• 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 separating hydrogen sulphide from clarified green liquor, including precarbonating green liquor with a carbon dioxide rich gas, adding alkali bicarbonate to the precarbonated green liquor and stripping hydrogen sulphide therefrom forming simultaneously alkali carbonate, and preparing the alkali bicarbonate used in the process from the alkali carbonate formed. The process of the invention is carried out by performing the hydrogen sulphide stripping without crystallizing the alkali carbonate formed, preparing the alkali bicarbonate partly from alkali carbonate-alkali sulphide solution obtained in the precarbonation step and partly from the non-crystallized alkali carbonate solution, feeding at least a portion of the alkali carbonate - alkali sulphide solution through the carbonation step, and passing the carbon dioxide rich gas first through the carbonation step and thereafter through the precarbonation step.
    公开号:SU965340A3
    申请号:SU742078679
    申请日:1974-11-27
    公开日:1982-10-07
    发明作者:Вильгельм Романтчук Хякан；Юхани Туомо
    申请人:Ой Тампелла А Б (Фирма)；
    IPC主号:
    专利说明:

    solution with a half of an alkali metal bicarbonate and hydrogen sulfide stripping, the alkaline solution after contact with gases at the preliminary carbonization stage is divided into two streams in a ratio of 1: 1-3) one of which is fed to the carbonization stage, and the second hydrogen sulfide, and the resulting alkali metal carbonate is partially returned to the stage of carbonization.
    The proposed method allows to increase the degree of utilization of carbon dioxide from 15 to 70%, i.e. / 5 times. .
    The selected numerical interval characterizing the quantitative ratio of the flows directed to carbonization and stripping is due to the fact that 25-50 CO - containing gas must be fed to carbonization in order to quantitatively transfer it to bicarbonate, and the rest of it is fed to stripping to achieve fuller utilization ecu-containing gas.
    Example 1. From a concentrated waste liquid burned in a furnace, a melt is obtained, 6 which is dissolved in water to obtain a green liquid, and the solid phase is removed from this liquid by means of sedimentation. The purified green liquid is pumped into a pre-carbonation column, where the sodium sulfide of the green liquid reacts with carbon dioxide waste gas to form a bisulfide; PIA. After the preliminary carbonization, the green liquid is divided into two streams in the ratio 1: 1-3, pumped partially into the carbonization stage and partially into the stripping stage, to which sodium bicarbonate obtained in the carbonation stage is simultaneously pumped. Steam is fed to the lower part of the stripping section in order to force the hydrogen sulfide to transfer from the solution to the vapor phase.
    Water vapor condenses from the gas mixture to the surface of the condenser. It has been found that the optimum pressure for stripping is a vacuum O, i (atm generated by a vacuum pump that simultaneously transfers hydrogen sulfide for combustion, for example, in a sulfur furnace.
    The solution phase, obtained from the bottom of the stripping section and containing mainly sodium carbonate and, in a smaller amount, sodium sulfide, sodium sulfate and sodium thiosulfate, is partially pumped into the carbonizer, and the residue is used for other purposes.
    At the stage of carbonation bicarbonate
    sodium is obtained from sodium carbonate by the absorption of carbon dioxide into the solution from the flue gases. The flue gases are injected into the carbonizer with the blower.
    Part of the gas from the carbonizer is circulated to the inlet side of the gas blower and the necessary gas is supplied as fresh gas from the autoclave. Part of the gases corresponding to the fresh gas is blown over by the gas blower to the pre-carbonation stage and released from there. In the pre-carbonation stage, the hydrogen sulfide produced in the carbonation stage is absorbed from the exhaust gas into the green liquid entering the process and having high alkalinity.
    As a result of at least partially producing bicarbonate directly from a pre-carbonated green liquid, the amount of solution treated in the stripping step and the amount of steam consumed is reduced. On the other hand, with an increase in the sulfide content in the solution that is carbonized, the amount of hydrogen sulfide separated in the carbonization step increases to such an extent that
     full recarbonisation of the green liquid in the pre-carbonation column cannot occur. Usually, because of this, a portion of the pre-carbonized liquid should
     go past the carbonation stage directly to the stripper and the sulfide content in the solution of the carbonation stage should be reduced by the solution from the stripper.
    权利要求:
    Claims (2)
    [1]
    Example 2. Green liquid is supplied at a rate of 10 MV4. concentration 180 g MagO / liter, content. sulphides 50. As a result, 5 kmol / h and Na2S T + jS kmol / h are obtained in the green liquid. The fluid is divided into two streams at a ratio of 1: 3. In order to carbonize the above amount of green liquid, the reaction requires 2Na, Sch-H O + -C02. 2NaHS-, (l OjSTt.S hmol / h kmol / h of carbon dioxide. To separate the hydrogen sulfide by stripping NaHCO-HJS- (2) sodium carbonate, it is necessary that at least its amount is equivalent to sodium bisulfide, t i.e., 5 kmol / h. But it is more advantageous to use sodium bicarbonate in excess, approximately 20-80% (18 kmol / h). To obtain the specified amount of bicarbonate during carbonization, carbon dioxide is required in accordance with the Na reaction. 2.CO + COA. 2MANSOZ (3) 0.518, kmol / h 9.2 kmol / h. Exhaust gases from the furnace contain k-} 6% dioxide There is a small amount of fresh gas. Carbon dioxide content in the gas decreases at the carbonation stage by about 15 to 10%, resulting in a need for fresh carbonization at a rate of 3500. The gas exits from the stage of carbonization with a speed of about 3300 and contains 3.7% CO. The gas circulates in the carbonizer with a speed of HOOO HMV4, i.e. total of 17,500 gas is injected through the carbonizer. All off-gas (about 3,300 nm / h) coming out of the carbonizer is fed to pre-carbonation, as a result of which hydrogen sulfide formed in the remaining sulphide can be reabsorbed into the pre-carbonization column from the off-gas to green liquid, preventing the ingress of it into the environment. In the preliminary carbonization stage, carbon dioxide (a zod is consumed in an amount of kmol / h, i.e. the gas leaving the preliminary carbonization stage (approximately 3130) contains 5 CO.) The degree of carbon dioxide used in the carbonization and preliminary carbonization stages is em 10%. Formula of the Invention A method for separating hydrogen sulfide from clarified green liquor, including pre-carbonation by contacting the liquor with flue gases containing carbon dioxide, carbonization of the solution with the charge alkali metal bicarbonate and hydrogen sulphide stripping, which is due to the fact that, in order to increase the degree of carbon dioxide utilization and simplify the process, the alkaline solution after contact with gases at the preliminary carbonization stage is divided into two streams in a 1: 1-3 ratio one of which is fed to the carbonization stage, and the second is directly sent to the hydrogen sulfide stripping stage, and the resulting alkali metal carbonate is partially returned to the carbonization stage. Sources of information taken into account during the examination 1. Cole AL, Rizenfeld F.S. Gas cleaning. M., Nedra, 1968, p. 88, 89.
    [2]
    2. Patent of the USSR No. 289580, cl. C 01 D 7/24, 1967 (prototype).
    类似技术:
    公开号 | 公开日 | 专利标题
    US3826710A|1974-07-30|Carbonation system for recovery of sodium base pulping liquor
    US1983789A|1934-12-11|Production of pulp and treatment of residual liquors, etc.
    SU965340A3|1982-10-07|Method for separating hydrogen sulfide from clarified green soda liquor
    US4098886A|1978-07-04|Gas purification liquors
    US2993753A|1961-07-25|Sodium sulphite liquor recovery
    US2841561A|1958-07-01|Recovery of chemicals from smelt solutions
    US3617434A|1971-11-02|Regeneration of cooking chemicals from spent alkaline cooking liquor
    US3941875A|1976-03-02|Process for treating gas containing hydrogen sulfide
    US4122148A|1978-10-24|Sulfur dioxide removal process
    CA1059726A|1979-08-07|Potassium carbonate recovery
    US3650889A|1972-03-21|Pollution controlled polysulfide recovery process
    US1570299A|1926-01-19|Ammonia soda process
    US1934655A|1933-11-07|Treatment of residual liquors
    US2909407A|1959-10-20|Method in the recovery of alkali and sulphur by carbonization of melt soda solutions obtained in the manufacture of cellulose
    US1542971A|1925-06-23|Process of producing alkali-metal carbonates
    US4083930A|1978-04-11|Method of treating alkali metal sulfide and carbonate mixtures
    US1653933A|1927-12-27|Gas-purification process
    CA1109231A|1981-09-22|Method of stripping ammonia from ammoniacal solutions
    US4079119A|1978-03-14|Sulfur dioxide removal process
    SU1303040A3|1987-04-07|Method for extracting chemicals from green lye containing chlorides
    US3402992A|1968-09-24|Method for recovering chemicals from waste liquor obtained during the production of cellulose
    US4153670A|1979-05-08|Method of treating an alkali metal sulfide liquor
    US2872289A|1959-02-03|Process in recovering sulphur from waste sulphite lye
    US3005686A|1961-10-24|Sodium sulfite recovery process
    US1992572A|1935-02-26|Process for producing sulphates and sulphur
    同族专利:
    公开号 | 公开日
    HU176587B|1981-03-28|
    FR2252290B1|1981-08-28|
    SE412772B|1980-03-17|
    CA1041708A|1978-11-07|
    SE7414894L|1975-05-29|
    US4049787A|1977-09-20|
    DE2449131C3|1979-07-26|
    FI49737C|1975-09-10|
    JPS5085596A|1975-07-10|
    FI49737B|1975-06-02|
    NO743726L|1975-06-23|
    DE2449131A1|1975-06-05|
    CS226157B2|1984-03-19|
    FR2252290A1|1975-06-20|
    NO141808C|1980-05-14|
    JPS5413237B2|1979-05-29|
    NO141808B|1980-02-04|
    DE2449131B2|1978-11-23|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2675297A|1954-04-13|Solution phase process of convert |
    US2864669A|1954-11-01|1958-12-16|Stora Kopparbergs Bergslags Ab|Method for recovering sulfur and alkali from waste liquors|
    DE1692877C3|1965-11-24|1975-10-02|Oy Tampella Ab, Tampere |Method and device for working up aqueous sulphide solutions, in particular green liquors containing sodium sulphide resulting from the production of alkaline sulphate cellulose|
    DE1692878C3|1966-05-25|1974-04-04|Oy Tampella Ab, Heinola |Process / to crystallize out alkali as carbonate from the melting solution resulting from the processing of the pulp waste liquor|
    US3826710A|1972-04-21|1974-07-30|Owens Illinois Inc|Carbonation system for recovery of sodium base pulping liquor|DE2506969C2|1975-02-19|1983-12-01|Metallgesellschaft Ag, 6000 Frankfurt|Process for avoiding the odor nuisance of the environment when concentrating pulp waste liquors|
    US4241041A|1979-01-22|1980-12-23|Mei Systems Inc.|Methods for the recovery of sulfur components from flue gas and recycle sodium sulfite by reduction-smelting and carbonating to strip hydrogen sulfide|
    FI67732C|1982-10-20|1985-05-10|Tampella Oy Ab|SAETT ATT AOTERVINNA KEMIKALIER FRAON KLORIDHALTIG GROENLUT|
    US6284199B1|1999-03-31|2001-09-04|Mcdermott Technology, Inc.|Apparatus for control of mercury|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FI733671A|FI49737C|1973-11-28|1973-11-28|Method for separating sulfur hydrogen sulphide from clarified green liquor obtained from the incineration of waste liquor.|
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