• 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 and apparatus for causing the sulfur dioxide of flue gases to react to form solid sulfates and sulfites which can be separated from the flue gases. Sulfur dioxide containing flue gases (16) are directed according to the invention into one end of an oblong reaction zone (4), in addition to which pulverous calcium compounds and water are directed separately into the reaction zone at several points, and finally from the opposite end a flue gas suspension is withdrawn and directed to dust separation (5). By feeding the pulverous reagent and the water separately into the reactor 4, the problems involved in the preparing, handling and spraying of an aqueous slurry are avoided, in addition to which the retention time and the reaction conditions can be regulated easily in the oblong reactor 4.
    公开号:SU1679969A3
    申请号:SU853974783
    申请日:1985-11-06
    公开日:1991-09-23
    发明作者:Хямяля Сирпа；Кенаккала Тимо；Янка Пентти；Руохола Туомо；Лехтимяки Мартти
    申请人:Ой Тампелла Аб (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to flue gas cleaning technology for S02 using alkali and alkaline earth metal oxides and can be used when burning sulfur-containing fuels such as coal or oil in furnaces.
    The purpose of the invention is to simplify the process by eliminating the recirculation of unreacted reagent.
    Figures 1 and 2 show schematically installations for the purification of gases from SOa.
    Inject 1 for combustion the sulfur-containing fuel 2 and the air stream 3. The flue gases containing 50a are cooled on the thermal surfaces 4 in the furnace and in the air heater 5. After the furnace, the flue gases 7 are directed to the elongated reactor 8,
    followed by a dust collector 9 and a chimney 10. The ratio of the length of the reactor to its effective diameter, calculated from the cross-sectional area, is greater than 10.
    The alkaline dusty reagent, preferably an alkali or alkaline earth metal oxide, designed to bind SO-2, is fed from the storage tank 11 through the metering feeders 12 into the air flow of the pneumatic blower 13, through which it is blown into the upper part of the furnace 1 through line 14 and / or through the pipeline 15 to the first part of the reactor 8 and possibly to some subsequent point of the reactor 8 through the pipeline 16.
    about VI th
    oh oh

    Ca
    The flue gas temperature supplied to the reactor is “90-200 ° С. Additionally, water is injected into the elongated reactor 8 through the nozzles 17, either only at the beginning or at several points high in the reactor. Additionally, warm air can be supplied to the reactor 8 at the corresponding point through line 18 or flue gases through line 19 to raise the temperature of the flue gases in the end of the reactor in front of the dust collector 9.
    The reagent is supplied in an excessive proportion with respect to the amount of sulfur contained in the fuel 2. It is introduced either directly into the furnace 1 through pipe 14 and / or directly into reactor 8 at one or several points (pipes 15 and 16), preferably through pipe 16 maximum 50% of the total reagent is served.
    By means of the pump 20, the amount of water supplied through the nozzles 17 is regulated so that it evaporates as completely as possible from the heat of the flue gases 7. However, when necessary, the temperature of the flue gases can be raised in the reactor 8 by supplying hot water to the end portion of the reactor 8 flue gases 7 in the form of a bypass flow through the pipeline 19.
    A fly ash separator is installed in front of the reactor, usually an electrostatic precipitator 21. In this case, the fly ash and, accordingly, calcium compounds, obtained as reaction products, can be substantially separated from each other. Behind the reactor there is a separate particulate separator, for example an electrostatic precipitator or other device.
    Instead of an alkali or alkaline earth metal oxide, such as calcium, alkali or alkaline earth metal carbonate, such as calcium carbonate carbonate, which is decomposed into an oxide in a furnace, can be fed into the furnace.
    You can use multiple reagents, selected for reasons of economy. In this case, the reactants can be fed in the mixture or separately to different points of the reactor.
    PRI me R 1. The process is carried out with a cross-sectional area of about 0.4x0.4 / m and
    about 20 m long. Flue gases, containing mainly pulverized CaO and about 900 ppm SO2, are blown into the reactor at various temperatures. Additionally in
    the reactor is injected with water. CaO and water in the flue gases form highly reactive Ca (OH) g, which then reacts with the oxidation of sulfur.
    The conditions in the reactor and the results of the analysis are given in Table 1, where Ca / S is the molar ratio of CaO to sulfur; Those - the temperature of the flue gas supplied to the reactor; Your temperature flue gas leaving the reactor.
    Example 2 Flue gases after the separation of fly ash by an electrostatic precipitator are fed to the reactor, CaO is introduced into the flue gases after the electrostatic precipitator before the reactor. The results are shown in table 2.
    Example 3: CaO is fed to the reactor according to Example 2 at the point after the electrostatic precipitator, and after the reactor, an oxidizing agent or an oxygen-containing gas is added to the flue gases, as a result of which CaO3 is oxidized to CaS04. The results are shown in the table.3.
    As follows from Tables 1-3, the proposed method provides a reduction in the S02 content in the flue gases by 82-98%. With this in
    Unlike the prior art method, recycle of unreacted reagent is not required, which simplifies the process of removing SOa from flue gases.
    35
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    A method of removing sulfur dioxide from flue gases, including the supply of flue gases to one end of an elongated
    reactor, separate introduction into the reactor of dust-like reagent with alkaline properties and water and / or steam and removal of flue gases with solid products of the interaction of sulfur dioxide with a reagent from
    the other end of the reactor, characterized in that, in order to simplify the process by eliminating the recirculation of the unreacted reagent, alkali oxides are used as the pulverized reagent
    and / or alkaline earth metals, and flue gases are fed to the reactor with a temperature of 90-200 ° C.
    Table 1
    / S ////////////////////////////////////////////
    1
    table 2
    Table 3
    / 2
    ////////////////////////////////////////////////// ///////////////,
    1
    类似技术:
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    同族专利:
    公开号 | 公开日
    PL148177B1|1989-09-30|
    SE461894B|1990-04-09|
    FI851624L|1986-10-25|
    FR2580951A1|1986-10-31|
    DE3539347A1|1986-10-30|
    CS808185A2|1990-09-12|
    FR2580951B1|1990-05-11|
    YU134687A|1988-10-31|
    FI78401B|1989-04-28|
    NZ213858A|1989-08-29|
    JPS61287421A|1986-12-17|
    GB2174081A|1986-10-29|
    HU210828B|1995-08-28|
    JPH0415008B2|1992-03-16|
    FI851624A0|1985-04-24|
    ES548284A0|1986-10-01|
    GB8527453D0|1985-12-11|
    IT8567944D0|1985-11-08|
    GB2174081B|1988-11-23|
    CN1004259B|1989-05-24|
    SE8505271L|1986-10-25|
    YU44529B|1990-08-31|
    BG60230B2|1994-01-18|
    CH672264A5|1989-11-15|
    SE461894C|1991-08-21|
    US4788047A|1988-11-29|
    ZA858478B|1986-07-30|
    AU575209B2|1988-07-21|
    AU4907885A|1986-10-30|
    DK515585D0|1985-11-08|
    YU173185A|1988-02-29|
    DK515585A|1986-10-25|
    CS274271B2|1991-04-11|
    DD239729A5|1986-10-08|
    SE8505271D0|1985-11-07|
    PL256164A1|1987-01-12|
    CN85107965A|1986-10-22|
    HUT48128A|1989-05-29|
    IT1185834B|1987-11-18|
    YU44953B|1991-04-30|
    BE903597A|1986-03-03|
    ES8700306A1|1986-10-01|
    CA1289335C|1991-09-24|
    NL8503080A|1986-11-17|
    引用文献:
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    FR1424831A|1965-02-17|1966-01-14|Escher Wyss Sa Soc|Method and device for preventing the emission of sulphurous and sulfuric gases with the exhaust gases of a fireplace|
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    DE2753902B1|1977-12-03|1979-03-15|Evt Energie & Verfahrenstech|Process for the operation of a steam generator system and steam generator system for the implementation of the process|
    BR8103078A|1980-05-24|1982-02-09|Hoelter H|PROCESS AND DEVICE FOR THE DISPOSAL OF Sulfurous Anhydride AND OTHER HARMFUL SUBSTANCES OF SMOKE GAS|
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    DE3026867A1|1980-07-16|1982-03-04|Hölter, Heinz, Dipl.-Ing., 4390 Gladbeck|Dry gas purificn. esp. after power station - by impacting with ozone to convert sulphur di:oxide to tri:oxide before forming calcium sulphate hemi:hydrate|
    CA1152294A|1980-10-08|1983-08-23|Xuan T. Nguyen|Fluidized bed sulfur dioxide removal|
    DE3106580A1|1981-02-21|1982-09-02|L. & C. Steinmüller GmbH, 5270 Gummersbach|METHOD FOR MINIMIZING EMISSIONS FROM POLLUTION PLANTS|
    AT372876B|1981-11-19|1983-11-25|Oesterr Draukraftwerke|METHOD AND DEVICE FOR THE DESCULATION OF FLUE GAS DESULFURING COAL BURNERS AFTER THE DRY ADDITIVE METHOD|
    DE3235341A1|1982-09-24|1984-03-29|Deutsche Babcock Anlagen Ag, 4200 Oberhausen|METHOD FOR PURIFYING EXHAUST GASES|
    AT26545T|1982-12-22|1987-05-15|Smidth & Co As F L|METHOD AND DEVICE FOR REMOVING SULFUR OXIDS FROM HOT EXHAUST GASES.|
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    US4559211A|1983-08-05|1985-12-17|Research-Cottrell, Inc.|Method for reduced temperature operation of flue gas collectors|DK548786A|1985-11-28|1987-05-29|Aalborg Vaerft As|PROCEDURE FOR CLEANING, SPECIFICALLY SULFURATION, OF ROEGGAS|
    FI81024B|1987-05-11|1990-05-31|Tampella Oy Ab|FOERFARANDE FOER OEVERFOERING AV GASFORMIGA SPAORAEMNESPARTIKLAR FRAON STROEMMANDE HET GAS TILL DAMM MED HJAELP AV VATTEN.|
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    US5006323A|1988-06-27|1991-04-09|Detroit Stoker Company|Method of desulfurizing combustion gases|
    DE3828327A1|1988-08-20|1990-02-22|Steag Ag|Method for producing an aggregate for building materials|
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    FI84435C|1990-02-23|1995-02-22|Ahlstroem Oy|Method and apparatus for cleaning contaminants containing gases|
    US5344614A|1992-09-11|1994-09-06|Foster Wheeler Energy Corporation|Reactor for reducing sulfur oxides emissions in a combustion process|
    US5439658A|1993-09-03|1995-08-08|The Babcock & Wilcox Company|Regenerable magnesium dry scrubbing|
    US5470556A|1993-12-22|1995-11-28|Shell Oil Company|Method for reduction of sulfur trioxide in flue gases|
    DE4405010C2|1994-02-17|1997-07-17|Hoelter Abt Gmbh|Process for cleaning a combustion exhaust gas|
    SE506249C2|1996-04-04|1997-11-24|Flaekt Ab|Apparatus for dispensing and distributing an absorbent material in a flue gas duct|
    US6146607A|1997-07-24|2000-11-14|Lavely, Jr.; Lloyd L.|Process for producing highly reactive lime in a furnace|
    CN100421770C|2004-09-22|2008-10-01|兰特杰斯有限公司|Flue-gas purification system|
    US9429274B2|2010-12-22|2016-08-30|Alstom Technology Ltd|Slurry control system|
    DE102018105892A1|2017-12-20|2019-06-27|Drysotec Gmbh|Process for the treatment of exhaust gases containing sulfur oxides|
    法律状态:
    2007-09-20| REG| Reference to a code of a succession state|Ref country code: RU Ref legal event code: MM4A Effective date: 20031107 |
    优先权:
    申请号 | 申请日 | 专利标题
    FI851624A|FI78401B|1985-04-24|1985-04-24|FOERFARANDE OCH ANORDNING FOER ATT BRINGA ROEKGASERNAS GASFORMIGA SVAVELFOERENINGAR SAOSOM SVAVELDIOXID ATT REAGERA TILL FASTA FOERENINGAR SOM SEPARERAS FRAON ROEKGASERNA.|LV920548A| LV5586A3|1985-04-24|1992-12-29|Attenuation for dumgazu detachment from serkabes anhydride|
    LTRP1229A| LT2548B|1985-04-24|1993-09-28|SULFUR ANHYDROID DISTRIBUTION CHARGES ARE DUMU DUJU|
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