CN213873905U - A dilute wind heat transfer system for urea denitration of hydrolysising - Google Patents
A dilute wind heat transfer system for urea denitration of hydrolysising Download PDFInfo
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- CN213873905U CN213873905U CN202021690606.XU CN202021690606U CN213873905U CN 213873905 U CN213873905 U CN 213873905U CN 202021690606 U CN202021690606 U CN 202021690606U CN 213873905 U CN213873905 U CN 213873905U
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- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 239000004202 carbamide Substances 0.000 title claims abstract description 29
- 238000012546 transfer Methods 0.000 title abstract description 10
- 238000010790 dilution Methods 0.000 claims abstract description 66
- 239000012895 dilution Substances 0.000 claims abstract description 66
- 230000007062 hydrolysis Effects 0.000 claims abstract description 23
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 23
- 238000002955 isolation Methods 0.000 claims description 22
- 238000004891 communication Methods 0.000 claims description 9
- 238000011144 upstream manufacturing Methods 0.000 claims description 5
- 239000007789 gas Substances 0.000 abstract description 48
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 13
- 239000003546 flue gas Substances 0.000 abstract description 13
- 238000010438 heat treatment Methods 0.000 abstract description 13
- 238000000034 method Methods 0.000 abstract description 11
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000007865 diluting Methods 0.000 abstract description 5
- 239000002918 waste heat Substances 0.000 abstract description 5
- 238000005485 electric heating Methods 0.000 abstract description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 32
- 229910021529 ammonia Inorganic materials 0.000 description 16
- 230000008569 process Effects 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- 238000005299 abrasion Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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- Exhaust Gas After Treatment (AREA)
Abstract
The utility model provides a dilution air heat exchange system for urea hydrolysis denitration, which relates to the technical field of SCR denitration, and comprises a cold primary air duct, a gas-gas heat exchanger, an SCR reactor and a hot air duct, wherein the cold primary air duct is connected with the gas-gas heat exchanger; the gas-gas heat exchanger is arranged in an outlet flue of the SCR reactor; and the gas-gas heat exchanger is connected with the ammonia-air mixer through the hot air pipeline. The utility model provides a dilute wind heat transfer system for urea denitration of hydrolysising sets up the gas-gas heat exchanger in the export flue through with the gas-gas heat exchanger, utilizes the waste heat of flue gas to heat the dilute wind in the gas-gas heat exchanger, when guaranteeing that the temperature of diluting the wind satisfies the system demand, does not need the heating methods that use power consumptions such as electric heating, steam heating to heat diluting the wind to can reduce the energy consumption, improve the economic nature of system operation.
Description
Technical Field
The utility model relates to a SCR denitration technical field particularly, relates to a dilute wind heat transfer system for urea denitration of hydrolysising.
Background
A power plant denitration system mostly adopts a selective catalytic reduction process (SCR technology) and is matched with a urea hydrolysis denitration system; the urea hydrolysis denitration system generally requires that the dilution air source is not lower than 150 ℃, and the denitration dilution air of the existing urea hydrolysis denitration system generally adopts electricity or steam as a heating heat source to improve the temperature of the denitration dilution air so as to enable the temperature of the dilution air to meet the requirements of the urea hydrolysis denitration system; however, the heating mode of the dilution air can cause the energy consumption of the urea hydrolysis denitration system to increase.
SUMMERY OF THE UTILITY MODEL
The utility model provides a problem how to reduce urea denitration system's energy consumption of hydrolysising.
In order to solve the problems, the utility model provides a dilution air heat exchange system for urea hydrolysis denitration, which comprises a cold primary air duct, an air-gas heat exchanger, an SCR reactor and a hot air duct, wherein,
the cold primary air channel is connected with the air-air heat exchanger;
the gas-gas heat exchanger is arranged in an outlet flue of the SCR reactor;
and the gas-gas heat exchanger is connected with the ammonia-air mixer through the hot air pipeline.
Optionally, the gas-gas heat exchanger comprises a tubular heat exchanger.
Optionally, the gas-gas heat exchanger comprises an inlet header, an outlet header, and a connecting pipe connected between the inlet header and the outlet header; the inlet main pipe is connected with the cold primary air channel; the outlet main pipe is connected with the hot air pipeline.
Optionally, the connecting pipe comprises a plurality of inlet headers vertically connected with the inlet header, a plurality of outlet headers vertically connected with the outlet header, and the outlet headers are matched with the inlet headers; the inlet collecting pipe and the outlet collecting pipe are connected through a communicating pipe; the pipe diameter of the inlet main pipe is the same as that of the outlet main pipe; the pipe diameters of the inlet collecting pipe and the outlet collecting pipe are the same; the pipe diameter of the inlet main pipe is larger than that of the inlet collecting pipe.
Optionally, each of the inlet headers is connected to two of the communicating tubes; the pipe diameter of the inlet collecting pipe is larger than that of the communicating pipe; the number of inlet headers and outlet headers is fifty-eight each.
Optionally, the dilution air heat exchange system adopts a unit system arrangement mode; the adjacent dilution air heat exchange systems are connected through a connecting pipeline; and the communication pipeline is provided with a communication valve.
Optionally, the connecting pipeline is connected with the hot air pipeline.
Optionally, a first isolation valve is arranged on the cold primary air duct; the hot air pipeline is provided with a second isolation valve and a third isolation valve which are respectively arranged at the upstream and the downstream of the communication pipeline.
Optionally, a first thermocouple and a first pressure transmitter are arranged on the cold primary air duct; and a second thermocouple and a second pressure transmitter are arranged on the hot air pipeline.
Optionally, a flow meter and a flow transmitter are further arranged on the hot air pipeline.
Compared with the prior art, the utility model provides a dilute wind heat transfer system for denitration of urea hydrolysis has following advantage:
the utility model provides a dilute wind heat transfer system for urea denitration of hydrolysising sets up the gas-gas heat exchanger in the export flue through with the gas-gas heat exchanger, utilizes the waste heat of flue gas to heat the dilute wind in the gas-gas heat exchanger, when guaranteeing that the temperature of diluting the wind satisfies the system demand, does not need the heating methods that use power consumptions such as electric heating, steam heating to heat diluting the wind to can reduce the energy consumption, improve the economic nature of system operation.
Drawings
FIG. 1 is a schematic structural diagram of a dilution air heat exchange system for urea hydrolysis denitration according to the present invention;
FIG. 2 is a schematic flow diagram of a dilution air heat exchange system for urea hydrolysis denitration according to the present invention;
FIG. 3 is a schematic structural diagram of the gas-gas heat exchanger according to the present invention;
fig. 4 is a side view of the gas-gas heat exchanger according to the present invention.
Description of reference numerals:
1-cooling the primary air duct; 11-a first isolation valve; 111-butterfly valve; 112-a pneumatic butterfly valve; 12-a first thermocouple; 13-a first pressure transmitter; 2-gas heat exchanger; 21-inlet header pipe; 22-outlet header; 23-a connecting tube; 231-an inlet header; 232-outlet header; 233-communicating tube; 3-an SCR reactor; 31-an outlet flue; 4-hot air pipes; 41-a second isolation valve; 42-a third isolation valve; 43-a second thermocouple; 44-a second pressure transmitter; 45-a flow meter; 46-a flow transmitter; 5-a communication pipeline; 51-communication valve.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary and intended to be used for explaining the present invention, and should not be construed as limiting the present invention, and all other embodiments obtained by those skilled in the art without creative efforts based on the embodiments of the present invention belong to the protection scope of the present invention.
In the description of the present invention, it is to be understood that the terms "first" and "second" are used merely for simplifying the description, and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, 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 specifically limited otherwise.
In order to make the aforementioned objects, features and advantages of the present invention more comprehensible, embodiments accompanied with figures are described in detail below.
For reducing the energy consumption of urea hydrolysis denitration system, the utility model provides a dilute wind heat transfer system for urea hydrolysis denitration, see fig. 1, fig. 2 show, this dilute wind heat transfer system includes the cold wind channel 1 that is used for carrying dilute cold wind, is used for heating gas-gas heat exchanger 2, SCR reactor 3 and is used for carrying out the hot-blast pipeline 4 of carrying dilute hot wind to dilute cold wind, wherein, cold wind channel 1 links to each other with gas-gas heat exchanger 2, carries dilute cold wind to gas-gas heat exchanger 2 through cold wind channel 1; the gas-gas heat exchanger 2 is arranged in an outlet flue 31 of the SCR reactor 3, and exchanges heat with high-temperature flue gas in the outlet flue 31 to increase the temperature of dilution cold wind, and the dilution cold wind at normal temperature is heated into dilution hot wind with the temperature of about 170 ℃; gas heat exchanger 2 links to each other with the empty blender of ammonia through hot-blast main 4 to carry the dilution hot-blast of exporting from gas heat exchanger 2 to the empty blender of ammonia through hot-blast main 4 and dilute the ammonia, dilute the ammonia to below 5%, satisfy the requirement of boiler SCR denitration technique.
The cold primary air duct 1 in the application specifically refers to a pipeline connected with an outlet of a primary air fan, so that dilution cold air conveyed through the cold primary air duct 1 is a primary air source directly output from the outlet of the primary air fan, the primary air source is a clean air source at normal temperature, and the clean air source directly output from the primary air fan is used as a dilution air source, so that the cleanness of the dilution air source can be improved, dust in the dilution air source is avoided, the dust content in the dilution air source is reduced, and therefore on one hand, serious abrasion when the denitration ammonia injection manual valve is fully opened due to overhigh dust content in the operation process of a system is avoided, the phenomenon of ammonia leakage due to abrasion of part of the structure is avoided, the service life of the denitration ammonia injection manual valve is prolonged, and the safety of the system is improved; on the other hand, the conditions of local ash blockage and flow reduction of a pipeline and a valve when the denitration ammonia injection manual valve is adjusted to be small in a closed mode in an optimized mode are avoided, and the temperature of the pipeline in the system is prevented from being gradually reduced; when the temperature of the pipeline in the system is lower than 140 ℃, water vapor in the hydrolysis gas is condensed into water, and the water is mixed with deposited ash and dissolved and crystallized ammonia and then adheres to a valve core of the valve and the inner wall of the pipeline, so that blockage is caused, and the ammonia spraying amount of the blocked area is directly influenced; therefore, the cold primary air channel 1 is connected with the air-air heat exchanger 2, and the primary air source in the cold primary air channel 1 is used as a dilution air source, so that the blockage of a valve and a pipeline can be avoided, the smooth production is ensured, and the production quality is ensured.
In addition, because the denitration ammonia injection branch pipe and the valve are difficult to clean in the operation process, the denitration efficiency of the boiler is directly influenced when the number of pipelines is too large, and the safety of a unit is also influenced when the pipelines are seriously blocked, so that the unit is forced to be shut down; consequently, this application is through using a wind regime as diluting the wind regime, when providing the security, guaranteeing production quality, can also improve denitration efficiency.
This application is through setting up gas heat exchanger 2 in SCR reactor 3's export flue 31, the waste heat of flue gas comes to heat the dilution wind regime in gas heat exchanger 2 among the utilization export flue 31, avoid using the heating methods of electric heating in the past, energy consumptive such as steam heating, utilize through the waste heat to in the flue gas to reduce the energy consumption on the one hand, improve the economic nature of system operation, on the other hand still is favorable to reducing the discharge temperature of flue gas, thereby improve the security of fume emission.
In addition, because the flow velocity of the flue gas at the outlet is far lower than that at the inlet, specifically, under normal conditions, the flow velocity of the flue gas at the inlet is about 15m/s, and the flow velocity at the outlet is about 5m/s, the gas-gas heat exchanger 2 is arranged in the outlet flue 31, which is beneficial to reducing the abrasion of the gas-gas heat exchanger 2 in the operation process and improving the reliability of the system operation.
Because the gas-gas heat exchanger 2 in this application is the dilution cold wind heating of normal atmospheric temperature for the temperature is about 170 ℃ dilutes hot-blastly, make this dilution hot-blastly can satisfy the minimum demand of temperature 150 ℃ of dilution wind on the one hand, on the other hand, adopt the hot primary air that air heater exit temperature is about 340 ℃ with former system as the wind regime direct access ammonia air-liquid mixer and dilute the processing and compare the ammonia, the operating temperature of system has greatly been reduced, thereby can reduce the requirement to the valve in the system, it selects from sodium parameter to reduce the system valve, be favorable to reducing equipment investment, and the cost is reduced.
The utility model provides a dilute wind heat transfer system for urea denitration of hydrolysising sets up gas heat exchanger 2 in outlet flue 31 through with gas heat exchanger 2, and the waste heat that utilizes the flue gas heats the dilute wind in gas heat exchanger 2, when guaranteeing that the temperature of dilute wind satisfies the system demand, does not need to use power-wasting heating methods such as electrical heating, steam heating to heat the dilute wind to can reduce the energy consumption, improve the economic nature of system operation.
The gas-gas heat exchanger 2 can be any heat exchanger, and the gas-gas heat exchanger 2 is preferably a tubular heat exchanger in the application.
Specifically, referring to fig. 3 and 4, the gas-gas heat exchanger 2 in the present application includes an inlet header 21, an outlet header 22, and a connecting pipe 23 connected between the inlet header 21 and the outlet header 22; the inlet main pipe 21 is connected with the cold primary air duct 1; the outlet main pipe 22 is connected with the hot air pipeline 4.
In the operation process of the system, dilution cold air passes through the inlet main pipe 21, the connecting pipe 3 and the outlet main pipe 22 from the cold primary air duct 1 in sequence and is output from the air-gas heat exchanger 2; because the gas-gas heat exchanger 2 is arranged in the outlet flue 21, in the process of passing through the gas-gas heat exchanger 2, the high-temperature flue gas positioned outside the gas-gas heat exchanger 2 exchanges heat with the cold dilution air in the gas-gas heat exchanger 2, the temperature of the cold dilution air is increased after absorbing heat, and the cold dilution air becomes hot dilution air and is output from the outlet main pipe 22, so that the temperature of the hot dilution air meets the system requirement.
Wherein the distribution direction of female pipe 21 of import, the female pipe 22 of export can be the same, also can be different, for convenient preparation and equipment layout, the female pipe 21 of preferred import and the female pipe 22 parallel arrangement of export in this application, and the female pipe 21 of import is the same with the female pipe 22's of export height.
Furthermore, in order to increase the heat exchange area of the gas-gas heat exchanger 2, the connecting pipe 23 in the present application includes a plurality of inlet headers 231 vertically connected to the inlet header 21, and a plurality of outlet headers 232 vertically connected to the outlet header 22, and the outlet headers 232 are adapted to the inlet headers 231; inlet header 231 and outlet header 232 are connected by communication pipe 233; the pipe diameter of the inlet main pipe 21 is the same as that of the outlet main pipe 22; inlet header 231 and outlet header 232 have the same pipe diameter; the pipe diameter of the inlet header 21 is larger than that of the inlet header 231; each inlet header 231 is connected to two communicating tubes 233; the pipe diameter of inlet header 231 is larger than the pipe diameter of communication pipe 233.
Dilution cold air enters the inlet main pipe 21 from the primary cold air duct 1 and then enters the plurality of inlet headers 231, dilution air in each inlet header 231 enters the two communicating pipes 233 respectively, the length of the communicating pipes 233 is long, the dilution air passes through the communicating pipes 233, meanwhile, the flue gas flowing out of the communicating pipes 233 exchanges heat with the dilution cold air in the communicating pipes 233, so that the dilution cold air absorbs heat, the temperature is increased, the dilution air after further temperature increase enters the corresponding outlet headers 232 from the communicating pipes 233, and the dilution air in different headers 232 is collected in the outlet main pipe 22 to obtain dilution hot air meeting production requirements.
This application is through setting up gas-gas heat exchanger 2 into the form that the pipeline of many less pipe diameters links to each other, increases the area of contact between flue gas and the gas-gas heat exchanger 2 to increase the heat transfer area of flue gas and dilution wind, improve heat exchange efficiency.
Wherein the number of the inlet collecting pipes 231 and the outlet collecting pipes 232 can be determined according to the pipe diameter, the length, the heat exchange requirement and the like of the inlet main pipe 21 in the gas-gas heat exchanger 2, and the optimization of the application is preferred
The number of each of inlet header 231 and outlet header 232 is fifty-eight, and it is further preferable that the specifications of each of inlet header 21 and outlet header 22 are phi 426 × 6mm, the specifications of fifty-eight inlet header 231 and outlet header 232 are phi 89 × 6mm, and the specification of each of communication tubes 233 is phi 57 × 3.5 mm.
In consideration of the parameter change of the unit under the working conditions of start-stop, deep peak regulation, RB action, low winter environmental temperature and the like, the cold air pressure at the primary air outlet is selected to be 8 kPa-12 kPa, the air temperature range is about (-13.8) DEG C-41.5 ℃, and the temperature range of the smoke side is 292-380 ℃. The primary air volume is selected to be the maximum ammonia consumption in unit hour, the pure ammonia consumption of each unit is 246kg/h according to the system design, and the dilution air volume is about 7000m3H is used as the reference value. Through design calculation, the gas-gas heat exchanger 2 adopts 116 phi 57 multiplied by 3.5mm 16Mn steel pipes which are arranged in the SCR outlet flue in two layers, and the heat exchange area is about 202m2The dilution air is heated to over 170 ℃, and the pressure loss of the dilution air is less than or equal to 1 kPa. For the reliability that further improves 2 bundles of gas-gas heat exchanger, this application further installs the abrasionproof angle steel additional at first layer tube bank windward side.
Furthermore, the dilution air heat exchange system in the application adopts a unit system arrangement mode, namely, the dilution air heat exchange system corresponding to the SCR reactor at the boiler A, B side adopts a unit system arrangement mode; the adjacent dilution air heat exchange systems are connected through a connecting pipeline 5; the connecting pipeline 5 is provided with a connecting valve 51 to ensure that two sides can be mutually standby when a unilateral air source or a heat exchanger fails, and the safety and reliability of the system operation are further improved.
Specifically, the connecting pipeline 5 is connected with the hot air pipeline 4, namely, the two ends of the connecting pipeline 5 are respectively connected with the hot air pipeline 4 in two adjacent dilution air heat exchange systems, so that dilution air in the two systems can be mutually reserved.
Further, a first isolating valve 11 is arranged on the cold primary air channel 1; the hot air duct 4 is provided with a second isolation valve 41 and a third isolation valve 42, and the second isolation valve 41 and the third isolation valve 42 are respectively arranged at the upstream and the downstream of the connecting pipeline 5.
The first isolation valve 11 arranged on the cold primary air duct 1 can be used as an isolation valve of a cold air source and used for cutting off the air source by closing the first isolation valve 11 under the conditions of pipeline maintenance and the like; the number of the first isolation valves 11 may be one or two, and it is further preferable that the first isolation valves 11 include a butterfly valve 111 and a pneumatic butterfly valve 112 disposed adjacent to each other, so as to improve the safety of the system.
In the application, the upstream and the downstream of the connecting pipeline 5 are both in terms of the flow direction of the dilution air in the hot air pipeline 4; an isolation valve is arranged at the upstream and the downstream of the connecting pipeline 5 on the hot air pipeline 4, so that the flow direction of dilution air in the hot air pipeline 4 is controlled by operating the isolation valve, and dilution air is reserved for each other.
Further, a first thermocouple 12 and a first pressure transmitter 13 are arranged on the cold primary air duct 1; the hot air pipeline 4 is provided with a second thermocouple 43 and a second pressure transmitter 44; so that the state of the dilution air in the hot air pipeline 4 is monitored through the first thermocouple 12, the first pressure transmitter 13, the second thermocouple 43 and the second pressure transmitter 44, and the heat exchange efficiency of the gas-gas heat exchanger 2 is calculated through the readings of the first thermocouple 12, the first pressure transmitter 13, the second thermocouple 43 and the second pressure transmitter 44, so as to ensure that the heated dilution hot air can meet the requirements of the boiler SCR denitration technology.
Further, still be provided with flowmeter 45 and flow transmitter 46 on hot-blast main 4 to measure the hot-blast flow of dilution in hot-blast main 4 through flowmeter 45 and flow transmitter 46, thereby judge the behavior of spouting ammonia pipeline according to the flow, go on smoothly with the assurance production.
Although the present disclosure has been described above, the scope of the present disclosure is not limited thereto. Those skilled in the art can make various changes and modifications without departing from the spirit and scope of the present disclosure, and such changes and modifications will fall within the scope of the present invention.
Claims (10)
1. A dilution air heat exchange system for urea hydrolysis denitration is characterized by comprising a cold primary air duct (1), an air-air heat exchanger (2), an SCR reactor (3) and a hot air duct (4),
the cold primary air channel (1) is connected with the air-air heat exchanger (2);
the gas-gas heat exchanger (2) is arranged in an outlet flue (31) of the SCR reactor (3);
the gas-gas heat exchanger (2) is connected with the ammonia-air mixer through the hot air pipeline (4).
2. The dilution air heat exchange system for urea hydrolysis denitration according to claim 1, wherein the gas-gas heat exchanger (2) comprises a tubular heat exchanger.
3. The dilution air heat exchange system for urea hydrolysis denitration according to claim 1, wherein the gas-gas heat exchanger (2) comprises an inlet header (21), an outlet header (22), and a connection pipe (23) connected between the inlet header (21) and the outlet header (22); the inlet main pipe (21) is connected with the cold primary air duct (1); the outlet main pipe (22) is connected with the hot air pipeline (4).
4. The dilution air heat exchange system for urea hydrolysis denitration according to claim 3, wherein the connection pipe (23) comprises a plurality of inlet headers (231) vertically connected to the inlet header (21), a plurality of outlet headers (232) vertically connected to the outlet header (22), and the outlet headers (232) are adapted to the inlet headers (231); the inlet header (231) and the outlet header (232) are connected through a communicating pipe (233); the pipe diameter of the inlet main pipe (21) is the same as that of the outlet main pipe (22); the pipe diameters of the inlet collection pipe (231) and the outlet collection pipe (232) are the same; the pipe diameter of the inlet main pipe (21) is larger than that of the inlet collecting pipe (231).
5. The dilution air heat exchange system for urea hydrolysis denitration according to claim 4, wherein each of the inlet headers (231) is connected to two of the communicating pipes (233); the pipe diameter of the inlet collecting pipe (231) is larger than that of the communicating pipe (233); the number of inlet headers (231) and outlet headers (232) is fifty-eight each.
6. The dilution air heat exchange system for urea hydrolysis denitration according to any one of claims 1 to 5, wherein the dilution air heat exchange system adopts a unit system arrangement mode; the adjacent dilution air heat exchange systems are connected through a connecting pipeline (5); and a connection valve (51) is arranged on the connection pipeline (5).
7. The dilution air heat exchange system for urea hydrolysis denitration according to claim 6, wherein the connecting pipeline (5) is connected with the hot air pipeline (4).
8. The dilution air heat exchange system for urea hydrolysis denitration according to claim 7, wherein the cold primary air duct (1) is provided with a first isolation valve (11); the hot air pipeline (4) is provided with a second isolation valve (41) and a third isolation valve (42), and the second isolation valve (41) and the third isolation valve (42) are respectively arranged at the upstream and the downstream of the communication pipeline (5).
9. The dilution air heat exchange system for urea hydrolysis denitration according to claim 6, wherein the cold primary air duct (1) is provided with a first thermocouple (12) and a first pressure transmitter (13); and a second thermocouple (43) and a second pressure transmitter (44) are arranged on the hot air pipeline (4).
10. The dilution air heat exchange system for urea hydrolysis denitration according to claim 6, wherein a flow meter (45) and a flow transmitter (46) are further arranged on the hot air pipeline (4).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021690606.XU CN213873905U (en) | 2020-08-14 | 2020-08-14 | A dilute wind heat transfer system for urea denitration of hydrolysising |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202021690606.XU CN213873905U (en) | 2020-08-14 | 2020-08-14 | A dilute wind heat transfer system for urea denitration of hydrolysising |
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| CN213873905U true CN213873905U (en) | 2021-08-03 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113932242A (en) * | 2021-11-12 | 2022-01-14 | 浙江天地环保科技股份有限公司 | A temperature-controllable flue gas heat exchange denitrification dilution air system and method |
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2020
- 2020-08-14 CN CN202021690606.XU patent/CN213873905U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113932242A (en) * | 2021-11-12 | 2022-01-14 | 浙江天地环保科技股份有限公司 | A temperature-controllable flue gas heat exchange denitrification dilution air system and method |
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