CN204694693U - A kind of full-scale catalyst for denitrating flue gas device for detecting performance - Google Patents
A kind of full-scale catalyst for denitrating flue gas device for detecting performance Download PDFInfo
- Publication number
- CN204694693U CN204694693U CN201520442863.4U CN201520442863U CN204694693U CN 204694693 U CN204694693 U CN 204694693U CN 201520442863 U CN201520442863 U CN 201520442863U CN 204694693 U CN204694693 U CN 204694693U
- Authority
- CN
- China
- Prior art keywords
- gas
- main pipe
- unit
- inlet main
- mass flow
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn - After Issue
Links
Landscapes
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The utility model relates to a kind of full-scale catalyst for denitrating flue gas device for detecting performance, comprise smoke modelling unit, reaction member, analytic unit, reaction member comprises inlet main pipe, give vent to anger female pipe, multiple reactor, smoke modelling unit comprises ammonia storage tank, sulphuric dioxide storage tank, nitrogen monoxide storage tank, air compressor machine, nitrogen making machine, steam generator, well heater, and analytic unit comprises multiple draft tube, multiple operation valve, analyser.The utility model configures simulated flue gas by adopting distribution method, detects full-scale catalyst for denitrating flue gas, adopts the smoke components that a set of analyser comes before and after detection reaction device, avoids the error that instrument produces, thus ensure that test result is more accurate; The utility model can make multiple reactor rotation to use by arranging switch valve, thus partly can isolate reactor so that more catalyst changeout, economize energy, and makes pick-up unit more efficient.
Description
Technical field
The utility model is specifically related to a kind of full-scale catalyst for denitrating flue gas device for detecting performance.
Background technology
At present, China's total particulate discharge capacity is controlled substantially, and SO2 emissions decline to some extent, but NOx discharge along with China's energy-consuming and vehicle guaranteeding organic quantity quick growth and rise rapidly.According to statistics, in China's airborne release pollutant, the release 60% of NOx derives from coal combustion, and the one ton of coal that often burns can produce 3 ~ 5Kg oxides of nitrogen, corresponding 400 ~ 600mg/m
3, and power plants Coal-fired capacity accounts for 70% of total Coal-fired capacity, so thermal power plant is the main source of discharged nitrous oxides, at present, the discharge of NOx considerably beyond air from net capacity.
SCR (SCR) denitration technology is widely used in the denitrating system of coal-burning power plant because having efficient, reliable denitration performance.In whole SCR denitration system, catalyzer is core component, and the proportion accounted in equipment direct investment is larger.The mode of appearance of SCR denitration has honeycomb fashion, flat and corrugated.The catalyst module major part of SCR denitration system takes high dirt arrangement, and the denitration performance running a period of time rear catalyst can decline, and causes catalyst deactivation.The reason of catalyst deactivation has a lot, the impact of existing operating condition, the infringement that such as, dust in flue gas and temperature fluctuation cause catalyzer macroscopic result, also have the effect of various poisonous and harmful chemical composition in flue gas, wherein the toxic action that has of arsenic element, alkaline metal, earth alkali metal and metal oxide is the most obvious.These factors make be only 2 to 3 years the serviceable life of SCR denitration, and the initial investment of catalyzer accounts for 40%-60% of SCR denitration system gross investment, these consumables making catalyzer become expensive.In addition inactivation SCR catalyst if not in addition suitably process cause extremely strong toxic action by human body and environment.Production cost so not only can be caused to improve, and the health of meeting harm humans.If the catalyzer of inactivation to be carried out regeneration process, SCR catalyst life cycle be can effectively extend, financial cost and toxic action reduced.Therefore regeneration is carried out to SCR denitration significant.
In recent years, domestic each colleges and universities and related scientific research institutes have put into research and development and the testing evaluation of SCR catalyst, and establish miniature test experimental bed or the lab scale test experimental bed of the test of various catalyst activity.But due to reasons such as the starting point of the research of constituent parts and the limitation of testboard bay itself, miniature/lab scale test experimental bed can only characterize the intrinsic chemomotive force coefficient of catalyzer, the activity of full-scale catalyst elements body cannot be reflected, be not suitable for inspect on colligated-function and the management of catalyzer.
Utility model content
Technical problem to be solved in the utility model is to provide a kind of pick-up unit that can carry out Performance Detection to full-scale catalyst for denitrating flue gas.
For solving above technical matters, the utility model takes following technical scheme:
A kind of full-scale catalyst for denitrating flue gas device for detecting performance, comprises smoke modelling unit, reaction member, analytic unit,
Described reaction member comprise the inlet main pipe entered for simulated flue gas, female pipe of giving vent to anger of discharging for waste gas, respectively by air intake branch with go out gas branch pipe and described inlet main pipe and to be connected with described female pipe of giving vent to anger and can multiple reactors of rotation, described full-scale catalyst for denitrating flue gas is placed in described reactor;
Described smoke modelling unit comprises for providing NH
3and the ammonia storage tank be connected with the inlet main pipe of described reaction member, for providing SO
2and the sulphuric dioxide storage tank be connected with the inlet main pipe of described reaction member, for NO is provided and the nitrogen monoxide storage tank be connected with the inlet main pipe of described reaction member, for generation of the air compressor machine of air, for producing N
2and the nitrogen making machine be connected with described air compressor machine, for the well heater providing the steam generator of water vapor, be connected with the inlet main pipe of described reaction member, described N
2, described air and described water vapor enters the inlet main pipe of described reaction member after the heating of described well heater;
Described analytic unit comprise one end portion not with the air intake branch of described inlet main pipe, described multiple reactors and the multiple draft tube going out gas branch pipe and be connected, being arranged on the multiple operation valves in described multiple draft tube, being connected with the other end of described multiple draft tube and analyser for analyzing smoke components.
Particularly, multiple described reactor air intake branch and go out on gas branch pipe to be provided with transfer valve.
Particularly, described pick-up unit also comprises the Tail gas cleanup unit for carrying out purified treatment to the waste gas of discharging in described female pipe of giving vent to anger.
More specifically, described pick-up unit also comprises the N had for described
2the flue passed through with described air, the exhaust piping that passes through for described waste gas and the heat of described waste gas can be passed to described N
2with the heat interchanger of described air, the entrance point of described flue is connected with the endpiece of described nitrogen making machine with the endpiece of described air compressor machine, endpiece is connected with the entrance point of described well heater, and female pipe is connected, endpiece is connected with described Tail gas cleanup unit for entrance point and described the giving vent to anger of described exhaust piping.
More specifically, described Tail gas cleanup unit comprises for by the NH in described waste gas
3, SO
2and SO
3the exhaust gas absorption device of removing, is connected for the refrigeratory of lowering the temperature to described waste gas with described exhaust gas absorption device with the endpiece of described exhaust piping respectively.
Particularly, described smoke modelling unit also comprises and to be arranged between described ammonia storage tank and described reaction member inlet main pipe and for described NH
3the first gas mass flow controller group that flow carries out regulating, to be arranged between described sulphuric dioxide storage tank and the inlet main pipe of described reaction member and for described SO
2the second gas mass flow controller group that flow carries out regulating, to be arranged between described nitrogen monoxide storage tank and the inlet main pipe of described reaction member and for described NO flow is regulated the 3rd gas mass flow controller group, be arranged on the endpiece of described nitrogen making machine, between the endpiece of described air compressor machine and described well heater and for described N
2the 4th gas mass flow controller group that regulates is carried out with described air mass flow.
More specifically, the first described gas mass flow controller group comprises two gas mass flow controllers that range of adjustment is respectively 20 ~ 800ppm and 20 ~ 500ppm, the second described gas mass flow controller group comprises two gas mass flow controllers that range of adjustment is respectively 0 ~ 1000ppm and 0 ~ 5500ppm, the 3rd described gas mass flow controller group comprises two gas mass flow controllers that range of adjustment is respectively 20 ~ 800ppm and 20 ~ 500ppm, it is 0 ~ 325Nm that the 4th described gas mass flow controller group comprises range of adjustment
3the gas mass flow controller of/h.
Particularly, described draft tube is provided with hot type SiC filtrator.
Particularly, described ammonia storage tank is connected with described inlet main pipe by pipeline, and the gas outlet of described pipeline is positioned on the axial line of described inlet main pipe, is provided with for ensureing NH in described inlet main pipe
3evenly enter the mixer in described reactor, described mixer comprises multiple flow deflector be obliquely installed.
Particularly, described pick-up unit also comprises the scattered control system for controlling and monitor described pick-up unit work.
Particularly, described pick-up unit also comprises multiple temperature point, multiple pressure-measuring-point, multiple flow measuring point, and described multiple temperature points, described multiple pressure-measuring-points, described multiple flow measuring points all access described scattered control system.
Adopt described pick-up unit to detect a detection method for full-scale catalyst for denitrating flue gas, comprise the steps:
Step (1), smoke components as required regulate the flow of the nitrogen of discharging in the flow of the air of discharging in the nitric oxide production flow of discharging in the flow of the sulphuric dioxide of discharging in the flow of the ammonia of discharging in described ammonia storage tank, described sulphuric dioxide storage tank, described nitrogen monoxide storage tank, described air compressor machine and described nitrogen making machine respectively;
Pass in described well heater together with step (2), water vapor that described air, described nitrogen are produced in described steam generator and heat, and the heating-up temperature of well heater described in controlling is 160 ~ 430 DEG C;
Step (3), full-scale catalyst for denitrating flue gas to be detected put into of described multiple reactors, and be warming up to temperature required to this reactor, described multiple reactor rotations use to improve service efficiency;
Step (4), by described ammonia, described sulphuric dioxide, described nitrogen monoxide, reacts in the described reactor after the air after heating, nitrogen and water vapor pass into heating;
Step (5), respectively by described analyser the air intake branch of the reactor reacted in step (4) and the smoke components gone out in gas branch pipe are analyzed and measured the concentration C of NOx in described air intake branch
1with the described concentration C going out NOx in gas branch pipe
2, the denitration efficiency of described full-scale catalyst for denitrating flue gas is calculated according to formula (),
Formula (one):
, wherein:
η is the denitration efficiency of full-scale catalyst for denitrating flue gas, %;
C
1for the concentration of the NOx in reactor air intake branch, mg/m
3;
C
2for reactor goes out the concentration of the NOx in gas branch pipe, mg/m
3.
Due to the enforcement of above technical scheme, the utility model compared with prior art tool has the following advantages:
The utility model configures simulated flue gas by adopting distribution method, make simulated flue gas and field working conditions completely the same, the utility model detects full-scale catalyst for denitrating flue gas, instead of the catalyst for denitrating flue gas after cutting is detected, the smoke components that the utility model adopts a set of analyser to come before and after detection reaction device, avoid the error that instrument produces, thus ensure that test result is more accurate;
The utility model can make multiple reactor rotation to use by arranging switch valve, thus partly can isolate reactor so that more catalyst changeout, economize energy, and makes pick-up unit more efficient.
Accompanying drawing explanation
Accompanying drawing 1 is structural representation of the present utility model;
Accompanying drawing 2 is the structural representation of analytic unit;
Accompanying drawing 3 is the pipeline of ammonia storage tank and the location diagram of inlet main pipe;
Accompanying drawing 4 is the structural representation of mixer;
Wherein, 1, reaction member; 2, ammonia storage tank; 3, sulphuric dioxide storage tank; 4, nitrogen monoxide storage tank; 5, air compressor machine; 6, nitrogen making machine; 7, steam generator; 8, well heater; 9, heat interchanger; 10, analytic unit; 11, reactor; 12, inlet main pipe; 21, the first gas mass flow controller group; 22, the second gas mass flow controller group; 23, the 3rd gas mass flow controller group; 24, the 4th gas mass flow controller group; 31, exhaust gas absorption device; 32, refrigeratory; 41, draft tube; 42, operation valve; 43, analyser; 44, hot type SiC filtrator; 45, collecting pipe; 51, pipeline; 52, flow deflector.
Embodiment
As shown in Figure 1, a kind of full-scale catalyst for denitrating flue gas device for detecting performance, comprises smoke modelling unit, reaction member 1, analytic unit 10, Tail gas cleanup unit, scattered control system etc.
Reaction member 1 comprise the inlet main pipe 12 entered for simulated flue gas, female pipe of giving vent to anger of discharging for waste gas, respectively by air intake branch with go out gas branch pipe and inlet main pipe 12 and to be connected with female pipe of giving vent to anger and can multiple reactors 11 of rotation, full-scale catalyst for denitrating flue gas is placed in reactor 11.The air intake branch of multiple reactor 11 and go out on gas branch pipe to be provided with transfer valve.Because the Test Cycle temperature of reactor 11 is higher, be generally 380 DEG C, and reactor 11 is stabilized to measurement condition temperature from room temperature, need general 3 hours, and reactor 11 is cooled to less than 100 DEG C from 380 DEG C, needs to reach more than 10 hours, and the replacing of catalyzer all adopts artificial replacing, therefore reactor 11 temperature must be reduced to safe temperature, just can complete manual operation, and carrying out test according to single-reactor 11 must waste the adjustment of plenty of time for operating mode.Application number be 201320466936.4 utility model patent described the setting of reaction member 1 in detail, repeat no more herein.Reaction member 1 can adjust only has partial reaction device 11 to participate in running, the reactor 11 having neither part nor lot in operation keeps cold conditions, installation or the replacing of catalyzer can be carried out, thus can ensure that the temperature, flow etc. of pick-up unit are in stable state always, reduce heat up cooling and other adjustment spent time and energy.
The preparation method adopting combustion method to carry out simulated flue gas is: methane is through gas burner mixing after-combustion, and after the high-temperature flue gas of generation flows through hot-water boiler, temperature is reduced to about 200 DEG C, and the water outlet of hot-water boiler returns water tank after air cooler cooling.The effect of air cooler is the portion of water removed when needed in flue gas, and cooling water source adopts river.In the flue gas that combustion method produces, water capacity is 16.9%, when actual measurement operating mode smoke moisture is lower than this value, just needs to carry out fume-dehydrating.By the control regulating the ratio of the flue gas flowing through air cooler and the flue gas flowing through bypass to realize dehydrating amount, when flue gas all flows through condenser, humidity of flue gas is minimum.Because combustion method exists governing speed slowly, the problem that precision is poor, therefore, the present embodiment adopts distribution method to carry out the configuration of simulated flue gas.
Smoke modelling unit comprises for providing NH
3and the ammonia storage tank 2 be connected with the inlet main pipe 12 of reaction member 1, for providing SO
2and the sulphuric dioxide storage tank 3 be connected with the inlet main pipe 12 of reaction member 1, for NO is provided and the nitrogen monoxide storage tank 4 be connected with the inlet main pipe 12 of reaction member 1, for generation of the air compressor machine 5 of air, for producing N
2and the nitrogen making machine 6 be connected with air compressor machine 5, for the well heater 8, N providing the steam generator 7 of water vapor, be connected with the inlet main pipe 12 of reaction member 1
2, air and water vapor enters the inlet main pipe 12 of reaction member 1 after well heater 8 heats.
Ammonia storage tank 2, sulphuric dioxide storage tank 3 and nitrogen monoxide storage tank 4 are all arranged in explosion-proof gas cabinet, are provided with ventilation blower and ensure sound ventilation environment, be also provided with air escape warning system in explosion-proof gas cabinet in explosion-proof gas cabinet.
The concrete structure of steam generator 7 has been record in detail in the utility model patent of 201320467781.6 at application number, repeats no more herein.
Smoke modelling unit also comprises and to be arranged between ammonia storage tank 2 and reaction member 1 inlet main pipe 12 and for NH
3the first gas mass flow controller group 21 that flow carries out regulating, be arranged on sulphuric dioxide storage tank 3 and reaction member 1 inlet main pipe 12 between and for SO
2the second gas mass flow controller group 22 that flow carries out regulating, be arranged on nitrogen monoxide storage tank 4 and reaction member 1 inlet main pipe 12 between and between the endpiece of the 3rd gas mass flow controller group 23 regulated NO flow, the endpiece being arranged on nitrogen making machine 6, air compressor machine 5 and well heater 8 and for N
2the 4th gas mass flow controller group 24 that regulates is carried out with air mass flow.
First gas mass flow controller group 21 comprises two gas mass flow controllers that range of adjustment is respectively 20 ~ 800ppm and 20 ~ 500ppm, NH
3the gas mass flow controller being first 20 ~ 800ppm through range of adjustment carries out coarse adjustment, and the gas mass flow controller being then 20 ~ 500ppm through range of adjustment carries out meticulous adjustment thus ensures NH
3the degree of accuracy of flow.
Second gas mass flow controller group 22 comprises two gas mass flow controllers that range of adjustment is respectively 0 ~ 1000ppm and 0 ~ 5500ppm, SO
2the gas mass flow controller being first 0 ~ 5500ppm through range of adjustment carries out coarse adjustment, then carries out meticulous adjustment through the gas mass flow controller that range of adjustment is 0 ~ 1000ppm thus ensure SO
2the degree of accuracy of flow.
3rd gas mass flow controller group 23 comprises two gas mass flow controllers that range of adjustment is respectively 20 ~ 800ppm and 20 ~ 500ppm, the gas mass flow controller that NO is first 20 ~ 800ppm through range of adjustment carries out coarse adjustment, then carries out meticulous adjustment through the gas mass flow controller that range of adjustment is 20 ~ 500ppm thus ensure the degree of accuracy of NO flow.
It is 0 ~ 325Nm that 4th gas mass flow controller group 24 comprises range of adjustment
3the gas mass flow controller of/h.
In order to reduce the waste of the energy, pick-up unit also comprises and has for N
2the flue passed through with air, the exhaust piping that passes through for waste gas and the heat of waste gas can be passed to N
2with the heat interchanger 9 of air, the entrance point of flue is connected with the endpiece of nitrogen making machine 6 with the endpiece of air compressor machine 5, endpiece is connected with the entrance point of well heater 8, the entrance point of exhaust piping with give vent to anger that female pipe is connected, endpiece is connected with Tail gas cleanup unit.N
2with air when the heat interchanger 9, in reactor 11, temperature is passed to N by reacted waste gas
2and air, make N
2tentatively heat up with air, then heater via 8 heats up, thus decrease the energy consumption of well heater 8, saved cost.
After full-scale catalyst for denitrating flue gas denitration process, containing SO in waste gas
2, SO
3, and the NO do not removed completely and escape NH
3if the not treated direct discharge of waste gas, certainly will cause environmental pollution.Therefore the Tail gas cleanup unit being used for the waste gas of discharging in female pipe of giving vent to anger being carried out to purified treatment is set before toxic emission.Tail gas cleanup unit comprises for by the NH in waste gas
3, SO
2and SO
3the exhaust gas absorption device 31 of removing, is connected for the refrigeratory 32 of lowering the temperature to waste gas with exhaust gas absorption device 31 with the endpiece of the exhaust piping of heat interchanger 9 respectively.What exhaust gas absorption device 31 adopted is that the method that drum spray is connected removes NH
3, SO
2and SO
3.
As shown in Figure 2, analytic unit 10 comprise one end portion not with the air intake branch of inlet main pipe 12, multiple reactor 11 and the multiple draft tube 41 going out gas branch pipe and be connected, being arranged on the multiple operation valves 42 in multiple draft tube 41, being connected with the other end of multiple draft tube 41 and analyser 43 for analyzing smoke components.Draft tube 41 is provided with hot type SiC filtrator 44, multiple draft tube 41 enters analyser 43 after being confluxed by collecting pipe 45.Operation valve 42 is high temperature pneumatic valve, and each high temperature pneumatic valve all controls the switch of this high temperature pneumatic valve by a road air inlet.
At the scene in denitrating system, ammonia district is autonomous control system, before catalyzer, also the devices such as rectifier are housed, object is the homogeneity in order to ensure by ammonia in flue gas distribution during catalyzer, but, because test traffic during experiment is little, pipeline is thin, is difficult to realize according to field working conditions multi-nozzle spray ammonia.Therefore, as shown in accompanying drawing 3 and accompanying drawing 4, ammonia storage tank 2 is connected with inlet main pipe 12 by pipeline 51, and the gas outlet of pipeline 51 is positioned on the axial line of inlet main pipe 12, is provided with for ensureing NH in inlet main pipe 12
3evenly enter the mixer in reactor 11, mixer comprises multiple flow deflector 52 be obliquely installed, and particularly, flow deflector 52 is for being evenly distributed on four flow deflectors 52 in inlet main pipe 12.
The present embodiment also comprises multiple temperature point, multiple pressure-measuring-point, multiple flow measuring point, pick-up unit also comprises the scattered control system (DCS) for controlling and monitor pick-up unit work, and multiple temperature point, multiple pressure-measuring-point, multiple flow measuring point all access scattered control system and monitor.Scattered control system display frame comprises overview panel, Process flow diaphragm, grouping picture, switch/Analog control picture and alarm screen etc., all can change at any time between all pictures, for each width display frame, all defining several can key swift to operate, to realize calling and switching in system between picture, all operable keys all have corresponding prompting when operating.
Adopt this pick-up unit to detect a detection method for full-scale catalyst for denitrating flue gas, comprise the steps:
Step (1), smoke components as required regulate the flow of the nitrogen of discharging in the flow of the nitric oxide production flow of discharging in the flow of the sulphuric dioxide of discharging in the flow of the ammonia of discharging in ammonia storage tank 2, sulphuric dioxide storage tank 3, nitrogen monoxide storage tank 4, the air of discharging in air compressor machine 5 and nitrogen making machine 6 respectively;
Step (2), air and nitrogen first heated through heat interchanger 9, meanwhile, exhaust gas temperature reduces;
Step (3), the nitrogen after the air after heating, heating is passed in well heater 8 and heats together with the water vapor produced in steam generator 7, and the heating-up temperature of control heater 8 is 160 ~ 430 DEG C;
Step (4), while carrying out step (1) to (3), one that full-scale catalyst for denitrating flue gas to be detected is put into multiple reactor 11, and being warming up to temperature required to this reactor 11, multiple reactor 11 rotation uses to improve service efficiency;
Step (5), by ammonia, sulphuric dioxide, nitrogen monoxide, reacts in the reactor 11 after the air after heating, nitrogen and water vapor pass into heating;
Step (6), respectively by analyser 43 air intake branch of the reactor 11 reacted in step 5 and the smoke components gone out in gas branch pipe are analyzed and measured the concentration C of NOx in air intake branch
1with the concentration C going out NOx in gas branch pipe
2, the denitration efficiency of described full-scale catalyst for denitrating flue gas is calculated according to formula (),
Formula (one):
Wherein:
η is the denitration efficiency of full-scale catalyst for denitrating flue gas, %;
C
1for the concentration of the NOx in reactor 11 air intake branch, mg/m
3;
C
2for reactor 11 goes out the concentration of the NOx in gas branch pipe, mg/m
3.
Above the utility model is described in detail; its object is to allow the personage being familiar with this art can understand content of the present utility model and be implemented; protection domain of the present utility model can not be limited with this; all equivalences done according to Spirit Essence of the present utility model change or modify, and all should be encompassed in protection domain of the present utility model.
Claims (10)
1. a full-scale catalyst for denitrating flue gas device for detecting performance, comprises smoke modelling unit, reaction member (1), analytic unit (10), it is characterized in that:
Described reaction member (1) comprise the inlet main pipe (12) entered for simulated flue gas, female pipe of giving vent to anger of discharging for waste gas, respectively by air intake branch with go out gas branch pipe and described inlet main pipe (12) and to be connected with described female pipe of giving vent to anger and can multiple reactors (11) of rotation, described full-scale catalyst for denitrating flue gas is placed in described reactor (11);
Described smoke modelling unit comprises for providing NH
3and the ammonia storage tank (2) be connected with the inlet main pipe (12) of described reaction member (1), for providing SO
2and the sulphuric dioxide storage tank (3) be connected with the inlet main pipe (12) of described reaction member (1), for NO is provided and the nitrogen monoxide storage tank (4) be connected with the inlet main pipe (12) of described reaction member (1), for generation of the air compressor machine (5) of air, for producing N
2and the nitrogen making machine (6) be connected with described air compressor machine (5), for the well heater (8) providing the steam generator of water vapor (7), be connected with the inlet main pipe (12) of described reaction member (1), described N
2, described air and described water vapor enters the inlet main pipe (12) of described reaction member (1) after the heating of described well heater (8);
Described analytic unit (10) comprise one end portion not with the air intake branch of described inlet main pipe (12), described multiple reactors (11) and the multiple draft tube (41) going out gas branch pipe and be connected, being arranged on the multiple operation valves (42) in described multiple draft tube (41), being connected with the other end of described multiple draft tube (41) and analyser (43) for analyzing smoke components.
2. pick-up unit according to claim 1, is characterized in that: described pick-up unit also comprises the Tail gas cleanup unit for carrying out purified treatment to the waste gas of discharging in described female pipe of giving vent to anger.
3. pick-up unit according to claim 2, is characterized in that: described pick-up unit also comprises the N had for described
2the flue passed through with described air, the exhaust piping that passes through for described waste gas and the heat of described waste gas can be passed to described N
2with the heat interchanger (9) of described air, the entrance point of described flue is connected with the endpiece of described nitrogen making machine (6) with the endpiece of described air compressor machine (5), endpiece is connected with the entrance point of described well heater (8), and female pipe is connected, endpiece is connected with described Tail gas cleanup unit for entrance point and described the giving vent to anger of described exhaust piping.
4. pick-up unit according to claim 3, is characterized in that: described Tail gas cleanup unit comprises for by the NH in described waste gas
3, SO
2and SO
3the exhaust gas absorption device (31) of removing, is connected for the refrigeratory (32) of lowering the temperature to described waste gas with described exhaust gas absorption device (31) with the endpiece of described exhaust piping respectively.
5. pick-up unit according to claim 1, is characterized in that: described smoke modelling unit also comprises and to be arranged between described ammonia storage tank (2) and described reaction member (1) inlet main pipe (12) and for described NH
3the first gas mass flow controller group (21) that flow carries out regulating, to be arranged between described sulphuric dioxide storage tank (3) and the inlet main pipe (12) of described reaction member (1) and for described SO
2the second gas mass flow controller group (22) that flow carries out regulating, to be arranged between described nitrogen monoxide storage tank (4) and the inlet main pipe (12) of described reaction member (1) and for described NO flow is regulated the 3rd gas mass flow controller group (23), be arranged on the endpiece of described nitrogen making machine (6), between the endpiece of described air compressor machine (5) and described well heater (8) and for described N
2the 4th gas mass flow controller group (24) that regulates is carried out with described air mass flow.
6. pick-up unit according to claim 5, it is characterized in that: the first described gas mass flow controller group (21) comprises two gas mass flow controllers that range of adjustment is respectively 20 ~ 800ppm and 20 ~ 500ppm, the second described gas mass flow controller group (22) comprises two gas mass flow controllers that range of adjustment is respectively 0 ~ 1000ppm and 0 ~ 5500ppm, the 3rd described gas mass flow controller group (23) comprises two gas mass flow controllers that range of adjustment is respectively 20 ~ 800ppm and 20 ~ 500ppm, it is 0 ~ 325Nm that the 4th described gas mass flow controller group (24) comprises range of adjustment
3the gas mass flow controller of/h.
7. pick-up unit according to claim 1, is characterized in that: described draft tube (41) is provided with hot type SiC filtrator (44).
8. pick-up unit according to claim 1, it is characterized in that: described ammonia storage tank (2) is connected with described inlet main pipe (12) by pipeline (51), the gas outlet of described pipeline (51) is positioned on the axial line of described inlet main pipe (12), is provided with for ensureing NH in described inlet main pipe (12)
3evenly enter the mixer in described reactor (11), described mixer comprises multiple flow deflector (52) be obliquely installed.
9. pick-up unit according to claim 1, is characterized in that: described pick-up unit also comprises the scattered control system for controlling and monitor described pick-up unit work.
10. pick-up unit according to claim 9, it is characterized in that: described pick-up unit also comprises multiple temperature point, multiple pressure-measuring-point, multiple flow measuring point, described multiple temperature points, described multiple pressure-measuring-points, described multiple flow measuring points all access described scattered control system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520442863.4U CN204694693U (en) | 2015-06-25 | 2015-06-25 | A kind of full-scale catalyst for denitrating flue gas device for detecting performance |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520442863.4U CN204694693U (en) | 2015-06-25 | 2015-06-25 | A kind of full-scale catalyst for denitrating flue gas device for detecting performance |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204694693U true CN204694693U (en) | 2015-10-07 |
Family
ID=54234970
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520442863.4U Withdrawn - After Issue CN204694693U (en) | 2015-06-25 | 2015-06-25 | A kind of full-scale catalyst for denitrating flue gas device for detecting performance |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204694693U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104965050A (en) * | 2015-06-25 | 2015-10-07 | 苏州西热节能环保技术有限公司 | Full-size flue gas denitrification catalytic performance detecting device and method |
-
2015
- 2015-06-25 CN CN201520442863.4U patent/CN204694693U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104965050A (en) * | 2015-06-25 | 2015-10-07 | 苏州西热节能环保技术有限公司 | Full-size flue gas denitrification catalytic performance detecting device and method |
| CN104965050B (en) * | 2015-06-25 | 2016-10-12 | 苏州西热节能环保技术有限公司 | A kind of full-scale catalyst for denitrating flue gas device for detecting performance and detection method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104965050B (en) | A kind of full-scale catalyst for denitrating flue gas device for detecting performance and detection method | |
| CN207591613U (en) | A kind of regenerated SCR system of low-temperature SCR catalyst | |
| CN104722203B (en) | A kind of SCR denitration control system of flue gas of heating furnace and method | |
| CN203396763U (en) | Performance evaluation device for mercury removal adsorbent | |
| CN204044136U (en) | A kind of experimental provision evaluated for SCR denitrating flue gas honeybee shape catalyst activity | |
| CN102565274A (en) | Modifying method for catalyst activity in power plant SCR (selective catalytic reduction) denitration system | |
| CN207654927U (en) | A kind of coke oven flue gas desulfurization and dedusting denitration coprocessing system | |
| CN103424515A (en) | Method for detecting activity of catalyst of selective catalytic reduction (SCR) denitration system, and system thereof | |
| CN203673364U (en) | Selective catalytic reduction (SCR) denitration efficiency monitoring and controlling system for cement mill | |
| CN105510532A (en) | Denitration catalytic performance evaluation system and method | |
| CN103728994A (en) | Cement plant SCR denitration efficiency monitoring control method | |
| CN104965021A (en) | Performance evaluation device and performance evaluation method of coal-fired flue gas denitration catalyst | |
| CN204359763U (en) | Shaping SCR catalyst activation evaluating system | |
| CN107913598A (en) | A kind of municipal solid waste incinerator SCR low-temperature denitration catalyst on-line regeneration systems and its renovation process | |
| CN111398512A (en) | Catalyst performance detection system and detection method based on-site flue gas denitration device | |
| CN203405452U (en) | Catalyst activity detecting device of SCR (Selective Catalytic Reduction) de-nitration system | |
| CN108392956A (en) | Desulfurization and denitrification system and method for coke oven flue gas | |
| CN109387606A (en) | A kind of SCR denitration full-scale performance evaluation system | |
| CN206730850U (en) | A kind of desulphurization denitration dust arrester of coke oven flue gas | |
| CN103529161A (en) | Detection device and method for activity of catalyst of selective catalytic reduction method denitration system | |
| CN205787818U (en) | A kind of coal-burning power plant SCR denitration device on-line monitoring system | |
| CN203364109U (en) | SCR temperature regulating system of boiler | |
| CN204694693U (en) | A kind of full-scale catalyst for denitrating flue gas device for detecting performance | |
| CN107402278B (en) | Performance pilot-scale device of SCR denitration catalyst | |
| CN207856938U (en) | A kind of SCR catalyst situ regeneration device applied to consumer waste incineration |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20151007 Effective date of abandoning: 20161012 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |