• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    For scrubbing C2+ or C3+ hydrocarbons from gaseous mixture containing hydrocarbons and/or inerts like H2, N2, CO and possibly acid gases, e.g. CO2H2S, COS e.g., natural gas and the like, the scrubbing medium consists essentially of compounds having one to two rings formed by 5 or 6 carbon atoms, wherein the compounds comprise, in total, at least 9 and at most 17 carbon atoms, and the rings are saturated unsaturated or partially saturated especially alkylated ring compounds of 9 or 10 carbon atoms, e.g. isomeric forms of trimethylbenzene, propylbenzene, propylcyclohexane, tetrahydronaphthalene, decahydronaphthalene.
    公开号:SU1535376A3
    申请号:SU864027965
    申请日:1986-08-13
    公开日:1990-01-07
    发明作者:Ландекк Гейнер；Ранке Герхард
    申请人:Линде Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a means for separating light hydrocarbons from a gas mixture, specifically to the use of butylbenzene or propylcyclohexane, or indane, or tetralin, or decalin as a means for separating. Neither Cr or C J4. hydrocarbons from the gas mixture.
    The aim of the invention is to reduce the energy consumption in the process of separating the Ca or Cj4 hydrocarbons from the gas mixture.
    Figures 1 and 2 show an installation in which G.J. and C3 hydrocarbons are released, respectively.
    Example 1. Hydrocarbons Cg are recovered from the gas mixture in the plant, the scheme of which is shown in Fig. 1.
    The source gas under pressure through the pipeline I is fed to the washing column 2, in which it is treated with a washing agent that dissolves the Cr + hydrocarbons. The washed gas, containing methane and nitrogen, leaves the column through conduit 3. In order to maintain a constant temperature, in the lower part of column 2 there is an absorption heat that is not compensated by an increase in
    . the temperature of the washing agent is removed with the help of a refrigerant circulating through the cooling coil 4. The loaded washing agent is removed from the bottom of column 2 via line 5 and after depressurization is fed to the separator 6. The gas withdrawn from the separator 6 compress in compressor 7 and through pipeline 8 resl
    with
    SP
    00

    about

    O4
    circulate to the source gas. The liquid phase separated in the separator 6 is expanded into the second separator 9, the liquid phase of which is expanded into the third set 10. The liquid phase separated in the separator 10 is fed by means of a pump 11 into the washing column 2 through the pipeline 12.
    A portion of the liquid phase is withdrawn through the pipeline 13, heated in the heat exchanger 14 and fed to the column 15 for treatment with washing gas supplied through the pipeline 16. The bottom product of the column 15 is withdrawn by means of a pump 17, cooled in the heat exchanger 14 and fed to the column. 2 through line 18 and cooler 19.
    The head fraction of the column 15 through the pipeline 20 is fed into the gas withdrawn from the separator 10 through the pipeline 21. Both streams are compressed in the compressor 22 and cooled in the cooler 23. Then they are combined with the gas withdrawn from the separator 9 through the pipeline 24. The combined streams are compressed into the compressor 25, is cooled in the cooler 26 and is fed to the methane-discharge column 27, the lower part of which is equipped with a heating device 28. The bottom product of the column 27 containing all hydrocarbons C is discharged through the pipe 29. The head fraction Hydrocarbons and nitrogen are compressed in compressor 30, cooled in cooler 31, and recirculated to the source gas through conduit 32.
    Hydrocarbons 2 are separated from the gas mixture in the installation, the scheme of which is shown in FIG. The plant of Figure 2 differs from Figure 1 in that it serves to separate the hydrocarbons Cj. from a gas stream containing carbon dioxide. At the same time, hydrocarbons C, and Cr and carbon dioxide are withdrawn through conduit 3. In addition, the head fraction of column 15, containing some heavy hydrocarbons and carbon dioxide, is withdrawn through conduit 33 and is not recycled to the process. In addition, the column 27 serves to distill off the ethna, so that the bottom product discharged through line 29 contains


    ,
    0
    levorododa CI. The head fraction is not recycled to the source gas, and after being compressed in compressor 30 and cooled in cooler 31, is withdrawn through conduit 34 and combined with product withdrawn through conduit 3.
    Table 1 summarizes the physical parameters of the process when using as a means for separating the hydrocarbons Cj or C3 + washing agents listed in Table. 2 and 3; B- Table 2 - data on the process parameters and energy consumption in the separation of hydrocarbons С Jf from the gas of mol% used in the amount of 1000 mol / s: mol 1.%: nitrogen 1.68; methane 81.13; ethane 8.71; propane 4.79; butane 2.41; pentane 0.97; hexane 0.31 using various washing agents.
    The data presented in Table 2 for the various scrubbing agents are based on a yield of 85% ethane based on the ethane contained in the feed gas.
    Table 3 summarizes the process parameters and energy consumption for the separation of hydrocarbons C from the gas of mol% used in an amount of 1000 mol / s: carbon dioxide 10; methane 80.8; ethane 5.5; propane 2.2; butane 1.0; pentane 0.3; hexane 0,2 using various washing agents.
    The data presented in Table 3 for the various scrubbing agents is based on a 95% propane yield, calculated on the propane content in the feed gas.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    The use of butylbenzene or propylclohexane, or indane, or tetralin, nli decalin as a means for separating hydrocarbons C. or C 3 from the gas mixture.
    Priority featured:
    08/14/85 - the use of butylbenzo-g
    la
    10/07/85 - use of propylcyclohexane, indane, tetralin, decalin.
    2
    Table 1
    Hydrocarbon finishing
     Simple polyethylene glycol diethyl ester.
    Just dinetpovy zfkr polyethylene glycol.
    8L $ 7 5
    fuz.2
    Editor N.Gunko Tehred M.Hodanich
    Order 58 Circulation 345 Subscription
    VNIIPI State Committee for Inventions and Discoveries at the State Committee on Science and Technology of the USSR 113035, Moscow, Zh-35, Raushsk nab. 4/5
    . - - -. - - .., -.- -. - ----- - - - -- - -- - - -- -one-- - -
    Production and publishing plant Patent, Uzhgorod, st. Gagarin, 101
    W
    J2
    24
    cW
    w
    29
    Proofreader V.Kabatsiy
    类似技术:
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    US4042669A|1977-08-16|Process for separation and recovery of carbon monoxide
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    同族专利:
    公开号 | 公开日
    CN1012573B|1991-05-08|
    IN167636B|1990-11-24|
    CN86105297A|1987-02-11|
    US4810267A|1989-03-07|
    DE3535764A1|1987-02-26|
    AR246939A1|1994-10-31|
    NO166637B|1991-05-13|
    EP0211447B1|1991-12-04|
    US4797140A|1989-01-10|
    AU6089386A|1987-02-19|
    AU587629B2|1989-08-24|
    MX168221B|1993-05-13|
    NO863271D0|1986-08-13|
    NO166637C|1991-08-21|
    EP0211447A1|1987-02-25|
    NO863271L|1987-02-16|
    DE3682719D1|1992-01-16|
    引用文献:
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    DE936650C|1952-11-29|1955-12-15|Lurgi Ges Fuer Waermetechnik M|Process for the selective scrubbing of gas components|
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    DE1123428B|1959-11-07|1962-02-08|Linde S Eismaschinen Ag Zweign|Process for the desulphurisation of dry natural gas containing hydrogen sulphide|
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    DE2909335A1|1979-03-09|1980-09-18|Linde Ag|METHOD AND DEVICE FOR DISASSEMBLING NATURAL GAS|
    AU540081B2|1981-01-16|1984-11-01|Ciba-Geigy Ag|Gas purification process|
    US4417092A|1981-03-16|1983-11-22|Exxon Research And Engineering Co.|Sputtered pin amorphous silicon semi-conductor device and method therefor|
    AU530246B2|1981-04-30|1983-07-07|Nippon Steel Corporation|Process for separating carbon monoxide from a gas mixture|
    SU1115786A1|1983-04-08|1984-09-30|Всесоюзный научно-исследовательский институт природных газов|Absorbent for cleaning natural gas from mercaptans and propane-butane fraction|US5047074A|1989-01-25|1991-09-10|Macgregor Douglas|Purging of nitrogen from natural gas|
    ZA899705B|1989-01-26|1990-09-26|Aeci Ltd|Purification of gases|
    US5837037A|1996-07-17|1998-11-17|Texaco Inc|Gas handling for plastics liquefaction|
    GB9702742D0|1997-02-11|1997-04-02|Ici Plc|Gas absorption|
    US5922109A|1997-03-11|1999-07-13|The Dow Chemical Company|Gas drying process using glycol solution solubility suppressants|
    US6605138B2|1999-04-21|2003-08-12|Matthew T. Frondorf|Apparatus and method for exclusively removing VOC from regeneratable solvent in a gas sweetening system|
    US7550033B2|2002-01-21|2009-06-23|Conocophillips Company|Process for removing sulfides|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3529216|1985-08-14|
    DE19853535764|DE3535764A1|1985-08-14|1985-10-07|METHOD FOR OBTAINING C2 +HYDROCARBONS|
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