CN219663369U - SCR denitration system coupling urea hydrolysis - Google Patents
SCR denitration system coupling urea hydrolysis Download PDFInfo
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- CN219663369U CN219663369U CN202320629756.7U CN202320629756U CN219663369U CN 219663369 U CN219663369 U CN 219663369U CN 202320629756 U CN202320629756 U CN 202320629756U CN 219663369 U CN219663369 U CN 219663369U
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- flue gas
- scr denitration
- heat exchanger
- ammonia
- dust
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- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 title claims abstract description 35
- 239000004202 carbamide Substances 0.000 title claims abstract description 35
- 230000007062 hydrolysis Effects 0.000 title claims abstract description 20
- 238000006460 hydrolysis reaction Methods 0.000 title claims abstract description 20
- 230000008878 coupling Effects 0.000 title description 3
- 238000010168 coupling process Methods 0.000 title description 3
- 238000005859 coupling reaction Methods 0.000 title description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 94
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 71
- 239000003546 flue gas Substances 0.000 claims abstract description 71
- 239000000428 dust Substances 0.000 claims abstract description 65
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 42
- 238000002347 injection Methods 0.000 claims abstract description 12
- 239000007924 injection Substances 0.000 claims abstract description 12
- 230000001105 regulatory effect Effects 0.000 claims abstract description 10
- 239000003500 flue dust Substances 0.000 claims abstract description 4
- 238000010790 dilution Methods 0.000 claims description 27
- 239000012895 dilution Substances 0.000 claims description 27
- 238000007664 blowing Methods 0.000 claims description 10
- 238000005507 spraying Methods 0.000 claims description 9
- 239000000779 smoke Substances 0.000 abstract description 20
- 230000000694 effects Effects 0.000 abstract description 16
- 239000000203 mixture Substances 0.000 abstract description 8
- 238000005299 abrasion Methods 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 239000002918 waste heat Substances 0.000 abstract description 3
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 230000009467 reduction Effects 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 10
- 239000007789 gas Substances 0.000 description 6
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 108700018263 Brassica oleracea SCR Proteins 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model relates to the technical field of flue gas SCR denitration, in particular to an SCR denitration system coupled with urea hydrolysis, which comprises a heat exchanger, an ammonia air mixer, a urea hydrolyzer, an ammonia injection grid and an SCR denitration reactor, wherein the heat exchanger, the ammonia air mixer, the ammonia injection grid and the SCR denitration reactor are sequentially communicated, and the urea hydrolyzer is communicated with the ammonia air mixer; the flue gas inlet pipeline of the heat exchanger is internally provided with a flue dust filter screen, and the flue gas inlet pipeline of the heat exchanger is provided with a flow regulating valve and a temperature sensor. The system not only recycles the waste heat of the flue gas and avoids the abrasion of the smoke and dust mixture in the high-temperature flue gas to equipment, but also can realize energy conservation and consumption reduction, and can intelligently regulate and control the dust removal effect and the heat exchange effect.
Description
Technical Field
The utility model relates to the technical field of flue gas SCR denitration, in particular to an SCR denitration system coupled with urea hydrolysis.
Background
SCR flue gas denitration technology, ammonia or urea is used as a denitration agent to be sprayed into a high-temperature flue gas denitration system, and NO in flue gas is treated by a catalyst x Decomposition into N 2 And H 2 O, thus achieve the purpose of purifying the flue gas, the reaction is best under the action of catalyst when the flue gas temperature is 300-400 ℃, the system is stable in operation, the denitration efficiency can reach more than 90%, no wastewater is discharged, and the method has strong advantages.
In order to reduce the risk of liquid ammonia in the transportation and storage process as an SCR denitration reducing agent, more and more urban power plant SCR denitration systems adopt urea pyrolysis or hydrolysis technology to prepare ammonia required in SCR denitration reaction.
At present, the existing urea hydrolysis system is that 40% -60% urea solution enters a hydrolysis reactor through a urea solution delivery pump and the like, steam is utilized to carry out heating hydrolysis on the urea solution, ammonia gas, carbon dioxide and water vapor generated after urea hydrolysis are mixed with dilution air to the volume ratio of ammonia gas of 5% at the temperature of 120-150 ℃, and the volume ratio of dilution air is large, so that the temperature of the mixed urea solution is close to the temperature of dilution air. If the temperature is low, crystallization occurs, resulting in a decrease in the amount of ammonia injected, and in severe cases, the pipe is clogged.
To above-mentioned problem, select among the prior art to set up the heat exchanger in the flue, with the flue gas with the air heating to the temperature of needs, although it has practiced thrift the energy, because of the heat transfer area is in the flue, overhaul difficulty to unable temperature interval of adjusting, once the host computer load changes, flue gas temperature changes, also can change to the heat transfer of air. In addition, the high-temperature flue gas used for heat exchange is a mixture of gas and smoke dust, so that heat exchange facilities are easy to be blocked, the heat exchange effect is easy to be influenced, and equipment abrasion is easy to be caused by frequent dust flushing, so that the period of main functions of the equipment is shortened.
In view of this, the utility model proposes a novel SCR denitration system coupled with urea hydrolysis.
Disclosure of Invention
The utility model aims to provide an SCR denitration system coupled with urea hydrolysis, which not only recycles the waste heat of flue gas and avoids the abrasion of a smoke and dust mixture in high-temperature flue gas to equipment, but also can intelligently regulate and control the dust removal effect and the heat exchange effect, thereby saving energy and reducing consumption.
The utility model provides an SCR denitration system coupled with urea hydrolysis, which comprises a heat exchanger, an ammonia-air mixer, a urea hydrolyzer, an ammonia-spraying grid and an SCR denitration reactor,
the heat exchanger, the ammonia air mixer, the ammonia spraying grid and the SCR denitration reactor are sequentially communicated, and the urea hydrolyzer is communicated with the ammonia air mixer;
the flue gas inlet pipeline of the heat exchanger is internally provided with a flue dust filter screen, and the flue gas inlet pipeline of the heat exchanger is provided with a flow regulating valve and a temperature sensor.
As the preferable technical scheme, the device also comprises a dust remover, wherein the dust remover is communicated with the heat exchanger, and flow sensors are arranged on a pipeline of a dust remover flue gas inlet and a pipeline of the dust remover communicated with the heat exchanger.
As the technical proposal, preferably, the dust collector is internally provided with a dust collecting hopper, a filter bag and a dust blowing pipe in sequence along the flow direction of the flue gas,
wherein the filter bag is fixedly arranged in the dust remover, the outlet of the filter bag is arranged opposite to the air nozzle of the ash blowing pipe, the ash collecting hopper is arranged at the bottom of the dust remover in a conical structure.
As the outside of this technical scheme preferably, the dust remover is provided with compressed air package, compressed air package's one end is through air compressor machine and dust remover flue gas outlet pipeline intercommunication, the other end with the blowing pipe intercommunication, just be provided with the solenoid valve on the compressed air package.
As the technical scheme, preferably, the heat exchanger is internally provided with a plurality of heat exchange tubes in a spiral manner, and the inner side wall of the heat exchanger is provided with a plurality of first baffle plates in a staggered manner.
As the technical scheme, preferably, two opposite surfaces of the heat exchanger which are communicated are respectively provided with a flue gas inlet chamber and a flue gas outlet chamber, and two side walls adjacent to the two opposite surfaces of the heat exchanger which are communicated are respectively provided with a dilution air inlet chamber and a dilution air outlet chamber which are communicated with the heat exchange tube.
Preferably, in the technical scheme, a temperature sensor and a flow regulating valve are arranged on a pipeline for communicating the dilution air outlet chamber with the ammonia air mixer.
Preferably, in this technical scheme, a plurality of second baffle plates are staggered on the inner side wall of the ammonia air mixer.
As the preferred mode of this technical scheme, ammonia injection grid with the flue gas pipeline intercommunication of SCR denitration reactor front end, and flue gas pipeline is close to be provided with a plurality of third baffle that turn over on the inside wall of ammonia injection grid department crisscross.
Compared with the prior art, the SCR denitration system coupled with urea hydrolysis has at least the following technical effects:
the SCR denitration system for coupling urea hydrolysis comprises a heat exchanger, an ammonia-air mixer, a urea hydrolyzer, an ammonia spraying grid and an SCR denitration reactor, wherein a smoke dust filter screen arranged at a smoke gas inlet pipeline of the heat exchanger can primarily filter out smoke dust mixtures in smoke gas tail gas of a power plant so as to prevent impurities in high-temperature smoke gas from blocking the heat exchanger and affecting heat exchange effect, and simultaneously can reduce abrasion of dust on equipment such as the heat exchanger, the ammonia-air mixer, the ammonia spraying grid and the SCR denitration reactor, and improve the running period of the equipment; the diluted air is heated to 160-180 ℃ by a heat exchanger, mixed with ammonia generated by a urea hydrolyzer, and sprayed into an SCR denitration reactor through an ammonia spraying grid after reaching 150 ℃, so that the problem of urea hydrolysis and crystallization is avoided, and the energy consumption is saved. Therefore, the system not only recycles the waste heat of the flue gas and avoids the abrasion of the smoke and dust mixture in the high-temperature flue gas to equipment, but also can realize energy conservation and consumption reduction, and can intelligently regulate and control the dust removal effect and the heat exchange effect.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are needed in the description of the embodiments or the prior art will be briefly described, and it is obvious that the drawings in the description below are some embodiments of the present utility model, and other drawings can be obtained according to the drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of an SCR denitration system coupled with urea hydrolysis according to the present utility model;
fig. 2 is a schematic diagram of an SCR denitration reactor in an SCR denitration system coupled with urea hydrolysis according to the present utility model.
Reference numerals illustrate:
1: a dust remover; 2: a heat exchanger; 3: an ammonia-air mixer; 4: a urea hydrolyzer; 5: an ammonia spraying grid; 6: an SCR denitration reactor; 7: a flow sensor; 8: a flow regulating valve; 9: a temperature sensor; 10: an ash collecting hopper; 11: a filter bag; 12: a lance tube; 13: a compressed air bag; 14: a smoke dust filter screen; 15: a heat exchange tube; 16: a first baffle; 17: a flue gas inlet chamber; 18: a flue gas outlet chamber; 19: a dilution wind inlet chamber; 20: a dilution air outlet chamber; 21: a second baffle; 22: and a third baffle.
Detailed Description
The technical solutions of the present utility model will be clearly and completely described in connection with the embodiments, and it is apparent that the described embodiments are some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
In the description of the present utility model, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present utility model and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more of the described features. In the description of the present utility model, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. Furthermore, the terms "mounted," "connected," "coupled," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.
As shown in fig. 1-2, the embodiment provides an SCR denitration system coupled with urea hydrolysis, which comprises a heat exchanger 2, an ammonia air mixer 3, a urea hydrolyzer 4, an ammonia injection grid 5 and an SCR denitration reactor 6, wherein the heat exchanger 2, the ammonia air mixer 3, the ammonia injection grid 5 and the SCR denitration reactor 6 are sequentially communicated, and the urea hydrolyzer 4 is communicated with the ammonia air mixer 3; the flue gas inlet pipeline of the heat exchanger 2 is internally provided with a flue dust filter screen 14, and the flue gas inlet pipeline of the heat exchanger 2 is provided with a flow regulating valve 8 and a temperature sensor 9.
The smoke filter screen 14 arranged in the smoke inlet pipeline of the heat exchanger can primarily filter out smoke and dust mixtures in the smoke and tail gas of the power plant so as to prevent impurities in high-temperature smoke from blocking the heat exchanger 2 and affecting the heat exchange effect, meanwhile, the abrasion of dust to equipment such as the heat exchanger 2, the ammonia air mixer 3, the ammonia injection grid 5, the SCR denitration reactor 6 and the like can be reduced, the running period of the equipment is prolonged, in addition, the heat exchanger 2 is arranged outside a flue, the overhaul is convenient, the temperature of dilution air after heat exchange can be adjusted, the operation is more flexible, the flow of the high-temperature smoke can be adjusted through the flow adjusting valve 8 arranged at the front end of the heat exchanger 2 during use, the heat exchange effect of dilution air is controlled, and intelligent regulation and control are realized; the diluted wind is heated to 160-180 ℃ by the heat exchanger 2, mixed with ammonia generated by the urea hydrolyzer 4, and sprayed into the SCR denitration reactor 6 by the ammonia spraying grid 5 after reaching 150 ℃, so that the problem of urea hydrolysis and crystallization is avoided, and the energy consumption is saved.
In addition, in order to further improve the dust removal effect, can also set up dust remover 1 in the front end of heat exchanger 2 to, on the pipeline of dust remover 1 flue gas entry, on the pipeline that dust remover and heat exchanger 2 communicate all be provided with flow sensor 7, but the data real-time supervision dust removal efficiency of dust remover 1 through flow sensor 7 detects to in time wash dust remover 1, prevent high-load operation.
On the basis of the above technical scheme, further, along the direction of flue gas flow, the inside of dust remover 1 has set gradually album ash bucket 10, filter bag 11 and blowing pipe 12, wherein, filter bag 11 is fixed to be set up the inside of dust remover 1, just the export of filter bag 11 with the jet of blowing pipe 12 sets up relatively, album ash bucket 10 is the toper structure setting and is in the bottom of dust remover 1.
The high-temperature flue gas enters the interior of the dust remover 1 from the flue gas inlet of the dust remover 1, flows out from the flue gas outlet of the dust remover 1 after being filtered by the filter bag 11, and the flue gas mixture filtered by the filter bag 11 can fall into the dust collecting hopper 10. In actual operation, the flow of the flue gas at the flue gas inlet pipeline and the flue gas outlet pipeline of the dust remover 1 can be monitored in real time, the filtering efficiency of the filter bag 11 is judged, and when the flow of the flue gas at the flue gas outlet pipeline of the dust remover 1 is lower, the filter bag 11 can be blown through the ash blowing pipe 12 so as to remove the dust mixture adhered to the outer surface of the filter bag 11.
In this embodiment, the outside of dust remover 1 still is provided with compressed air package 13, and, compressed air package 13's one end is through air compressor machine and dust remover 1 flue gas outlet pipeline intercommunication, the other end with blow down pipe 12 intercommunication, just be provided with the solenoid valve on the compressed air package 13, blow down pipe 12 can utilize the high temperature flue gas after dust remover 1 purification treatment in real time promptly, and on the one hand high temperature flue gas can effectively avoid the low temperature to lead to filter bag 11 corruption or hardening, has improved filter bag 11's life, on the other hand, has reduced the energy consumption of air supply heating, has improved unit operating efficiency.
When the dust remover is used, the high-temperature purified smoke discharged from the smoke outlet of the dust remover 1 is compressed through the air compressor and is reserved in the compressed air bag 13, and the compressed high-temperature purified smoke is sprayed out through the electromagnetic valve, so that dust adhered to the surface of the filter bag 11 is removed.
On the basis of the above technical solution, it is further preferable that the heat exchanger 2 is internally provided with a plurality of heat exchange tubes 15 in a spiral manner, and the inner side wall of the heat exchanger 2 is provided with a plurality of first baffle plates 16 in a staggered manner.
The heat exchange tube 15 is internally provided with cold source dilution air, the heat exchanger 2 is internally provided with heat source high-temperature flue gas, and the dilution air is heated in a mode of wrapping the cold source by the heat source, so that the heat exchange effect of the dilution air can be remarkably improved. The heat exchange tube 15 is arranged in a spiral structure, so that the heat exchange area can be increased, and the heat exchange capacity is improved; the inner side wall of the heat exchanger 2 is provided with the plurality of first baffle plates 16 in a staggered manner, so that the turbulence effect of the high-temperature flue gas can be further increased, the flow velocity of the high-temperature flue gas is reduced, the action time of the high-temperature flue gas and the dilution wind is prolonged, and the heat exchange efficiency of the high-temperature flue gas and the dilution wind is further improved.
In this embodiment, specifically, two opposite surfaces of the heat exchanger 2 that are communicated are respectively provided with a flue gas inlet chamber 17 and a flue gas outlet chamber 18, that is, the high-temperature flue gas after dust removal enters the flue gas inlet chamber 17 first, then enters the heat exchanger 2, is discharged by the flue gas outlet chamber 18 after heat exchange, two opposite side walls that are adjacent to the two opposite surfaces that are communicated with the heat exchanger 2 are respectively provided with a dilution wind inlet chamber 19 and a dilution wind outlet chamber 20 that are communicated with the heat exchange tube 15, and similarly, the dilution wind enters the dilution wind inlet chamber 19 first, then enters the heat exchange tube 15, and is discharged by the dilution wind outlet chamber 20 after heat exchange, which provides a certain buffer space for the dilution wind and the high-temperature flue gas.
On the basis of the above technical solution, it is further preferable that a temperature sensor 9 and a flow rate regulating valve 8 are provided on a pipe through which the dilution air outlet chamber 20 communicates with the ammonia air mixer 3.
The temperature of the heated dilution air can be monitored in real time through the temperature sensor 9, the flow at the smoke inlet of the heat exchanger 2 is regulated in real time, and the flow regulating valve 8 can control the flow of the heated dilution air entering the ammonia-air mixer 3, so that the volume concentration of the mixed ammonia gas is ensured to be 5%.
In addition, in order to further improve the mixing effect of the ammonia gas and the diluted air after heat exchange in the ammonia air mixer 3 and ensure the uniformity of the ammonia gas mixing, a plurality of second baffle plates 21 are staggered on the inner side wall of the ammonia air mixer 3, and the second baffle plates 21 can be vertically arranged or obliquely arranged.
On the basis of the above technical solution, more preferably, the ammonia injection grid 5 is communicated with a flue gas pipeline at the front end of the SCR denitration reactor 6, and a plurality of third baffle plates 22 are staggered on the inner side wall of the flue gas pipeline close to the ammonia injection grid 5.
The diluted ammonia gas has a certain temperature, and when the diluted ammonia gas is mixed with the flue gas, the temperature difference between the diluted ammonia gas and the flue gas is relatively small, so that the rapid diffusion of the ammonia gas is facilitated, and in addition, a plurality of third baffle plates 22 can be staggered on the inner side wall of the flue gas pipeline, which is close to the ammonia injection grid 5, so as to further improve the mixing effect with the flue gas.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present utility model, and not for limiting the same; although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the utility model.
Claims (9)
1. The SCR denitration system coupled with urea hydrolysis is characterized by comprising a heat exchanger (2), an ammonia-air mixer (3), a urea hydrolyzer (4), an ammonia-spraying grid (5) and an SCR denitration reactor (6),
the heat exchanger (2), the ammonia air mixer (3), the ammonia spraying grid (5) and the SCR denitration reactor (6) are sequentially communicated, and the urea hydrolyzer (4) is communicated with the ammonia air mixer (3);
the flue gas inlet pipeline of the heat exchanger (2) is internally provided with a flue dust filter screen (14), and the flue gas inlet pipeline of the heat exchanger (2) is provided with a flow regulating valve (8) and a temperature sensor (9).
2. The SCR denitration system according to claim 1, further comprising a dust remover (1), wherein the dust remover (1) is communicated with the heat exchanger (2), and flow sensors (7) are arranged on a pipeline of a flue gas inlet of the dust remover (1) and on a pipeline of the dust remover (1) communicated with the heat exchanger (2).
3. The SCR denitration system according to claim 2, wherein an ash collecting hopper (10), a filter bag (11) and an ash blowing pipe (12) are sequentially arranged in the dust remover (1) along the flow direction of the flue gas,
the dust collector comprises a dust collector body, a dust collecting hopper (10), a dust blowing pipe (12) and a filter bag (11), wherein the filter bag (11) is fixedly arranged in the dust collector body (1), an outlet of the filter bag (11) is opposite to the air nozzle of the dust blowing pipe (12), and the dust collecting hopper (10) is arranged at the bottom of the dust collector body (1) in a conical structure.
4. The SCR denitration system according to claim 3, wherein a compressed air bag (13) is arranged outside the dust remover (1), one end of the compressed air bag (13) is communicated with a flue gas outlet pipeline of the dust remover (1) through an air compressor, the other end of the compressed air bag is communicated with the ash blowing pipe (12), and an electromagnetic valve is arranged on the compressed air bag (13).
5. SCR denitration system according to claim 1, characterized in that the heat exchanger (2) is internally provided with a plurality of heat exchange tubes (15) in a spiral, and the inner side wall of the heat exchanger (2) is provided with a plurality of first baffle plates (16) in a staggered manner.
6. The SCR denitration system according to claim 5, wherein two pairs of through surfaces of the heat exchanger (2) are respectively provided with a flue gas inlet chamber (17) and a flue gas outlet chamber (18), and two side walls adjacent to the two pairs of through surfaces of the heat exchanger (2) are respectively provided with a dilution air inlet chamber (19) and a dilution air outlet chamber (20) which are communicated with the heat exchange tube (15).
7. SCR denitration system according to claim 6, characterized in that the dilution air outlet chamber (20) is provided with a temperature sensor (9) and a flow regulating valve (8) on the conduit communicating with the ammonia air mixer (3).
8. SCR denitration system according to claim 1, characterized in that the ammonia air mixer (3) is provided with a plurality of second baffle plates (21) on the inner side wall in a staggered manner.
9. The SCR denitration system according to claim 1, wherein the ammonia injection grid (5) is communicated with a flue gas pipeline at the front end of the SCR denitration reactor (6), and a plurality of third baffle plates (22) are staggered on the inner side wall of the flue gas pipeline close to the ammonia injection grid (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320629756.7U CN219663369U (en) | 2023-03-27 | 2023-03-27 | SCR denitration system coupling urea hydrolysis |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320629756.7U CN219663369U (en) | 2023-03-27 | 2023-03-27 | SCR denitration system coupling urea hydrolysis |
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| CN219663369U true CN219663369U (en) | 2023-09-12 |
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| CN202320629756.7U Active CN219663369U (en) | 2023-03-27 | 2023-03-27 | SCR denitration system coupling urea hydrolysis |
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