CN115779628A - Waste incineration flue gas treatment method - Google Patents
Waste incineration flue gas treatment method Download PDFInfo
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- CN115779628A CN115779628A CN202211480747.2A CN202211480747A CN115779628A CN 115779628 A CN115779628 A CN 115779628A CN 202211480747 A CN202211480747 A CN 202211480747A CN 115779628 A CN115779628 A CN 115779628A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 239000003546 flue gas Substances 0.000 title claims abstract description 84
- 238000000034 method Methods 0.000 title claims description 26
- 238000004056 waste incineration Methods 0.000 title claims description 13
- 239000003054 catalyst Substances 0.000 claims abstract description 60
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims abstract description 11
- 230000006698 induction Effects 0.000 claims abstract description 4
- 238000001179 sorption measurement Methods 0.000 claims description 61
- 239000010410 layer Substances 0.000 claims description 20
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 12
- 230000008569 process Effects 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical class [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 11
- 239000007921 spray Substances 0.000 claims description 11
- 239000011229 interlayer Substances 0.000 claims description 8
- AOSFMYBATFLTAQ-UHFFFAOYSA-N 1-amino-3-(benzimidazol-1-yl)propan-2-ol Chemical compound C1=CC=C2N(CC(O)CN)C=NC2=C1 AOSFMYBATFLTAQ-UHFFFAOYSA-N 0.000 claims description 7
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 claims description 7
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 6
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- 235000013980 iron oxide Nutrition 0.000 claims 1
- VBMVTYDPPZVILR-UHFFFAOYSA-N iron(2+);oxygen(2-) Chemical class [O-2].[Fe+2] VBMVTYDPPZVILR-UHFFFAOYSA-N 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 9
- 150000001495 arsenic compounds Chemical class 0.000 abstract description 7
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 abstract description 7
- 239000000292 calcium oxide Substances 0.000 abstract description 7
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 abstract description 7
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- 238000007781 pre-processing Methods 0.000 abstract 3
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract 1
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Abstract
The application discloses msw incineration flue gas processing method, flue gas after msw incineration firstly gets into semi-dry reaction tower deacidification system and carries out the deacidification, flue gas after the deacidification gets into denitration preprocessing device and carries out the preliminary treatment, flue gas entering SCR system carries out denitration treatment after the denitration preprocessing, denitration preprocessing device includes the cavity, rotating magnetic pole and absorption storehouse, the absorption storehouse sets up in the cavity, the magnetic induction line of rotating magnetic pole passes the absorption storehouse, set up flue gas water conservancy diversion structure around the absorption storehouse in the cavity, the absorption ball surface is provided with modified oxidation graphite alkene layer, modified oxidation graphite alkene load has magnetic iron oxide, set up horizontal plate formula catalyst in the SCR system, horizontal plate formula catalyst surface sets up porosely. The flue gas is pretreated before SCR denitration, so that the content of arsenic compounds and calcium oxide in the flue gas is reduced, the influence of the arsenic compounds in the flue gas on a catalyst in an SCR system is reduced, and the denitration efficiency is obviously improved.
Description
Technical Field
The invention belongs to the field of environmental protection, and particularly relates to a waste incineration flue gas treatment method.
Background
In the prior art, the flue gas treatment process is desulfurization, dust removal and denitration, the conventional denitration process easily poisons a catalyst due to arsenic oxide contained in the flue gas, calcium oxide in the flue gas easily causes precipitation to be attached to the surface of the catalyst to influence the denitration effect, SO that the cost is overhigh, and in addition, in the SCR reaction process, the residual SO in the flue gas is caused 2 Ammonium bisulfite and ammonium bisulfate are easy to form and are attached to the surface of a catalyst to seriously affect catalytic reaction, so that the prior flue gas treatment process is difficult to ensure the denitration effect and causes the emission to reach the standard with great difficulty.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a waste incineration flue gas treatment method.
A waste incineration flue gas treatment method includes the steps that flue gas after waste incineration firstly enters a semi-dry reaction tower deacidification system for deacidification, flue gas after deacidification enters a denitration pretreatment device for pretreatment, flue gas after denitration pretreatment enters an SCR system for denitration treatment, the denitration pretreatment device comprises a cavity, a rotary magnetic pole and an adsorption bin, the adsorption bin is arranged in the cavity, magnetic induction lines of the rotary magnetic pole penetrate through the adsorption bin, a flue gas guide structure is arranged in the cavity in front of the adsorption bin and can guide the flue gas to form turbulent flow in the cavity, the flue gas after the turbulent flow is formed is adsorbed by the adsorption bin and then enters the denitration device, a plurality of interlayers are arranged in the adsorption bin, a plurality of partition bins are arranged in each interlayer, adsorption balls are arranged in each partition bin and can roll in each partition bin, a modified oxidized graphene layer is arranged on the surface of each adsorption ball, magnetic iron oxide is loaded on each modified oxidized graphene, adsorption efficiency is improved by controlling the roll of each adsorption ball through the rotary magnetic pole, a transverse plate type catalyst is arranged in the SCR system, and holes are formed in the surface of the transverse plate type catalyst.
Further, denitration is carried out in the incinerator before the smoke is discharged, urea with the concentration of 40% is sprayed into a hearth through compressed air, reduction reaction is carried out on oxynitride in the smoke, the oxynitride in the smoke is decomposed, an SNCR system is arranged in two layers in the boiler, 3 spray guns are respectively arranged on the left side wall and the right side wall of a first channel in each layer, the input temperature of the spray gun in the first layer is 880 ℃, and the exit temperature is 950 ℃; the input temperature of the spray gun at the second layer is 940 ℃, and the exit temperature is 1050 ℃.
Further, the denitration pretreatment device and the SCR reactor system are arranged behind the dust remover and the booster fan and before the induced draft fan, the temperature of the flue gas at the outlet of the booster fan is 140-150 ℃, the flue gas enters a GGH (flue gas/flue gas heat exchanger) before entering the SCR reactor, is heated to 200-210 ℃, and then enters an SGH (steam heater) for heating, so that the temperature of the flue gas reaches 230-260 ℃; the SCR denitration system adopts 40% concentration urea solution to prepare ammonia gas through a pyrolysis process, the ammonia gas is injected into a flue in front of an inlet of the SCR reactor through an ammonia injection grid, and the denitrated clean flue gas is extracted by an induced draft fan and then discharged to a chimney.
Furthermore, the inside of the adsorption ball is SiO 2 SiC or other light materials which do not react with the flue gas, and the modified graphene oxide is loaded on the surface of the adsorption ball by a powder metallurgy process.
Furthermore, the transverse plate type catalyst is of a split structure, 3-5 transverse plate type catalysts are a box body, a plurality of box bodies are arranged, two sides of a hole in the surface of each transverse plate type catalyst are horn-shaped, the speed of airflow in the hole can be increased through the horn-shaped arrangement, the hole and the surface of the catalyst are prevented from being blocked by ammonium bisulfate and ammonium bisulfite, and meanwhile, the surface area of the catalyst can be increased through the horn-shaped holes, so that the catalytic efficiency is improved.
Furthermore, the depth of the horn-shaped hole is 0.2-0.3mm, so that the surface area of SCR reaction is fully improved.
Furthermore, a filter screen is arranged between the adjacent box bodies, and holes of the filter screen and holes on the transverse plate type catalyst are arranged in a staggered mode.
Furthermore, the filter screen can roll, and the filter screen lower extreme sets up the scraper, can strike off the impurity of adhesion on the filter screen, and the filter screen after scraping can roll to next filter screen position.
Compared with the prior art, the application has the advantages that: in this application, combine SNCR and SCR, show to improve denitration efficiency, carry out the preliminary treatment to the flue gas before the SCR denitration, reduced the content that contains arsenic compound and calcium oxide in the flue gas, reduced the influence that contains arsenic compound to catalyst in the SCR system in the flue gas, show to improve denitration efficiency.
Specifically, 1, in the application, an SNCR system is arranged in an incinerator, denitration in the incinerator is carried out according to the temperature in the incinerator, the input temperature of a first layer of spray guns is 880 ℃, and the exit temperature is 950 ℃; the input temperature of the spray gun at the second layer is 940 ℃, the exit temperature is 1050 ℃, and high-efficiency denitration can be realized.
2. The deacidified flue gas is subjected to denitration pretreatment, the rotary magnetic poles and the adsorption balls formed specially are arranged, the rotary magnetic poles are used for driving the adsorption balls to roll in the adsorption process, the adsorption efficiency is obviously improved, arsenic-containing compounds and calcium oxide entering the flue gas of the denitration system are reduced, meanwhile, the pretreatment position is selected before the flue gas is heated, the solid content of the arsenic-containing compounds can be improved at a low temperature, the adsorption balls are fully utilized for adsorption, and the probability of catalyst poisoning in an SCR system is reduced.
3. Through the flue gas heating, heat cyclic utilization can be realized, the window temperature of SCR reaction is heated to the flue gas, and denitration efficiency is improved when cost is reduced.
4. The traditional honeycomb type or flat plate type SCR catalyst is improved into a horizontal flat plate type catalyst, the porosity of the traditional honeycomb type catalyst is high, but the accumulation of ammonium bisulfate and ammonium bisulfite is easily formed in small pore diameters, so that an adhesive covers the surface of the catalyst, the catalytic efficiency is seriously influenced, the whole catalyst needs to be frequently replaced, and the utilization rate of the catalyst is low. Adopt horizontal flat catalyst in this application, set up tubaeform hole on the dull and stereotyped surface, improve surface area on the one hand, improve catalyst reaction utilization rate, on the other hand sets up through tubaeform structure, can make the downthehole air velocity between the both sides loudspeaker accelerate, and the accumulations of adhesion thing can be avoided to the air current of acceleration to make the peripheral aperture in hole form the negative pressure, form the suction effect to the adhesion thing in the aperture.
5. The horizontal plate type catalyst is arranged to be of a split structure, 3-5 horizontal plate type catalysts are one box body, and a plurality of box bodies are arranged, so that the replacement flexibility of the catalyst can be improved, the problem that the catalyst is partially blocked and the whole catalyst needs to be replaced is solved, the use cost is reduced, and the utilization rate is improved.
6. According to the catalyst box, the filter screen is arranged between the horizontal flat-plate catalyst box bodies, and the holes of the filter screen and the holes on the horizontal flat-plate catalyst are arranged in a staggered manner, so that blown-out stickers can be collected, and the stickers are prevented from being attached to the surface of the catalyst of the next box body again; in addition, the filter screen is arranged to be capable of rolling, the scraper is arranged at the lower end of the filter screen, impurities adhered to the filter screen can be scraped, the scraped filter screen can roll to the position of the next filter screen, and the service efficiency of the filter screen is improved.
Drawings
FIG. 1 is a schematic view of the structure of a denitration pretreatment apparatus of the present invention
FIG. 2 is a schematic view of a structure of a horizontal plate type catalyst
Reference numerals: 1. cavity, 2, adsorption bin, 3, flue gas diversion structure, 4, rotary magnetic pole, 5, interlayer, 6, adsorption ball, 7, transverse plate type catalyst, 8, filter screen, 9, scraper
A method for treating waste incineration flue gas comprises the steps of enabling the flue gas after waste incineration to enter a semi-dry reaction tower deacidification system for deacidification, enabling the flue gas after deacidification to enter a denitration pretreatment device for pretreatment, enabling the flue gas after denitration pretreatment to enter an SCR system for denitration treatment, as shown in figure 1, the denitration pretreatment device comprises a cavity 1, the cavity 1 can be a cylinder or a cuboid, a rotary magnetic pole 4 and an adsorption bin 2, the adsorption bin 2 is arranged in the cavity 1, magnetic induction lines of the rotary magnetic pole 4 penetrate through the adsorption bin 2, a flue gas guide structure 4 is arranged in front of the adsorption bin 2 in the cavity 1, the flue gas guide structure can guide flue gas to form turbulent flow in the cavity, the flue gas after the turbulent flow is formed enters the denitration device after being adsorbed by the adsorption bin, as shown in fig. 1, the flue gas guiding structure is preferably a structure which is in arc transition from the middle upper part of the inlet of the cavity to the inner wall of the cavity and is in arc bending towards the center of the cavity when approaching the adsorption bin 2, the structure can guide most of the flue gas to enter the cavity after entering the cavity, airflow flowing to the middle is formed under the guide of the flue gas guide structure, the flow speed of the flue gas is reduced due to the alternate formation before entering the adsorption bin 2, the retention time of the flue gas in the adsorption bin 2 can be increased, a plurality of separation layers 5 are arranged in the adsorption bin 2, a plurality of compartments are arranged in the separation layers 5, adsorption balls 6 are arranged in the compartments, the adsorption balls 6 can roll in the compartments, holes with the diameter smaller than that of the adsorption balls 6 are arranged on the compartments, a modified graphene oxide layer is arranged on the surface of each adsorption ball 6, the modified graphene oxide is loaded with magnetic iron oxide, the adsorption efficiency is improved by controlling the rolling of the adsorption balls through the rotating magnetic poles, a transverse plate type catalyst is arranged in the SCR system, and holes are formed in the surface of the transverse plate type catalyst. Wherein, modified graphene oxide's preparation belongs to prior art, utilizes the iron oxide of load to improve the adsorption effect on magnetic iron oxide load on graphene oxide among the prior art usually to utilize magnetism to improve recovery efficiency, adopt the outer rotatory magnetic pole of cavity to realize the roll control to adsorbing the ball in this application, can realize adsorbing the controllable motion of ball, adsorb the roll of ball in the adsorption process and can improve adsorption efficiency, improve the utilization ratio that adsorbs the ball.
Preferably, as shown in fig. 1, the distribution mode of the compartments in the compartments 5 is non-uniform, the compartments on adjacent compartments 5 are complementarily densely distributed, for example, the compartments in the middle area on the first compartment 5 are dense, the compartments in the edge area are sparse, the apertures of the ventilation holes in the compartments in the dense compartment area are larger than the apertures of the sparse compartment area, the compartments in the middle area are sparse, and the compartments in the edge area are dense, so that the flue gas is preferentially concentrated in the dense compartment area when passing through the adsorption compartment 2, and the flue gas is more drained to the dense compartment area at the edge due to the large resistance of the sparse zone directly facing the dense compartment in front of the second compartment 5, and the subsequent compartments can be analogized, and such a design mode not only increases the residence time of the flue gas in the adsorption compartment 2, but also concentrates the area with large flue gas flow, and improves the adsorption efficiency.
Experiments show that the adsorption efficiency of arsenic compounds and calcium oxide in the flue gas can be obviously improved by adopting the rotary magnetic pole to control the adsorption balls to roll in the flue gas adsorption process at the rotating speed of 100-150 r/min. When the adsorption ball adopts SiO 2 The material is prepared by adopting a powder metallurgy process to obtain a hollow and porous structure with the particle size of 1mm, the content of the modified graphene oxide loaded on the surface and the inside of the hollow and porous structure is 0.4g, the interlayer 5 is arranged into 6 layers, when the weight ratio of the adsorption balls in the compartment dense area to the compartment sparse area in the interlayer 5 is 7, after adsorption is not adopted, the content of arsenic compounds in the flue gas is reduced by 60 percent and the content of calcium oxide is reduced by 50 percent, when the magnetic pole is adopted to perform rotary adsorption at 120r/min, the content of arsenic compounds in the flue gas is reduced by 66 percent and the content of calcium oxide is reduced by 53 percent, and thus the adsorption efficiency can be further improved by adopting the rotary magnetic pole.
In an optional embodiment, denitration is carried out in an incinerator before smoke is discharged, urea with the concentration of 40% is sprayed into a hearth through compressed air, reduction reaction is carried out on oxynitride in the smoke, the oxynitride in the smoke is decomposed, an SNCR system is arranged in a boiler in two layers, 3 spray guns are respectively arranged on the left side wall and the right side wall of a first channel in each layer, the input temperature of the spray gun in the first layer is 880 ℃, and the exit temperature is 950 ℃; the input temperature of the spray gun at the second layer is 940 ℃, and the exit temperature is 1050 ℃.
In an optional embodiment, the denitration pretreatment device and the SCR reactor system are arranged behind the dust remover and the booster fan and before the induced draft fan, the semi-dry type reaction tower deacidification system is arranged before the booster fan, the temperature of flue gas at the outlet of the booster fan is 140-150 ℃, the flue gas enters a GGH (flue gas/flue gas heat exchanger) before entering the SCR reactor, is heated to 200-210 ℃, and then enters an SGH (steam heater) for heating, so that the temperature of the flue gas reaches 230-260 ℃; the SCR denitration system adopts 40% concentration urea solution to prepare ammonia gas through a pyrolysis process, the ammonia gas is injected into a flue in front of an inlet of the SCR reactor through an ammonia injection grid, and the denitrated clean flue gas is extracted by an induced draft fan and then discharged to a chimney.
In an alternative embodiment, as shown in fig. 2, the horizontal plate catalyst 7 is a split structure, 3 to 5 horizontal plate catalysts 7 are a box, a plurality of boxes are provided, two sides of the hole on the surface of the horizontal plate catalyst 7 are horn-shaped, the interior of the hole is a porous structure, the horn-shaped arrangement can increase the speed of the airflow in the hole between the horns, prevent ammonium bisulfate and ammonium bisulfite from blocking the hole and the surface of the catalyst, and the horn-shaped hole can increase the surface area of the catalyst and increase the catalytic efficiency. In the application, the horizontal plate type catalyst base material is TiO 2 The active substance is V 2 O 5 The catalyst with conventional components can reduce cost, and the influence of ammonium bisulfate and ammonium bisulfite on the catalyst can be reduced through the improvement of a catalyst mechanism, so that the utilization rate of the catalyst is improved, and the service life of the catalyst is prolonged.
In an alternative embodiment, the depth of the flared holes is 0.2-0.3mm, substantially increasing the surface area of the SCR reaction.
In an optional embodiment, a filter screen 8 is arranged between adjacent box bodies, holes of the filter screen 8 are arranged in a staggered manner with holes on the transverse plate type catalyst, and a groove structure is arranged between the holes on the filter screen 8, so that sticky substances can be prevented from falling off from the filter screen 8 and entering the next catalyst box body.
In an alternative embodiment, the filter screen 8 may roll, and a scraper 9 may be disposed at a lower end of the filter screen 8, so as to scrape off impurities adhered to the filter screen 8, and the scraped filter screen 8 may roll to a next filter screen 8.
The service life of the catalyst with the same content can be doubled by the horn-shaped design of the transverse plate type catalyst and the filtering action of the filter screen 8 on the ammonium bisulfate and the ammonium bisulfite.
In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, but are not intended to indicate or imply that the device or element so referred to must have a particular orientation, be constructed in a particular orientation, and be operated in a particular manner, and are not to be construed as limiting the invention. Furthermore, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art. In the description of the present invention, reference to the description of "one embodiment", "some embodiments", "illustrative embodiments", "examples", "specific examples", or "some examples" or the like means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention.
In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. While embodiments of the invention have been shown and described, it will be understood by those of ordinary skill in the art that: various changes, modifications, substitutions and alterations can be made to the embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the claims and their equivalents.
Claims (8)
1. A method for treating waste incineration flue gas is characterized in that the denitration pretreatment device comprises a cavity, a rotary magnetic pole and an adsorption bin, the adsorption bin is arranged in the cavity, magnetic induction lines of the rotary magnetic pole penetrate through the adsorption bin, a flue gas guide structure is arranged in front of the adsorption bin in the cavity and can guide flue gas to form turbulent flow in the cavity, the flue gas after the turbulent flow is formed is adsorbed by the adsorption bin and then enters the denitration device, a plurality of interlayers are arranged in the adsorption bin, adsorption balls are arranged in the interlayers and can roll in the interlayers, a modified graphene oxide layer is arranged on the surfaces of the adsorption balls, the modified graphene oxide is loaded with magnetic iron oxides, the rolling of the adsorption balls is controlled through the rotary magnetic pole to improve the adsorption efficiency, a horizontal plate type catalyst is arranged in the SCR system, and holes are formed in the surface of the horizontal plate type catalyst.
2. The method for treating the waste incineration flue gas according to claim 1, wherein denitration is performed in the incinerator before the flue gas is discharged, 40% concentration urea is injected into a hearth through compressed air, reduction reaction is performed on oxynitride in the flue gas, the oxynitride in the flue gas is decomposed, an SNCR system is arranged in two layers in the boiler, 3 spray guns are respectively arranged on the left side wall and the right side wall of a first channel in each layer, the input temperature of the spray gun in the first layer is 880 ℃, and the exit temperature is 950 ℃; the input temperature of the spray gun at the second layer is 940 ℃, and the exit temperature is 1050 ℃.
3. The method for treating the flue gas generated by the incineration of the garbage according to claim 1, wherein the denitration pretreatment device and the SCR reactor system are arranged behind the dust remover and the booster fan and before the induced draft fan, the temperature of the flue gas at the outlet of the booster fan is 140-150 ℃, the flue gas enters a GGH (flue gas heat exchanger) before entering the SCR reactor, is heated to 200-210 ℃, and then enters an SGH (steam heater) for heating, so that the temperature of the flue gas reaches 230-260 ℃; the SCR denitration system adopts 40% concentration urea solution to prepare ammonia gas through a pyrolysis process, the ammonia gas is injected into a flue in front of an inlet of the SCR reactor through an ammonia injection grid, and the denitrated clean flue gas is extracted by an induced draft fan and then discharged to a chimney.
4. The method for treating waste incineration flue gas according to claim 1, wherein SiO is arranged inside the adsorption balls 2 Or SiC material, and loading the modified graphene oxide on the surface of the adsorption sphere through a powder metallurgy process.
5. The method for treating waste incineration flue gas according to claim 1, wherein the horizontal plate catalyst is a split structure, 3-5 horizontal plate catalysts are one box, a plurality of boxes are arranged, the two sides of the hole on the surface of the horizontal plate catalyst are horn-shaped, the horn-shaped arrangement can increase the speed of airflow in the hole, prevent ammonium bisulfate and ammonium bisulfite from blocking the hole and the surface of the catalyst, and the horn-shaped hole can increase the surface area of the catalyst and increase the catalytic efficiency.
6. The waste incineration flue gas treatment method according to claim 1, wherein the depth of the trumpet-shaped hole is 0.2-0.3mm.
7. The method according to claim 1, wherein a filter screen is disposed between adjacent boxes, and holes of the filter screen are staggered with holes of the horizontal plate catalyst.
8. The method according to claim 1, wherein the filter screen is rollable, a scraper is provided at a lower end of the filter screen, and the filter screen after the scraper is rolled to a next filter screen position.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211480747.2A CN115779628B (en) | 2022-11-23 | 2022-11-23 | Method for treating waste incineration flue gas |
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| CN115779628B (en) | 2023-07-04 |
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