CN220990289U - Industrial kiln flue gas denitrification device containing high concentration NOX - Google Patents
Industrial kiln flue gas denitrification device containing high concentration NOX Download PDFInfo
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- CN220990289U CN220990289U CN202322703549.4U CN202322703549U CN220990289U CN 220990289 U CN220990289 U CN 220990289U CN 202322703549 U CN202322703549 U CN 202322703549U CN 220990289 U CN220990289 U CN 220990289U
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 48
- 239000003546 flue gas Substances 0.000 title claims abstract description 48
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 66
- 239000003054 catalyst Substances 0.000 claims abstract description 48
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 21
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 6
- 238000002156 mixing Methods 0.000 claims abstract description 3
- 239000000428 dust Substances 0.000 claims description 15
- 239000002245 particle Substances 0.000 claims description 9
- 230000001105 regulatory effect Effects 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 5
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims description 3
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 3
- 239000004202 carbamide Substances 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims description 2
- 230000009977 dual effect Effects 0.000 claims 1
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 15
- 229910021529 ammonia Inorganic materials 0.000 abstract description 9
- 230000009849 deactivation Effects 0.000 abstract description 2
- 238000005245 sintering Methods 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 4
- 239000000919 ceramic Substances 0.000 description 4
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000012798 spherical particle Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The utility model relates to the field of flue gas treatment, and provides a flue gas denitration device for an industrial kiln containing high-concentration NO X, which comprises a mixer, a denitration reactor, a secondary heat exchanger, an induced draft fan and a desulfurizing tower which are sequentially connected, wherein the problems of catalyst sintering deactivation, large resistance of a multistage series reactor and large ammonia escape amount caused by temperature flying in high-concentration NO X flue gas treatment are solved; mixing the flue gas and the reducing agent in a mixer; the denitration reactor is of a radial cylinder structure, and comprises an inner cylinder, a middle cylinder catalyst layer and an outer cylinder from inside to outside in sequence; the hot air outlet end of the secondary heat exchanger is communicated with the inlet of the mixer through a first pipeline, a primary reducing agent feeder is arranged in the first pipeline, and the primary reducing agent feeder is communicated with a reducing agent supply device. The utility model can reduce resistance drop, reduce ammonia escape rate and prolong catalyst life while ensuring that the emission index of nitrogen oxides meets the requirements of related standards.
Description
Technical Field
The utility model relates to the field of flue gas treatment, in particular to a flue gas denitration device for an industrial kiln containing high-concentration NO X.
Background
Traditional flue gas denitration methods comprise SNCR denitration, biological calcium denitration, PNCR denitration and SCR denitration. The first three are only suitable for denitration under the working condition of high temperature combustion, and the denitration efficiency is low, the economy is poor and the secondary pollution is serious. When the SCR denitration technology of honeycomb, plate-type, ripple and other catalysts is adopted to treat high-concentration NO X, the multistage reactors are required to be connected in series, so that the denitration system has the defects of large resistance reduction, serious ammonia escape, short service life of the catalyst caused by the temperature runaway caused by reaction heat and the like, and meanwhile, the problems of corrosion and blockage of subsequent equipment, difficulty in treating subsequent desulfurization ammonia nitrogen-containing wastewater and the like are also caused.
Patent CN208626983U discloses a high concentration nitrogen oxide flue gas denitration system, which comprises a draught fan, a liquid oxidation liquid storage tank, an ozone generating device, an absorption tower and a flue gas inlet; the flue gas inlet is communicated with a boiler tail gas discharge port, the flue gas inlet is provided with an induced draft fan, and the tail end of the induced draft fan is connected with a primary oxidation device; the tail end of the preliminary oxidation device is communicated with a plasma flue gas purification device, the tail end of the plasma flue gas purification device is communicated with an ozone injection device, and the tail end of the ozone injection device is communicated with the absorption tower through a flue gas pipeline. The utility model controls the content of nitrogen oxides in the flue gas to be below 50mg/Nm 3, has NO NO 2 emission and NO nitrite generation, avoids secondary pollution, has lower operation cost, and is favorable for popularization and application of ultralow emission. But the absorption tower adopts a spraying device to absorb N 2O5, and the absorption efficiency is limited. There is a need for an ideal solution.
Disclosure of Invention
The utility model provides a flue gas denitration device for an industrial kiln containing high-concentration NO X, which aims to solve the problems of catalyst sintering deactivation, large resistance reduction of multistage serial reactors and large ammonia escape caused by temperature flying in high-concentration NO X flue gas treatment, and achieves the aims of reducing resistance reduction, reducing ammonia escape rate and prolonging the service life of a catalyst while ensuring that emission indexes of nitrogen oxides meet the requirements of relevant standards.
In order to achieve the above purpose, the present utility model adopts the following technical scheme:
A flue gas denitration device for an industrial kiln containing high-concentration NO X comprises a mixer, a denitration reactor, a secondary heat exchanger, an induced draft fan and a desulfurizing tower which are connected in sequence; mixing the flue gas and the reducing agent in a mixer; the denitration reactor is of a radial cylinder structure, and comprises an inner cylinder, a middle cylinder catalyst layer and an outer cylinder from inside to outside in sequence; the hot air outlet end of the secondary heat exchanger is communicated with the inlet of the mixer through a first pipeline, a primary reducing agent feeder is arranged in the first pipeline, and the primary reducing agent feeder is communicated with a reducing agent supply device.
Preferably, the denitration reactor is a two-stage serial reactor, the first-stage denitration reactor and the two-stage denitration reactor are integrally connected in series, the first-stage denitration reactor comprises a first-stage denitration reactor center inner cylinder, a first-stage denitration reactor middle cylinder catalyst layer and a first-stage denitration reactor outer cylinder from inside to outside in sequence, the first-stage denitration reactor center inner cylinder is communicated with the mixer, and flue gas enters from the first-stage denitration reactor center inner cylinder, passes through the first-stage denitration reactor middle cylinder catalyst layer and enters into the first-stage denitration reactor outer cylinder after undergoing denitration reaction; the secondary denitration reactor is sequentially provided with a secondary denitration reactor center inner cylinder, a secondary denitration reactor middle cylinder catalyst layer and a secondary denitration reactor outer cylinder from inside to outside, wherein the secondary denitration reactor center outer cylinder is communicated with the primary denitration reactor outer cylinder, flue gas enters from the secondary denitration reactor outer cylinder, passes through the secondary denitration reactor middle cylinder catalyst layer, enters the secondary denitration reactor center inner cylinder after undergoing denitration reaction, and the secondary denitration reactor center inner cylinder is communicated with an inlet of the secondary heat exchanger.
Preferably, a primary heat exchanger is arranged between the primary denitration reactor and the secondary denitration reactor, the outer cylinder of the primary denitration reactor is communicated with the inlet of the primary heat exchanger, and the outlet of the primary heat exchanger is communicated with the outer cylinder of the secondary denitration reactor. The primary heat exchanger removes the denitration reaction heat, prevents the temperature of the flue gas from flying, and ensures that the temperature of the flue gas entering the secondary denitration reactor is within an allowable range.
Preferably, the central outer cylinder of the secondary denitration reactor is communicated with the outlet of the primary heat exchanger through an inlet flue of the secondary denitration reactor, a secondary reducing agent feeder is arranged on the inlet flue of the secondary denitration reactor, and the secondary reducing agent feeder is communicated with the reducing agent supply equipment.
Preferably, the primary reducing agent feeder is communicated with the reducing agent supply equipment through a third pipeline, and a primary reducing agent regulating valve and a primary reducing agent flowmeter are arranged on the third pipeline; and/or; the secondary reducing agent feeder is communicated with the reducing agent supply equipment through a fourth pipeline, and a secondary reducing agent regulating valve and a secondary reducing agent flowmeter are arranged on the fourth pipeline.
Preferably, the reducing agent feeder is a double-flow atomizing spray gun or a multi-nozzle grid; and/or; the reducing agent is gaseous ammonia, aqueous ammonia solution or urea solution.
Preferably, the catalyst is in the form of cylindrical particles, clover-like particles or spherical particles. More preferably, the catalyst is in the form of cylindrical particles of phi (3-6) mm (5-12), and still more preferably, phi (4-5) mm (5-7). Preferably, the catalyst is a medium-low temperature catalyst at 180-280 ℃ or a high-medium temperature catalyst at 300-420 ℃.
Preferably, the catalyst bed thickness of each reactor is 300-1200 mm, the flue gas flow rate is 0.20-0.50 m/s, the resistance of the catalyst bed layer of the single reactor is reduced to be less than or equal to 1500Pa, and more preferably, the resistance of the catalyst bed layer of the single reactor is reduced to be less than or equal to 900Pa.
Preferably, the secondary heat exchanger is connected with the air blower, a branch second pipeline is arranged on the first pipeline, the second pipeline is communicated with the hot blast stove, and the hot blast stove consists of a body, a combustor and a combustion-supporting blower. The hot blast stove can be selectively configured according to the working condition.
Preferably, the flue gas is located in an industrial kiln, and the industrial kiln is connected with the dust collector and the mixer in sequence. As a further preferred, the dust collector is a ceramic filter, a metal filter, a filter bag filter or an electric dust collector, and a ceramic filter dust collector is further preferred. The components, temperature and humidity of the flue gas determine whether to arrange the dust collector and what type of dust collector is selected.
Therefore, the utility model has the beneficial effects that: the SCR denitration reactor adopting the traditional honeycomb type, plate type and corrugated type catalysts has the advantages that the system resistance is reduced (the design resistance of a 4-layer single-stage reactor is reduced by 1000pa, the running resistance is reduced by 1300-1500 pa), and the ammonia escape concentration is as high as (15-45 ppm); the utility model adopts the particle catalyst and the radial structure reactor, the design resistance of the single-stage reactor is reduced by 300-600 pa, and the running resistance is reduced by 500-900 pa; the flue gas distribution on the surface of the catalyst is more uniform, the flow rate of the catalyst passing through the catalyst layer is low (0.2-0.35 m/s), and the ammonia escape concentration is low (3-6 ppm). The purposes of reducing resistance drop, reducing ammonia escape rate, prolonging the service life of the catalyst and the like are achieved while the emission index of the nitrogen oxides meets the requirements of related standards.
Drawings
FIG. 1 is a schematic diagram of a flue gas denitration device for a high-concentration NO X industrial kiln.
In the figure: 1. the industrial kiln, 2, the dust collector, 3, the mixer, 4, the first-stage denitration reactor inlet flue, 5, the first-stage denitration reactor, 5-1, the first-stage denitration reactor urceolus, 5-2, the first-stage denitration reactor middle barrel catalyst layer, 5-3, the first-stage denitration reactor inner tube, 6, the second-stage denitration reactor outlet flue, 7, the second-stage heat exchanger, 8, the draught fan, 9, the desulfurizing tower, 10, the air blower, 11, first pipeline, 12, the second pipeline, 12-1 hot blast furnace, 12-1a, the combustor, 12-1b, the combustion-supporting fan, 12-1c, the body, 13, the third pipeline, 13-1, the first-stage reducing agent governing valve, 13-2, the first-stage reducing agent flowmeter, 13-3, the first-stage reducing agent feeder, 14, the fourth pipeline, 14-1, the second-stage reducing agent governing valve, 14-2, the second-stage reducing agent flowmeter, 14-3, the second-stage reducing agent feeder, 15, the reducing agent supply equipment, 15-1, the reducing agent delivery pump, 16, the first-stage denitration reactor, 17, the second-stage denitration reactor inlet, 19, the second-stage denitration reactor, the second-stage reactor inlet, 19-1, the second-stage denitration reactor 19, the second-stage reactor 19, the first-stage denitration reactor 19, the second-stage reactor 19.
Detailed Description
The utility model is further described below with reference to the drawings and detailed description.
As shown in figure 1, the high-concentration NO X industrial kiln flue gas denitration device comprises an industrial kiln 1, a mixer 3, a denitration reactor, a secondary heat exchanger 7, an induced draft fan 8 and a desulfurizing tower 9 which are connected in sequence.
The denitration reactor is a two-stage serial reactor, and the first-stage denitration reactor 5 and the second-stage denitration reactor 19 are both radial cylinder structures and are integrally connected in series. The primary denitration reactor 5 is sequentially provided with a primary denitration reactor center inner cylinder 5-3, a primary denitration reactor middle cylinder catalyst layer 5-2 and a primary denitration reactor outer cylinder 5-1 from inside to outside, and the primary denitration reactor center inner cylinder 5-3 is communicated with the mixer 3 through a primary denitration reactor inlet flue 4; the secondary denitration reactor 19 is sequentially provided with a secondary denitration reactor center inner cylinder 19-3, a secondary denitration reactor middle cylinder catalyst layer 19-2 and a secondary denitration reactor outer cylinder 19-1 from inside to outside, and the secondary denitration reactor center inner cylinder is communicated with the inlet of the secondary heat exchanger. A primary heat exchanger 17 is arranged between the primary denitration reactor 5 and the secondary denitration reactor 19, the primary heat exchanger 17 is provided with a cooling water inlet 17-1 and a water outlet 18-2, the outer cylinder 5-1 of the primary denitration reactor is communicated with the inlet of the primary heat exchanger 17 through a primary denitration reactor outlet flue 16, and the outlet of the primary heat exchanger 17 is communicated with the outer cylinder 19-1 of the secondary denitration reactor through a secondary denitration reactor inlet flue 18.
The hot air outlet end of the secondary heat exchanger 7 communicates with the inlet of the mixer 3 via a first conduit 11. The apparatus further comprises a reducing agent supply device 15, the reducing agent feeder being a dual-flow atomizing spray gun or a multi-nozzle grid, the reducing agent being gaseous ammonia, an aqueous ammonia solution or a urea solution. The reducing agent supply device 15 is connected with the reducing agent delivery pump 15-1, the reducing agent delivery pump 15-1 is respectively connected with the third pipeline 13 and the fourth pipeline 14, a first-stage reducing agent regulating valve 13-1, a first-stage reducing agent flowmeter 13-2 and a first-stage reducing agent feeder 13-3 are sequentially arranged on the third pipeline 13, and the first-stage reducing agent feeder 13-3 is arranged in the first pipeline 11; the fourth pipeline 14 is sequentially connected with a secondary reducing agent regulating valve 14-1, a secondary reducing agent flowmeter 14-2 and a secondary reducing agent feeder 14-3, and the secondary reducing agent feeder 14-3 is arranged in the inlet flue 18 of the secondary denitration reactor.
Preferably, the catalyst is in the form of cylindrical particles, clover-like particles or spherical particles. Further preferably, the catalyst is in a cylindrical particle shape with a diameter of phi (3-6) mm (5-12), and in this embodiment, a cylindrical particle shape with a diameter of phi (4-5) mm (5-7) mm is selected. Preferably, the catalyst is a medium-low temperature catalyst at 180-280 ℃ or a high-medium temperature catalyst at 300-420 ℃. The catalyst bed thickness of each stage of the reactor is 300-1200 mm, the flue gas flow rate is 0.20-0.50 m/s, the resistance of the catalyst bed of the single reactor is reduced by less than or equal to 1500Pa, and the single reactor catalyst with the resistance of the catalyst bed reduced by less than or equal to 900Pa is selected in the embodiment.
Preferably, a dust collector 2 is arranged between the industrial kiln 1 and the mixer 3. The smoke composition, temperature and humidity determine whether to arrange the dust collector or not, and what type of dust collector is selected, such as ceramic filter, metal filter, filter bag filter or electric dust collector. The embodiment adopts a ceramic filter dust collector.
Preferably, the secondary heat exchanger 7 is connected with the air blower 10, the first pipeline 11 is provided with a branch, namely a second pipeline 12, the second pipeline 12 is communicated with the hot blast stove 12-1, and the hot blast stove 12-1 consists of a body 12-1c, a burner 12-1a and a combustion-supporting blower 12-1 b. And the hot blast stove is selected according to the working condition requirement to be configured or not.
When the device is operated, raw flue gas with high concentration NO X flows from the industrial kiln 1 to the dust remover 2 for dust removal and cleaning, reducing agent is added into the raw flue gas through the primary reducing agent feeder 13-3, and the raw flue gas flows to the denitration reactor after being mixed with the reducing agent in the mixer 3, specifically: raw flue gas containing reducing agent enters from the central inner cylinder 5-3 of the primary denitration reactor, NO 2 and NH 3 in the flue gas undergo chemical reaction in the middle cylinder catalyst layer 5-2 of the primary denitration reactor to be reduced into N 2 and H 2 O, the flue gas after denitration enters the primary heat exchanger 17 through the outer cylinder 5-1 of the primary denitration reactor and the outlet flue 16 of the primary denitration reactor, the denitration reaction heat is removed, the flue gas temperature is prevented from flying, and the flue gas temperature entering the secondary denitration reactor is in an allowable range. The outlet of the primary heat exchanger 17 is connected with the inlet flue 18 of the secondary denitration reactor, a denitration reducing agent is added into the inlet flue 18 of the secondary denitration reactor through the secondary reducing agent feeder 14-3, then the flue enters the secondary denitration reactor 19, mixed flue gas containing the reducing agent enters from the outer cylinder 19-1 of the secondary denitration reactor, when the flue gas passes through the middle cylinder catalyst layer 19-2 of the secondary denitration reactor, NO and NO 2 in the flue gas react with NH 3 and are reduced into N 2 and H 2 O, the flue gas after denitration is discharged from the inner cylinder 19-3 of the secondary denitration reactor, and the flue gas is connected with the secondary heat exchanger 7 through the outlet flue 6 of the second reactor; the outlet of the secondary heat exchanger 7 is connected with the inlet of the induced draft fan 8; the outlet of the induced draft fan 8 is connected with the inlet of the desulfurizing tower 9, and is discharged into the atmosphere through desulfurization treatment.
The above embodiments are merely illustrative embodiments of the present utility model, but the technical features of the present utility model are not limited thereto, and any changes or modifications made by those skilled in the art within the scope of the present utility model are included in the scope of the present utility model.
Claims (10)
1. The industrial kiln flue gas denitration device containing high-concentration NO X is characterized by comprising a mixer, a denitration reactor, a secondary heat exchanger, an induced draft fan and a desulfurizing tower which are connected in sequence; mixing the flue gas and the reducing agent in a mixer; the denitration reactor is of a radial cylinder structure, and comprises an inner cylinder, a middle cylinder catalyst layer and an outer cylinder from inside to outside in sequence; the hot air outlet end of the secondary heat exchanger is communicated with the inlet of the mixer through a first pipeline, a primary reducing agent feeder is arranged in the first pipeline, and the primary reducing agent feeder is communicated with a reducing agent supply device.
2. The device according to claim 1, wherein the denitration reactor is a two-stage series reactor, the first-stage denitration reactor is integrally connected with the two-stage denitration reactor in series, the first-stage denitration reactor is sequentially a first-stage denitration reactor center inner cylinder, a first-stage denitration reactor middle cylinder catalyst layer and a first-stage denitration reactor outer cylinder from inside to outside, and the first-stage denitration reactor center inner cylinder is communicated with the mixer; the secondary denitration reactor is sequentially provided with a secondary denitration reactor center inner cylinder, a secondary denitration reactor middle cylinder catalyst layer and a secondary denitration reactor outer cylinder from inside to outside, wherein the secondary denitration reactor center outer cylinder is communicated with the primary denitration reactor outer cylinder, and the secondary denitration reactor center inner cylinder is communicated with an inlet of the secondary heat exchanger.
3. The device according to claim 2, wherein a primary heat exchanger is arranged between the primary denitration reactor and the secondary denitration reactor, the outer cylinder of the primary denitration reactor is communicated with the inlet of the primary heat exchanger, and the outlet of the primary heat exchanger is communicated with the outer cylinder of the secondary denitration reactor.
4. The device according to claim 2, wherein the central outer cylinder of the secondary denitration reactor is communicated with the outlet of the primary heat exchanger through an inlet flue of the secondary denitration reactor, and a secondary reducing agent feeder is arranged on the inlet flue of the secondary denitration reactor and is communicated with the reducing agent supply equipment.
5. The device according to claim 4, wherein the primary reducing agent feeder is communicated with the reducing agent supply equipment through a third pipeline, and a primary reducing agent regulating valve and a primary reducing agent flowmeter are arranged on the third pipeline; and/or; the secondary reducing agent feeder is communicated with the reducing agent supply equipment through a fourth pipeline, and a secondary reducing agent regulating valve and a secondary reducing agent flowmeter are arranged on the fourth pipeline.
6. The apparatus of claim 1, wherein the reductant feeder is a dual stream atomizing spray gun or a multi-nozzle grid; and/or; the reducing agent is gaseous ammonia, aqueous ammonia solution or urea solution.
7. The device according to claim 1, wherein the catalyst is in the form of cylindrical particles of Φ (3-6) mm x (5-12); and/or; the catalyst is a medium-low temperature catalyst at 180-280 ℃ or a high-medium temperature catalyst at 300-420 ℃.
8. The apparatus of claim 1 or 7, wherein each stage of the reactor catalyst bed is 300-1200 mm a thick.
9. The device according to claim 1, wherein the secondary heat exchanger is connected with an air blower, a branch second pipeline is arranged on the first pipeline, the second pipeline is communicated with a hot blast stove, and the hot blast stove consists of a body, a combustor and a combustion fan.
10. The apparatus according to claim 1 or 9, wherein the flue gas is located in an industrial kiln, which is connected in turn with a dust collector and the mixer.
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| CN202322703549.4U CN220990289U (en) | 2023-10-10 | 2023-10-10 | Industrial kiln flue gas denitrification device containing high concentration NOX |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322703549.4U CN220990289U (en) | 2023-10-10 | 2023-10-10 | Industrial kiln flue gas denitrification device containing high concentration NOX |
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| CN220990289U true CN220990289U (en) | 2024-05-24 |
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| CN202322703549.4U Active CN220990289U (en) | 2023-10-10 | 2023-10-10 | Industrial kiln flue gas denitrification device containing high concentration NOX |
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