• 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:
    Process and apparatus 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, with a raw gas side between 80 ° C and 300 ° C fluctuating Temperatur.Die flue gases (A) are in alternating Direction by at least two channels (14), each with at least two heat storage modules (15) for regenerative heat exchange with the flue gases (A) passed. Catalytic reduction of the nitrogen oxides (NOx) of the flue gases (A) is carried out in at least one catalyst (6) arranged between the heat storage modules (15) with a reaction temperature range of 160 ° C to 550 ° C. The losses of heat displacement of the regenerative heat exchange are at least partially offset by regenerative afterburning of the carbon monoxide (CO) and gaseous organic substances in the flue gases (A) in a combustion chamber (16) located between the at least two channels (14). The reaction temperature range of the catalyst (6) is maintained by cooling and / or heating the flue gases (A).
    公开号:AT513597A4
    申请号:T50357/2013
    申请日:2013-05-27
    公开日:2014-06-15
    发明作者:
    申请人:Scheuch Gmbh；
    IPC主号:
    专利说明:

    1
    The invention relates to a method for catalytic Entsti-ckung and regenerative thermal afterburning of carbon monoxide and gaseous organic substances containing flue gases, in particular from the cement clinker production, with a Rohgasseitig between 80 ° C and 300 ° C fluctuating temperature, the flue gases in an alternating direction by at least two channels each having at least two heat storage modules for regenerative heat exchange with the flue gases are passed, wherein a catalytic reduction of the nitrogen oxides of the flue gases in at least one arranged between the heat storage modules catalyst is carried out with a reaction temperature range of 160 ° C to 550 ° C, 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 substances in the flue gases in one between the at least two channels ordered combustion chamber are balanced.
    Furthermore, the invention relates to a device for catalytic denitrification and regenerative thermal afterburning of carbon monoxide and gaseous organic substances containing flue gases with rohgasseitig between 80 ° C and 300 ° C fluctuating temperature, in particular from the cement clinker production, with at least two in the direction of through-flow channels wherein each channel has at least two heat storage modules for regenerative heat exchange with the flue gases, and wherein at least one catalyst for the catalytic reduction of the nitrogen oxides is provided between the at least two heat storage modules of the channels, which has a reaction temperature range of 160 ° C to 550 ° C. , and wherein between the at least two channels, 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 in the Wärmespe Iermodulen is arranged.
    Such a device or such a method are known from AT 507 773. 2/31 2
    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 are usually preheated in a preheating tower consisting of several consecutively arranged cyclones before they enter 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 ° C to 900 ° C may be provided. At most, additional 3/31 3
    Fuels and combustion air 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 the heating of the flue gases could advantageously be considerably reduced. However, it has proved to be problematic that the temperature of the flue gases on the raw gas side can be subject to considerable fluctuations. Such fluctuations can be caused for example by different operating conditions in the cement clinker production. Disadvantageously, the changes in the temperature of the raw gases can lead to the reaction temperature range of the catalyst over- or. is fallen short of. Exceeding the reaction temperature of the catalyst may cause damage to the catalyst surface, thereby greatly restricting the activity of the catalyst. On the other hand, an undershooting of the temperature window on the catalyst can result in deposits on the catalyst, for example of ammonium hydrogensulfate, occurring. This also affects the activity of the catalyst.
    Accordingly, the object of the present invention is to overcome or mitigate the disadvantages of the prior art. Accordingly, the invention has the particular aim of reliably avoiding restrictions on the function of the catalyst during operation when the temperature of the flue gases fluctuates due to the process in a temperature interval of between 80 ° C and 300 ° C.
    This object is achieved by a method as set out in claim 1 and an apparatus as specified in claim 10. Advantageous embodiments of the invention are contained in the dependent claims.
    According to the invention, therefore, the reaction temperature range of the catalyst is maintained by cooling and / or heating the flue gases. 4/31 4
    The thermal afterburning of the carbon monoxide and the gaseous organic substances in the combustion chamber preferably proceeds at a temperature between 750 ° C and 900 ° C. 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 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. To operate the catalyst reliably in the reaction temperature range of between 160 ° C and 550 ° C, the flue gases can be cooled on the one hand, when the temperature of the flue gases increases on the raw gas side. On the other hand, the flue gases can be heated when the temperature of the flue gases on the raw gas side drops. Advantageously, this can reliably ensure that the temperature at the catalyst is kept between the lower and the upper limit of the reaction temperature range. The reaction temperature range here refers to the temperature profile of the catalyst between the side facing away from the combustion chamber side and the side facing the combustion chamber. By adhering to the reaction temperature range on the catalyst, on the one hand, the formation of deposits, in particular ammonium hydrogen sulfate, can be avoided. On the other hand, damage to the catalyst surface can be prevented. The cooling or heating of the flue gases counteracts the heat recovery in the heat storage modules in such a way that the catalyst is kept in the reaction temperature range. Thus, a particularly energy-efficient operation is possible. Accordingly, in particular, the problem can be solved or alleviated that it may come at too low temperatures on the catalyst in the presence of sulfur dioxide with the reducing agent ammonia to the undesirable formation of ammonium bisulfate, the formation temperature of ammonium hydrogen sulfate is the lower the higher the sulfur dioxide concentration. The ammonium hydrogen sulfates could be deposited on the pores of the catalyst and thus block the active centers of the catalyst, which would occur in a short time high losses of catalyst activity. This reduction in activity would therefore lead to economic stagnation. On the other hand, excessively high temperatures on the catalyst would lead to deactivation of the catalyst due to thermal damage to the surface. If the temperatures exceed the design temperature of the catalyst, sintering of the surface can result in a reduction in the specific surface area of the catalyst and hence a reduction in activity. Changes in the process can cause the inlet temperatures and thus also the temperatures at the catalyst to fluctuate. To make matters worse, the fluctuations in the inlet temperature, that occur by changing the direction of flow temperature peaks in both directions. The catalyst works as well as the heat exchanger modules as a regenerator, which stores the heat energy or releases again after flow reversal. Accordingly, in each cycle, both the minimum and the maximum temperature of the reaction temperature range could be temporarily undershot and / or exceeded. This could lead to the abovementioned side reactions such as ammonium hydrogen sulfate formation or thermal damage to the catalyst. These adverse effects are inventively eliminated or at least significantly attenuated that the reaction temperature range of the catalyst is constantly maintained by cooling and / or heating the flue gases.
    According to a particularly preferred embodiment, the flue gases are cooled or heated to maintain the reaction temperature range in at least one of the channels between two catalysts. If in each case at least two catalysts are provided in the at least two channels, it is preferably provided that the flue gases in both channels, in each case between the catalysts, be cooled or heated with regard to the maintenance of the reaction temperature range. This embodiment has proven to be a particularly favorable compromise between optimizing the heat energy required for cooling or heating the raw gases, which is the higher the lower the temperature of the flue gases, and an optimization with respect to the temperature profile along the catalyst at which the temperature the side facing away from the combustion chamber side of the catalyst 6/31 6 is to be kept low, exposed.
    According to a further embodiment, the temperature of the catalyst at the side facing away from the combustion chamber by cooling and / or heating the flue gases between the catalyst and the heat exchanger module facing away from the combustion chamber is substantially constant, in particular at a temperature between 160 ° C and 350 ° C, preferably essentially 250 ° C, held. In this embodiment, therefore, the temperature of the catalyst is set at the side facing away from the combustion chamber side. For this purpose, the flue gases are cooled or heated at the inlet to the catalyst accordingly. This embodiment has the particular advantage that a drop below the inlet temperature and thus the formation of deposits on the catalyst can be reliably avoided. On the other hand, this embodiment has the disadvantage that the cooling or heating of the flue gas due to the relatively low temperature on the raw gas side is associated with a higher energy input.
    According to a further embodiment, the temperature of the catalyst on the combustion chamber side facing by cooling and / or heating the flue gases between the catalyst and the combustion chamber facing heat exchanger module is substantially constant, in particular at a temperature between 350 ° C and 550 ° C, preferably substantially 450 ° C, held. Accordingly, the cooling or heating of the flue gases in this embodiment takes place at the outlet of the catalyst. Since the temperature of the flue gases to the combustion chamber increases, the flue gases are cooled or heated in this embodiment based on a relatively high temperature level. As a result, the cooling or heating of the flue gases can be made particularly energy efficient. On the other hand, in this embodiment, a comparatively high inlet temperature is effected in the catalyst. This can be disadvantageous if the catalyst is designed for low temperatures on the side facing away from the combustion chamber.
    According to a further embodiment, the temperature of the flue gases at the side remote from the combustion chamber side of the heat storage module 7 is kept substantially constant by cooling and / or heating. Accordingly, the flue gases in this embodiment are cooled or heated prior to entering the heat storage modules to operate the catalyst in the predetermined reaction temperature range. Preferably, the cooling or heating of the flue gases takes place here in the raw gas, which has a temperature of between 80 ° C and 300 ° C.
    For heating and / or cooling the flue gases, it is particularly advantageous if a gaseous cooling or heating means, in particular air or exhaust gases, is introduced into the flue gases. An advantage of the use of the gaseous coolant is in particular that the denitrification system usually already has suitable air or exhaust gas streams, which can be used for cooling or heating the flue gases. Advantageously, therefore, only small structural adaptations are required.
    Moreover, it may be advantageous if, for cooling the flue gases, a liquid coolant, in particular water, and / or for heating the flue gases a vaporous heating medium, in particular steam, is introduced into the flue gases. The use of a liquid coolant has the particular advantage that smaller amounts of liquid coolant are required compared to gaseous coolants.
    According to an alternative embodiment, the heating and / or cooling of the flue gases takes place indirectly by heat exchange with a heat exchange medium. In this embodiment, therefore, no cooling or. Heating medium introduced into the flue gases, but the flue gases heat is removed or supplied by heat exchange with a heat exchange medium to increase or decrease the temperature of the flue gases to maintain the reaction temperature range of the catalyst.
    In order to be able to react sensitively to fluctuations in the temperature of the supplied flue gases, it is advantageous if the temperature of the flue gases is measured at at least one point in the channels, wherein the flue gases depend on the measured flue gases
    Temperature are cooled or heated in at least one location such that the reaction temperature range of the catalyst is maintained. Accordingly, a control loop is provided in this embodiment, in which the temperature of the flue gases at the measuring point serves as an input variable, which is brought by cooling or heating the flue gases to the predetermined temperature.
    The object underlying the invention is also achieved by a device of the type mentioned, in which at least one cooling and / or heating is provided for cooling and / or heating the flue gases to the reaction temperature range of the catalyst at Rohgasseitig fluctuating temperature of the flue gases observed. With regard to the advantages of this device, reference is made to the above statements.
    Particularly favorable is an embodiment in which at least one cooling and / or heating device is arranged to maintain the reaction temperature range between two catalysts.
    To maintain the reaction temperature range during operation of the catalyst, on the one hand, at least one cooling and / or heating device can be arranged between the catalytic converter and the heat exchanger module facing away from the combustion chamber. In this way, the temperature of the catalyst can be controlled or regulated on the side facing away from the combustion chamber side.
    On the other hand, to maintain the reaction temperature range, at least one cooling and / or heating device can be arranged between the catalyst and the heat exchanger module facing the combustion chamber. In this embodiment, therefore, the temperature of the catalyst is controlled or regulated at the combustion chamber side facing.
    In order to cool or heat the flue gases to maintain the reaction temperature range of the catalyst, it is advantageous for the at least one cooling and / or heating device to be at least one feed element, in particular a nozzle element
    Incorporation of a cooling or heating means in the flue gases, wherein preferably a plurality of supply elements are arranged in a plane perpendicular to the flow direction of the flue gas. Accordingly, the cooling or heating means is introduced via the feed element in the flue gas stream.
    To achieve a structurally simple embodiment, it is preferably provided that the feed element for introducing the cooling and / or heating means is also designed as a device for introducing ammonia or ammonia-releasing compounds into the flue gases. Accordingly, in this embodiment, the apparatuses commonly used in generic denitrification plants for introducing the ammonia compounds can advantageously also be used to introduce the cooling or heating agent into the flue gas stream with a view to maintaining the reaction temperature range of the catalyst.
    According to an alternative embodiment, at least one cooling and / or heating device is formed by a heat exchanger, which is preferably arranged perpendicular to the flow direction of the flue gas. The heat exchanger is preferably arranged outside the channels with the heat exchanger modules and the catalysts in a crude gas line.
    For monitoring the temperature profile in the channels, it is favorable if a measuring device is provided with at least one measuring element for measuring the temperature of the flue gases at at least one point in the channels, wherein preferably a measuring element for measuring the temperature of the flue gases between the catalyst and the remote from the combustion chamber heat exchanger module and / or another measuring element for measuring the temperature of the flue gases between the catalyst and the combustion chamber facing the heat exchanger module is provided.
    According to a particularly preferred embodiment, the measuring device is connected to a control device which is adapted to regulate the temperature of the flue gases to maintain the reaction temperature range of the catalyst via the cooling and / or heating device. Accordingly, the temperature profile along the catalyst is maintained by controlling the cooling or heating device.
    The device can be operated particularly efficiently if the control device is set up to lower the temperature of the flue gases at the side of the catalytic converter facing away from the combustion chamber above a lower threshold value, which is preferably between 160 ° C. and 350 ° C., in particular substantially 250 ° C. is to be held. Preferably, the temperature of the flue gases at the side facing away from the combustion chamber side of the catalyst is maintained between 250 ° C and 500 ° C. It is particularly preferred in this case if the temperature of the flue gases is kept substantially constant on the raw gas side of the catalyst. If several catalysts are provided in the channels, the temperature of the flue gases is preferably controlled on the side facing away from the combustion chamber side of the catalyst furthest away from the combustion chamber.
    On the other hand, the reaction temperature range of the catalyst can be maintained in an advantageous manner, when the control device is adapted to the temperature of the flue gases on the combustion chamber side facing the catalyst below an upper threshold, which is preferably between 350 ° C and 550 ° C, in particular substantially 450 ° C, is to keep. It is particularly preferred in this case if the temperature of the flue gases is kept substantially constant on the combustion chamber side of the catalyst. If several catalysts are provided in the channels, the temperature of the flue gases is preferably controlled on the combustion chamber side facing the closest to the combustion chamber catalyst.
    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. 11/31 11
    FIG. 2 shows an embodiment of a denitrification device according to the present invention, in which the flue gases, relative to the shown flow direction, are cooled or heated in front of a catalyst in each of the channels; FIG.
    3 shows a further embodiment of a denitrification device according to the present invention, in which the flue gases, relative to the shown flow direction, are cooled or heated after the catalyst in each of the channels;
    4 shows a further embodiment of a denitrification device according to the present invention, in which the flue gases, relative to the shown flow direction, are cooled or heated between two catalysts in each of the channels;
    5 shows a further embodiment of a denitrification device according to the present invention, in which the flue gases are cooled or heated by means of a heat exchanger in a crude gas line;
    Fig. 6 shows another embodiment of a denitrification device according to the present invention in which the flue gases are cooled or heated by means of a heat exchanger between two catalysts in each of the channels; and
    7a, 7b each show a diagram for illustrating the effects of the cooling device according to the invention (FIG. 7a) or heating device (FIG. 7b) on the temperature profile along a channel of the denitrification device.
    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 materials for the production of cement clinker are fired. Usually, the raw materials in a preheating tower 2, which may consist of a plurality of superimposed cyclones 3, 12-31 12 warmed up. 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 Ä flow against the flow of the 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 enter the atmosphere via a chimney 9.
    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.
    Fig. 2 therefore shows an embodiment of such a device 13/31 13 for catalytic denitrification, which is arranged after dedusting and in front of the fireplace and also wherein a regenerative afterburning of carbon monoxide and / or gaseous organic substances in the flue gases A is made. In this embodiment, the flue gases A in an alternating direction by 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 passed. 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 is effected by corresponding control means 21. 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 are post-combusted. It should also be noted that the arrangement of the channels 14 on both sides of the combustion chamber 16 may 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). 14/31 14
    As shown in FIG. 2, the device 1 'in the illustrated embodiment also has cooling and / or heating devices 19 with which the flue gases A are optionally cooled or heated in such a way that fluctuations in the temperature of the flue gases A between 80 ° C and 300 ° C on the raw gas side. Thus, the catalyst 6 can be maintained in the predetermined reaction temperature range.
    According to FIG. 2, the cooling and / or heating device 19 is arranged between the catalytic converter 6 and the heat exchanger module 15 facing away from the combustion chamber 16. In this embodiment, therefore, the flue gases, based on the shown flow direction of the channels 14, can be cooled or heated prior to entry into the heat exchanger module 15 facing away from the combustion chamber 16, when the temperature of the flue gases A rises or falls on the raw gas side. In the embodiment of FIG. 2, both channels 14 each have a cooling and / or heating device 19. The cooling and / or heating device 19 has, according to FIGS. 2, 3, 4, in each case a feed element 20 for introducing a cooling or heating means into the flue gases A. The feed element 20 may have at least one nozzle element (not shown), wherein preferably a plurality of nozzle elements are arranged in a plane perpendicular to the flow direction of the flue gas A. With the aid of the feed element 20, a gaseous coolant, such as air or exhaust gases, or a liquid coolant, such as water, can be introduced into the flue gases A. For heating the flue gases A on the one hand, a gaseous heating means, such as air or exhaust gases, or a vaporous heating means, such as water vapor, can be used. In the embodiment shown, the cooling and / or heating device 10 is also designed as a device for introducing ammonia or ammonia-releasing compounds into the flue gases.
    As is further apparent from FIG. 2, a measuring device 22 with at least one measuring element 22 'for measuring the temperature of the flue gases A at at least one point in the channels 14 is additionally provided. According to FIG. 2, the measuring element 22 'for measuring the temperature of the flue gases A between the catalytic converter 6 and the heat exchanger module 15 facing away from the combustion chamber 16 is arranged. The measuring device 22 is connected to a control device 23, which is adapted to control the temperature of the flue gases A to maintain the reaction temperature range of the catalyst 6 via the cooling and / or heating device 19. For this purpose, the cooling and / or heating device 19 is controlled via the control device 23 such that the temperature of the flue gases A at the side facing away from the combustion chamber 16 side of the catalyst 6 above a lower threshold, which preferably between 160 ° C and 350 ° C. , in particular substantially 250 ° C, is to be held. Preferably, the temperature of the flue gases A before the entry into the catalyst 6 is kept substantially constant at the lower threshold. In the embodiment shown, a further measuring element 24 is also provided for measuring the temperature of the flue gases A between the catalytic converter 6 and the heat exchanger module 15 'facing the combustion chamber 16, which is likewise connected to the control device 23. However, the further measuring element 24 can also be omitted in this embodiment.
    According to FIG. 3, the cooling and / or heating device 19 is arranged to maintain the reaction temperature range between the catalytic converter 6 and the heat exchanger module 15 'facing the combustion chamber. In this embodiment, therefore, the flue gases A, based on the shown flow direction of the channels 14, after exiting the heat exchanger module 15 'are cooled or heated. It can thus be prevented that the reaction temperature range of the catalyst 6 is exceeded or fallen below as a result of temperature fluctuations of the supplied flue gases A. The control device 23 is connected to the cooling and / or heating device 19 such that the temperature of the flue gases A at the combustion chamber 16 side facing the catalyst 6 below an upper threshold, which preferably between 350 ° C and 550 ° C, in particular Substantially 450 ° C, is held. Preferably, the temperature of the flue gases A, based on the flow direction shown, after the catalyst 6 is set substantially constant to the predetermined upper threshold. In the embodiment shown, the control device is connected both to the measuring element 16/31 16 22 'and to the further measuring element 24.
    According to FIG. 4, the cooling and / or heating device 19 is arranged to maintain the reaction temperature range between two catalysts 6 ', 6 ". In this embodiment, therefore, the flue gases A between the combustion chamber 16 facing away from the catalyst 6 'and the combustion chamber 16 facing the catalyst 6' 'are cooled or heated.
    According to FIG. 5, the cooling and / or heating device 19 is formed by a recuperator or heat exchanger 25, which is arranged outside the channels 14. When an increase in the temperature of the flue gases A is detected, the flue gases A in the heat exchanger 25 can be cooled so as to maintain the reaction temperature range along the catalyst 6. On the other hand, the flue gases A in the heat exchanger 25 can be heated to compensate for a decrease in the temperature of the flue gases A. Accordingly, the heat exchange in the heat exchanger 25 for maintaining the reaction temperature range of the catalyst 6 can be continuously adjusted.
    The embodiment of FIG. 6 differs from that of FIG. 5 only in that each one heat exchanger 25 is arranged in the channels 14 between the heat storage modules 15.
    7 shows a diagram for illustrating the influence of the cooling or heating device 19 on the temperature profile along the channels 14 of the denitrification device 1 '. Depending on the temperature of the flue gases A on the raw gas side, the reaction temperature range of the catalyst 6 can be maintained either by cooling the flue gases A (Figure 7a) or by heating the flue gases A (Figure 7b).
    In Fig. 7, the temperature of the flue gases A in dependence on the position x along the channel 14 in the direction of the combustion chamber 16 through the example of the embodiment of the cooling or heating device 19 shown in FIG. 2 is shown. Accordingly, the heat storage module 15 facing away from the combustion chamber 16, the catalyst 6 and the 17/31 17
    Combustion chamber 16 facing heat storage module 15 'sections 26, 27, 28 are assigned along the channel 14, in which the temperature of the flue gases A respectively in the direction of the combustion chamber 16 increases. The temperature T4 in the combustion chamber 16 is about 850 ° C. In the example shown, a linear increase in temperature in the direction of the combustion chamber 16 is assumed, wherein the temperature profile in practice may of course also deviate.
    In Fig. 7a curve 29 shows the temperature profile for the case that the flue gases A rohgasseitig have a temperature T3, which is between the stated minimum temperature of about 80 ° C and the stated maximum temperature T2 of about 300 ° C. In this case, the catalyst 6 can be operated without further measures in the predetermined reaction temperature, wherein the temperature of catalyst 6 is on the side facing away from the combustion chamber 16 side above the lower threshold and on the combustion chamber 16 side facing the upper threshold of the reaction temperature range.
    According to curve 30 of FIG. 7a, the flue gases A on the raw gas side have the maximum temperature T2. This has the consequence that the temperature of the catalyst 6 increases in sections above the upper value of the reaction temperature range of about 550 ° C.
    According to curve 31 of FIG. 7a, therefore, the temperature of the flue gases A is lowered by means of the cooling device 19 in order to maintain the reaction temperature range of the catalyst 6. In the embodiment shown, the flue gas A is cooled at the side facing away from the combustion chamber 16 side of the catalyst 6, in particular by introducing a coolant, such that the reaction temperature range of the catalyst 6 is maintained, see.
    Arrow 19 '.
    Fig. 7b shows the case that the flue gases A rohgasseitig the minimum temperature T3 of about 80 ° C, so that the temperature of the catalyst 6 without further measures below the lower value of the reaction temperature range of about 160 ° C drops (Kur / 31 18 ve 32). In order to comply with the reaction temperature range of the catalyst 6, the temperature of the flue gases A on the side facing away from the combustion chamber 16 side of the catalyst 6 is accordingly increased according to curve 33 by means of the heater 19 (see arrow 19 ''). In comparison, curve 29 shows the Temperaturver run in the event that the flue gases A rohgasseitig a Tempe ture T3 between the minimum temperature T3 of about 80 ° C and the stated maximum temperature of about 300 ° C have. 19/31
    权利要求:
    Claims (19)
    [1]
    19. A method 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, with a Rohgasseitig between 80 ° C and 300 ° C fluctuating temperature, wherein the flue gases (A) in an alternating direction by at least two channels (14) each having at least two heat storage modules (15, 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, 15 ') arranged catalyst (6) is carried out with a reaction temperature range of 160 ° C to 550 ° C, and wherein the losses of the heat transfer of the regenerative heat exchange at least partially by regenerative afterburning of the carbon monoxide (CO) and the gaseous organic matter in the Flue gases (A) in a between the at least two channels (14) arranged combustion chamber (16) are compensated, characterized in that the reaction temperature range of the catalyst (6) by cooling and / or heating the flue gases (A) is maintained.
    [2]
    2. The method according to claim 1, characterized in that the flue gases (A) for maintaining the reaction temperature range in at least one of the channels (14) between two catalysts (6) are cooled or heated.
    [3]
    3. The method according to claim 1 or 2, characterized in that the temperature of the catalyst (6) on the side facing away from the combustion chamber (16) by cooling and / or heating the flue gases (A) between the catalyst (6) and the combustion chamber (16) facing away from the heat exchanger module (15) substantially constant, in particular at a temperature between 160 ° C and 350 ° C, preferably substantially 250 ° C, is maintained.
    [4]
    4. The method according to any one of claims 1 to 3, characterized in that the temperature of the catalyst (6) on the 20/31 20 combustion chamber (16) side facing by cooling and / or heating the flue gases (A) between the catalyst ( 6) and the combustion chamber (16) facing the heat exchanger module (15 ') is substantially constant, in particular at a temperature between 350 ° C and 550 ° C, preferably substantially 450 ° C, is maintained.
    [5]
    5. The method according to any one of claims 1 to 4, characterized in that for heating and / or cooling the flue gases (A), a gaseous cooling or heating means, in particular air or exhaust gases, is introduced into the flue gases.
    [6]
    6. The method according to any one of claims 1 to 5, characterized in that for cooling the flue gases, a liquid coolant, in particular water, and / or for heating the flue gases a vaporous heating medium, in particular steam, is introduced into the flue gases.
    [7]
    7. The method according to any one of claims 1 to 6, characterized in that the heating and / or cooling of the flue gases takes place indirectly by heat exchange with a heat exchange medium.
    [8]
    8. The method according to any one of claims 1 to 7, characterized in that the temperature of the flue gases at at least one point in the channels (14) is measured, wherein the flue gases (A) depending on the measured temperature at least one point cooled or be heated, that the reaction temperature range of the catalyst (6) is maintained.
    [9]
    9. Device (1 ') for the catalytic denitrification and regenerative thermal afterburning of carbon monoxide (CO) and gaseous organic substances containing flue gases (A) with a Rohgasseitig between 80 ° C and 300 ° C fluctuating temperature, in particular from the cement clinker production, with at least two each channel (14) having at least two heat storage modules (15, 15 ') for regenerative heat exchange with the flue gases (A), and wherein between the at least two heat storage modules (15, 15') of the channels (14) in each case at least one catalyst (6) is provided for the catalytic reduction of the nitrogen oxides (NOX), which has a reaction temperature range from 160 ° C. to 550 ° C., 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) to Au the losses of the heat displacement in the heat storage modules (15, 15 ') is arranged, characterized in that at least one cooling and / or heating means (19) for cooling and / or heating the flue gases (A) is provided to the reaction temperature range of Catalyst (6) to comply with the raw gas side fluctuating temperature of the flue gases (A).
    [10]
    10. Device (1 ') according to claim 9, characterized in that at least one cooling and / or heating device (19) for maintaining the reaction temperature range between two catalysts (6) is arranged.
    [11]
    11. Device (1 ') according to claim 9 or 10, characterized in that at least one cooling and / or heating device (19) for maintaining the reaction temperature range between the catalyst (6) and the combustion chamber (16) facing away from the heat exchanger module (15) is arranged.
    [12]
    12. Device (1) according to one of claims 9 to 11, characterized in that at least one cooling and / or heating device (19) for maintaining the reaction temperature range between the catalyst (6) and the combustion chamber (16) facing the heat exchanger module (15 ') is arranged.
    [13]
    13. Device (1 ') according to one of claims 9 to 12, characterized in that the at least one cooling and / or heating device (19) at least one feed element (20), in particular a nozzle element, for introducing a cooling or heating means in the flue gases (A), wherein preferably a plurality of supply elements (20) are arranged in a plane perpendicular to the flow direction of the flue gas (A). 22/31 22
    [14]
    14. Device (1 ') according to one of claims 9 to 13, characterized in that the feed element (20) for introducing the cooling and / or heating means is also designed as a device for introducing ammonia or ammonia donating compounds in the flue gases ,
    [15]
    15. Device (1 ') according to one of claims 9 to 14, characterized in that at least one cooling and / or heating device (19) by a heat exchanger (25) is formed, which is preferably arranged perpendicular to the flow direction of the flue gas (A) is.
    [16]
    16. Device (1 ') according to one of claims 9 to 15, characterized in that a measuring device (22) with at least one measuring element (22', 24) for measuring the temperature of the flue gases (A) at at least one point (x) is provided in the channels (14), wherein preferably a measuring element (22 ') for measuring the temperature of the flue gases (A) between the catalyst (6) and the combustion chamber (16) facing away from the heat exchanger module (15) and / or another measuring element (24) for measuring the temperature of the flue gases (A) between the catalyst (6) and the combustion chamber (16) facing the heat exchanger module (15 ') is provided.
    [17]
    17. Device (1 ') according to claim 16, characterized in that the measuring device (22) is connected to a control device (23) which is adapted to the temperature of the flue gases (A) to maintain the reaction temperature range of the catalyst (6). via the cooling and / or heating device (19) to regulate.
    [18]
    18. Device (1 ') according to claim 17, characterized in that the control device (23) is adapted to the temperature of the flue gases (A) on the side facing away from the combustion chamber (16) side of the catalyst (6) above a lower threshold, which is preferably between 160 ° C and 350 ° C, in particular substantially 250 ° C, to keep. 23/31 23
    [19]
    19. Device (1 ') according to claim 17 or 18, characterized in that the control device (23) is adapted to the temperature of the flue gases (A) on the combustion chamber (16) facing side of the catalyst (6) below an upper Threshold, which is preferably between 350 ° C and 550 ° C, in particular substantially 450 ° C, to keep. 24/31
    类似技术:
    公开号 | 公开日 | 专利标题
    AT513597B1|2014-06-15|Process for catalytic denitrification and regenerative thermal afterburning
    EP3099647B1|2018-03-14|Method for heat-treating a material flow and for cleaning resulting exhaust gases
    EP3095505B1|2018-03-07|Process and system for the purification of waste gases charged with nitrogen oxides
    EP3043889A1|2016-07-20|Method and installation for the purification of exhaust gases, having a regenerative post-combustion installation
    WO2015155339A1|2015-10-15|Method and system for the denitrification of flue gases by means of sncr | and downstream catalyst for ammonia decomposition
    WO2015189154A1|2015-12-17|Installation comprising an exhaust gas-generating treatment device, an oxidation catalytic converter and a reduction catalytic converter, as well as a method for treating exhaust gas in such an installation
    CH698991B1|2009-12-31|Exhaust gas flow cleaning method for use in cement clinker producing system in cement industry, involves spraying nitrogenous reducing agent downstream in exhaust gas flow, before exhaust gas flow reaches catalyzer
    EP3265733B1|2019-05-08|Method and plant for denitrifying bypass gases in a multi-stage system of mixing chambers in a plant for producing cement clinker
    EP2444145B1|2017-03-15|Exhaust gas purification stage with multi-layered scr catalyst
    WO2018073239A1|2018-04-26|Method and installation for cleaning pre-heater exhaust gases of an installation for the cement and/or mineral industry
    AT513851B1|2014-08-15|Device for catalytic denitrification and regenerative thermal afterburning
    EP3655134B1|2021-05-05|Method for cleaning a gas stream and corresponding cement manufacture plant
    EP3347660B1|2019-07-17|Method and apparatus for reducing nox emissions in a rotary kiln
    EP3149422B1|2019-05-01|Apparatus for producing cement clinker
    DE102011050125B4|2019-04-18|Flue gas cleaning plant of a cement clinker production plant
    EP3417226B1|2020-01-22|Installation comprising an exhaust gas-generating treatment device and method for treating exhaust gas in such an installation
    EP3155342B1|2018-10-24|Method for exhaust gas treatment, and system comprising an exhaust gas treatment device
    AT17227U1|2021-09-15|Process for cleaning a flue gas
    DE102016121301A1|2018-05-09|Plant and method for cleaning an exhaust gas of a processing apparatus of the cement, lime or mineral industry
    DE102012200337A1|2012-08-23|Method and device for increasing the temperature of a waste or process gas with an oxidizable fraction
    DE102016207313A1|2017-11-02|Plant for the production of cement or processing of ores and method for operating such a plant
    DE102008012449A1|2009-07-23|Denitrification system for cylindrical rotary cement furnace in cement industry, has reduction catalyst with reduction medium supply for reduction of nitrogen oxide, where catalyst is located between filter devices
    WO2012013383A1|2012-02-02|Flue gas cleaning installation for a cement clinker production installation
    同族专利:
    公开号 | 公开日
    DE102014106387A1|2014-11-27|
    AT513597B1|2014-06-15|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    EP0326388A2|1988-01-29|1989-08-02|Johnson Matthey, Inc.,|Waste heat recovery having combined CO and NOx removal apparatus and method|
    DE102005055177B3|2005-11-18|2007-01-11|Siemens Ag|Plant for reducing nitrogen oxide concentration in combustion engine exhaust gas, includes SCR catalyst, ammonia producer and plasma reactor as combined hydrogen and nitrogen oxide production unit|
    CH698991B1|2006-11-02|2009-12-31|Elex Ag|Exhaust gas flow cleaning method for use in cement clinker producing system in cement industry, involves spraying nitrogenous reducing agent downstream in exhaust gas flow, before exhaust gas flow reaches catalyzer|
    AT507773A4|2009-07-15|2010-08-15|Scheuch Gmbh|METHOD AND APPARATUS FOR RELIEVING SMOKE GASES|
    US20110311424A1|2010-06-22|2011-12-22|2E Environmental, LLC|BIOMASS BOILER SCR NOx AND CO REDUCTION SYSTEM|WO2016030207A1|2014-08-29|2016-03-03|Dürr Systems GmbH|Purification device, use of a purification device and method for purifying a waste-gas flow|
    WO2016030200A1|2014-08-29|2016-03-03|Dürr Systems GmbH|Treatment device and method for treating an exhaust stream|
    DE102015208029A1|2015-04-30|2016-11-03|Dürr Systems GmbH|Cleaning device, calciner and method for purifying a raw gas stream|
    AT523972A1|2020-06-29|2022-01-15|Scheuch Gmbh|Process for cleaning flue gases from cement clinker production, and process and device for producing cement clinker|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    ATA50357/2013A|AT513597B1|2013-05-27|2013-05-27|Process for catalytic denitrification and regenerative thermal afterburning|ATA50357/2013A| AT513597B1|2013-05-27|2013-05-27|Process for catalytic denitrification and regenerative thermal afterburning|
    DE201410106387| DE102014106387A1|2013-05-27|2014-05-07|Process for catalytic denitrification and regenerative thermal afterburning|
    [返回顶部]