• 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:
    A method for manufacturing sulphuric acid from sulphur-dioxide containing gas, particularly furnace gas obtained from metallurgical processes by oxidation to sulphur trioxide in the presence of a catalyst and conversion of the sulphur trioxide to sulphuric acid. The sulphur dioxide is first separated from the gas preferably converted to liquid form and is then subsequent to being vaporized in a stoichiometric excess oxidized with oxygen.
    公开号:SU1331422A3
    申请号:SU823392949
    申请日:1982-02-18
    公开日:1987-08-15
    发明作者:Арвид Петерссон Стиг；Кристер Ваара Улф
    申请人:Болиден Актиеболаг (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to methods for producing sulfuric acid from highly concentrated sulfur gases.
    The aim of the invention is to simplify the process and the possibility of regulating the temperature in the catalyst bed during the processing of highly concentrated sulfur gases.
    One of the factors arising from the production of sulfuric acid 1 from a centered 1, gx sulfurous gas, 1.x gases and technical oxygen is the loss of catalyst activity caused by a sharp rise in temperature, and the associated difficulty in controlling the latter. To avoid this, oxidation is concentrated
    SO is carried out with respect to S (3/0 "9-16, i.e. with a lack of oxygen). In addition, to avoid overheating of the catalyst, part of the sulfur dioxide in liquid form is fed directly to the catalyst bed.
    ha 35
    The drawing shows the scheme. The master mixture was introduced into the catalyst bed with a thickness of 300-400 mm. The catalyst brand VL F 04-10 is made in the form of 6-mil.time rods with a total weight of 100-150 g containing V.O,
    30 components of 6 wt.%. Temperature
    the layer was adjusted continuously. The input and temperature values in the set conditions are given in the table.
    together with other experimental data-.
    In all cases, with the exception of experiment 5, almost 100% of oxygen was produced. The best temperatures were observed in experiments 3 and 4. In experiments 1 and 2, the gas mixture was preheated to achieve stable oxidation. In Run 5, the catalyst collapsed as a result of a strong temperature rise, but this could have been avoided, according to the invention, if part of the sulfur dioxide was introduced in the liquid state and cooled the catalyst bed. Other catalysts - Degas 1% Ft on silicon and Haldor50 Topsø K-38A, made in the form
    rings 4x7 mm, 7% V, jO 5, gave similar positive results.
    As follows from the table, when exiting the way.
    Liquid sulfur dioxide from tank 1 through line 2 is directed to the evaporator 3, where the evaporation SOj is carried out by steam or hot. The resulting zoo-shaped sulfur dioxide, having a temperature of -25 ° C, flows through conduit 4 to heat exchanger 5, where SO is heated by oxygen supplied through conduit 6. The gas mixture is preheated via conduit 7 to contact apparatus 8, in which SO o is oxidized to SO, to the oil in the presence of a catalyst, for example vanadium pentoxide. In cases where the NeoRhol stacks, the imo catalyst is intensively cooled, liquid sulfur dioxide), directly into the catalyst bed.
    As a result of the exothermic reaction, the gas mixture) is heated to
    ten,
    650 C, then through the pipe line U it is passed through the boiler-cooler where the temperature of the mixture decreases to 400 ° C .; after it passes through the pipeline 11, it enters the contact apparatus 12, and then into the heat exchanger 5 through the pipeline 13. Then through the pipeline 14, the gas mixture is fed to the absorption column 15, which is irrigated with sulfuric acid circulating through the pipes (5pins 16, 17. To the sulfuric acid solution through the pipeline for the proposed ratio. Gg the catalyst overheats during operation and quickly collapses the contact site, the replacement of the catalyst, thereby complicates the process.
    Two of the 18 add water in an amount corresponding to the amount of sulfur trioxide. Unabsorbed in absorption
    column 15 enters the heat exchanger 5 via conduit 19, and hot sulfuric acid with absorbed sulfur dioxide is supplied to heat exchanger 20 via conduit 16 for cooling with water. Part of the acid through line 21 is sent to a stripping column 22, from which line 6 stripped 30 and oxygen is fed into the heat exchanger 5.
    Example. In order to study the properties of the catalysts used in the oxidation of pure gaseous sulfur dioxide with pure oxygen to sulfur trioxide, a series of experiments was carried out. The magnitudes of the gas flows were recorded by a flow meter for each component separately, after which the gas1 was mixed before heating. Then preheated gas for the proposed ratio. gg, the catalyst during operation overheats and quickly collapses, which entails stopping the contact node, replacing the catalyst, thereby complicating the process.
    the same need to install cooling editors M.Tsitkina
    Compiled by V.Trubchenko
    Tehred-M.Morg Enta Corrector N.Korol
    Order 6183 Circulation 456 Subscription
    VNIIPN USSR State Committee
    on affairs of inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
    Production and printing company, Uzhgorod, Projecto st., D
    rata,
    权利要求:
    Claims (1)
    [1]
    METHOD FOR PRODUCING SULFURIC ACID, including oxidation of concentrated> sulfur dioxide to oxygen trioxide in the presence of a catalyst at 400-680 ° C, recycling of unreacted sulfur dioxide to oxidation steel, absorption of sulfur trioxide by sulfuric acid, characterized in that, in order to simplify the process and improving temperature control in the catalyst bed during the processing of highly concentrated gases, oxygen is supplied to the sulfur dioxide oxidation stage in an amount providing a sulfur dioxide / oxygen ratio of 9-16.
    SU „„ 1331422 AZ do 18 add water in an amount corresponding to the amount of sulfur trioxide. The gas not absorbed in the absorption column 15 enters the heat exchanger 5 through a pipe 19, and hot sulfuric acid with absorbed sulfur dioxide is fed into the heat exchanger 20 through a pipe 16 for cooling 10 with water. A part of the acid is sent through a pipe 21 to a stripping column 22, from which SO is stripped off via a pipe 6, and oxygen is supplied to a heat exchanger 5.
    15 Example. To study the properties of the catalysts used in the oxidation of pure gaseous sulfur dioxide with pure oxygen to sulfur trioxide, a number of experiments were carried out. The quantities of gas streams recorded flow meter for each component individually, hours after which the gases are mixed before heating. Then, the preheated gas mixture was introduced into the catalyst layer 300-400 mm thick. The catalyst brand FΛ F 04-10 is made in the form of 6 mm rods with a total weight of 100-150 g with a V ^ Oj content of 6 wt.%. The temperature of the layer was continuously adjusted. The inlet and outlet temperatures under steady conditions are given in the table together with other experimental data ·.
    In all cases, with the exception of experiment 5, there was an almost 100% oxygen release. The best temperatures were observed in experiments 3 and 4. In experiments 1 and 2, the gas mixture had to be preheated to achieve stable oxidation. In experiment 5, the catalyst was destroyed as a result of a sharp increase in temperature, but this could have been avoided if, in accordance with the invention, part of the sulfur dioxide had been introduced in the liquid state and cooled the catalyst layer. Other Degass 1% Pt catalysts on silicon and Haldor 5Q Topsyo K-38A, made in the form of rings 4x7 mm, 7% V 2 0 5 , gave similar positive results.
    As follows from the table, when the proposed SO ^ / O ^ 55 ratio is exceeded, the catalyst overheats and quickly collapses during operation, which entails the stop of the contact node, replacing the catalyst, thereby complicating the process.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1331422A3|1987-08-15|Method of production of sulfuric acid
    AU2007315318B2|2013-05-30|Process and apparatus for the catalytic oxidation of SO2-Containing gases by means of oxygen
    US7544344B2|2009-06-09|Process for recovering sulphur from a gas stream containing hydrogen sulphide
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    US4212855A|1980-07-15|Process for producing concentrated sulfuric acid
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    WO2008064698A1|2008-06-05|Process for the production of sulfuric acid
    US3374061A|1968-03-19|Process for obtaining sulfuric acid
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    US4419337A|1983-12-06|Process and apparatus for reacting sulphur-containing material with oxidizing gas
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    US4331630A|1982-05-25|Apparatus for incineration of sulfur plant tail gas
    US3755549A|1973-08-28|Catalytic oxidation of so2 to so3
    US3780166A|1973-12-18|Process of catalytically reacting so2 to form so3 and of producing sulfuric acid
    US4088742A|1978-05-09|Contact sulfuric acid process employing double conversion/double absorption
    KR19980703355A|1998-10-15|Liquid phase conversion of sulfur dioxide to sulfuric acid
    GB2187444A|1987-09-09|Treatment of gas stream comprising H2S
    US2588331A|1952-03-04|Recovery of alkylation sludge acids
    US1923256A|1933-08-22|Process of making contact sulphuric acid
    CA1337318C|1995-10-17|Treatment of gas streams
    US4241040A|1980-12-23|Incineration of sulfur plant tail gas
    US1995360A|1935-03-26|Manufacture of sulphuric acid
    同族专利:
    公开号 | 公开日
    GR74935B|1984-07-12|
    EP0042829B1|1985-04-24|
    WO1981003654A1|1981-12-24|
    PT73153A|1981-07-01|
    RO84467B|1984-09-30|
    EP0042829A1|1981-12-30|
    SE422317B|1982-03-01|
    US4520003A|1985-05-28|
    ZA813880B|1982-06-30|
    SE8004588L|1981-12-20|
    ES503137A0|1982-04-16|
    PT73153B|1982-07-16|
    JPS57500827A|1982-05-13|
    RO84467A|1984-08-17|
    CA1182275A|1985-02-12|
    ES8203795A1|1982-04-16|
    FI67833C|1985-06-10|
    FI820410L|1982-02-09|
    YU153981A|1983-06-30|
    DE3170107D1|1985-05-30|
    AT12925T|1985-05-15|
    FI67833B|1985-02-28|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2457173C2|2007-03-29|2012-07-27|Уде Гмбх|Method of producing sulphuric acid and apparatus for realising said method|
    RU2697563C1|2018-05-25|2019-08-15|Публичное акционерное общество "Газпром"|Method of producing sulfuric acid|CA469958A|1950-12-12|Cathala Joseph|Process for the manufacture of sulphur trioxide|
    US723596A|1902-06-12|1903-03-24|Gen Chemical Corp|Process of making sulfuric anhydrid.|
    US1344905A|1919-06-09|1920-06-29|Laist Frederick|Method of producing sulfur dioxid|
    US1520093A|1923-10-13|1924-12-23|Hercules Powder Co Ltd|Process of making sulphuric acid|
    BE406758A|1933-12-13|1900-01-01|
    BE483396A|1941-02-24|
    GB637585A|1946-01-16|1950-05-24|Pietro Guareschi|Process for the manufacture of oleum|
    CH523204A|1967-11-25|1972-05-31|Bayer Ag|Process for the catalytic oxidation of SO2 to SO3|
    NO131417L|1970-05-01|
    DE2114667A1|1971-03-26|1972-10-05|Bayer|Process, device and catalyst for the production of oleum and sulfuric acid by catalytic ^ oxidation of SO deep 2 to SO deep 3|
    BE792061A|1971-12-02|1973-05-29|Bayer Ag|PRODUCTION OF SULFURIC ANHYDRIDE AND SULFURIC ACID|
    JPS4954295A|1972-03-21|1974-05-27|
    DE2223131C3|1972-05-12|1979-10-11|Davy Powergas Gmbh, 5000 Koeln|Process for the production of sulfuric acid from sulfur and oxygen|
    DE2307973A1|1973-02-17|1974-08-29|Metallgesellschaft Ag|METHOD OF CATALYTIC IMPLEMENTATION FROM SO DEEP 2 TO SO DEEP 3|
    SE382967B|1973-10-15|1976-02-23|Boliden Ab|PROCEDURE FOR EXTRACTING LIQUID SULFUR DIOXIDE FROM GASES CONTAINING SULFUR DIOXIDE|
    DE2418216C2|1974-04-13|1983-02-17|Hoechst Ag, 6000 Frankfurt|Process for the production of sulfur trioxide from sulfur dioxide and oxygen|
    JPS51103895A|1975-03-11|1976-09-14|Nissan Eng|Sansankaiono seizohoho|
    EP0004745A1|1978-04-07|1979-10-17|BOC Limited|Process for the catalytic oxidation of sulphur dioxide to form sulphur trioxide|
    JPS5722393A|1980-07-14|1982-02-05|Mitsubishi Electric Corp|Controlling device for transistor motor|SE437013B|1981-10-26|1985-02-04|Boliden Ab|VIEW TO USE FROM DISCONTINUOUS PROCESSES CONCERNING SULFUR Dioxide INCLUDING PROCESS GASES IN THE PRODUCTION OF SULFURIC ACID IN A CONTACT PLANT|
    US4902493A|1988-05-04|1990-02-20|The Dow Chemical Company|Process for the generation of sulfur trioxide reagent and sulfonation of the surface of polymeric resins|
    US4915912A|1988-05-04|1990-04-10|The Dow Chemical Company|Apparatus for the generation of sulfur trioxide reagent and sulfonation of the surface of polymeric resins|
    DE3819417C2|1988-06-07|1990-10-18|Utab Gesellschaft Fuer Umwelttechnischen Anlagenbau Mbh, 4100 Duisburg, De|
    US5458861A|1992-04-15|1995-10-17|Mobil Oil Corporation|Desulfurizing a gas stream|
    US5591417A|1992-04-15|1997-01-07|Mobil Oil Corporation|Removing SOx, CO and NOx from flue gases|
    US5514351A|1992-04-15|1996-05-07|Mobil Oil Corporation|Desulfurizing tailgas from sulfur recovery unit|
    US5292492A|1992-05-04|1994-03-08|Mobil Oil Corporation|Recovering sulfur from ammonia acid gas stream|
    US5851265A|1996-09-03|1998-12-22|Monsanto Company|Selective removal and recovery of sulfur dioxide from effluent gases using organic phosphorous solvents|
    WO2000014011A1|1998-09-03|2000-03-16|Cansolv Technologies Inc.|Sulphuric acid conversion process|
    US20080213149A1|2004-08-09|2008-09-04|Richard Gauthier|Process for producing steam and/or power from oil residues|
    US7361326B2|2005-11-15|2008-04-22|Haldor Topsoe A/S|Process for the production of sulfuric acid|
    LU92547B1|2014-09-17|2016-03-18|Cppe Carbon Process & Plant Engineering S A|METHOD FOR THE CATALYTIC REMOVAL OF SULFUR DIOXIDE FROM EXHAUST GASES|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE8004588A|SE422317B|1980-06-19|1980-06-19|PROCEDURE FOR THE PRODUCTION OF Sulfuric Acid from Sulfur Dioxide CONTAINING GAS|
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