EP0387128A1 - Verfahren und Vorrichtung zur Rückgewinnung der schwersten Kohlenwasserstoffe aus einer Gasmischung - Google Patents

Verfahren und Vorrichtung zur Rückgewinnung der schwersten Kohlenwasserstoffe aus einer Gasmischung Download PDF

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Publication number
EP0387128A1
EP0387128A1 EP90400549A EP90400549A EP0387128A1 EP 0387128 A1 EP0387128 A1 EP 0387128A1 EP 90400549 A EP90400549 A EP 90400549A EP 90400549 A EP90400549 A EP 90400549A EP 0387128 A1 EP0387128 A1 EP 0387128A1
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EP
European Patent Office
Prior art keywords
column
hydrogen
remaining mixture
mixture
condenser
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
EP90400549A
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English (en)
French (fr)
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EP0387128B1 (de
Inventor
Denis Chretien
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.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication of EP0387128A1 publication Critical patent/EP0387128A1/de
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Publication of EP0387128B1 publication Critical patent/EP0387128B1/de
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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
    • F25J3/0204—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
    • 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
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • 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
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • 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
    • F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation 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
    • 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 present invention relates to the technique for recovering the heaviest hydrocarbons from a gas mixture. It relates more particularly to a process for recovering the heaviest hydrocarbons from a gaseous mixture further containing lighter constituents including hydrogen, in particular for the recovery of LPG (C3+) from a residual gas from an oil refinery.
  • the object of the invention is to provide a clearly more economical method eliminating all these drawbacks.
  • the method according to the invention is characterized in that: - part of the hydrogen is removed from the mixture; the remaining mixture is introduced at an intermediate level of a distillation column comprising a top condenser which provides reflux in the column, this condenser being cooled by a cooling device capable of providing a cold temperature TF of the order of -40 ° C or higher than this value; and the hydrogen content of said remaining mixture is determined so that the dew point, at column pressure, of the fraction of this remaining mixture constituted by said lighter constituents is greater than the temperature TF but close to it .
  • the partial elimination of the hydrogen is carried out by permeation.
  • this elimination partial hydrogen is carried out by PSA adsorption (Pressure Swing Adsorption), said remaining mixture being constituted by the residual gas from this adsorption and being compressed before being introduced into the column, the composition of said remaining mixture being optionally adjusted by permeation.
  • PSA adsorption Pressure Swing Adsorption
  • the invention also relates to an installation intended for the implementation of such a method.
  • This installation is characterized in that it includes: - means for removing part of the hydrogen from the mixture, providing a remaining mixture; and a distillation column supplied with this remaining mixture and comprising a top condenser which provides reflux in the column, this condenser being cooled by a cooling device capable of providing a cold temperature TF of the order of -40 ° C or greater than this value; the means for partial elimination of hydrogen being adapted so that the fraction of said remaining mixture constituted by said lighter constituents has, at column pressure, a dew point above the temperature TF but close to it.
  • an oil refinery waste gas of the following typical composition is treated: 74% H2, 12.2% C1, 9.5% C2, 2.7% C3, 1.6% C4 +, as well as traces of benzene compounds and water, in order to recover LPG (C3+).
  • the gas to be treated is introduced at 31 bars, via a line 1, into the high-pressure space of a permeator 2.
  • the permeate forming approximately two-thirds of the initial flow rate and consisting of hydrogen at a purity of 98 to 99% is removed from the permeator at low pressure under a few bars, via a line 3.
  • the residue from the permeation containing almost all of the hydrocarbons, has the following composition: 21.3% H2, 36.7% C1, 28.9% C2, 8.2% C3, 4.9% C4+, as well as traces of benzene compounds and water.
  • This residue is dried in a desiccator 4, then cooled in a heat exchanger. indirect heat 5, then introduced at about 30 bars at an intermediate level of a distillation column 6.
  • the column 6 is equipped in the tank with a reboiler 7 operating at approximately 100 ° C, and at the head of a condenser 8 operating at approximately -40 ° C and refrigerated by a cooling device 9 consisting of a refrigeration unit, for example in "Freon", on one floor.
  • the overhead vapor of the column is partially condensed by the condenser 8 and then separated into a vapor phase and a liquid phase in a phase separator 10.
  • the vapor phase contains almost all of the hydrogen, methane and ethane contained in the permeation residue, and is discharged via a pipe 11 as waste gas from the installation after having cooled the heat exchanger 5.
  • the liquid phase is returned to reflux at the top of the column 6.
  • the LPG are drawn off in the column tank by a line 12.
  • the residue from the permeation contains a quantity of light hydrocarbons C1 and C2 imposed by the composition of the starting gas. Its hydrogen content is determined by an appropriate dimensioning of the permeator 2, so that the mixture of these light hydrocarbons and hydrogen (that is to say in practice the waste gas) has, at the pressure of the column 6, a dew point slightly higher than the coldest temperature which the condenser 8 can reach with a refrigeration unit 9 with a single stage, ie approximately -40 ° C.
  • the upper part of column 6 performs an almost perfect elimination of hydrogen by washing, so that the only loss of LPG is that which occurs in the permeator 2.
  • the minimum compatible with a refrigeration unit 9 with a single stage is kept the amount of hydrogen eliminated by permeation, and therefore the loss of LPG. In practice, it is found that this loss can be made negligible, so that the extraction efficiency of LPG is close to 100%.
  • the benzene compounds in the starting gas have no drawbacks and are simply found in the LPG produced.
  • the desiccator 4 can possibly be dispensed with.
  • FIG. 2 differs from that of FIG. 1 only by the treatment of the gas upstream of the heat exchanger 5. It is particularly suitable when it is desired to produce very pure hydrogen, for example intended to electronic applications.
  • the starting gas is firstly treated by PSA adsorption (Pressure Swing Adsorption) in a 2A adsorption device, which removes about the same amount of hydrogen as before.
  • PSA adsorption Pressure Swing Adsorption
  • the remaining mixture consisting of the waste gas from the device 2A, is available at a low pressure typically close to atmospheric pressure. It is recompressed to around 30 bars by a compressor 13, then cooled in the exchanger 5, then introduced into the column 6 as before.
  • the invention can be applied to other cases of recovery of heavy hydrocarbons.
  • it is possible to recover only the C4+s by choosing the pressure of the column and the hydrogen content of the mixture introduced into this column so that the dew point of the mixture H2 , C1, C2 and C3 constituting the waste gas of the column is greater than -40 ° C; we will choose a cooling device 9 adapted to this temperature, this device possibly being constituted by a simple circulation of water at room temperature.

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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)
  • Separation By Low-Temperature Treatments (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
EP90400549A 1989-03-09 1990-02-28 Verfahren und Vorrichtung zur Rückgewinnung der schwersten Kohlenwasserstoffe aus einer Gasmischung Expired - Lifetime EP0387128B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8903073A FR2644160B1 (fr) 1989-03-09 1989-03-09 Procede et installation de recuperation des hydrocarbures les plus lourds d'un melange gazeux
FR8903073 1989-03-09

Publications (2)

Publication Number Publication Date
EP0387128A1 true EP0387128A1 (de) 1990-09-12
EP0387128B1 EP0387128B1 (de) 1991-11-27

Family

ID=9379512

Family Applications (1)

Application Number Title Priority Date Filing Date
EP90400549A Expired - Lifetime EP0387128B1 (de) 1989-03-09 1990-02-28 Verfahren und Vorrichtung zur Rückgewinnung der schwersten Kohlenwasserstoffe aus einer Gasmischung

Country Status (7)

Country Link
US (1) US5053067A (de)
EP (1) EP0387128B1 (de)
CA (1) CA2011311A1 (de)
DE (1) DE69000004D1 (de)
ES (1) ES2026741T3 (de)
FR (1) FR2644160B1 (de)
NO (1) NO901038L (de)

Families Citing this family (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5504677A (en) * 1992-10-15 1996-04-02 Pollin; Robert E. Automated payment system
US5966698A (en) * 1992-10-15 1999-10-12 Pollin; Robert E. Automated payment system and method
US5647227A (en) * 1996-02-29 1997-07-15 Membrane Technology And Research, Inc. Membrane-augmented cryogenic methane/nitrogen separation
US5634354A (en) * 1996-05-08 1997-06-03 Air Products And Chemicals, Inc. Olefin recovery from olefin-hydrogen mixtures
US6159272A (en) * 1997-01-24 2000-12-12 Membrane Technology And Research, Inc. Hydrogen recovery process
US5769927A (en) * 1997-01-24 1998-06-23 Membrane Technology And Research, Inc. Monomer recovery process
US5785739A (en) * 1997-01-24 1998-07-28 Membrane Technology And Research, Inc. Steam cracker gas separation process
US5980609A (en) * 1997-01-24 1999-11-09 Membrane Technology And Research, Inc. Hydrogen recovery process
US6011192A (en) * 1998-05-22 2000-01-04 Membrane Technology And Research, Inc. Membrane-based conditioning for adsorption system feed gases
US6165350A (en) * 1998-05-22 2000-12-26 Membrane Technology And Research, Inc. Selective purge for catalytic reformer recycle loop
US6264828B1 (en) 1998-05-22 2001-07-24 Membrane Tehnology And Research, Inc. Process, including membrane separation, for separating hydrogen from hydrocarbons
US6171472B1 (en) 1998-05-22 2001-01-09 Membrane Technology And Research, Inc. Selective purge for reactor recycle loop
US6190540B1 (en) 1998-05-22 2001-02-20 Membrane Technology And Research, Inc. Selective purging for hydroprocessing reactor loop
US6179996B1 (en) 1998-05-22 2001-01-30 Membrane Technology And Research, Inc. Selective purge for hydrogenation reactor recycle loop
US6190536B1 (en) 1998-05-22 2001-02-20 Membrane Technology And Research, Inc. Catalytic cracking process
WO1999067587A1 (en) * 1998-06-25 1999-12-29 Process Systems International, Inc. Cryogenic and membrane synthesis gas production
US6183628B1 (en) 1999-03-19 2001-02-06 Membrane Technology And Research, Inc. Process, including PSA and membrane separation, for separating hydrogen from hydrocarbons
US6592749B1 (en) 1999-03-19 2003-07-15 Membrane Technology And Research, Inc. Hydrogen/hydrocarbon separation process, including PSA and membranes
US6389845B1 (en) * 1999-10-05 2002-05-21 American Air Liquide, Inc. Method and apparatus for separation of SF6 from CF4 /air-containing gas stream
US6589303B1 (en) 1999-12-23 2003-07-08 Membrane Technology And Research, Inc. Hydrogen production by process including membrane gas separation
US6568206B2 (en) * 2001-07-18 2003-05-27 Air Products And Chemicals, Inc. Cryogenic hydrogen and carbon monoxide production with membrane permeate expander
US7780747B2 (en) * 2003-10-14 2010-08-24 Advanced Technology Materials, Inc. Apparatus and method for hydrogen generation from gaseous hydride

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3250080A (en) * 1962-11-07 1966-05-10 Kerr Mc Gee Oil Ind Inc Method of separating gaseous mixtures by diffusion and fractionation
US4284423A (en) * 1978-02-15 1981-08-18 Exxon Research & Engineering Co. Separation of carbon dioxide and other acid gas components from hydrocarbon feeds containing admixtures of methane and hydrogen
US4374657A (en) * 1981-06-03 1983-02-22 Fluor Corporation Process of separating acid gases from hydrocarbons
US4411677A (en) * 1982-05-10 1983-10-25 Air Products And Chemicals, Inc. Nitrogen rejection from natural gas
US4681612A (en) * 1984-05-31 1987-07-21 Koch Process Systems, Inc. Process for the separation of landfill gas
US4732583B1 (en) * 1984-12-03 1990-05-15 Gas separation
US4595404A (en) * 1985-01-14 1986-06-17 Brian J. Ozero CO2 methane separation by low temperature distillation
US4602477A (en) * 1985-06-05 1986-07-29 Air Products And Chemicals, Inc. Membrane-aided distillation for carbon dioxide and hydrocarbon separation

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Eléments de la technique relevés: néant. *

Also Published As

Publication number Publication date
US5053067A (en) 1991-10-01
DE69000004D1 (de) 1992-01-09
NO901038D0 (no) 1990-03-06
FR2644160B1 (fr) 1991-05-10
NO901038L (no) 1990-09-10
ES2026741T3 (es) 1992-05-01
CA2011311A1 (fr) 1990-09-09
EP0387128B1 (de) 1991-11-27
FR2644160A1 (fr) 1990-09-14

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