• 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:
    Device (1 ') and method for the catalytic denitrification and regeneration thermal afterburning of carbon monoxide (CO) and gaseous organic substances containing flue gases (A), in particular from the cement clinker production, with at least two alternatingly permeable channels (14), each channel (14) at least two heat storage modules (15) for regenerative heat exchange with the flue gases (A), and wherein between the at least two heat storage modules (15) of the channels (14) at least one catalyst (6; 6 ', 6' ', 6' '' ) is provided for the catalytic reduction of the nitrogen oxides (NOx), and wherein between the at least two channels (14) a combustion space (16) for the regenerative afterburning of the carbon monoxide (CO) and the gaseous organic matter in the flue gases (A) to compensate for the losses of heat displacement the heat storage modules (15) is arranged. The at least one catalyst (6; 6 ', 6' ', 6' '') has a different chemical composition than the one facing the combustion chamber (16) to match a temperature profile along the channel (14) at the side away from the combustion chamber (16) on.
    公开号:AT513851A4
    申请号:T50355/2013
    申请日:2013-05-27
    公开日:2014-08-15
    发明作者:
    申请人:Scheuch Gmbh；
    IPC主号:
    专利说明:

    1
    The invention relates to a device for catalytic Ent-embroidery and regenerative thermal afterburning of carbon monoxide and gaseous organic substances containing flue gases, in particular from the cement clinker production, with at least two flowed through in alternating direction channels, each channel has at least two heat storage modules for regenerative heat exchange with the flue gases and wherein at least one catalytic converter for the catalytic reduction of the nitrogen oxides is provided between the at least two heat storage modules of the ducts, and wherein between the at least two ducts a combustion chamber for the regenerative afterburning of the carbon monoxide and the gaseous organic substances in the flue gases to compensate for the losses of heat displacement is arranged in the heat storage modules.
    Furthermore, the invention relates to a method for catalytic denitrification and regenerative thermal afterburning of carbon monoxide and gaseous organic substances containing flue gases, in particular from cement clinker production, wherein the flue gases are passed in alternating direction through at least two channels, each with at least two heat storage modules for regenerative heat exchange with the flue gases wherein a catalytic reduction of the nitrogen oxides of the flue gases is carried out in at least one arranged between the heat storage modules catalyst, which has a lower temperature than on the side facing the combustion chamber due to the regenerative heat exchange with the heat storage modules at the side facing away from the combustion chamber side, and wherein the losses the heat displacement of the regenerative heat exchange at least partially by regenerative afterburning of the carbon monoxide and the gaseous organic n substances are compensated in the flue gases in a combustion chamber arranged between the at least two channels.
    Such a device or such a method are known from AT 507 773.
    When producing cement clinker in rotary kilns, the raw materials required for cement clinker formation are heated to temperatures of 1350 ° C to 1700 ° C. The raw materials 2/23 2 are usually preheated in a preheating tower consisting of several consecutively arranged cyclones before they reach the rotary kiln. The exhaust gases flow through the production process in countercurrent to the material flow and, after leaving the last cyclone heat stage, are fed to an exhaust gas purification system. In the denitrification, which is part of the exhaust air purification, with so-called SCR (Selective Catalytic Reduction) catalysts by adding ammonia or ammonia releasing compounds, such as. Ammonia-water or urea, at optimum operating temperature, a split of nitrogen oxides N0X in the exhaust gases in environmentally neutral nitrogen N2 and H20 reached. After a possible cooling or heat recovery, the exhaust gases finally reach a filter stage where they are dedusted before they escape into the atmosphere. The filter stage before the exit of the exhaust gases into the atmosphere can be formed for example by electric or bag filters. The relatively high dust content of the raw gases, especially in the cement clinker production, leads to a rapid clogging of the catalysts. To increase the service life of the catalyst, the catalysts are often left on the clean side, i. after the dedusting of the raw gases, arranged. The disadvantage here is that the flue gases before the catalytic reduction to the necessary reaction temperature of usually 160 ° C to 500 ° C must be heated. This heating of the flue gases is often carried out by a recuperator or heat exchanger, which extracts the heat from the denitrified flue gases and supplies the flue gases before the catalytic reduction.
    In the method of AT 507 773, the heat transfer losses of the heat exchange are at least partially offset by regenerative afterburning of the carbon monoxide and the gaseous organic substances. In the thermal afterburning combustion temperatures in the range of about 750 to 900 ° C may be provided. At most additional fuel and combustion air are added. The energy produced during the post-combustion is used to increase the temperature of the flue gases to the catalytic reaction temperature.
    With this method, the energy input for heating 3/23 3 of the flue gases could be considerably reduced. In practice, however, it was observed that the separation efficiency of the catalysts could not be optimally utilized. In addition, an exchange of catalysts was often required, for which the plant had to be temporarily taken out of service.
    Accordingly, the object of the present invention is to overcome or alleviate the disadvantages of the prior art. Accordingly, on the one hand to increase the separation efficiency of the catalysts in the channels and on the other hand, the cost of maintaining the system can be reduced.
    This object is solved by a device as set forth in claim 1, and a method as stated in claim 14. Advantageous embodiments of the invention are contained in the dependent claims.
    According to the invention, the at least one catalyst for adaptation to a temperature profile along the channel at the of
    Combustion chamber side facing away from a different chemical composition than on the combustion chamber side facing.
    The invention is therefore based in particular on the finding that the efficiency of the catalysts is increased if a different chemical composition is provided on the side of the combustion chamber than on the side of the raw gas. As mentioned, the thermal afterburning of the carbon monoxide and the gaseous organic substances in the combustion chamber at a temperature between 750 ° C and 900 ° C from. In contrast, the flue gases are fed on the raw gas side at a temperature of between 80 ° C and 300 ° C. For this reason, a temperature profile Tempe is formed in the channels, which is characterized in particular by the fact that the temperature of the flue gases along the channels to the combustion chamber increases. Accordingly, the cata- tors are exposed in the flow direction of a considerable temperature spread, wherein the catalyst is preferably operated in a reaction temperature range of between 160 ° C and 550 ° C. This temperature gradient has led to problems in the known plants to the denitrification of the flue gases. According to the invention, the locally varying temperature in the 4/23 4
    Channels taken into account that the catalyst has at least two different chemical compositions. Advantageously, the separation efficiency along the catalyst can be optimized hereby. The different chemical composition is particularly adapted to the average gas temperature to provide sufficient active sites for the denitrification reaction available. At the same time, the chemical composition must be chosen so that undesirable side reactions such as e.g. the oxidation of sulfur dioxide (S02) is suppressed at higher temperatures. In addition, the service life of the catalysts can be increased because the decrease in the separation efficiency is at least delayed in operation.
    In addition, it is advantageous that only a part of the catalyst or one of several catalysts connected in series is loaded with the higher, the service life of the catalyst impairing temperature.
    In order to adapt the chemical composition of the catalyst to the temperature profile along the channel, it is favorable if the at least one catalyst on the side facing away from the combustion chamber a higher proportion of a catalytically active material, in particular vanadium pentoxide and / or tungsten trioxide, or other active material has as at the combustion chamber side facing. The reactions proceed more slowly at lower temperatures, and accordingly are accelerated at the side remote from the combustion chamber by a catalyst having a higher number of active sites. The higher reaction temperature at the combustion chamber side requires a less active catalyst to accelerate the desired depletion reactions. The base material of the catalyst is preferably titanium dioxide, which is mixed with the catalytically active material. Such catalysts for selective catalytic reduction are generally known, for example, from DE 3 805 564 A1 or US Pat. No. 4,085,193 A, which are incorporated by reference into the present disclosure in each case with regard to the structure of the catalyst.
    Alternatively, according to the prevailing reaction temperatures, different types of catalysts, in particular zeolites, for example ZSM-5, can be used on a ceramic support which can catalyze the denitrification reaction by incorporating iron or copper compounds into the chemical structure. Accordingly, it is possible to use a catalyst with an iron zeolite as the active material at temperatures above 500 ° C on the side facing the combustion chamber. At lower temperatures on the side facing away from the combustion chamber, a copper zeolite can be used below 300 ° C.
    According to a first preferred embodiment, the at least one catalyst in a layer facing away from the combustion chamber has a different chemical composition, in particular a higher proportion of catalytically active material, than in a layer facing the combustion chamber. In this embodiment, the catalyst disposed between the heat storage modules has a multilayered construction, the individual layers having different chemical compositions. The chemical compositions of the layers are in this case to the lower temperature on the side facing away from the combustion chamber side, which is in particular between 160 ° C and 350 ° C, and to the higher temperature on the side facing the combustion chamber, which in particular between 350 ° C and 550 ° C, adjusted. The layers of the catalyst differ in particular with regard to the proportion of the catalytically active material, wherein the layer of catalyst flowing through at a lower temperature on the side facing away from the combustion chamber has a higher proportion of catalytically active material than the layer through which the combustion chamber flows at a higher temperature Side of the catalyst may have.
    In practice, it has proved to be advantageous if the proportion of the catalytically active material, in particular vanadium pentoxide, the layer facing away from the combustion chamber is between 2 and 5 mass percent, in particular between 2 and 3 mass percent.
    In addition, it has been found in studies to be advantageous if the proportion of catalytically active material, 6/23 6 particular vanadium pentoxide, the combustion chamber facing layer between 0 and 2 percent by mass, in particular between 0.5 and 1.0 percent by mass. By using these values for the proportions of the catalytically active material, the catalyst can be operated particularly efficiently, whereby a loss of activity in the continuous operation of the plant is significantly delayed.
    According to a particularly preferred embodiment, between the layer facing the combustion chamber and the layer facing away from the combustion chamber, the catalyst has an intermediate layer, which preferably has a proportion of the catalytically active material, in particular vanadium pentoxide, of between 1 and 3 percent by mass. Accordingly, in this embodiment, the catalyst has at least three layers whose proportion of the catalytically active material is the higher the closer the respective layer is arranged to the combustion chamber.
    For manufacturing reasons, it is preferable if the layer facing the combustion chamber and the layer of the catalyst facing away from the combustion chamber are formed on the surfaces of the catalyst. To form the layers with the different chemical compositions, a base body of the catalyst is preferably provided, which has a homogeneous distribution of the catalytically active material. Subsequently, the base body is immersed on at least one side in a bath with the catalytically active material, so that a layer corresponding to the immersion depth is formed with the higher proportion of the catalytically active material. To form the three-layer catalyst, the main body can be immersed on both sides in the bath with the catalytically active material.
    According to an alternative embodiment, at least two catalysts are provided in at least one of the channels, the catalyst facing away from the combustion chamber having a different chemical composition, in particular a higher proportion of catalytically active material or another catalytically active material than the catalyst facing the combustion chamber. Accordingly, in this embodiment, two individual, connected in series Kata- 7/23 7 lysatoren provided, which are successively flowed through by the flue gas. The catalyst remote from the combustion chamber is flowed through at a lower temperature and the catalyst facing the combustion chamber at a higher temperature, wherein the chemical compositions of the catalysts are adapted to the different temperatures in the range of the catalysts. When the separation efficiency of one of the catalysts falls after a certain operating time, advantageously only one replacement of this catalyst is necessary. Thus, the effort for the maintenance of the system can be reduced.
    Advantageously, the proportion of the catalytically active material, in particular vanadium pentoxide, of the catalyst remote from the combustion chamber is between 2 and 5 percent by mass, in particular between 2 and 3 percent by mass.
    It has also proven advantageous if the proportion of the catalytically active material, in particular vanadium pentoxide, of the catalyst facing the combustion chamber is between 0 and 2 percent by mass, in particular between 0.5 and 1.0 percent by mass.
    As is known per se, in at least one of the channels between the catalyst remote from the combustion chamber and the catalyst facing the combustion chamber, a device for introducing ammonia or ammonia-releasing compounds into the flue gases can be provided.
    According to a further embodiment, a further catalyst is provided between the catalyst facing away from the combustion chamber and the catalyst facing the combustion chamber, which has a smaller proportion of catalytically active material than the catalyst remote from the combustion chamber and a higher proportion of catalytically active material than the catalyst facing the combustion chamber having.
    To adapt the chemical composition of the catalyst to the temperature profile in the channel, it is favorable if the proportion of catalytically active material of the further catalyst 8/23 is between 1 and 3 percent by mass.
    In terms of the method, the object of the invention is achieved in that the flue gases are passed through the at least one catalyst on the side facing away from the combustion chamber side by a different chemical composition than on the combustion chamber side facing. With regard to the advantages of this method, reference is made to the above statements.
    The present invention will be further explained with reference to the accompanying drawings. Show:
    Figure 1 is a schematic representation of a plant for cement clinker production according to the prior art.
    Fig. 2 is a schematic view of another plant for cement clinker production according to the prior art;
    3a shows an embodiment of a denitrification device according to the present invention;
    FIG. 3b shows a schematic view of a two-layered catalyst for arrangement in the denitrification device according to FIG. 3a; FIG.
    FIG. 3c shows a schematic view of a three-layered catalyst for arrangement in the denitration device according to FIG. 3a; FIG.
    4 shows a further embodiment of a denitrification device according to the present invention; and
    5 shows another embodiment of a denitrification device according to the present invention.
    Fig. 1 shows a schematic view of a device 1 'for cement clinker production according to the prior art. The device for cement clinker production consists of a furnace plant, in particular a rotary kiln 1, in which the raw material 9/23 9 fe are burned to produce the cement clinker. Usually, the raw materials in a preheating tower 2, which may consist of a plurality of superimposed cyclones 3, preheated. For this purpose, the raw materials are placed on a material task 4 in the preheating tower 2. According to the countercurrent principle, the raw material enters the rotary kiln 1, whereas the flue gases A flow against the flow of raw material through the preheating tower 2. After the preheating tower 2, the raw gases A, which contain both nitrogen oxides N0X and dust, pass into a filter 5, where the dust content of the raw gases A is correspondingly reduced. Thereafter, the raw gases A enter a catalyst 6, in which the nitrogen oxides N0X are partly converted into nitrogen N2 and water H20 by a corresponding catalytic reaction. The denitrated raw gases A are passed through a possible cooling device 7, on the one hand to lower the flue gases A to a temperature which is suitable for a subsequent filter stage 8 for dedusting the flue gases A. After the catalyst 6, the raw material of the cement clinker production process carried with the flue gases A passes into a mill 10 where fresh raw material is ground and dried before use in the process. The cooled exhaust gases A are in the filter stage 8, which may be formed by bag filter or electrostatic precipitator, passed and dedusted. After the filter stage 8, the denitrified and dedusted flue gases A pass through a chimney 9 into the atmosphere.
    In order to increase the service life of the catalyst, the catalysts are arranged in the following versions after the dedusting of the raw gases and in front of the fireplace. For this purpose, the flue gases must be heated to the necessary reaction temperature of usually 160 ° C to 550 ° C before the catalytic reduction. This heating of the flue gases is carried out by a recuperator or heat exchanger, which removes the heat from the denitrified flue gases and supplies the flue gases before the catalytic reduction. As already mentioned, it would not be possible by the heat recovery without additional measures to heat the flue gases A to the required reaction temperature of preferably 160 ° C to 500 ° C for the catalytic reduction in the catalyst 6. 10/23 10
    Fig. 2 therefore shows an embodiment of such a device for catalytic denitrification, which is arranged after dedusting and in front of the fireplace and wherein also a regenerative afterburning of the carbon monoxide and / or the gaseous organic substances in the flue gases A is made. This device is disclosed in EP 2 454 008. In this embodiment, the dedusted flue gases A are passed in an alternating direction through two channels 14 with a plurality of successive heat storage modules 15 and an interposed combustion chamber 16 for regenerative combustion of the carbon monoxide CO and / or the gaseous organic matter of the flue gases A. By the direction of flow, the heat energy is removed or supplied to the flue gases A in the heat storage modules 15, which is required to bring the flue gases A to the reaction temperature TR of the catalysts 6. Via a line 17 fuel such as e.g. Natural gas to be supplied. Via corresponding lines 18 and 18a after the flow reversal, the substances required for the catalytic reduction in the catalysts 6, preferably ammonia, are added. The control of the alternating flow direction takes place by means of corresponding control devices 22 (compare FIGS. 3a, 4, 5). The heat storage modules 15 may be formed by ceramic honeycomb bodies. The embodiment according to FIG. 2 requires catalysts 6 having a comparatively large reaction temperature range of about 160 ° C. to 550 ° C., since the temperature can not be kept constant by the alternating direction of the flue gases A. The catalysts 6 comprise a base material, in particular titanium dioxide, and a catalytically active material, in particular vanadium pentoxide. In this embodiment, therefore, the losses of the heat shift in the heat storage modules 15 can be compensated by the fact that the carbon monoxide CO and / or the gaseous organic substances in the flue gases A in the combustion chamber 16 are post-combusted.
    3a shows a device 1 'for the catalytic denitrification and regenerative thermal afterburning of carbon monoxide (CO) and gaseous organic substances containing flue gases (A). The structure of this device 1 'corresponds to that of FIG. 2, so that reference may be made essentially to the preceding embodiments. Accordingly, in the embodiment shown, the device 1 'has two channels 14 through which it is possible to flow in an alternating direction, in each of which two heat storage modules 15 are provided for regenerative heat exchange with the flue gases A. Between the two channels 14, a combustion chamber 16 for the regenerative afterburning of the carbon monoxide and the gaseous organic substances in the flue gases (A) is arranged. Thus, as described above, the losses of the heat shift in the heat storage modules 15 can be compensated. In addition, in Fig. 3a control means 22 can be seen, with which the flow direction of the device 1 'can be switched. Such valve controls are well known in the art, so that more detailed explanations can do it unnecessary. In addition, in Fig. 3a, a line 17 is schematically drawn, with which fuel such. Natural gas can be fed directly into the combustion chamber 16 (see also Fig. 4, 5). It should also be noted that the arrangement of the channels on both sides of the combustion chamber 16 can differ in many ways from the embodiment shown. For example, the channels 14 and the combustion chamber 16 may be arranged in a straight line.
    In this case, the channels 14 and the combustion chamber 16 form successive sections of a continuous flow-through space (not shown).
    As can also be seen from FIG. 3 a, the channels 14 in this embodiment each have exactly one catalyst 6 between the two heat storage modules 15. To adapt the catalysts 6 to the temperature profile in the channels 14, the catalysts 6 have a different chemical composition on the side facing away from the combustion chamber 16 than on the side facing the combustion chamber 16. The different chemical composition of the catalyst 6 relates in particular to the proportion of catalytically active material, in particular vanadium pentoxide and / or tungsten trioxide, which is lower on the side of the combustion chamber 16 than on the side of the supply and discharge of the flue gas A.
    For this purpose, the catalysts 6 according to FIG. 3 have a layer structure, wherein in FIGS. 3b, 3c an embodiment of the multilayer catalyst 6 can be seen in each case. 12/23 12
    According to FIG. 3b, the catalyst 6 is formed in two layers with a layer 19 facing away from the combustion chamber 16 and with a layer 20 facing the combustion chamber 16. In the embodiment shown, the proportion of vanadium pentoxide on the side facing away from the combustion chamber 16 layer 19 between 2 and 5 percent by mass, in particular between 2 and 3 percent by mass, and at the combustion chamber 16 facing layer between 0 and 2 percent by mass, in particular between 0.5 and 1.0 percent by mass.
    According to FIG. 3 c, the catalyst 6 is formed in three layers, an intermediate layer 21 being provided between the layer 20 facing the combustion chamber 16 and the layer 19 facing away from the combustion chamber 16. In the embodiment shown, the proportion of vanadium pentoxide of the intermediate layer 21 can be between 1 and 3 percent by mass.
    As can be seen from FIGS. 3b, 3c, the layer 19 facing the combustion chamber 16 and the layer 20 of the catalytic converter 6 facing away from the combustion chamber 16 are formed on the surfaces of the catalytic converter 6 arranged transversely to the throughflow direction.
    FIG. 4 shows an alternative embodiment in which two catalysts 6 are provided in each of the channels 14. The catalysts 6 have a substantially homogeneous distribution of the catalytically active material. Unlike in accordance with FIG. 3, the catalysts 6 ', 6 "therefore have no layer structure in particular. The catalyst 6 'facing away from the combustion chamber 16 in this case has a higher proportion of catalytically active material than the catalyst 6' facing the combustion chamber 16. In the embodiment shown, the proportion of the catalytically active material, in particular vanadium pentoxide, of the catalyst 6 'facing away from the combustion chamber 16 can be between 2 and 5 percent by mass, in particular between 2 and 3 percent by mass, and the proportion of the catalytically active material, in particular vanadium pentoxide, of the combustion chamber 16 facing catalyst 6 '' between 0 and 2 percent by mass, in particular between 0.5 and 1 mass percent, amount. In addition, in at least one of the channels 14 between the catalyst 6 'facing away from the combustion chamber 16 and the catalyst 6' 'facing the combustion chamber 16, an inlet 13, 13 for discharging ammonia or ammonia-releasing compounds into the flue gases A may be provided (Not shown).
    FIG. 5 shows a further embodiment in which a further, third catalytic converter 6 '' 'is provided between the catalyst 6' facing away from the combustion chamber 16 and the catalytic converter 6 'facing the combustion chamber 16. The further catalyst 6 '' 'has a smaller proportion of catalytically active material than the catalyst 6' facing away from the combustion chamber 16 and a higher proportion of catalytically active material than the catalyst 6 'facing the combustion chamber 16. The proportion of catalytically active material of the further catalyst 6 "may be between 1 and 3 percent by mass. 14/23
    权利要求:
    Claims (14)
    [1]
    14. A device (1 ') for the catalytic denitrification and regenerative thermal afterburning of carbon monoxide (CO) and gaseous organic substances containing flue gases (A), in particular from the cement clinker production, with at least two passages in the alternating direction (14), wherein each channel (14) has at least two heat storage modules (15) for regenerative heat exchange with the flue gases (A), and wherein between the at least two heat storage modules (15) of the channels (14) at least one catalyst (6; 6 ', 6' ') , 6 '' ') is provided for the catalytic reduction of nitrogen oxides (N0X), and wherein between the at least two channels (14) a combustion chamber (16) for the regenerative afterburning of the carbon monoxide (CO) and the gaseous organic substances in the flue gases (A ) is arranged to compensate for the losses of heat displacement in the heat storage modules (15), characterized in that the while a catalyst (6; 6 ', 6' ', 6' '') to adapt to a temperature profile along the channel (14) on the side facing away from the combustion chamber (16) side has a different chemical composition than at the combustion chamber (16) facing side.
    [2]
    2. Device (1 ') according to claim 1, characterized in that the at least one catalyst (6; 6', 6 '', 6 '' ') on the side facing away from the combustion chamber (16) side a higher proportion of a catalytically active Material, in particular vanadium pentoxide and / or tungsten trioxide, or another active material than on the combustion chamber (16) facing side.
    [3]
    3. Device (1 ') according to claim 1 or 2, characterized in that the at least one catalyst (6; 6', 6 '', 6 '' ') in a combustion chamber (16) facing away from the layer (19) another Chemical composition, in particular a higher proportion of catalytically active material, as in a combustion chamber (16) facing the layer (20).
    [4]
    4. Device (1 ') according to claim 3, characterized in that the proportion of the catalytically active material, in particular vanadium pentoxide, of the combustion chamber (16) facing away layer 15/23 15 (19) between 2 and 5 mass percent, in particular between 2 and 3 percent by mass.
    [5]
    5. Device (1 ') according to claim 3 or 4, characterized in that the proportion of the catalytically active material, in particular vanadium pentoxide, the combustion chamber (16) facing layer (20) between 0 and 2 percent by mass, in particular between 0.5 and 1.0 mass percent, is.
    [6]
    6. Device (1 ') according to claim 5, characterized in that the catalyst (6; 6', 6 '', 6 '' ') between the combustion chamber (16) facing the layer (20) and the combustion chamber ( 16) facing away from the layer (19) has an intermediate layer (21), which preferably has a proportion of the catalytically active material, in particular vanadium pentoxide, of between 1 and 3 percent by mass.
    [7]
    7. Device (1 ') according to one of claims 3 to 6, characterized in that the combustion chamber (16) facing layer (20) and the combustion chamber (16) facing away from layer (19) of the catalyst (6; 6 '', 6 '' ') are formed on the surfaces of the catalyst (6, 6', 6 '', 6 '' ').
    [8]
    8. Device (1 ') according to one of claims 1 to 7, characterized in that in at least one of the channels (14) two catalysts (6) are provided, wherein the combustion chamber (16) facing away from the catalyst (6') another Chemical composition, in particular a higher proportion of catalytically active material or another catalytically active material, as the combustion chamber (16) facing the catalyst (6 '').
    [9]
    9. Device (1 ') according to claim 8, characterized in that the proportion of the catalytically active material, in particular vanadium pentoxide, of the combustion chamber (16) facing away from the catalyst (6') between 2 and 5 percent by mass, in particular between 2 and 3 percent by mass, is.
    [10]
    10. Device (1 ') according to claim 8 or 9, characterized in that the proportion of the catalytically active material, in particular vanadium pentoxide, of the combustion chamber (16) facing 16/23 16 th catalyst (6' ') between 0 and 2 Mass percent, in particular between 0.5 and 1.0 mass percent is.
    [11]
    11. Device (1 ') according to one of claims 1 to 11, characterized in that in at least one of the channels (14) between the combustion chamber (16) facing away from the catalyst (6') and the combustion chamber (16) facing catalyst ( 6 '') a device for introducing ammonia or ammonia-releasing compounds in the flue gases (A) is provided.
    [12]
    12. Device (1 ') according to one of claims 1 to 11, characterized in that between the combustion chamber (16) facing away from the catalyst (6') and the combustion chamber (16) facing the catalyst (6 ''), a further catalyst ( 6 '' ') is provided which has a smaller proportion of catalytically active material than the catalyst (6') facing away from the combustion chamber (16) and a higher proportion of catalytically active material than the catalyst (6 '') facing the combustion chamber (16). ) having.
    [13]
    13. Device (1 ') according to claim 12, characterized in that the proportion of catalytically active material of the further catalyst (6' '') is between 1 and 3 percent by mass.
    [14]
    14. A process for catalytic denitrification and regenerative thermal afterburning of carbon monoxide (CO) and gaseous organic substances containing flue gases (A), in particular from the cement clinker production, wherein the flue gases (A) in an alternating direction by at least two channels (14) each having at least two Heat storage modules (15) for regenerative heat exchange with the flue gases (A) are passed, wherein a catalytic reduction of the nitrogen oxides (NOx) of the flue gases (A) in at least one between the heat storage modules (15) arranged catalyst (6; 6 ', 6' ' , 6 '' '), which due to the regenerative heat exchange with the heat storage modules (15) on the side facing away from the combustion chamber (16) side has a lower temperature than on the combustion chamber (16) facing side, and wherein the losses of heat displacement the regenerative heat exchange at least partially by regenerative afterburning of the coal stoffmonoxids (CO) and the gaseous organic substances in the flue gases (A) in 17/23 17 a between the at least two channels (14) arranged combustion chamber (16) are compensated, characterized in that the flue gases (A) when flowing through the at least a catalyst (6; 6 ', 6' ', 6' '') are guided on the side facing away from the combustion chamber (16) by a different chemical composition than on the side facing the combustion chamber (16). 18/23
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    同族专利:
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    ATA50355/2013A|AT513851B1|2013-05-27|2013-05-27|Device for catalytic denitrification and regenerative thermal afterburning|ATA50355/2013A| AT513851B1|2013-05-27|2013-05-27|Device for catalytic denitrification and regenerative thermal afterburning|
    DE201410106991| DE102014106991A1|2013-05-27|2014-05-19|Device for catalytic denitrification and regenerative thermal afterburning|
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