée de méthane et monoxyde de carbone

Families Citing this family (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5114451A (en) * 1990-03-12 1992-05-19 Elcor Corporation Liquefied natural gas processing
US5026408A (en) * 1990-06-01 1991-06-25 Union Carbide Industrial Gases Technology Corporation Methane recovery process for the separation of nitrogen and methane
US5390499A (en) * 1993-10-27 1995-02-21 Liquid Carbonic Corporation Process to increase natural gas methane content
FR2718725B1 (fr) * 1994-04-13 1996-05-24 Air Liquide Procédé et installation de séparation d'un mélange gazeux.
US5568737A (en) * 1994-11-10 1996-10-29 Elcor Corporation Hydrocarbon gas processing
US5588308A (en) * 1995-08-21 1996-12-31 Air Products And Chemicals, Inc. Recompression cycle for recovery of natural gas liquids
US5596883A (en) * 1995-10-03 1997-01-28 Air Products And Chemicals, Inc. Light component stripping in plate-fin heat exchangers
DE10005722A1 (de) * 2000-02-09 2001-08-16 Linde Ag Verfahren zur Tieftemperaturzerlegung eines im wesentlichen aus Wasserstoff, Methan und C3-, C4- oder C3/C4-Kohlenwasserstoffen bestehenden Stromes
EP1311789A4 (fr) * 2000-08-11 2005-09-21 Fluor Corp Processus de recuperation de propane de haute teneur et agencements
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AU613180B2 (en) 1991-07-25
ES2027431T3 (es) 1992-06-01
AU3371789A (en) 1989-11-02
DE3814294A1 (de) 1989-11-09
EP0340465B1 (fr) 1991-10-16
US4966612A (en) 1990-10-30
EP0340465A3 (en) 1990-03-21
DE58900372D1 (de) 1991-11-21

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