• 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:
    Regenerative process for removing mercaptans contained in a gas by means of an absorbing agent based on at least one metal oxide capable of chemically fixing the mercaptans and comprising an absorption step (1a) to fix the mercaptans on the absorbing agent and a regeneration step (1b) for regenerating the absorbing agent laden with sulphur-containing products resulting from said fixation. The regeneration is carried out by sweeping the absorbing agent with a hot inert gas (32, 28, 11, 1b, 17, 22) to bring said absorbing agent to a temperature comprised between 250 and 500<o>C and desorb the sulphur-containing products, and by contacting the absorbing agent thus treated with a gas containing free oxygen (34, 28, 11, 1b, 17, 22) to reoxidize the absorbing agent and by cooling the reoxidized absorbing agent by sweeping with a cold inert gas (25, 11, 1b, 17, 22). Said regeneration enables to maintain a high activity of the absorbing agent.
    公开号:SU1582975A3
    申请号:SU874028781
    申请日:1987-01-09
    公开日:1990-07-30
    发明作者:Вуарен Робер；Эльг Жан
    申请人:Сосьете Насьональ Елф Акитэн (Продюксьон) (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to processes for the purification of gases from mercaptans by their chemical conversion and may find its application in the chemical industry.
    The purpose of the invention is to increase the service life of the adsorbent.
    The method is implemented as follows.
    Example 1. When working at the facility, industrial natural gas containing 150 ob.m.d. methyl mercaptan, 50 vol.d. propyl-mercaptan, 5 ppm hydrogen sulphide and 2000 ppm hydrocarbons Cf-Cj.
    For this treatment, each of the two reactors of the plant contains 6.5 m3 of adsorbent in the form of balls with a diameter of approximately 5 mm consisting of alumina impregnated as the active metal oxide with 10 wt.% Copper (II) oxide, and the specific surface of said adsorbent is approximately 190 m2 / g. The dynamic adsorption capacity of the new adsorbent corresponds to the adsorption of the amount of sulfur compounds such as mercaptans, which is 3.5 g per 100 g of adsorbent in terms of sulfur.
    cl
    $
    ho
    -h
    SP

    The reactors operate alternately in the adsorption cycle and in the regeneration cycle under the following specific operating conditions, the adsorption cycle. The gas to be treated that enters the reactor during the adsorption stage has the following parameters: flow rate 41,667 Nm3 / H pressure 70 bar, adsorption temperature 30 ° C adsorption cycle time 12 hrs Regeneration cycle; Decompression Phase: duration 15 min; decompression rate 5 bar / min; 1 purge of the adsorbent to be regenerated with a hot inert gas: purge gas flow rate of 3850 norms, mea / h, purge gas temperature at the exit - 350 ° C9 from the furnace, sweep duration 4 h 45 min, gas descent through valve 100, nitrogen injection through valve 100 m / h; re-oxidation of the adsorbent: duration 2 hours, the temperature of the gas again. The second oxidation at the exit of the 350 ° C furnace is the oxygen content in the gas for re-oxidation of 1% by volume; cooling of the reoxidized adsorbent: duration 4 h 45 min, cooling gas flow rate 3850 normal m 3 / h, cooling gas temperature 30 ° Cj recompression of the cooled regenerated reactor with purified gas: duration 15 min, recompression rate 5 bar / min.
    In the purified gas, the total content of sulfur compounds is below 10 vol. ”Ppm.
    After 150 cycles of adsorption and regeneration, the dynamic adsorption capacity of the regenerated adsorbent is still almost equal to the dynamic adsorption capacity of the new adsorbent.
    Example 2 When working at a facility, industrial natural gas containing 52 vol. D. methyl mercaptan, 18 vol., Ppm, propylmer captan, 5 ppm hydrogen sulphide and 2000 ppm hydrocarbons.
    For this treatment, each of the two reactors of the plant contains 1.5 tons of adsorbent, identical to that used in Example 1,
    The reactors operate alternately in the v adsorption cycle and in the regeneration cycle under the following specific operating conditions. Absorption cycle. The gas to be processed through the pipe into the reactor, which is at the stage of adsorption, has the following parameters: flow rate 41667 Nm3 / h, pressure 70 bar, adsorption temperature 30 C. The duration of the adsorption cycle is 12 h.
    Regeneration cycle. Decompression phase: duration 15 minutes, decompression speed 5 bar / min; blowing of the adsorbent to be regenerated with a hot inert gas: the flow rate of the purge gas is 1500 Nm3 / h, the temperature of the purge gas at the outlet of the preheater is 350 ° C, the duration of the purge is 3 4J re-oxidation of the adsorbent: the duration is 2 h, the temperature of the gas for re-oxidation at the exit from preheater, the oxygen content in the gas for re-oxidation is 1.5 o6.% j cooling of the re-oxidized adsorbent: duration 6.5 h, flow rate of the cooling gas 750 norms m³ / h, temperature of the cooling gas entering through pipe 30 °, recompression of cooled regenerated reactor with purified gas; the duration is 15 minutes, the recompression rate is 5 bar / min.
    In the purified gas, the total sulfur content is below 2 kg / normal m3,
    Example 3. When working at the facility, industrial natural gas containing 52 ob.m. methyl mercaptan, 18 ob.m. propyl-mercaptan ,, 5 ppm, hydrogen sulfide and 2000 ppm hydrocarbons
    For this treatment, each of the three reactors of the plant contains 1.5 tons of adsorbent, identical to the adsorbent used in Example 1,
    The reactors operate sequentially in the adsorption cycle, in the regeneration cycle and in the cooling cycle under the following specific operating conditions.
    Adsorption cycle.
    The gas to be treated, which enters the reactor at the stage of adsorption, has the following parameters: flow rate 41,667 m3 / h; pressure 70 bar; adsorption temperature 306С {adsorption cycle time 12 h.
    Regeneration cycle. Decompression Phase: 1 hour duration} Decompression rate 1.15 bar / min; purging the adsorbent to be regenerated with a hot inert gas with regeneration; flow rate of the purge gas 750 normal m3; the temperature of the purge gas at the exit of the furnace; purge duration 6 hours; re-oxidation of the adsorbent; duration 4 hours; re-oxidation gas temperature at the outlet of the preheater oxygen content in the re-oxidation gas of 1% by volume; recompressing the regenerated reactor with purified gas; duration 1 h, recompression rate 1.15 bar / min.
    Cooling cycle
    Cooling of the reoxidized adsorbent: duration: 12 hours. Cooling gas flow rate: 750 Nm. 3 / Cooling gas temperature at the pipe inlet is 30 ° C.
    1582975
    0
    five
    a heater of 450 ° C and with a duration of purging with said re-oxidation gas for 1.5 hours while the remaining operating conditions corresponded to the conditions of example 2.
    The purified gas contained a total sulfur concentration of less than 1.8 kg / norm.m3.
    When carrying out the method of gas purification by a known method, the sulfur compounds accumulate in the pores of the adsorbent, which causes a rapid loss of the activity of the adsorbent and a decrease in its service life.
    权利要求:
    Claims (2)
    [1]
    1. The method of purification of gas from mercaptans, including the adsorption of hydroxy; Example 4. Acted in a us-JQ house of metal deposited on a solid
    porous carrier at a temperature of 100 °
    of example 3 using. adsorption temperature of 40 ° C, temperate, followed by thermal regeneration of the adsorbent and its cooling-. different in that
    The inert purge gas at the exit from the furnace is 300 ° C, the purge duration is 7 hours, the temperature of the re-oxidation gas at the exit from the furnace is 300 ° C and the cooling gas temperature is 40 ° C, while the remaining operating conditions correspond to example 3.
    The purified gas contained a total sulfur concentration below 2 mg / normal m3.
    Example 5. Operated under conditions of example 2 using a purge inert gas temperature at the outlet of the 450 C heater, with a purge duration of the specified inert gas of 2.5 hours, with a re-oxidation gas temperature at the outlet of 100 °
    followed by thermal regeneration of the adsorbent and its cooling, characterized in that
    that, in order to increase the service life of the adsorbent, regeneration is carried out in two stages, with the first adsorbent being purged with an inert gas at 300-450 ° C, and at the second with oxygen-containing gas with oxygen content of 1-1.5 vol 7, at 300- 450 C followed by inert gas purging of the bed until oxygen is completely removed.
    I
    [2]
    2. A method according to claim 1, characterized in that copper (II) oxide deposited on alumina is used as the adsorbent.
    类似技术:
    公开号 | 公开日 | 专利标题
    US3974256A|1976-08-10|Sulfide removal process
    EP1651565B1|2011-08-24|Processes and systems for making phosgene
    US4008174A|1977-02-15|Process for regenerating a solid copper-chromium reactant used in the removal of hydrogen sulfide from hydrogen recycle gas
    US4251495A|1981-02-17|Process for purifying a hydrogen sulfide containing gas
    US6610264B1|2003-08-26|Process and system for desulfurizing a gas stream
    US5458861A|1995-10-17|Desulfurizing a gas stream
    TWI450752B|2014-09-01|Contaminant removal from a gas stream
    CN1105175A|1995-07-12|Method for removing sulphur compounds from a residual gas such as a residual gas from a claus process sulphur plant, and recovering said compounds as sulphur
    SU1722210A3|1992-03-23|Method of cleaning humid gas from hydrogen sulfide
    RU2142405C1|1999-12-10|Method and catalyst for oxidation of h2s containing in gas at small concentration to sulfur by catalytic method
    CN1043029C|1999-04-21|Method for removing hydrogen sulphide from a gas and recovering in the form of sulphur
    RU2107024C1|1998-03-20|Method and catalyst for directly oxidizing hydrogen sulfide into sulfur
    FR2587236A1|1987-03-20|PROCESS FOR REMOVING SULFUR OXIDES FROM A GAS USING A REGENERABLE ABSORPTION MASS BY REACTION WITH HYDROGEN SULFIDE
    JP3766100B2|2006-04-12|H {circle around |} SO and SO {circle around 2} methods of catalytic desulfurization of gases containing compounds, and catalysts for carrying out the method
    EA002246B1|2002-02-28|Method for direct oxidation in sulphur by catalytic process and in vapour phase of low content h2s in a gas
    SU1582975A3|1990-07-30|Method of purifying gases from mercaptanes
    US5492684A|1996-02-20|Graded-bed system for improved separations
    US4871521A|1989-10-03|Sulfur recovery process using metal oxide absorbent with improved purge
    CA1296508C|1992-03-03|Removal of water vapor diluent after regeneration of metal oxide absorbent to reduce recycle stream
    US4855117A|1989-08-08|Process for removing sulfur oxides from a gas by means of an absorption mass regenerable by reaction with elemental sulfur
    AU664754B2|1995-11-30|Process and apparatus for recovery of sulphur from a gas stream containing hydrogen sulphide
    JPH08257369A|1996-10-08|Method for desulfurization of h2s-containing gas
    JPH0776348B2|1995-08-16|Refining method for high temperature reducing gas
    EP0514941A1|1992-11-25|Process for the separation of sulphur oxides from offgases
    US4781903A|1988-11-01|Process for removing sulfur oxides from a gas by means of an absorption mass regenerable by reaction with elemental sulfur
    同族专利:
    公开号 | 公开日
    EP0221942B1|1989-08-16|
    DE3665026D1|1989-09-21|
    JPH0576325B2|1993-10-22|
    EP0221942A1|1987-05-20|
    WO1986006649A1|1986-11-20|
    CA1267269A|1990-04-03|
    FR2581560A1|1986-11-14|
    FR2581560B1|1987-06-05|
    US4774067A|1988-09-27|
    JPS62502815A|1987-11-12|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2259409A|1938-06-03|1941-10-14|Walter H Duisberg|Process for reactivating desulphurizing masses|
    US2551905A|1946-04-29|1951-05-08|Phillips Petroleum Co|Desulfurization of gases|
    US2747968A|1951-05-07|1956-05-29|Pigache Pierre Gustave Adolphe|Dry process for the recovery of sulfur from gases|
    BE661165A|1964-03-17|1965-07-16|US5114689A|1987-10-05|1992-05-19|Uop|Integrated process for the removal of sulfur compounds from fluid streams|
    JPH0790137B2|1988-02-10|1995-10-04|財団法人電力中央研究所|Refining method for high temperature reducing gas|
    JP2651381B2|1988-09-13|1997-09-10|財団法人電力中央研究所|Purification method of high-temperature reducing gas|
    CA2120046C|1994-01-27|1999-09-14|M-I L.L.C.|Separately removing mercaptans and hydrogen sulfide from gas streams|
    GB9908752D0|1999-04-16|1999-06-09|Bp Oil Int|Purification process|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FR8507121A|FR2581560B1|1985-05-10|1985-05-10|REGENERATIVE PROCESS FOR THE REMOVAL OF MERCAPTANS CONTAINED IN A GAS|
    [返回顶部]