• 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 relates to a process for the removal of hydrogen sulfide from gases by passing the gases in the presence of oxygen and steam over a catalytic absorption mass which contains inert porous support materials as support and catalytically active metal sulfides and/or metal oxides for the selective oxidation of hydrogen sulfide to elemental sulfur, the sulfur formed being simultaneously deposited on the absorption mass, and regenerating the charged catalytic absorption mass.
    公开号:SU1722210A3
    申请号:SU884613150
    申请日:1988-11-25
    公开日:1992-03-23
    发明作者:Й.Й.Ван Дер Валь Вильям；Б.Тьепкема Ринко；Хейкоп Герард
    申请人:Вег Газинститут Н.В.(Фирма)；Компримо Б.В. (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to processes for the purification of gases from hydrogen sulphide by oxidizing it to elemental sulfur in the presence of a catalytic chemisorption mass.
    The purpose of the invention is to increase the degree of conversion of hydrogen sulfide into elemental sulfur.
    Example 1: A 1.5 cm cylindrical reactor with a diameter of 1.5 cm is filled with 10.2 ml of the catalytic chemisorption mass obtained by a known method. This mass contains 20 wt.% Iron sulphide deposited on a fine inert carrier with a particle size of less than 40 nm. Iron oxide is administered in the form of 0.5 g of iron hydroxide. A gas mixture containing 200 ppm of HaS, 2000 ppm of oxygen, 2% by weight of water and the rest is nitrogen, is passed over the mass at room temperature with a bulk velocity of 5000 hours (850 ml / min). The H2S content at the outlet of the reactor is less than 1 ppm. After 2 hours, the H2S concentration in the exhaust gas begins to slowly increase, reaching 70 ppm after 3.5 hours.
    At the beginning of the desulfurization process, the oxygen content in the exhaust gas is 1000 ppm. During this process, the oxygen concentration in the exhaust gas slowly rises to 1400 ppm. The consumption of oxygen during the desulfurization process indicates that most of the hydrogen sulfide is directly converted to elemental sulfur. When the H2S concentration in the exhaust gas rises to 200 ppm, the chemisorption process is terminated. The amount of chemisorbed hydrogen sulfide, expressed as the molar ratio of H2S to iron, is 2.8, which corresponds to a saturation of 10 wt.% Ele.
    mental sulfur per catalytic adsorption mass. After the breakthrough of hydrogen sulfide, the chemisorbent is regenerated by removing elemental sulfur from the surface of the chemisorbent. The regeneration process includes the following stages: drying the chemisorbent at 100 ° C with nitrogen; evaporation of elemental sulfur at 300 ° C by blowing the layer with nitrogen; rehydration of the chemisorbent at 50 ° C in a stream of gaseous nitrogen containing 2% by weight of water. At the stage of regeneration, elemental sulfur, which is deposited on the surface of the chemisorbent, is removed from the reaction zone as elemental sulfur. Not detected SOa. After regeneration, 20 wt.% Iron oxide in the chemisorbent is present as iron sulfide with a particle size of less than 40 nm.
    PRI mme R 2. The chemisorption mass of Example 1 is used for the desulfurization process. Under the conditions of Example 1, no hydrogen sulfide was detected at the reactor exit for 20 hours. During cycles of selective oxidation and chemisorption, the oxygen concentration in the gas is about 1000 ppm, which indicates that 50 wt.% Of oxygen is converted to hydrogen sulfide into elemental sulfur. During this cycle, 100 wt.% H2S is converted to elemental sulfur, which corresponds to the direct oxidation reaction. After 20 hours, hydrogen sulfide appears in the exhaust gas, with a breakthrough of 200 ppm H2S, the molar ratio of hydrogen sulfide to iron is 19.5, which corresponds to an absorption of 70% by weight of sulfur. At the regeneration stage, according to the conditions of Example 1, no gases were detected in the gases leaving the reactor. S02- The total amount of sorbed sulfur is isolated as elemental sulfur.
    PRI me R 3. Desulfurization catalytic adsorption mass, obtained by the method of example 2.
    The amount of catalytic absorption mass and desulfurization conditions are the same as in Example 1. After 2 hours, H2S is determined in the off gas from the reactor. Oxygen concentration graphs during desulfurization are comparable to those obtained in Example 1. The sulfur absorption during the desulfurization process is approximately 8% by weight, which corresponds to the molar ratio of H2S to Fe 2.23. The regeneration of the catalytic absorption mass was carried out in the same manner as in Examples 1 and 2. No gas was detected in the effluent gas from the reactor during regeneration. During the pre-sulphidation stage, 30 wt.% - iron oxides are converted
    iron sulfide with a particle size less than 40 nm.
    PRI me R 4 .. Second absorbent desulfurization cycle. Conducted in the same way
    as in example 2. After 15 hours, H2S is determined in the off-gas from the reactor. At this time, the oxygen concentration in the waste gas from the reactor begins to slowly increase. An increase in oxygen concentration corresponds to an increase in H2S concentration. After a breakthrough of 200 ppm H2S, the molar ratio of H2S to Fe is 21, which corresponds to an absorption of 75% by weight of elemental sulfur calculated on the basis of catalytic
    mass of The regeneration is carried out in the manner described in examples 1-3. During regeneration in the waste gases S02 was not detected. PRI me R 5. The fourth cycle of the desulfurization of the absorbent.
    The amount of absorbent is 10.2 ml (5 g). The reaction gas contains 2000 ppm H2S, 2000 ppm oxygen, 2 May. % water and the rest is nitrogen. Bulk velocity during selective oxidation and absorption
    is 2500 (gas flow 425 ml / min). For 60 hours, H2S was not detected in the waste gas from the reactor and the oxygen consumption in the feed gas was 50% by weight, which indicates that the total amount of H2S
    is converted to elemental sulfur according to the indicated reaction. After 60 hours, the concentration of H2S increases dramatically. For leakage of H2S 200 ppm, the molar ratio of H2S to Fe is 22.3, which indicates
    that the sulfur loading is more than 80% by weight. Regeneration is carried out as in Examples 1-4. During regeneration, S02 was not detected.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    The method of purification of gas containing water vapor from hydrogen sulfide, including its contact with a catalytic chemisorption mass containing at least 1% by volume of sulfides or metal oxides deposited on an inert porous carrier, and the subsequent regeneration of a saturated gray mass by evaporating sulfur from purging with heated gas, characterized in that, in order to increase the degree of conversion of hydrogen sulfide into elemental sulfur, the contacting is carried out at a temperature not higher than 90 ° C and a mass containing 2030% by weight of jelly sulphides is used or chromium with a particle size of less than 40 nm, deposited on a finely dispersed carrier, and passing an inert gas at a temperature below the melting of sulfur before blowing the saturated mass.
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    同族专利:
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    AT101806T|1994-03-15|
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    US5152970A|1992-10-06|
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    AU2631488A|1989-06-01|
    NO171626C|1993-04-14|
    EP0324091A3|1989-08-09|
    DK659288A|1989-05-29|
    引用文献:
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    FR2119803B1|1970-09-08|1973-11-23|Aquitainechimie|
    US3890120A|1972-04-18|1975-06-17|Aquitaine Petrole|Process to recover sulphur from the sulphur compounds contained in residual gases|
    FR2224196B1|1973-04-06|1975-12-26|Aquitaine Petrole|
    FR2277877B1|1974-07-11|1976-12-24|Aquitaine Petrole|
    JPS5248585A|1975-10-16|1977-04-18|Unitika Ltd|Method for regenerating carbonaceous catalyst|
    US4311683A|1976-06-28|1982-01-19|Union Oil Company Of California|Process for removal of hydrogen sulfide from gas streams|
    JPS5339286A|1976-09-22|1978-04-11|Hitachi Ltd|Regenerating method for iron oxide removing agent|
    JPS607536B2|1979-02-19|1985-02-25|Nagao Sooda Kk|
    DE3131257C2|1981-08-07|1986-10-30|VEG-Gasinstituut N.V., Apeldoorn|Process for removing hydrogen sulfide from gases|
    DE3228482C2|1982-07-30|1986-09-11|VEG-Gasinstituut N.V., Apeldoorn|Process for the reaction of carbon monoxide with water vapor to form carbon dioxide and hydrogen and the use of a catalyst therefor|
    NL8600959A|1986-04-16|1987-11-16|Veg Gasinstituut Nv|CATALYST FOR THE SELECTIVE OXYDATION OF SULFUR-CONTAINING COMPOUNDS, IN PARTICULAR SULFUR HYDROGENIC TO ELEMENTAL SULFUR; METHOD FOR PREPARING THE CATALYST AND METHOD FOR SELECTIVE OXIDIZATION OF SULFUR CONTAINERS, IN THE PARTICULAR SULFUR HYDROGENIC SODIUM SULFUR.|US5766567A|1990-02-13|1998-06-16|Elf Aquitaine Production|Method for desulphurising a gaseous mixture containing H2 S and SO.sub.|
    DE4104202A1|1991-02-12|1992-08-13|Bayer Ag|CATALYSTS FOR THE REMOVAL OF SULFUR COMPOUNDS FROM TECHNICAL GASES, METHOD FOR THE PRODUCTION AND USE THEREOF|
    CA2087265C|1991-05-13|2002-03-26|Kalabeerappa N. Mahadev|Catalyst and process for removal of sulphur compounds and oxides from fluid streams|
    US5401475A|1991-07-08|1995-03-28|G.E. Environmental Services, Inc.|Process and apparatus for generating elemental sulfur and re-usable metal oxide from spent metal sulfide sorbents|
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    FR2702673B1|1993-03-16|1995-04-28|Elf Aquitaine|Process for removing the H2S contained in a gas in a concentration of less than 5% by volume with recovery of this H2S in the form of sulfur.|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3740439A|DE3740439C2|1987-11-28|1987-11-28|
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