• 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 invention is directed to a process for the recovery of sulfur from a hydrogen sulfide containing gas, which comprises oxidizing hydrogen sulfide with oxygen, and then reacting the product gas of this oxidation further by using at least two catalytic stages, in accordance with the equation: 2H2S + SO2 2H2O + 3/n Sn. In order to improve the process and the process control, the invention is characterized in that the H2S concentration in the gas leaving the last catalytic stage (17) is controled (23) to have a value ranging between 0.8 and 3% by volume by reducing the quantitiy of combustion or oxidation air passed to the oxidation stage (2) and/or causing a portion of the hydrogen sulfide containing feedstock gas to bypass (25) the oxidation stage and to be added to the gas flowing to a catalytic stage.
    公开号:SU1709900A3
    申请号:SU4202432
    申请日:1987-04-16
    公开日:1992-01-30
    发明作者:Адольф Лагас Йоханнес Борсбом Ян；Хильдегардус Бербен Питер；Вильхельм Гэс Джон
    申请人:Вег-Газинститут Н.В. (Фирма)；Компримо Б.В. (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to methods for the purification of gases from hydrogen sulfide to obtain elemental sulfur according to the Claus method.
    The aim of the invention is to simplify the process and increase the sulfur yield.
    The drawing shows a diagram explaining the implementation of the proposed method.
    The source of the gaseous raw material with a hydrogen sulfide content of 10-90% through the pipeline 1 is fed into the burner of the combustion chamber 2.
    The amount of combustion-supporting air, controlled by the metering controller 3 and the hydrogen sulfide analyzer, is fed through line 4 to the burner. The heat released in the process of gas combustion (1200 ° C) is removed in a boiler 5 with heated exhaust gas forming a stream discharged through pipeline 6.
    The Claus reaction takes place in the burner and the combustion chamber. The sulfur formed is condensed in the boiler 5 (150 ° C) and discharged through line 7. The gas enters through line 8 to the heater 9. in which it is heated to the required reaction temperature of 250 ° C, and then fed through line 10 to the first reactor 11 Klaus. In the reactor 11, the Claus reaction proceeds again, with the formation of sulfur. The gas is withdrawn through conduit 12 to sulfuric condenser 13. Liquefied sulfur (150 ° C) is discharged through conduit 14. Thereafter, the gas is passed through conduit 15 to the next reactor stage, which includes heater 16. reactor 17 and sulfuric condenser
    18. In this reactor, the Claus reaction proceeds again. Condensed sulfur is discharged through line 19. Steam formed in sulfuric capacitors is discharged through lines 20 and 21.
    The concentration of hydrogen sulfide in the residual gas pipeline is controlled by the analyzer 23 hydrogen sulfide and maintained in the range of 0.8-3.0 vol.%. The hydrogen sulfide analyzer 23 controls the operation of the distribution valve in the pipeline .24 of the supply of air that supports the burner or the distribution valve on the pipeline 25 for the supply of hydrogen gray. The pipeline 25 part of the hydrogen sulfide can flow directly to the first catalytic stage, mine thermal stage.
    The residual gas is then passed through conduit 22 to the sulfur removal stage 26. The sulfur removal step is a known sulfur removal process, such as a dry bed oxidation step, an absorption step or a liquid phase oxidation step. The air required for oxidation is supplied through conduit 27. The resulting sulfur is discharged through conduit 28, and the gas through conduit 29 through the afterburner 30 is discharged into the vent pipe 31.
    Example1. According to the proposed scheme, the process is carried out in a Claus converter having two catalytic zones. The feed gas supplied to the thermal stage contains 90% by volume of hydrogen sulfide. corresponding to 90 kmol / h, 5 vol.% of carbon dioxide and 5 vol.% of water, and also 43.33 kmol / h of oxygen {deficit in 3.3) in the form of oxygen. The content of hydrogen sulfide in the residual gas after the second catalytic stage is 0.8%, and the content of sulfur dioxide in it is 0.03%.
    S02 is oxidized in a dry layer using a water-insensitive catalyzed oxidation catalyst, comprising a carrier — a-alumina (Fluhz, specific surface 6.5 m / g), which is applied to 4.5% by weight of Pe203 and 0.5. % CrO2 as a catalytically active material, which, after granulation and calcination, has a BET specific surface area of 6.94 and less than 1% of the total pore volume constitutes pores of radius. When using such a catalyst, which provides an oxidation efficiency of 80%, a total sulfur recovery of 99.1% is achieved.
    Example 2 The process is carried out in a Claus converter having two catalytic zones. Gas is supplied to the thermal stage. containing 90% by volume of hydrogen sulfide. 5% by volume of carbon dioxide (deficiency) of 6.0% in the form of oxygen. The content of hydrogen sulfide in the residual gas after the second
    the catalytic stage - 2.03%, the content of sulfur dioxide in it was immeasurably small, the water content - 35.8% by volume.
    The oxidation of the dry layer is carried out with iso; Use of water insensitive oxidation catalysts, containing a carrier of a-alumina (specific surface 6.5 m / g), on which 4.5 wt.% Re203 and 0.5 wt.% Cr20z were deposited as catalytically active materials which, after granulation and calcination, has a BET specific surface area of 6.94 m / g and less than 1.0% of the total pore volume are pores having a radius of 5-500 A. Using
    this catalyst with oxidizing efficiency-. 90%, get 99.2% sulfur recovery. Example 8 p 3. The process is carried out similarly to Examples 1 and 2, however, the residual content of H2S in the gas after the 2nd catalytic stage is 3.0% by volume.
    Oxidation is carried out in a dry bed using a catalyst that is insensitive to oxidation and includes a carrier — a-alumina (Fluka, specific
    6.5 m / g surface, on which 4.5 mass% of ReaOz and 0.5% by mass of Cr 20z are deposited as a catalyst / ethically active material, which has a BET surface area of 6.94 m / g for granulation and calcination. ,
    L less than 1% of the total pore volume constitutes pores with a radius of less than 500 D. When using such a catalyst, which provides an oxidation efficiency of 95%, total sulfur recovery is achieved
    99.1%.
    EXAMPLE 4. The process is carried out on a Claus converter having two catalytic zones. Gas containing 90 vol.% Hydrogen sulfide, corresponding to 81 kmol / h, 5 vol.% Of carbon dioxide and 5 vol.% Of water, and also 40.95 kmol / h oxygen (i.e. no deficit) is supplied to the thermal stage. . However, the pipeline 25 in, the first catalytic zone serves 8.1 kmol / h of hydrogen sulfide (9.0% of the source gas). The volume of hydrogen sulfide in the residual gas after the second catalytic stage was 3.13%, the content of sulfur dioxide in it was immeasurably low.
    After removal of sulfur and water and using the oxidation process in the liquid phase to absorb and oxidize hydrogen sulfide during the absorption and oxidation effect
    权利要求:
    Claims (4)
    [1]
    Claim
    1. A method of extracting sulfur from hydrogen sulfide-containing gases, including the thermal stage of oxidation of hydrogen sulfide by oxygen, air, cooling them, subsequent catalytic interaction of hydrogen sulfide with sulfur dioxide formed in the thermal stage at least in two stages with an intermediate separation of sulfur after each stage and additional oxidation of residual hydrogen sulfide to sulfur in the presence of a catalyst supported on a carrier, characterized in that, for the sake of simplification. process and increase the yield of sulfur, in the gas leaving the last catalytic stage, maintain a concentration of hydrogen sulfide of 0.8-3 vol.% by reducing the amount of air supplied to the thermal stage, or by introducing into the gas mixture before the first catalytic stage an additional amount of is10 hydrogen sulfide-containing gas.
    [2]
    2. The method according to claim 1, characterized in that air is supplied to the thermal stage in an amount of 94-96.7% of stoichiometry.
    [3]
    3. The method according to claim 1, characterized
    15 in that 9 vol% of the feed gas is introduced into the gas mixture before the first catalytic stage.
    [4]
    4. The method according to claim 1, characterized in that at the stage of additional oxidation
    20 residual hydrogen sulfide use an iron-chromium oxide catalyst containing iron oxide 4.5 wt.% And chromium oxide 0.5 wt.%, The rest is a carrier with a specific surface area of 6.9 ^ m 2 / g and with a volume pore radius of 5 - 500 A in an amount of less than 1% of the total pore volume.
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    同族专利:
    公开号 | 公开日
    NO871561D0|1987-04-13|
    FI871614A0|1987-04-13|
    PT84677A|1987-05-01|
    CN1015536B|1992-02-19|
    CA1323173C|1993-10-19|
    MX169298B|1993-06-29|
    NO871561L|1987-10-19|
    JPS62297202A|1987-12-24|
    US4988494A|1991-01-29|
    EP0242006A1|1987-10-21|
    PT84677B|1989-12-29|
    DE3780682D1|1992-09-03|
    DE3780682T2|1992-12-10|
    DK183087D0|1987-04-10|
    AU7149787A|1987-10-22|
    AU583982B2|1989-05-11|
    BR8701855A|1988-01-26|
    NO173134C|1993-11-03|
    DK183087A|1987-10-17|
    FI81073C|1990-09-10|
    EP0242006B1|1992-07-29|
    YU45819B|1992-07-20|
    FI81073B|1990-05-31|
    ES2033800T3|1993-04-01|
    UA5550A1|1994-12-28|
    CN87103563A|1988-01-06|
    NO173134B|1993-07-26|
    AT78794T|1992-08-15|
    GR3005393T3|1993-05-24|
    JPH0551522B2|1993-08-02|
    DK168700B1|1994-05-24|
    YU68387A|1988-10-31|
    FI871614A|1987-10-17|
    NL8600960A|1987-11-16|
    IN169395B|1991-10-12|
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    法律状态:
    2006-07-20| REG| Reference to a code of a succession state|Ref country code: RU Ref legal event code: PC4A Effective date: 20060605 |
    优先权:
    申请号 | 申请日 | 专利标题
    NL8600960A|NL8600960A|1986-04-16|1986-04-16|METHOD FOR EXTRACTING SULFUR FROM SULFUR-CONTAINING GASES|
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