• 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:
    Selective removal of nitrogen oxides in the waste gas of furnaces. Nitrogen oxides are reduced to molecular nitrogen by the addition of ammonia to the waste gases and accelerating the reaction by a catalyst. The procedure is to feed the waste gases through the catalyst in one zone and, in another zone separated from this, to feed the fresh air which is to be fed into the furnace as combustion air. The location of the zones which are traversed by the flow of the waste gases or fresh air are continually or progressively modified in such a way that the zones which were previously traversed by the waste gases are then traversed by fresh air, and vice versa. The ammonia is mixed with the fresh air before its entry into the catalyst, combined on the surface of the catalytically operating material and then entrained into the zone traversed by the waste gases, where the reduction of nitrogen oxide then takes place.
    公开号:SU1729278A3
    申请号:SU864027392
    申请日:1986-04-28
    公开日:1992-04-23
    发明作者:Рикерт Лотар；Коттер Михаэль
    申请人:Крафтанлаген Аг (Инопредприятие)；
    IPC主号:
    专利说明:

    The invention relates to devices for the selective removal of nitrogen oxides from waste gases from furnaces by reduction using an externally supplied chemical compound, preferably ammonia in the presence of a catalyst.
    The purpose of the invention is to prevent ammonium hydrosulfate deposits on the catalyst surface and ammonia into the environment.
    FIG. 1 shows a block diagram of a furnace with a catalyst and a regenerative heat exchanger connected after it; in fig. 2 is a block diagram of a furnace installation in which a catalyst connected after it and a regeneration heat exchanger are brought together in a common unit.
    The device contains a reactor 1, which is divided into a catalysis zone A and a cooling zone B. A carrier filled with the elements of catalyst 2 for the selective reduction of nitrogen oxides with ammonia is placed in the reactor.
    The actuator 3 is designed for continuous or stepwise rotational movement of the carrier with the catalyst relative to the catalysis and cooling zones.
    The catalysis zone A of the reactor is equipped with a pipeline 4 for supplying exhaust gases from
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    furnace 5 and pipeline 6 to remove exhaust gases from the catalysis zone. The pipeline 7 for supplying air to the combustion installation is connected to the cooling zone of the reactor before the combustion installation.
    The ammonia tank 8 is connected to the air supply pipeline in front of the cooling zone of the pipeline 9. The ammonia-air mixing section 10 can be connected to the air supply pipeline by pipes 11 and 12. The rotating regenerative heat exchanger 13 is connected to the exhaust gas discharge pipe 6 from the catalysis zone and the pipeline 14 supply air to the cooling zone of the reactor. The heat exchanger is equipped with a pipeline 15 of exhaust gases cooled in the heat exchanger and a pipeline 16 of fresh air heated in a heat exchanger.
    In the device shown schematically in FIG. 1. The flue gases from the furnace 5 pass through the conduit 4 to the catalyst 2, which can be formed by catalyst elements located in a continuously or stepwise rotating carrier by means of an actuator 3. The flue gases fed through conduit 4 flow through the catalyst 2 Catalysis zone A, where the catalytic reduction of nitrogen oxides contained in the exhaust gases occurs. Exhaust gases from the catalyst, enriched with molecular nitrogen and water, then pass through conduit 6 into a rotating regenerative heat exchanger 13 to transfer the heat of the exhaust gases to fresh air supplied to the secondary installation 5 as combustion air. After the rotating regenerative heat exchanger, the exhaust gases are then transferred through the exhaust gas pipeline 15 to the installation for separating sulfur compounds and reheating to enter the chimney (not shown).
    Fresh air supplied to the combustion installation 5 as combustion air, first enters through the pipe 16 into the rotating regenerative heat exchanger 13, is heated in it in countercurrent to the exhaust gases, then through the pipeline 14 is fed to the reactor 1 and passes through the catalyst in cooling zone B. Then fresh air flows through line 7 to the furnace installation 5,
    The feed through the carrier with the ammonia catalyst required for the reduction of nitrogen oxides is carried out in a fresh air pipe 14 connecting
    regenerative heat exchanger and reactor cooling zone, with a partial stream of fresh air directed to the pipeline 11 to the mixing section 10, into which from tank 8, ammonia is fed and metered into the partial stream of fresh air. A partial stream of fresh air is then returned through conduit 12 to the main stream of fresh air and is thus supplied to a stepwise or continuously rotating carrier with catalyst 2. In the cooling zone through which fresh air flows, ammonia contained in fresh air is adsorbed catalytically the active compound, then, due to the rotation of the carrier, is transferred to a catalysis zone through which the waste gases pass, where the targeted reduction of nitrogen oxides occurs
    0 to nitrogen and water.
    In principle, separate drives can be given to the catalyst carrier and the regenerative heat exchanger. In order to reduce the construction costs, it is recommended to give both units a joint drive, for example, by simply driving a regenerative heat exchanger from the engine and coupling the catalyst carrier to the heat exchanger via a shaft.
    0 In the device shown in FIG. 2, the catalyst carrier and the regenerative heat exchanger are combined into a joint functional unit 17, when, in general, the rotationally controlled carrier is disposed elements of the accumulative mass of the regenerative heat exchanger, which are coated with a catalytically active compound, for example, with a crystalline vanadium titanium, so that these storage elements are thus simultaneously given the function of transferring heat from the exhaust gases to the fresh air and Catalytic active surfaces in the waste gas stream. By combining the catalyst with a regenerative heat exchanger, the need for pipelines 6, 11, 12, 14 (FIG. 1) is eliminated.
    0 In the exemplary embodiment according to FIG. 2 The ammonia is supplied from the tank 8 through the pipeline 9 to the fresh air coming in through the pipeline 16, which is then completely directed through section 10
    5 mixing prior to entering the functional unit 17, in which the regenerative heat exchanger and the catalyst are located.
    In versions of the device, the catalyst carrier 2 may have a separate drive, independent of the drive
    regenerative heat exchanger 13, so that it is possible to continuously or stepwise conduct a catalyst independently of the drive of the heat exchanger. Ammonia dispensing in the exemplary embodiment shown in Fig. 2 may (in accordance with the exemplary embodiment of Fig. 1) also be discharged into a partial stream leaving the fresh air stream, which, after mixing with ammonia, is then returned to the main fresh air stream. . In any case, it is only significant that ammonia is supplied to the catalyst with fresh air flowing in and bound by a catalytically active compound, and then transferred in the catalyst itself to the zone through which the off-gas flows.
    The catalytically active compounds used for the catalyst, for example the crystalline compounds of vanadium with titanium, have a pronounced effect of binding ammonia vapor. This task is solved by mixing ammonia to fresh air before entering the catalyst. Thus, the introduction of ammonia, necessary for the reduction of nitrogen oxides, into the exhaust gases is no longer carried out in the pipeline section of the exhaust gases located in front of the catalyst, but by mixing with fresh air supplied to the catalyst. Ammonia, due to the binding effect of the catalytically active substance, is then held in the catalyst and transferred to the zone through which the exhaust gases flow, where the ammonia then carries out the target catalytic reduction of the nitrogen oxides contained therein in the exhaust gases and decomposes into molecular oxygen. and water.
    Ammonia is admixed to fresh air, preferably in such an amount that it is in the catalyst zone through which the compressed air flows, largely bound by the surface of the catalytically active material and during the subsequent flow of flue exhaust gases are largely completely consumed to reduce the nitrogen oxides containing in them. In this case, in this case (due to the absence of ammonia) ammonium nitrosulfate cannot occur in the stream of exhaust gas entering the catalyst, and the ammonia supplied from the fresh air rtoron is largely completely consumed in the catalyst itself to reduce nitrogen oxides.
    that this harmful salt almost never occurs in the catalyst itself. However, even if the dosed addition of ammonia to fresh air is made by quantity so that some of the ammonia remains in the fresh air and
    then it is fed to the combustion installation; this does not mean that ammonia is then released from the combustion installation together with the exhaust gases. Ammonia entering with fresh air at temperatures available in
    The flue installations decompose so that, in the extreme case, a slightly increased amount of molecular nitrogen may be contained in the exhaust gases, which is not dangerous.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    A device for removing nitrogen oxides from flue gases from a flue system, comprising a catalytic reactor divided into a catalytic zone and a cooling zone
    a carrier filled with elements of a catalyst for the selective reduction of nitrogen oxides with ammonia, pipelines for the supply to the catalysis zone and removal of exhaust gases from it, a drive for continuous
    or stepwise rotational movement of the carrier relative to the catalysis and cooling zones, the air supply pipe to the furnace installation and the ammonia tank, for entry into the reactor, characterized by
    the fact that, in order to prevent ammonium hydrogensulfate deposits on the catalyst surface and ammonia into the environment, the air supply pipe to the furnace installation is connected to
    the cooling zone of the reactor, and the ammonia tank is connected to the air supply pipe in front of the cooling zone, with the catalyst elements made of ammonia adsorbing material.
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    同族专利:
    公开号 | 公开日
    EP0195075A1|1986-09-24|
    DE3569884D1|1989-06-08|
    FI861735A0|1986-04-24|
    DK186686D0|1986-04-23|
    DK161675C|1992-02-24|
    DK186686A|1986-04-23|
    DK161675B|1991-08-05|
    EP0195075B1|1989-05-03|
    JPS62500366A|1987-02-19|
    AU4964885A|1986-03-24|
    FI81504B|1990-07-31|
    FI861735A|1986-04-24|
    DE3431730A1|1986-03-06|
    WO1986001431A1|1986-03-13|
    FI81504C|1990-11-12|
    JPH0622655B2|1994-03-30|
    US4719094A|1988-01-12|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE2360255A1|1973-12-04|1975-06-05|Reinhold Dipl Ing Schmidt|Eliminating nitrogen oxides from ammonia combustion gases - by catalytically splitting ammonia and reducing nitrogen oxides in effluents|
    JPS5230285A|1975-09-03|1977-03-07|Seitetsu Kagaku Co Ltd|Regeneration method of catalyst|
    US4199554A|1977-01-21|1980-04-22|Kureha Kagaku Kogyo Kabushiki Kaisha|Method of and apparatus for removing nitrogen oxides from the gases containing nitrogen oxides|
    JPS55144528U|1979-04-04|1980-10-17|DE3505416A1|1985-02-16|1986-08-21|Kraftanlagen Ag, 6900 Heidelberg|METHOD FOR THE SELECTIVE REMOVAL OF NITROGEN OXIDS FROM EXHAUST GASES|
    DE3523326A1|1985-06-29|1987-01-08|Steag Ag|METHOD FOR SEPARATING NOXFROM GASES, ESPECIALLY SMOKE GASES|
    DK164729C|1990-08-01|1992-12-28|Topsoe Haldor As|PROCEDURE FOR CLEANING OF SMOKE AND WASTE GAS|
    EP0502192B1|1990-08-31|1995-11-29|Institut Kataliza Sibirskogo Otdelenia Akademii Nauk Sssr|Method for removal of nitrogen oxides from exhaust gases|
    DE59202832D1|1991-03-04|1995-08-17|Siemens Ag|Regenerative preheater and method of operating the same.|
    DE4110333A1|1991-03-28|1991-09-19|Siemens Ag|METHOD AND DEVICE FOR CATALYTIC REDUCTION|
    US5269143A|1992-12-07|1993-12-14|Ford Motor Company|Diesel engine turbo-expander|
    US5307772A|1992-12-16|1994-05-03|Ford Motor Company|Redox catalysis of NOx in internal combustion engines|
    DE4301760A1|1993-01-23|1994-08-11|Rothemuehle Brandt Kritzler|Method and device for a regenerative heat exchanger for the treatment of pollutant-containing exhaust gases|
    DE4423003C2|1993-07-06|1999-01-21|Ford Werke Ag|Method and device for reducing NO¶x¶ in exhaust gases from automotive internal combustion engines|
    US5985222A|1996-11-01|1999-11-16|Noxtech, Inc.|Apparatus and method for reducing NOx from exhaust gases produced by industrial processes|
    WO2002032553A1|2000-10-17|2002-04-25|Robert Bosch Gmbh|Exhaust gas cleaning system with a catalyst arrangement and method for cleaning exhaust gases|
    DE102005061873A1|2005-12-23|2007-07-05|Robert Bosch Gmbh|Method and control unit for operating an integrated SCR / DPF system|
    US7891324B2|2007-06-06|2011-02-22|Franklin David A|Method and apparatus for heating a circulating fluid in an indirect heat exchanger|
    US9642858B2|2012-10-30|2017-05-09|University of Pittsburgh—of the Commonwealth System of Higher Education|Use of resazurin, or analogs thereof, for antibacterial therapy|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3431730A|DE3431730A1|1984-08-29|1984-08-29|METHOD AND DEVICE FOR SELECTIVELY CATALYTICALLY REMOVING STICKOXYDES FROM THE EXHAUST GASES FROM COMBUSTION PLANTS|
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