• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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    • 专利摘要:
    The purpose of the present invention is to suppress wear on a denitration catalyst by ash particles with a diameter of 100 μm or greater. An exhaust gas treatment device is provided with a denitration device 10 having a denitration catalyst 10b for reducing nitrogen oxides in exhaust gas from a coal fired boiler 1 and a duct that guides the exhaust gas from the coal fired boiler to the denitration device, said duct having a horizontal duct 8 connected to an exhaust gas outlet 7 of the coal fired boiler, a vertical duct 9 connected to the horizontal duct, and a hopper 15 provided below the connection part for the horizontal duct and the vertical duct. The exhaust gas treatment device is characterized in that a collision plate 16 for knocking down ash particles in the exhaust gas into the hopper by collision is provided at an upper end opening part of the hopper 15.
    公开号:ES2644888A2
    申请号:ES201790035
    申请日:2016-04-07
    公开日:2017-11-30
    发明作者:Noriyuki Imada；Massaki ISHIOKA；Akihiro Yamada；Goki Sasaki；Katsumi Yano；Keigo UCHIYAMA
    申请人:Mitsubishi Hitachi Power Systems Ltd；
    IPC主号:
    专利说明:

    Technical Field
    5The present invention relates to a chimney gas treatment apparatus, andparticularly with a chimney gas treatment apparatus that includes an apparatus fordenitration that reduces the nitrogen oxides contained in the chimney gasfrom a boiler (for example, for electric power generation) using
    10 coal as fuel and remove the resulting products.
    Prior art
    For example, to remove nitrogen oxides (NOx) in the flue gas
    From a coal combustion boiler for electric power generation, a denitration apparatus that injects a reducing agent (for example, ammonia) into the flue gas is typically used to reduce NOx to N2 with a denitration catalyst. The denitration apparatus is configured to guide the chimney gas that has escaped from the heat exchanger, such as a super heater and an economizer (economizer
    20 coal) from a boiler that uses coal as fuel, to an upper portion of the denitration apparatus via a horizontal duct and a vertical duct as described, for example, in Patent Literature 1. The denitration apparatus has a denitration catalyst that reduces nitrogen oxides, and a reducing agent is injected into the chimney gas through nozzles supplied in a vertical duct on the upstream side
    25 of the denitration catalyst or a duct on the side facing the entrance of the denitration apparatus. The denitration catalyst is typically formed by laminating a plurality of catalysts each formed in a plate-like form or a honeycomb-like form on each other to form a laminar structure, and the resulting catalyst layer typically has openings that have each a size that varies from about 5 to
    30 6mm
    On the other hand, a coal combustion boiler burns crushed coal with a mill in tiny particles of coal that have an average diameter smaller than or equal to 100 µm, supplied in an oven, and burned. The dust or ash (hereinafter collectively referred to as ash particles) produced by combustion typically has a size smaller than or equal to several tens of micrometers. When the scum and the clinker


    they have adhered to the heat transfer tube and the side wall of the boiler is blown, for example, with a soot blower, however, ash masses are produced that have sizes ranging from about 5 to 10 mm, traveling together with the chimney gas to the denitration apparatus, and cause deposits to be generated in the catalyst layer. When the ash masses are deposited on the surface of the catalyst, the deposited ash mass undesirably blocks the flow of the chimney gas and therefore prevents the denitration reaction.
    To solve the inconvenience caused by the ash masses, there is a proposal to supply a hopper below the connecting portion where the horizontal duct and the vertical duct connect with each other and collect the ash masses in the hopper, as It was described in Patent Literature 1 or 2. There is another proposal to slow down the chimney gas flowing through the duct that guides the chimney gas from the boiler to the denitration apparatus and collects the ash masses with a sieve Metal mesh arranged in the horizontal or vertical duct. There is yet another proposal to arrange a slat formed of a plurality of plate-shaped members in an inner wall portion of the vertical duct or to provide an obstruction plate to collect the ash masses and cause the ash masses to fall into the hopper below the vertical duct.
    Patent Literature 3 proposes to arrange a plate member that deflects the flow of chimney gas downward on the upstream side in the horizontal duct to deflect the ash particles towards the inner wall of the horizontal duct and collect the ash particles in a hopper Patent Literature 3 further proposes to provide a collection plate in such a way that it extends from the bottom wall of the horizontal duct to a point above the hopper and uses the whirlpools produced when chimney gas flows around the plate collection to collect ash particles in the hopper. Patent literature 3 further proposes to provide a horizontal deflection plate in the portion where the hopper with which the chimney gas flowing through the horizontal duct collides is connected to a vertical duct such that the deflection plate protrudes at a point above the hopper and allows the deflection plate to guide the flow of the gas flowing into the hopper to a lower surface of the collection plate described above to improve the effect of collecting the ash particle.
    List of Appointments Patent Literature Patent Literature 1: JP-A-2-95415


    Patent Literature 2: JP-A-8-117559 Patent Literature 3: USP 7, 556, 674 B2 Summary of the Invention Technical Problem
    In the Patent Literatures described above, however, consideration is not given to a case where ash particles include those having diameters ranging from 100 to 300 µm. That is, in China, India, and other countries, they plan to introduce combustion boilers with coal that use not only high-quality coal produced in Australia, but coal that has a large amount of ash that makes it difficult to crush coal into tiny particles. . For example, the results of the measurement of the technical analysis values of the coal produced in a district of Inner Mongolia of China (coal A) and the distribution of the diameter of the ash particles contained in the chimney gas show that the proportion of ash in coal A is as high as 47% compared to the proportion of ash in coal produced in Australia (coal B), which is approximately 13%. In relation to the distribution of the ash particle size, 99% of the carbon particles B have smaller or equal diameters of 100 µm, while the proportion of the carbon particles A having smaller diameters
    or equal to 100 µm is simply about 50%. That is, in the case of carbon A, half of the ashes are formed of particles that have diameters greater than or equal to 100 µm.
    As described above, it has been shown that a situation in which the chimney gas contains ash that has 30-40% or more or a situation in which the chimney gas contains ash particles having large diameters greater than or equal to 100 µm cause a new problem of wear of a catalyst of denitration in a short period. For example, the metal mesh screen proposed in some Patent Literatures can remove ash masses having sizes ranging from about 5 to 10 mm, which are larger than the openings of the catalyst layer, but cannot remove the masses of ash that have sizes that vary from 100 µm to 5 mm, which are smaller than the sizes described above.
    On the other hand, when the size of the openings of the metal mesh sieve is adjusted, for example, to 100 µm, not only does the loss of pressure in the duct increase undesirably, but the frequency of occurrence of sieve plugging increases. undesirably Also, since the ash particles that have


    diameters that vary from 100 to 300 µm accompany the chimney gas flowing at a flow rate of several meters / second, the slats formed of a plurality of plate-shaped members arranged in the inner wall of the duct cannot solve the problem of wear of the catalyst of denitration since the ash that has collided with the slats accompanies the flow of chimney gas again and is blown towards the side of the downstream stream.
    An object to be solved by the present invention is to provide a chimney gas treatment apparatus capable of suppressing wear of a denitration catalyst due to ash particles having diameters greater than or equal to 100 µm Solution to the Problem
    The inventors of the present invention have used a numerical analysis approach to intensively conduct a study on the paths of ash particles that accompany the guided chimney gas from a boiler outlet via a horizontal duct and a vertical duct to a denitration apparatus and that they have found that the ash particles having diameters of 30 µm disperse approximately uniformly in the ducts and reach the denitration apparatus while the ash particles having a diameter of 200 µm are locally present in a lower portion of the horizontal duct and accompany the chimney gas, as will be described later.
    The present invention relates to a chimney gas treatment apparatus that includes a denitration apparatus having a denitration catalyst that reduces nitrogen oxides in the chimney gas escaped from a coal combustion boiler, and a duct that guides the chimney gas from the coal combustion boiler to the denitration apparatus, the duct is formed from a horizontal duct connected to a chimney gas outlet from the coal combustion boiler, a vertical duct connected to the horizontal duct, and a hopper supplied below a connecting portion where the horizontal duct and the vertical duct connect with each other, and as a first feature of the present invention, a crash plate that causes the ash particles in the gas of Chimney collide with the shock plate and fall towards the hopper supplied in an upper end opening section of the hopper.
    In accordance with the present invention having the first feature, supplying the shock plate, which causes the ash particles in the chimney gas to collide with the plate


    of impact and fall into the hopper, in the opening section of the upper end of the hopper, that is, in an extension plane of the lower wall of the horizontal duct allows ash particles to have diameters greater than or equal to 100 µm that are locally present in a lower portion of the horizontal duct and accompany the chimney gas to collide with the shock plate for the selective collection of ash particles in the hopper. As a result, particles having diameters greater than or equal to 100 µm can be collected in the hopper with high efficiency, whereby a situation in which large diameter ash particles wear out a denitration catalyst can be avoided .
    In this case, the shock plate is preferably formed in a rectangular shape and is arranged in such a way that the long lower edge of the shock plate is located in an upper end opening plane of the hopper corresponding to a plane of extension of a lower wall of the horizontal duct and the long lower edge extends in a direction across the horizontal duct. The shock plate thus configured allows the ash particles to have diameters greater than or equal to 100 µm that are locally present in a lower portion of the horizontal duct and accompany the chimney gas to effectively collide with the shock plate and fall into the hopper Since the shock plate only needs to have a rectangular shape that has short edges that correspond to the region where ash particles that have diameters greater than or equal to 100 µm are present locally on the side facing the bottom wall of the horizontal duct and they disperse, by means of which the pressure loss of the chimney gas flow can be suppressed to a small value.
    The shock plate can be supplied in a range that is measured from the far side end of the upper end opening of the hopper viewed from a side facing the horizontal duct and corresponding to a quarter to three quarters of a length of one upper end opening. Additionally, the shock plate is preferably supplied in order to lean towards the horizontal duct by an established angle "a" (0 ° <to ≤ 90 °) with respect to the upper end opening plane of the hopper.
    As a second feature of the present invention, a partition plate is additionally provided in the hopper in order to be perpendicular to an extension of the horizontal duct and extend downward in a vertical direction.
    According to the second feature, the partition plate can suppress (reduce) the chimney gas flowing through the horizontal duct collides with the wall surface of the


    Hopper, travels along the side wall of the hopper towards the bottom of the hopper, revolves around the bottom where the collected ash particles are deposited, and travels upwards. As a result, a situation can be avoided in which the ash particles collected in the hopper are dispersed again, whereby the number of particles having different diameters greater than or equal to 100 µm reaching the denitration catalyst is They can suppress. In this case, the partition plate is preferably supplied in a position that is measured from a far side end of the upper end opening of the hopper viewed from a side facing the horizontal duct and corresponds to half the length of the upper end opening, that is, a central position of the upper end opening.
    The present invention is characterized in that the chimney gas outlet, to which the horizontal duct is connected, is formed in a side wall of a chimney gas channel down in which the heat recovery / heat transfer tube of The coal combustion boiler is arranged, and that an outstanding section is supplied in the chimney gas channel in order to protrude from the side wall of the chimney gas channel above the horizontal duct at a chimney gas outlet .
    Advantageous Effects of the Invention
    The present invention allows the suppression of wear of the denitration catalyst due to ash particles having diameters greater than or equal to 100 µm Brief description of the drawings
    [Figure 1] Figure 1 is a total configuration diagram of a first embodiment of the chimney gas treatment apparatus according to the present invention [Figure 2] Figures 2 (a) and 2 (b) are perspective views enlarged and a cross-sectional view of hoppers that characterize the first embodiment.
    [Figure 3] Figure 3 is a perspective view of an example of a denitration catalyst in the first embodiment [Figure 4] Figure 4 shows an example of the ash particle diameter distribution showing the difference in the type of coal. [Figure 5] Figure 5 shows results of the technical analysis values of the two types of coal and result in ash composition analysis. [Figure 6] Figure 6 (a) shows a numerical analysis of a path of dispersion of ash particles from a boiler outlet via a horizontal duct and a duct


    vertical to a desulfurization device, and Figure 6 (b) shows the numerical analysis of the path of dispersion of ash particles having a different size. [Figure 7] Figure 7 shows a result of the analysis of the gas flow velocity distribution in the case where a crash plate is arranged in the first embodiment. [Figure 8] Figure 8 shows a result of the analysis of the path of the large diameter ash particles in the case where the shock plate is arranged in the first embodiment [Figure 9] Figure 9 shows a result of the analysis of the distribution of the gas flow rate in the case of a redispersor that prevents the plates from being arranged in the first embodiment. [Figure 10] Figure 10 shows the results of the examination of the position of the shock plate in the first embodiment. [Figure 11] Figure 11 shows the results of the redispersor shape test that avoids the plates in the first embodiment. [Figure 12] Figure 12 shows the differences in the percentages of ash particle collection between various forms of the plates that prevent redispersion [Figure 13] Figure 13 shows the proportions of the dispersion particles having diameters of 100, 200, and 360 µm in the first embodiment compared to the related technique. [Figure 14] Figure 14 describes a variation in which an outstanding section is supplied at the outlet of the boiler to which the horizontal duct is connected in the first embodiment [Figure 15] Figure 15 shows a difference in the percentage of ash particle collection between the presence and absence of an outstanding section in Figure 13 [Figure 16] Figure 16 is a configuration diagram of key parts in a second embodiment of the chimney gas treatment apparatus according to the present Invention [Figure 17] Figure 17 shows the results of the calculation of the percentage of ash particle collection versus an angle α of the sidewall crash plates in the second embodiment. [Figure 18] Figure 18 shows the results of the calculation of the percentage of ash particle collection versus a β angle of the sidewall shock plates in the second embodiment. [Figure 19] Figure 19 shows the results of the calculation of the percentage of ash particle collection versus the width d of the sidewall crash plates in the second embodiment


    [Figure 20] Figure 20 shows the results of the calculation of the percentage of ash particle collection versus a distance L1 between the lower ends of the sidewall crash plates in the second embodiment and the upper portions of the hoppers. [Figure 21] Figure 21 shows details on a ceiling crash plate in a third embodiment
    Description of the Accomplishments
    A chimney gas treatment apparatus according to the present invention will be described below on the basis of the embodiments.
    (First realization)
    The total configuration of the first embodiment of the chimney gas treatment apparatus according to the present invention will be described with reference to Figure 1. A coal combustion boiler 1 includes a burner 4, which uses the combustion gas 3 for burn coal 2 crushed by a crusher that is not shown, such as a mill. The coal combustion boiler 1 further includes a plurality of heat recovery / heat transfer tubes 5, through which water flows, in an oven and a chimney gas channel of the coal combustion boiler 1, and an economizer (coal economizer) 6, which is 1 of the heat recovery / heat transfer tubes 5, which are further supplied in a downstream portion of the chimney gas channel of the coal combustion boiler 1. The coal combustion boiler 1 is thus configured to produce steam that drives an electric power generating turbine that is not shown.
    An outlet 7 of the chimney gas of the coal combustion boiler 1 is supplied through the boiler side wall below the economizer 6, and a horizontal duct 8 is connected to the outlet 7 of the chimney gas. The other end of the horizontal duct 8 is connected to the side wall of the vertical duct 9, and the upper end of the vertical duct 9 is connected to an inlet duct 10 a of the denitration apparatus 10. The chimney gas produced when the coal combustion boiler 1 burns the coal is guided through the outlet 7 of the chimney gas via the horizontal duct 8 and the vertical duct 9 to an upper portion of the denitration apparatus 10. The denitration apparatus 10 is thus configured such that the interior thereof is filled with a denitration catalyst 10b, shown in Figure 3, and ammonia is injected as a reducing agent through a nozzle 10c of


    ammonia supply, which is supplied somewhere in the middle of the vertical pipeline 9. The denitration apparatus 10 is thus configured to reduce the nitrogen oxides (NOx) contained in the chimney gas and the resulting products escape. The chimney gas from which the NOx has been removed and escaping from the denitration apparatus 10 travels through the air heater 11, which heats the burned gas, a dust collector 12, and a desulfurization device 13 and discharges into outside a chimney 14 towards the air.
    The configuration of a characteristic portion of the present invention will be described later. A plurality of hoppers 15 are disposed below the vertical duct 9, which is connected to the end of the horizontal duct 8, along the wide direction of the horizontal duct 8, as shown in Figures 1 and 2. The plane The upper end opening of each of the hoppers 15 is arranged in order to be in accordance with the position of the surface of the lower wall of the horizontal duct 8. A shock plate 16 is provided in order to be located along the opening planes of the upper end of the hoppers 15 and causes the ash particles in the chimney gas to collide with the shock plate 16 and fall towards the hoppers 15. The shock plate 16 of the present embodiment is shaped in a rectangular shape and is arranged such that the lower longitudinal edge of the shock plate 16 is located in the opening planes of the upper end of the hoppers that they correspond to an extension plane of a lower wall of the horizontal duct 8 and the lower longitudinal edge extends in the wide direction of the horizontal duct 8, as shown in Figure 2 (a). The width of the short edges of the shock plate 16 is determined according to the thickness of the flow of the large diameter ash particles, which are dispersed along the bottom wall of the horizontal duct 8, as described below. For example, the width of the short edges of the shock plate 16 can be selected from values within the range of 2 to 7% of the vertical width H of the horizontal duct 8 and is determined in consideration of the relationship between the pressure loss of the chimney gas flow and the percentage of ash particle collection. In addition, the shock plate 16 is supplied in order to lean towards the horizontal duct 8 with respect to the opening planes of the upper end of the hoppers 15, as shown in Figure 2 (b). The angle "a" of inclination can be any value within the range of 0 ° <to ≤ 90 ° to make the ash particles collide with the shock plate 16 and effectively fall into the hoppers 15.
    A partition plate 17 that prevents redispersion is disposed in each of the hoppers 15. That is, the partition plate 17 is supplied in each of the hoppers 15 in order to be perpendicular to an extension of the horizontal duct 8 and stretch down in the direction


    vertical. The partition plates 17 thus arranged can suppress (reduce) the chimney gas flowing through the horizontal duct 8, collides with the wall surfaces of the vertical duct 9 and the hoppers 15, travels along the side walls of the hoppers 15 towards the lower parts thereof, rotates around in the lower parts where the collected ash particles are deposited, and travels upward, whereby a situation in which the collected ash particles are dispersed from can be avoided new.
    With reference to the first embodiment thus configured of the present invention, the action of the coal combustion boiler 1 will be described with reference to a case where the coal combustion boiler 1 is operated when using coal A, which is a coal of low quality, as shown in Figure 5. The coal combustion boiler 1, in which the coal 2 and the air as the combustion gas 3 are supplied to the burner 4, burn the coal A. The heat generated by The combustion reaction of coal A heats the water via a wall that cools the water that is not shown, a heat transfer tube, super heaters 5, the economizer 6, and other heat recovery / heat transfer tubes to produce steam, which allows a turbine generator that is not shown to produce electricity.
    The chimney gas produced when the coal combustion boiler 1 burns the coal A escapes via the outlet 7 of the chimney gas, which is located on the side facing the economizer 6 outlet. At this point, the gas The chimney contains a large amount of ash that has diameters that vary from 100 to 300 µm since coal A is a low quality coal. Ash particles of large diameter (diameter varying from 100 to 300 µm, for example), in the chimney gas are collected, when they flow through the horizontal duct 8, into an inner wall portion of the horizontal duct 8. The large diameter ash particles collected in the lower wall portion of the horizontal duct 8 then collide with the shock plate 16, which is disposed below the vertical duct 9, and fall into the hoppers 15. Since the plate Partition 17 is disposed in each of the hoppers 15, the collected large-sized ash particles are not dispersed again but are kept in the hoppers 15.
    Ammonia is supplied through the ammonia supply nozzle 10c, which is disposed in the vertical duct 9, to the chimney gas from which most of the large diameter ash particles have been removed as described above, and the resulting chimney gas is guided to the denitration catalyst 10b. The NOx in the chimney gas, when the chimney gas passes through the denitration catalyst 10b, is


    Reduces to nitrogen and water. Since most of the ash particles larger than
    or equal to 100 µm have been removed from the chimney gas passing through the denitration catalyst 10b, the denitration catalyst 10b hardly wears out. The chimney gas then passes through an air heater 11, where the chimney gas undergoes heat exchange with the combustion air and is therefore cooled. After the ash particles are removed by the dust collector 12, and the sulfur oxides are removed by the desulfurization device 13, the resulting chimney gas is discharged via the chimney 14 into the air.
    The effect of removing large diameter ash particles in the first embodiment will now be described in detail with reference to Figures 6 to 9. First, in the process of achieving the present invention, the findings obtained by numerical analysis will be described. Figure 6 shows the results of the ash particle path analysis from the outlet 7 of the chimney gas to the denitration catalyst 10b. In the numerical analysis, the flow of the chimney gas and the paths of the ash particles was determined on the assumption that the crash plate 16 or the partition plate 17 was not supplied in the first embodiment and the ash particles were they dispersed evenly in the outlet plane of the economizer 6 of the coal combustion boiler 1. Figure 6 (a) shows the path in a case where the ash particles have a diameter of 30 µm, and Figure 6 (b) shows the path in a case where the diameter is 200 µm. These figures show that the ash particles having the diameter of 30 µm disperse approximately uniformly in the ducts and reach the catalyst 10 b of denitration. In contrast, Figure 6 (b) shows that the ash particles having the diameter of 200 µm are locally present in a lower position of the horizontal duct 8 at the entrance of the vertical duct 9. In consideration of the results described above, in the first embodiment, the hoppers 15 are arranged below the vertical duct 9, and the shock plate 16 is disposed above the hoppers 15, such that the ash particles that are Locally present in the lower portion of the horizontal duct 8 and dispersed are selectively guided and collected in the hoppers 15.
    Figure 8 shows a result of the numerical analysis in the case where the shock plate 16 is disposed above the hoppers 15. Figure 8 shows that the ash particles locally present in the lower portion of the horizontal duct 8 collide with the shock plate 16, as indicated by the path 20, and are collected in the hoppers 15. Figure 7 shows a result of the calculation of the flow velocity distribution in this case. The flow rate of the chimney gas in the hoppers 15 is lowered several


    meters / second or less, by means of which the proportion of the red particles of ash redispersed in the hoppers 15 can be lowered.
    In addition, Figure 9 shows a result of the numerical analysis in the case where the partition plates 17 are arranged in the hoppers 15. Arranging the partition plates 17 in the hoppers 15 can suppress the flow of chimney gas in the hoppers 15 by therefore greatly reduce the amount of redispersed ash collected in hoppers 15.
    Figure 10 shows a test result of an optimal position where the shock plate 16 is arranged.
    The results of the evaluation of the percentage of soot collection with the position of the shock plate 16 changed as shown in Fig. 10 (a) and are shown in Figure 10 (b). The position of the shock plate 16 is established with respect to the base point 0 at the far side end of the openings at the upper end of the hoppers 15 viewed from the side facing the horizontal duct 8, and the position is adjusted in the base 0 point and the points changed towards the horizontal duct 8 and corresponding to a quarter to three quarters of the length L of the upper end openings of the hoppers. As a result, Figure 10 (b) shows that the collection percentage decreases when the shock plate 16 is arranged at the 0 base point. The results shown in Figure 10 (b) indicate that the shock plate 16 is effectively located in a position changed from the base point 0 to a quarter to three quarters of the length L shown in Fig. 10 (a). Furthermore, in consideration of the influence of chimney gas flow, it is believed that the optimum position of the shock plate 16 is the position that is changed from the base point 0 to a quarter of the length L and where the plate 16 Shock does not block the flow of chimney gas.
    Figures 11 and 12 show results of the examination of the shape of partition plates 17 that prevent redispersion. The partition plates 17 are supplied in a position changed from the base point 0 to the hoppers 15 described above, in approximately half of the length L of the upper end openings of the hoppers, as in the case of the shock plate 16, such that the partition plates 17 extend vertically downwards, as shown in Figures 11 (a) to 11 (d). Figure 11 (a) shows a case where the partition plates 17 are arranged along the full height of the hoppers 15. Figure 11 (b) shows a cover where a quarter of the lower portion of each of The partition plates 17 is cut. Figure 11 (c) shows a case where a quarter of the upper portion of each of the partition plates 17 is cut.


    Figure 11 (d) shows a case where a quarter of the upper and lower portions of each of the partition plates 17 are cut. As a result, Figure 12 shows that differences in shape do not greatly affect the redispersion prevention effect, and that the vertical length of the partition plates 17 does not greatly affect the redispersion prevention effect.
    As described above, according to the first embodiment, approximately all ash particles having a diameter of at least 100 µm can be collected in hoppers 15 before the ash particles reach the denitration catalyst 10b. As a result, the amount of large diameter ash particles that reach the denitration catalyst 10b can be markedly reduced, whereby the amount of wear of the denitration catalyst 10b can be suppressed.
    That is, coal A is, for example, coal produced in the Inner Mongolia district of China, and coal B is coal produced in Australia, as shown in Figures 4 and 5. The technical analysis values in the Figure 5 and the measured results of the particle diameter distribution of the ash particles contained in the chimney gas show that the proportion of the ash in coal A is as high as 47%. In addition, the distribution of the ash particle diameter shown in Fig. 4 shows that 99% of the carbon particles B have diameters smaller than or equal to 100 µm, while only about 50% of the carbon particles A have diameters less than or equal to 100 µm, which means that half of the carbon ash particles A are formed from ash particles greater than or equal to 100 µm
    In the case where the chimney gas contains ash that has 30-40% or more, as in the case of the fuel formed in coal A or in the case where the chimney gas contains ash particles that have larger or larger diameters equal to 100 µm, the denitration catalyst undesirably wears out in a short period. For example, the metal mesh sieve proposed in Patent Literature 1 and supplied to remove ash masses having sizes ranging from about 5 to 10 mm can remove ash masses having sizes ranging from about 5 to 10 mm, which are larger than the openings of the catalyst layer, but cannot remove ash masses that have sizes ranging from 100 µm to 5 mm that are smaller than the sizes described above. On the contrary, when the size of the openings of the metal mesh sieve is adjusted, for example, to 100 µm, not only does the loss of pressure in the duct increase undesirably, but the frequency of the


    occurrence of sieve plugging increases undesirably. In addition, since the ash particles having diameters ranging from 100 to 300 µm accompany the chimney gas flowing at a flow rate of several meters / seconds, the slats formed of a plurality of plate-shaped members arranged in The inner wall of the duct results in even wear of the denitration catalyst since the ashes that have collided with the slats accompany the flow of chimney gas again and are blown towards the downstream side of the stream. The first embodiment of the present invention can solve the problem with the related technique and avoid, with a simple configuration, the wear and damage of the denitration catalyst due to the chimney gas containing the ash particles greater than or equal to 100 µm even when coal containing ash particles greater than or equal even when coal containing ash particles greater than or equal to 100 µm is used.
    (Variation of the First Realization)
    In the case where the outlet 7 of the chimney gas, to which the horizontal duct 8 is connected, is formed below the side wall of the economizer 6, an outstanding section 23, which protrudes from the side wall above the opening of the outlet 7 of the chimney gas can be supplied in the chimney gas channel, in addition to the first embodiment, as shown in Figure 14 (a). That is, the outlet 7 of the chimney gas, to which the horizontal duct 8 is connected, is formed in the side wall of the chimney gas channel down in which the economizer 6, which is one of the recovery pipes of Heat / heat transfer of coal burning boiler 1, is arranged. In particular, the protruding section 23 is supplied in the chimney gas channel in order to project from the side wall of the chimney gas channel above the horizontal duct at the outlet 7 of the chimney gas. Figure 14 (b) corresponds to the first embodiment, in which the outstanding section 23 is not supplied.
    According to the following variation, supplying the outstanding section 23 markedly improves a percentage A, of ash particle collection, compared to the percentage B of ash particle collection in the case where the outstanding section 23 is not supplied, as shown in Figure 15. A conceivable reason for this is that supplying the outstanding section 23 improves the effect of collecting ash particles in a lower portion of the horizontal duct for improvement in the percentage of ash particle collection in the hoppers 15 The greater the outstanding amount of the outstanding section 23, the greater the effect of separation of the ash particle


    expected, but the outstanding amount is desirably adjusted to approximately a quarter of the channel width to the maximum in consideration of an increase in the energy required to operate a fan in accordance with an increase in pressure loss. (Second Embodiment)
    Figure 16 is a diagram of configuration of key parts in a second embodiment of the chimney gas treatment apparatus according to the present invention. The second embodiment differs from the first embodiment in that the side wall shock plate is supplied in the horizontal duct 8 and the other points are the same as those in the first embodiment. The same constituent parts therefore have the same reference characters and will not be described.
    Figure 16 (a) is a transparent side view of the inside of the horizontal duct 8 and one of the hoppers 15, and Figure 16 (b) is a transparent plan view showing the inside of the horizontal duct 8 and the hopper 15. A pair of sidewall crash plates 31a and 31b are supplied symmetrically on the side walls of the horizontal duct 8 facing each other, as shown in Figure 16 (b). The pair of impact plates 31a and 31b of the side wall are provided in order to lean at an angle α with respect to the side walls upstream of the horizontal duct 8, as shown in Figure 16 (b). The side wall impact plates 31a and 31b are further supplied in order to lean at angle β with respect to the bottom wall upstream of the horizontal duct 8, as shown in Figure 16 (a). In addition, the positions of the lower ends of the side wall crash plates 31a and 31b are adjusted in order to be separated from the position where the horizontal duct 8 is connected to the hopper 15 towards the upstream side a distance L1 and it is also separated from the bottom wall of the horizontal duct 8 by a distance L2. The width d of the side wall crash plates 31a and 31b are adjusted to a selected value of values ranging from 2 to 7% of the lateral width D of the horizontal duct 18.
    The angles α and β of inclination and the width D of the impact plates 31a and 31b of the side wall and the distance L1 thereof are determined on the basis of the calculated percentages of ash particle collection shown in Figures 17 a 20. That is, Figure 17 shows the relationship between the angle α and the percentage of ash particle collection. Increasing the angle α decreases the pressure loss of the chimney gas flow due to the pair of sidewall impact plates 31a and 31b, as shown in Figure
    17. A conceivable reason for this is that the area of the region where the chimney gas flow separates decreases as the angle α increases. But nevertheless,


    Since the percentage of ash particle collection follows a convex shape upward in the range of α = 30 ° to 60 ° with the percentage of ash particle collection maximized at 45 °, it is believed that α is more preferably adjusted to 45 °. In addition, the percentages of ash particle collection decrease in the range beyond α = 45 °. In consideration of the facts described above, although the angle α may be any of the values of 30 ° to 60 °, the angle α is preferably selected from values of 30 ° to 45 °.
    On the other hand, angles β less than 45 ° are undesirable because the horizontal length of the sidewall shock plates is increased. In contrast, angles β greater than 45 ° slightly increase the percentage of particle collection, but the amount of increase is small, as shown in Figure 18. However, when angle β is adjusted to 80 °, the loss of pressure decreases markedly, and the percentage of ash particle collection also tends to decrease accordingly. In consideration of the facts described above, the angle β is selected from values ranging from 45 ° to 70 °, preferably from 60 to 70 °.
    The width d of the sidewall crash plates 31a and 31b do not significantly improve the percentage of ash particle collection in the region where d / D varies from 7 to 20% but increases the pressure loss, as shown in the Figure 19. In consideration of the facts described above, the width d is preferably selected from values ranging from 2 to 7% of the width D of the horizontal duct.
    Additionally, the distance L1 between the lower ends of the sidewall crash plates 31a, 31b and the position in the horizontal duct 8 is connected to the hopper 15 does not affect the percentage of ash particle collection, specifically, even when the distance L1 is increased, as shown in Figure 20. In addition, an increase in distance L1 simply slightly decreases the pressure loss. The lower ends of the side wall impact plates 31a and 31b may therefore be located in the position of the upper end opening of the hopper 15, that is, the position corresponding to L1 =
    0.
    The distance L2, by means of which the lower ends of the sidewall crash plates 31a and 31b are separated from the bottom wall of the horizontal duct 8, determines the fact that the ash particles collected by the plates 31a and 31b of sidewall collision fall into the bottom wall of the horizontal duct 8. No problem


    even if the distance L2 is set to 0 because most of the ash particle falls are eventually recovered in the hoppers 15.
    According to the second embodiment thus configured, in the case where the large diameter ash particles accompany the flow of chimney gas not only along the bottom wall of the horizontal duct 8 but also the side walls thereof, The pair of sidewall crash plates 31a and 31b can further improve the percentage of ash particle collection compared to the first embodiment. In particular, since the side wall shock plates 31a and 31b allow the collection of large-sized ash particles without a large increase in pressure loss, the combination of the second embodiment with the first embodiment can effectively improve the percentage of large diameter ash particle collection.
    (Third Embodiment)
    Figure 21 shows a configuration diagram of key parts of a third embodiment of the chimney gas treatment apparatus according to the present invention. The third embodiment differs from the first and second embodiments in that the roof wall of the horizontal duct 8 is supplied with a roof crash plate that extends vertically from the roof wall. The other points are the same as those in the first and second embodiments, and the same constituent parts therefore have the same reference characters and will not be described.
    Figures 21 (a) are transparent side views of the interior of the horizontal duct 8 and one of the hoppers 15, and Figure 21 (b) is a transparent plan view showing the inside of the horizontal duct 8 and the hopper 15. A Roof crash plate 32 is supplied in order to extend vertically from the roof wall of the horizontal duct 8, as shown in Figures 21a and 21b. The ceiling crash plate 32 is supplied in order to be located in a position upstream of the pair of sidewall crash plates 31a and 31b. The ceiling crash plate 32 is formed of a pair of pieces 32a and 32b of plates, which extends from a central portion across the ceiling wall to the side walls on opposite sides, and the angle γ between the pair of pieces of plate a value is varied that varies from 45 to 70º, preferably from 60 to 70º. In addition, the surfaces of the pair of plate pieces 32a and 32b are inclined towards the upstream side of the horizontal duct 8 by an angle δ ranging from 30 to 60 °, preferably from 45 to 60 ° with respect to the roof wall. Moreover, the pair of plate pieces 32a and 32b of the roof crash plate 32 is


    supplies in such a way that the end portions thereof on the sides facing the opposite side walls are separated from the corresponding side walls at least by the width (height) of the side wall crash plates.
    The third embodiment is preferable in the case where a coal combustion boiler 1 has a rotary combustion furnace. That is, in a rotary combustion furnace, in whose larger diameter the ash particles disperse towards the roof wall of the horizontal duct 8 in some cases, the ash particles cause them to collide with the roof crash plate 32 and are collected. The situation in which the ash particles greater than 100 µm reach the denitration catalyst 10b can therefore be avoided, whereby the amount of catalyst wear can be markedly reduced.
    A distance L3 whereby the pair of plate pieces 32a and 32b of the roof crash plate 32 are separated from the corresponding side walls is at least the width d of the side wall crash plates 31a and 31b, or the pair of plate pieces 32a and 32b are supplied in order to be separated by a smaller distance of L3 = dtanα. That is, the distance L3 is preferably smaller than the width that relates to the sidewall crash plates 31a and 31b (= dtanα).
    According to the third embodiment in combination with the first or second embodiment, the percentage of large diameter ash particle collection can be effectively improved by using the third embodiment even when using a coal combustion boiler 1 having an oven of rotary combustion.
    The present invention has been described above on the basis of the embodiments, but the present invention is not limited thereto. It is evident to a person skilled in the art that the present invention can be executed in a modified or changed form to the extent that the modification or change falls within the scope of the substance of the present invention, and the form thus modified or changed. , of course, belongs to the claims of the present application.
    List of Reference Signs
    one coal combustion boiler
    7 chimney gas outlet
    8 horizontal duct
    9 vertical duct


    10 denitration apparatus 10b denitration catalyst 10c ammonia supply nozzle 15 hopper
    5 16 shock plate 17 partition plate

    权利要求:
    Claims (12)
    [1]
    1. A chimney gas treatment apparatus comprising: a denitration apparatus having a denitration catalyst that reduces nitrogen oxides in the chimney gas escaped from a coal combustion boiler; and a duct that guides the chimney gas from the coal combustion boiler to the denitration apparatus, the duct is formed from a horizontal duct connected to a chimney gas outlet from the boiler, a vertical duct connected to the horizontal duct, and a hopper supplied below a connecting portion where the horizontal duct and the vertical duct are connected to each other, where a shock plate that causes ash particles in the chimney gas collides with the crash plate and falls inside the hopper is supplied in an upper end opening section of the hopper
    [2]
    2. The chimney gas treatment apparatus according to claim 1, wherein the shock plate is formed in a rectangular shape and arranged such that the lower longitudinal edge of the shock plate is located in an opening plane of the upper end of the hopper corresponding to an extension plane of a lower wall of the horizontal duct and the lower longitudinal edge extends in a direction to the horizontal duct boat.
    [3]
    3. The chimney gas treatment apparatus according to claim 1, wherein the shock plate is supplied in a range that is measured from a far side end of an upper end opening of the hopper viewed from the facing side. the horizontal duct and corresponds to a quarter to three quarters of the length of the upper end opening.
    [4]
    Four. The chimney gas treatment apparatus according to claim 2, wherein the shock plate is supplied in a range that is measured from a far side end of an upper end opening of the hopper viewed from a facing side. the horizontal duct and corresponds to a quarter to three quarters of the length of the upper end opening

    [5]
    5. -The chimney gas treatment apparatus according to any one of claims 1 to 4, wherein the shock plate is supplied in order to lean towards the horizontal duct by an angle adjusted "a" (0 ° <a ≤ 90º) with respect to the upper end opening plane of the hopper
    [6]
    6. The chimney gas treatment apparatus according to any one of claims 1 to 4, wherein a partition plate is also supplied in the hopper in order to be perpendicular to a horizontal duct extension and downward extension. in the vertical direction
    [7]
    7. The chimney gas treatment apparatus according to claim 6, wherein the partition plate is supplied in a position that is measured from a far side end of the opening of the upper end of the hopper viewed from a facing side. the horizontal duct and corresponds to half a length of the upper end opening.
    [8]
    8. The chimney gas treatment apparatus according to any one of claims 1 to 4, wherein The chimney gas outlet is formed in a side wall of a chimney gas channel down in which the pipe of Heat recovery / heat transfer of the coal combustion boiler is arranged, and an outstanding section is supplied in the chimney gas channel in order to protrude from the side wall of the chimney gas channel above the horizontal duct at the outlet of the chimney gas.
    [9]
    9. -The chimney gas treatment apparatus according to claim 8, wherein the horizontal duct is supplied with a pair of sidewall shock plates that are located in a separate position from the hopper and upstream thereof and It extends from an upper end to a lower end of a pair of side walls that face each other.
    [10]
    10. -The chimney gas treatment apparatus according to claim 9, wherein the sidewall shock plates are supplied in order to lean at an angle ranging from 30 ° to 60 °, preferably from 30 ° to 45 ° with respect to the side walls stream

    above the horizontal duct and lean further at an angle ranging from 45 to 70 °, preferably from 60 to 70 ° with respect to the bottom wall upstream of the horizontal duct.
    11. The chimney gas treatment apparatus according to claim 10, wherein the side wall shock plates each have a width adjusted to a value ranging from 2 to 7% of the lateral width of the horizontal duct , and the side wall shock plates are supplied such that the lower ends thereof are separated from the wall
    10 lower horizontal duct.
    [12]
    12. The chimney gas treatment apparatus according to claim 9, wherein a ceiling shock plate is supplied in the horizontal duct in order to extend
    15 vertically from the ceiling wall of this current upstream of the pair of sidewall crash plates, and the ceiling crash plate is formed from a pair of plate pieces extending from a central portion to the width of the wall from roof to the side walls on opposite sides, with an angle between the pair of plate pieces adjusted to a value ranging from 45 to 70 °, preferably from 60 to 70 ° and surfaces of the pair of plate pieces that are
    20 lean towards the upstream side of the horizontal duct by an angle that varies from 30º to 60º, preferably from 45º to 60º with respect to the roof wall.
    [13]
    13. The chimney gas treatment apparatus according to claim 12, wherein
    The ceiling impact plate is supplied in such a way that the end portions thereof that face the opposite side walls are separated from the corresponding opposite side walls are separated from the corresponding side walls at least by a height of the sidewall crash plates.




















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    同族专利:
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    ES2644888B2|2018-10-11|
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    JP6560007B2|2019-08-14|
    US20180085694A1|2018-03-29|
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    JP2016198701A|2016-12-01|
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    JP6513341B2|2014-05-23|2019-05-15|三菱日立パワーシステムズ株式会社|NOx removal equipment and catalyst replacement method|JP6093101B1|2016-09-12|2017-03-08|中国電力株式会社|NOx removal catalyst and method for producing the same|
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    法律状态:
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    优先权:
    申请号 | 申请日 | 专利标题
    JP2015079210A|JP6560007B2|2015-04-08|2015-04-08|Exhaust gas treatment equipment|
    JP2015-079210|2015-04-08|
    PCT/JP2016/061375|WO2016163449A1|2015-04-08|2016-04-07|Exhaust gas treatment device|
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