• 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:
    The present invention deals with a process for removal of H2S and CO2 from a gas mixture in which: (a) the gas mixture is contacted at elevated pressure countercurrently with lean solvent which comprises a tertiary amine and a physical absorbent; (b) the loaded solvent obtained is flashed; (c) the flash gas set free in step (b) is contacted countercurrently with lean solvent under conditions which are selective for H2S removal; (d) part of the loaded solvent obtained after flashing is stripped with the gas obtained in step (c); (e) the stripped solvent obtained in step (d) is introduced as semilean solvent in step (a); (f) the gas obtained in step (d) is contacted countercurrently with lean solvent under conditions which are selective for H2S removal; and (g) loaded solvent obtained in steps (c), (b) and (f) is regenerated to yield lean solvent, wherein a gas with an H2S concentration suitable to be used in a Claus process is obtained.
    公开号:SU1537125A3
    申请号:SU823450444
    申请日:1982-06-14
    公开日:1990-01-15
    发明作者:Мария Ван-Дер Хильда；Пас-Тоорнстра
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий Б.В. (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to processes for the removal of hydrogen sulphide and carbon dioxide from a gas mixture to produce a gas suitable for use in a Claus process.
    The aim of the invention is to increase the selectivity of the process for hydrogen sulfide and reduce energy consumption.
    Example. 10,000 kmol / h of gas mixture, which contains 171 kmol HZS, 4431 kmol COZ, 2775 kmol CO, 2578 kmol Na, 37 kmol N2 and 8 kmol COS, are introduced at 40 ° C and 44 bar pressure at the bottom of the absorber, which has 30 valve trays. Contact is carried out in the
    cm
    with a depleted absorber containing 50% by weight of methyldiethanol-amine, 25% by weight of sulfolane and 25% by weight of odes. The specified absorber is introduced in the amount of 155 m3 / h at 40 ° C in the upper part of the absorber. At the same time, a half-depleted solvent, which contains 617 kmol / h of C04, 75 kmol / h, is served on the 3rd plate on top of the absorber. , at JSC C, with a pressure of 43.7 bar in an amount of 615 me / min Purified gas with an amount of 8704.8 kmol / h containing 3358 kmol CO, 2753 kmol CO, 2556 kmol N., 37 kmol N, 0.8 kmol COS and less than 200 hours per million vol. H 5, withdrawn from the absorber.
    The rich solvent is removed from the absorber at 68 ° C and at a pressure of i4 bar in the amount of 770 me / h. The enclosed solvent contains 246 kmol / h. and 1,690 kmol / h. C02 It is heated in the evaporator with low pressure steam and instantly evaporated in the evaporator to a pressure of 1.5 bar at 60 ° C. After expansion, the gases are fed to the primary absorber and they are contacted at 40 ° C and 1.4 bar pressure with 200 m3 / h of lean solvent, which is 6/8 parts of the total amount. The gases released in this process are fed to a stripping column, into which also 615 m3 / h are fed. enriched solvent obtained by evaporation and containing 140 kmol / h and 617 kmop / h С0г. For the rest of the rich solvent obtained in the evaporator, heat is exchanged with the lean solvent, after which it is fed to the regenerator. The semi-poor solvent obtained in from the steam column is fed to the absorber in an amount, at the temperature and pressure specified above. The gas leaving the stripping column is fed to the secondary absorber, where it contacts with 252 me / h of depleted solvent, fed at 30 ° C and 1.1 bar pressure. From the secondary absorber, from 770.5 kmol / h of gas which 1 will gain 0.3 kmol, 725.5 kmol Pog, 22 kmol CO, 22 kmol and 0.7 kmol COS. The enriched solvent withdrawn from the secondary absorber in the amount of 252 me / h contains 68.9 kmol / h. and 120 kmol / h.S0g. Gl and combined with enriched rzst
    0
    Q
    5 5
    0
    five
    0
    five
    0
    by evaporators from the primary absorber. Their total number is 607. Then they are fed to the regenerator, which is heated by steam. The gas that leaves the regenerator within 5 hours (530.5 kmol) contains 176.5 kmol H2S, 353.3 kmol C02.0.7 kmol COS, and the molar percentage is 33%. Further, heat exchange between the regenerated (607 m / h) and enriched solvent is carried out, after which it is fed to the absorbers in quantities of 155, 200 and 252 m3 / h, respectively.
    权利要求:
    Claims (2)
    [1]
    1. A method for purifying gas from hydrogen sulphide and carbon dioxide, including their absorption by an absorber containing alkanolamine, sulfolane and water at elevated temperature and pressure, followed by regeneration of the saturated absorber by purging with heated gas, in order to increase the hydrogen sulfide selectivity of the process and reduce energy consumption, the absorber after absorption is subjected to instantaneous evaporation to a pressure less than the total partial pressure of hydrogen sulfide and carbon dioxide, while producing acid gas and a saturated absorber, then the acid gas is in contact with the absorber that has passed the regeneration, and the latter is sent for regeneration, and part of the saturated absorber in the amount of 6/8 of the total amount is fed to the stripper, and the gas obtained after treatment is used as a stripping agent acid gas from the evaporation stage absorber that has undergone regeneration, after which the absorber obtained in the stripping stage is returned to the upper absorption zone, and the saturated acid gas is in contact with the regeneration absorbed The tele and the latter are returned to the regeneration stage, while the remaining part of the absorber after evaporation is directly sent to the regeneration.
    51537125 .6
    [2]
    2. The method according to claim 1, of tl and h of diethanolamine, 25% by weight of sulfolane, and with the use of absorbed and 25% by weight of water, and cleaning is carried out with a containing 50% by weight. % methyl- temperature 40 ° С and pressure 40 bar.
    类似技术:
    公开号 | 公开日 | 专利标题
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    CA1252608A|1989-04-18|Method and apparatus for selective absorption ofhydrogen sulphide from gas streams containinghydrogen sulphide and carbon dioxide
    US4100257A|1978-07-11|Process and amine-solvent absorbent for removing acidic gases from gaseous mixtures
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    US4057403A|1977-11-08|Gas treating process
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    WO1986005474A1|1986-09-25|Selective absorption of hydrogene sulfide from gases which also contain carbon dioxide
    US4504449A|1985-03-12|Process of regenerating absorbent solutions for sulfur-containing gases
    US4299801A|1981-11-10|Regenerating alkanolamine desulfurizer solutions
    GB1589231A|1981-05-07|Process for the removal of acidic gases
    CA1181081A|1985-01-15|Removal of degradation product from gas treatingsolution
    US3656275A|1972-04-18|Process for the removal and concentration of a component gas from a multi-gaseous stream
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    引用文献:
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB8118300|1981-06-15|
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