CN110433633A - A kind of sintering machine desulfuration denitration disappears white integral control system - Google Patents
A kind of sintering machine desulfuration denitration disappears white integral control system Download PDFInfo
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- CN110433633A CN110433633A CN201910830659.2A CN201910830659A CN110433633A CN 110433633 A CN110433633 A CN 110433633A CN 201910830659 A CN201910830659 A CN 201910830659A CN 110433633 A CN110433633 A CN 110433633A
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 71
- 238000005245 sintering Methods 0.000 title claims abstract description 47
- 239000003546 flue gas Substances 0.000 claims abstract description 144
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 134
- 230000023556 desulfurization Effects 0.000 claims abstract description 45
- 239000000428 dust Substances 0.000 claims abstract description 45
- 238000000034 method Methods 0.000 claims abstract description 44
- 230000008569 process Effects 0.000 claims abstract description 35
- 238000006243 chemical reaction Methods 0.000 claims abstract description 30
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 12
- 239000012717 electrostatic precipitator Substances 0.000 claims abstract description 12
- 238000003860 storage Methods 0.000 claims abstract description 9
- 238000012544 monitoring process Methods 0.000 claims description 25
- 238000002347 injection Methods 0.000 claims description 9
- 239000007924 injection Substances 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 8
- 239000004744 fabric Substances 0.000 claims description 5
- 239000000843 powder Substances 0.000 claims description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 4
- 235000019504 cigarettes Nutrition 0.000 claims description 4
- 239000005864 Sulphur Substances 0.000 claims description 3
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 3
- 230000003247 decreasing effect Effects 0.000 claims description 2
- 239000002737 fuel gas Substances 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 238000000605 extraction Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 18
- 239000003054 catalyst Substances 0.000 description 10
- 229910021529 ammonia Inorganic materials 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 7
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 6
- 239000000908 ammonium hydroxide Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000000446 fuel Substances 0.000 description 6
- 239000003517 fume Substances 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 5
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 5
- 230000008676 import Effects 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- 238000013517 stratification Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 238000007865 diluting Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000306 component Substances 0.000 description 1
- 239000008358 core component Substances 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 206010022000 influenza Diseases 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012946 outsourcing Methods 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 230000000644 propagated effect Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
- B01D46/023—Pockets filters, i.e. multiple bag filters mounted on a common frame
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/42—Auxiliary equipment or operation thereof
- B01D46/44—Auxiliary equipment or operation thereof controlling filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/346—Controlling the process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/90—Injecting reactants
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
Abstract
Disappear white integral control system the invention discloses a kind of sintering machine desulfuration denitration, which is based on the sintering machine desulfuration denitration white integral system that disappears and realizes；The sintering machine desulfuration denitration white integral system that disappears includes SDS dry desulfurization device, electrostatic precipitator, SDA semidry process desulfurizer, bag filter, SCR denitration device and control system；The controlled end of the SDS dry desulfurization device, SDA semidry process desulfurizer and SCR denitration device is separately connected the output end of control system；The SCR denitration device includes burner, GGH heat exchanger, SCR denitration reaction device and reducing agent storage preparing device；The control system includes SDS control subsystem, SDA control subsystem, bag-type dust control subsystem, SCR control subsystem and the PLC controller being electrically connected respectively with each control subsystem.The present invention has saved energy consumption, has reduced operating cost under the premise of flue gas emission meets the discharge standard of national regulation.
Description
Technical field
The present invention relates to sintering device flue gas processing technology field, especially a kind of sintering machine desulfuration denitration disappear it is white integration control
System processed.
Background technique
Sintering machine is applied to the sintering work of large-scale iron and steel industry sintering plant, it be for down draft sintering during main body
Equipment, can be blocking by different components, varigrained concentrate powder, rich ore powder sintering, and partially removes sulphur contained in ore,
The objectionable impurities such as phosphorus.
Existing sintering machine is equipped with head electrostatic precipitator, desulfurization method of limestone-gypsum and wet cottrell
It is increasingly severe Deng related environmental protection facility, but with environmentally friendly form, the discharge index of every pollutant require it is increasingly stringent under,
Sintering machine is necessarily required to using producer to sintering machine progress denitrating flue gas, disappear white improvement, to meet the discharge standard of national regulation
Requirement.
A kind of Chinese patent CN108704463A discloses sintering flue gas desulfurization denitration, flue gas disappears white total system and
Technique, the patent realize denitrating flue gas, and flue gas disappears the purpose of Bai Yu, meet the requirement of the discharge standard of national regulation.But
Be that there are the following problems in the patent: 1) for the patent using wet desulphurization, desulphurization reaction speed is fast, but after desulfurization
Flue-gas temperature is relatively low, is unfavorable for the exhaust diffusion of flue gas, and sulfur method the problem of there is waste water, and the later period also needs
Waste water is handled, equipment investment is big, and operating cost is high；2) technical solution provided in the patent is just in single flue knot
The sintering machine of structure disappears since existing sintering machine is mostly twin flue structure if carrying out desulphurization denitration using the scheme in the patent
Bai Yu needs to increase processing equipment, implements relatively complicated, cost is relatively high；3) fume treatment is being carried out in the patent
In the process, need manually to manually control the operation and stopping of each device according to the degree of fume treatment, intelligence degree is low.
Summary of the invention
Disappear white integral control system the technical problem to be solved by the invention is to provide a kind of sintering machine desulfuration denitration, energy
Enough degree according to fume treatment improve fume treatment effect come the operation and stopping of automatic control device, reduce operating cost.
In order to solve the above technical problems, the technical solution used in the present invention is as follows.
A kind of sintering machine desulfuration denitration disappears white integral control system, the control system be based on sintering machine desulfuration denitration disappear it is white
Integral system is realized；The sintering machine desulfuration denitration white integral system that disappears includes the middle and back that sintering machine large flue is arranged in
For reducing the SO in flue gas at bellows2The SDS dry desulfurization device of concentration, setting are used at SDS dry desulfurization device rear
The electrostatic precipitator of dust, setting are at electrostatic precipitator rear for further decreasing SO in removal flue gas2The SDA of concentration is half-dried
Method desulfurizer, be arranged in SDA semidry process desulfurizer rear for reducing dust concentration bag filter, be arranged in cloth bag
Deduster rear is for reducing NO in flue gasXThe SCR denitration device of concentration and the control to work for controlling above-mentioned each device
System；The controlled end of the SDS dry desulfurization device, SDA semidry process desulfurizer and SCR denitration device is separately connected control system
The output end of system；The SCR denitration device includes for improving the burner of flue-gas temperature, for carrying out high-temperature flue gas heat
The GGH heat exchanger of recycling prepares reducing agent NH for the SCR denitration reaction device of denitrating flue gas reaction and for storage3Reduction
Agent stores preparing device, and the output end of GGH heat exchanger cold end is connected to the input terminal of burner, the output end of burner by pipeline
The input terminal of SCR denitration reaction device is connected to by pipeline, the output end of SCR denitration reaction device connects GGH heat exchange by pipeline
The output end of the input terminal in device hot end, reducing agent storage preparing device is connected to the pipeline between burner and SCR denitration reaction device
On；The control system includes the SDS control subsystem that flue gas desulfurization is carried out for controlling SDS dry desulfurization device, for controlling
SDA semidry process desulfurizer processed carries out the SDA control subsystem of flue gas desulfurization, carries out flue gas ash removal for controlling bag filter
Bag-type dust control subsystem, for control SCR denitration reaction device carry out denitrating flue gas SCR control subsystem and point
The PLC controller not being electrically connected with each control subsystem.
A kind of above-mentioned sintering machine desulfuration denitration disappears white integral control system, and the electrostatic precipitator and SDA semidry method are de-
The first main exhauster for extracting flue gas in bag filter out and the second master are separately provided on the pipeline of sulphur device connection
Exhaust fan is provided with the first flue gas flow for monitoring flue gas flow in 1# pipeline on the pipeline at the first main exhauster rear and passes
Sensor is provided with the second flue gas flow sensing for monitoring flue gas flow in 2# pipeline on the pipeline at the second main exhauster rear
The output end of device, the first flue gas flow sensor and the second flue gas flow sensor is separately connected the input terminal of PLC controller,
The output end of PLC controller is separately connected the controlled end of the first main exhauster and the second main exhauster.
A kind of above-mentioned sintering machine desulfuration denitration disappears white integral control system, and the rear of the SCR denitration device is provided with
Booster fan for flue gas to be discharged is provided with the third flue gas for monitoring flue gas flow on the pipeline at booster fan rear
Flow sensor, the input terminal of the output end connection PLC controller of third flue gas flow sensor, the output end of PLC controller
Connect the controlled end of booster fan.
A kind of above-mentioned sintering machine desulfuration denitration disappears white integral control system, and the SDS control subsystem includes setting respectively
It sets in two flue bellows for monitoring SO in flue2First SO of concentration2Concentration sensor and the 2nd SO2Concentration sensor,
It is arranged inside SDS dry desulfurization device for monitoring SO in SDS dry desulfurization device23rd SO of concentration2Concentration sensor and
SDS dry desulfurization device power input is set for opening and closing the first switch valve of SDS dry desulfurization device, the first SO2It is dense
Spend sensor, the 2nd SO2Concentration sensor and the 3rd SO2The output end of concentration sensor is separately connected the input of PLC controller
End, the controlled end of the output end connection first switch valve of PLC controller.
A kind of above-mentioned sintering machine desulfuration denitration disappears white integral control system, and the SDA control subsystem includes that setting exists
For monitoring SO in SDA semidry process desulfurizer inside SDA semidry process desulfurizer24th SO of concentration2It concentration sensor and sets
It sets and is used to open and close the second switch valve of SDA semidry process desulfurizer outlet, the 4th SO in SDA semidry process desulfurizer output end2
The input terminal of the output end connection PLC controller of concentration sensor, the output end of PLC controller connect the controlled of second switch valve
End.
A kind of above-mentioned sintering machine desulfuration denitration disappears white integral control system, and the bag-type dust control subsystem includes setting
It sets at bag filter air-out passage for monitoring the sensor of dust concentration of dust concentration at bag filter air outlet, setting
It sets the pressure valve in the injection tube inside bag filter for controlling injection tube injection pressure and is arranged in bag filter
Bottom be used to control the third switch valve of discharge dust, the output end of sensor of dust concentration connects the input of PLC controller
End, the output end of PLC controller are separately connected the controlled end of pressure valve and third switch valve.
A kind of above-mentioned sintering machine desulfuration denitration disappears white integral control system, and the SCR control subsystem includes that setting exists
GGH heat exchanger cold end is used to detect the first temperature sensor of GGH heat exchanger cold end flue-gas temperature, setting is used in burner
The second temperature sensor of fuel gas temperature after detection burner heating is arranged in SCR denitration reaction device exit for examining
Survey NOXThe NO of concentrationXConcentration sensor and GGH heat exchanger hot end is set for detecting the of GGH heat exchanger hot end flue-gas temperature
Three-temperature sensor, the first temperature sensor, second temperature sensor, third temperature sensor and NOXConcentration sensor it is defeated
Outlet is separately connected the input terminal of PLC controller, and the output end of PLC controller is separately connected GGH heat exchanger, burner and SCR
The controlled end of Benitration reactor.
Due to using above technical scheme, the invention technological progress is as follows.
The present invention can carry out fume treatment to the sintering machine of twin flue, and be carried out by PLC controller to flue gas emission
Automatically control, under the premise of flue gas emission meets the discharge standard of national regulation, saved energy consumption, reduce operation at
This.
Detailed description of the invention
Fig. 1 is the structural diagram of the present invention；
Wherein: 1.1# flue, 2.2# flue, 3.SDS dry desulfurization device, 4. electrostatic precipitator, 5. first main exhausters, 6.
Ash cellar, 10.GGH heat exchanger, 11. burnings are concentrated in two main exhausters, 7.SDA semidry process desulfurizer, 8. bag filters, 9.
Device, 12.SCR Benitration reactor, 13. booster fans, 14. chimneys, the first flue gas flow of L1. sensor, the second flue gas flow of L2.
Sensor, L3. third flue gas flow sensor, the first SO of N1.2Concentration sensor, the 2nd SO of N2.2Concentration sensor, N3. third
SO2Concentration sensor, the 4th SO of N4.2Concentration sensor, N5. sensor of dust concentration, N6.NOXConcentration sensor, K1. first
Switch valve, K2. second switch valve, K3. third switch valve, the first temperature sensor of W1., W2. second temperature sensor, W3.
Three-temperature sensor.
Specific embodiment
Below in conjunction with the drawings and specific embodiments, the present invention will be described in further detail.
A kind of sintering machine desulfuration denitration disappears white integral control system, and structure is as shown in Figure 1, include SDS dry desulfurization
Device 3, electrostatic precipitator 4, the first main exhauster 5, the second main exhauster 6, SDA semidry process desulfurizer 7, bag filter 8,
Concentrate ash cellar 9, SCR denitration device, booster fan 13, chimney 14 and control system.The setting of SDS dry desulfurization device 3 is being sintered
The middle and back of machine 1# flue 1 and 2# flue 2, for reducing the SO in flue gas2Concentration；Electrostatic precipitator 4 is set as two, respectively
It is arranged on the pipeline at the rear of SDS dry desulfurization device 3, for removing the dust in flue gas；First main exhauster 5 and second
Main exhauster 6 is separately positioned on the rear of two electrostatic precipitator 4, for extracting the flue gas in two flues of sintering machine out；SDA
The rear of the first main exhauster 5 and the second main exhauster 6 is arranged in semidry process desulfurizer 7, is used to further reduction flue gas
In SO2Concentration；The rear of SDA semidry process desulfurizer 7 is arranged in bag filter 8, for reducing dust concentration；Concentrate ash
The outlet end of bag filter 8 is arranged in storehouse 9, for collecting dust；The rear of bag filter 8 is arranged in SCR denitration device,
For reducing NO in flue gasXConcentration；The rear of SCR denitration device is arranged in booster fan 13, for flue gas to be discharged；Chimney 14
The rear of booster fan 13 is set, for being vented；Control system is used to control above-mentioned each device work, SDS dry desulfurization
The controlled end of device 3, SDA semidry process desulfurizer 7 and SCR denitration device is separately connected the output end of control system.
SCR denitration device includes burner 11, GGH heat exchanger 10, SCR denitration reaction device 12 and reducing agent storage preparation
Device.Burner 11 is used to improve flue-gas temperature, and GGH heat exchanger 10 is used to recycle high-temperature flue gas heat, SCR denitration reaction
Device 12 is used to store to prepare reducing agent NH for denitrating flue gas reaction, reducing agent storage preparing device3.10 cold end of GGH heat exchanger
Output end is connected to the input terminal of burner 11 by pipeline, and it is anti-that the output end of burner 11 by pipeline is connected to SCR denitration
The input terminal of device 12 is answered, the output end of SCR denitration reaction device 12 connects the input terminal in 10 hot end of GGH heat exchanger by pipeline, also
The output end of former agent storage preparing device is connected on the pipeline between burner 11 and SCR denitration reaction device 12.
Burner 11 by burning coke-stove gas, generate a certain amount of high-temperature flue gas, then with enter the pervious burning of denitration
Knot flue gas is directly mixed, to be lifted into the boiler smoke temperature of denitrating system.GGH heat exchanger 10 is using rotary
Gas-to-gas heat exchanger carries out indirect exchange by heat, gives the heat transfer of the high-temperature flue gas of denitration outlet to import low temperature cigarette
The fuel consumption of denitrating system hot blast stove system may be greatly reduced in gas, reduce operating cost.
SCR denitration reaction device 12 is the core component of denitrification apparatus, is mainly urged by inlet flue duct, reactor body, denitration
Agent bed and acoustic wave ash ejector composition.The top of reactor body is arranged in inlet flue duct, and spray ammonia is provided in inlet flue duct
Grid, it is ensured that the NH of flue gas and penetrating3Uniformly mixing.Reactor body is used to reaction denitration, and channel entrance is respectively provided with honeycomb screen
Grid, it is ensured that the uniformity of channel flow field.The inside of reactor body is arranged in denitrating catalyst bed, for realizing that flue gas is de-
Nitre, in conjunction with sintering flue gas temperature, dustiness, SO in this project2Concentration and integrated artistic process select high temperature type cellular
Catalyst realizes sintering flue gas denitration, it is ensured that NOXConcentration < 50mg/Nm3.Denitrating catalyst bed is arranged in acoustic wave ash ejector
Top by the way that compressed air is converted to high-power sound wave, and is propagated in space in the form of dilatational wave, makes catalyst
The dust stratification adhered on surface is fallen off by under the dilatational wave repeated action alternately changed with certain frequency because fatigue is loose, with
Flue gas stream is taken away, thus reach deashing effect, it, can be to generate reverberation effect in reactor by reasonable layout designs, it is ensured that
Without dead angle in space；In addition, the wave length of sound of acoustic wave ash ejector generation is long, amplitude is big, energy attenuation is slow, diffracting power is strong, makees
It is big with range, and catalyst will not be caused to damage, the cycle of operation and each run time of acoustic wave ash ejector can be according to operations
It needs to be adjusted, with maltilevel security alarm, it can be achieved that unattended automatic control during on-line operation.
Reducing agent stores reducing agent in preparing device and uses NH3, preparation is evaporated by 20% concentration ammonium hydroxide of outsourcing.Ammonium hydroxide is logical
Piping is delivered to tank used for storing ammonia, carries out concentration storage, and cofferdam is arranged in tank used for storing ammonia region surrounding, and ceiling and spray is arranged in top
Device a collecting-tank and a waste water pump is arranged in cofferdam, for collecting waste water and periodically sending outside；Tank used for storing ammonia mating one
Desalination water pot, is placed on outside cofferdam, and for absorbing the gas ammonia of tank used for storing ammonia discharge, the ammonium hydroxide in tank used for storing ammonia passes through 2 ammonium hydroxide
Delivery pump send ammonium hydroxide to being evaporated in ammonium hydroxide evaporator tank.
Since the flue-gas temperature come out from bag filter is unable to satisfy the temperature requirement of denitration, need to heat up to flue gas
Processing is heated up by the way of burner heating；In order to reduce the fuel consumption of burner temperature elevation system, in denitrating system
Import and export be provided with GGH heat exchanger, recycled by the high-temperature flue gas heat exported to denitration, and transfer heat to
The fuel consumption of burner temperature elevation system can be greatly reduced in the low-temperature flue gas of denitration import.Into SCR denitration device
For flue gas after GGH heat exchanger and burner, temperature reaches 280 DEG C or so, before entering denitrating catalyst, by spraying ammonia lattice
Grid spray into the reducing agent (NH after diluting into flue3), denitrating catalyst is entered back into after air-flow even distributor, in the work of catalyst
NO under, in flue gasXWith NH3Selective catalytic reduction reaction occurs, generates N2And H2O ensures the NO that denitration exports from faceXIt is dense
Spend < 50mg/Nm3。
Control system includes SDS control subsystem, SDA control subsystem, bag-type dust control subsystem, SCR control
System and PLC controller.SDS control subsystem is used to control SDS dry desulfurization device 3 and carries out flue gas desulfurization, and SDA controls subsystem
System is used to control SDA semidry process desulfurizer 7 and carries out flue gas desulfurization, and bag-type dust control subsystem is used to control bag filter
8 carry out flue gas ash removal, and SCR control subsystem is used to control SCR denitration reaction device and carries out denitrating flue gas, and PLC controller is used to
Control each control subsystem work, SDS control subsystem, SDA control subsystem, bag-type dust control subsystem and SCR control
Subsystem is electrically connected with PLC controller respectively.
SDS control subsystem includes the first SO2Concentration sensor N1, the 2nd SO2Concentration sensor N2, the 3rd SO2Concentration passes
Sensor N3 and first switch valve K1.First SO2Concentration sensor N1 and the 2nd SO2Concentration sensor N2 is separately positioned on sintering machine
In 2 bellows of 1# flue 1 and 2# flue, for monitoring the SO in 1# flue 1 and 2# flue 22Concentration；3rd SO2Concentration sensor N3
The inside of SDS dry desulfurization device 3 is set, for monitoring SO in SDS dry desulfurization device2Concentration；First switch valve K1 is set
The power input in SDS dry desulfurization device 3 is set, for opening and closing SDS dry desulfurization device 3.First SO2Concentration passes
Sensor N1, the 2nd SO2Concentration sensor N2 and the 3rd SO2The output end of concentration sensor N3 is separately connected the input of PLC controller
End, the controlled end of the output end connection first switch valve K1 of PLC controller.
First SO2Concentration sensor N1 and the 2nd SO2Concentration sensor N2 is monitored respectively in 1# flue 1 and 2# flue 2
SO2Concentration, when monitoring SO2Concentration when being more than setting value, it is dry that PLC controller control first switch valve K1 starts SDS automatically
Method desulfurizer 3, by spraying into superfine powder NaHCO into flue3Particle powder decomposes under flue-gas temperature, and in flue gas
SO2Reaction, to reduce the SO in flue gas2Concentration, as the 3rd SO2Concentration sensor N3 monitors SO2Concentration is lower than setting value
When, PLC controller controls first switch valve K1 and closes, and SDS dry desulfurization device 3 is closed, as the first SO2Concentration sensor N1 and
2nd SO2Concentration sensor N2 monitors the SO in 1# flue 1 and 2# flue 2 respectively2Concentration be lower than setting value when, be not necessarily at this time
Start SDS dry desulfurization device 3.
The first flue gas flow sensor L1 is provided on the 1# pipeline at 5 rear of the first main exhauster, for monitoring 1# pipeline
Interior flue gas flow；The second flue gas flow sensor L2 is provided on the 2# pipeline at 6 rear of the second main exhauster, for monitoring 2# pipe
Flue gas flow in road.The output end of first flue gas flow sensor L1 and the second flue gas flow sensor L2 are separately connected PLC control
The input terminal of device processed, the output end of PLC controller are separately connected the controlled end of the first main exhauster 5 and the second main exhauster 6, when
When first flue gas flow sensor L1 and the second flue gas flow sensor L2 monitors that flue gas flow is less than setting value, PLC control
Device increases the first main exhauster 5 and 6 suction pressure of the second main exhauster, improves flue gas flow, guarantees that flue gas smooth can enter
SDA semidry process desulfurizer.
SDA control subsystem includes the 4th SO2Concentration sensor N4 and second switch valve K2, the 4th SO2Concentration sensor N4
The inside of SDA semidry process desulfurizer is set, for monitoring SO in SDA semidry process desulfurizer2Concentration；Second switch valve
The output end of SDA semidry process desulfurizer is arranged in K2, for opening and closing SDA semidry process desulfurizer outlet.4th SO2
The input terminal of the output end connection PLC controller of concentration sensor N4, the output end connection second switch valve K2's of PLC controller
Controlled end.
The flue gas come out from the first main exhauster of sintering machine and the second main exhauster enters SDA semi-dry desulphurization after converging and fills
It sets, by high-speed rotating atomizer by Ca (OH)2Slurries are sufficiently atomized into small droplet, great increasing specific surface area and and cigarette
Gas comes into full contact with and reacts, and gradually evaporates during the reaction, and final desulfurization product is at solid-state dry powder-shaped.4th SO2Concentration
Sensor N4 monitors the SO in SDA semidry process desulfurizer2Concentration, as monitoring SO2Concentration > 35mg/Nm3When, PLC controller is closed
Second switch valve is closed, flue gas carries out desulfurization in SDA semidry process desulfurizer；When monitoring SO2Concentration < 35mg/Nm3When, PLC
Controller is opened second switch valve K2, SDA semidry process desulfurizer outlet side and is opened, and flue gas is exported by pipeline, into cloth bag
Deduster.
Bag-type dust control subsystem includes sensor of dust concentration N5, pressure valve and third switch valve K3, dust concentration
Sensor N5 is arranged at the air-out passage of bag filter 8, for monitoring the dust concentration at bag filter air outlet, pressure
Power valve is arranged in the injection tube inside bag filter, and for controlling injection tube injection pressure, third switch valve K3 setting exists
The bottom of bag filter excludes dust for controlling bag filter.The output end connection PLC control of sensor of dust concentration N5
The input terminal of device processed, the output end of PLC controller are separately connected the controlled end of pressure valve and third switch valve K3.
Contain solid-state desulfurization product from the flue gas after the desulfurization that SDA semidry process desulfurizer comes out, needs to enter cloth bag
It is dusted in deduster, the ash-laden gas after desulfurization enters flue gas air intake passage from the air inlet of deduster, passes through ash bucket
Into filter chamber lower part, large dust particle settles fall into ash bucket in advance here, and thinner dust is upwardly into filter chamber's absorption
It intercepts in filter bag outer surface, clean gas enters air-purifying chamber and enter air-out passage through each Off-line valve through filter bag to be discharged by blower
Atmosphere.With the progress of filtration, when the dust of filter bag surface is continuously increased, dust remover resistance is caused to rise, by deashing control
Device processed is by pressure difference setting value or time setting value, and compressed air is from air-flow distributor in order through on pulse valve and injection tube
Nozzle is sprayed to cloth bag, and pressure when blowing in filter bag rapidly rises, and expands filter bag outward rapidly, when bag wall is expanded into the limit
When position, very big tension makes it by strong impact vibration and obtains maximum opposite acceleration, thus start to contract,
The dust layer of filter bag surface is attached to not by tension force effect, due to inertia force effect and fall off from filter bag and be settled down to ash bucket,
Similarly remove the dust stratification on other filter bags.Dust in ash bucket is discharged by defeated grey equipment.
When sensor of dust concentration N5 monitors dust concentration > 10mg/Nm3When, PLC controller controls pressure valve, increases
It is blown the pressure of pipe inspection, accelerates the filtering of dust；When sensor of dust concentration N5 monitors dust concentration < 10mg/Nm3When,
Pressure valve reduces, and the flue gas after dedusting enters subsequent handling from outlet from the air outlet of bag filter.PLC controller is according to setting
The dust of bag filter bottom is fallen into the concentration ash cellar of lower section, is avoided by fixed time time opening third switch valve K3
Dust stratification in bag filter.
SCR control subsystem include the first temperature sensor W1, second temperature sensor W2, third temperature sensor W3 and
NOXConcentration sensor N6.First temperature sensor W1 setting is used to detect GGH heat exchanger cold end cigarette in 10 cold end of GGH heat exchanger
Temperature degree, second temperature sensor W2 are arranged inside burner 11, for detecting the flue-gas temperature after burner heating, third
Temperature sensor W3 is arranged in GGH heat exchanger hot end, for detecting GGH heat exchanger hot end flue-gas temperature, NOXConcentration sensor N6
The exit of SCR denitration reaction device 12 is set, for detecting the NO after denitrating flue gasXConcentration.First temperature sensor W1,
Second temperature sensor W2, third temperature sensor W3 and NOXThe output end of concentration sensor N6 is separately connected PLC controller
Input terminal, the output end of PLC controller are separately connected the controlled of GGH heat exchanger 10, burner 11 and SCR denitration reaction device 12
End.
Flue gas after desulfurization and dedusting initially enters the cold end of GGH heat exchanger 10, after GGH heat exchanger, improves flue gas
Temperature reduces the fuel consumption of burner 11.Flue gas of the GGH heat exchanger cold end after heat exchange heating enters burner 11 and heats up
After system, by heating by ignition, flue-gas temperature is further increased to 280 DEG C or so, the temperature of SCR denitration reaction device is met
It is required that.Through the qualified flue gas of heating before entering denitrating catalyst, sprayed by ammonia-spraying grid into flue after diluting also
Former agent NH3, then enter back into SCR denitration reaction device 12.Containing NH3Flue gas enter SCR denitration reaction device after, it is uniform by urging
Agent bed, under the effect of the catalyst, the NO in flue gasXWith NH3Selective catalytic reduction reaction occurs, generates N2And H2O,
Ensure the NO that denitration exports from faceXConcentration < 50mg/Nm3.High-temperature flue gas after denitration enters back into the hot end of GGH heat exchanger, leads to
Heat exchange is crossed, the low-temperature flue gas of denitration import is transferred heat to, while reducing discharge flue-gas temperature, has also recycled big portion
The heat divided, reduces the fuel consumption of burner.
First temperature sensor W1 and third temperature sensor W3 detect GGH heat exchanger cold end and GGH exchanger heat respectively
The temperature at end, when the first temperature sensor W1 detects that flue-gas temperature detects flue-gas temperature lower than third temperature sensor W3,
PLC controller opens GGH heat exchanger, and GGH heat exchanger starts to work, the heat of GGH heat exchanger cold and hot end is swapped.
Second temperature sensor W2 detects the flue-gas temperature after burner heating, when second temperature sensor W2 detects flue-gas temperature <
At 280 DEG C, PLC controller opens burner, and burner is by combustion rise flue-gas temperature, when detecting that flue-gas temperature reaches
At 280 DEG C, PLC controller control burner stops working, and reduces the fuel consumption of burner.NOXConcentration sensor N6 inspection
Survey the NO in SCR denitration reaction device exitXConcentration, when detecting NOXConcentration > 50mg/Nm3When, it is de- that PLC controller opens SCR
The work of nitre reactor, carries out denitrating flue gas, when detecting NOXConcentration < 50mg/Nm3When, PLC controller controls SCR denitration reaction
Device stops working, and the flue gas after denitration enters the hot end of GGH heat exchanger, and the flue gas after exchanging heat is given off by booster fan
It goes.
Due to increasing desulfurization, dedusting, denitrating technique and flue gas pipe network in whole system, the resistance of flue gas increases
Add, one booster fan 13 is set in the end of whole system, overcomes flue gas resistance, it is ensured that the normal operation of whole system, it is real
The smooth discharge of flue gas after existing purified treatment.
Third flue gas flow sensor L3 is provided on the pipeline at 13 rear of booster fan, for monitoring booster fan pressurization
Flue gas flow afterwards, third flue gas flow sensor L3 output end connection PLC controller input terminal, PLC controller it is defeated
The controlled end of outlet connection booster fan.Flue gas flow in third flue gas flow sensor L3 real-time monitoring pipeline, works as flue gas
When flow becomes smaller, PLC controller controls booster fan, increases the pressure of booster fan, improves the flow of flue gas, work as flue gas flow
When becoming larger, PLC controller, which controls booster fan, reduces the pressure of booster fan, reduces the flow of flue gas, finally guarantees saving
Under the premise of the energy, guarantee that flue gas is smoothly discharged.
PLC controller is based on microprocessor, centralized watch and management, and system core module redundancy configures and has certainly
Diagnostic function improves the reliability of system, disperses risk.System has functional software abundant, directly can receive or handle
Various types of input and output signals, analog input, analog output, digital quantity input, digital output, pulse are defeated
Enter, process controller is able to achieve continuous control, discrete control and sequential control function, and the picture of PLC is that operator understands production
Process provides display window, supports following a few class pictures: overview panel, grouping picture, single-point picture, trend picture, alarm
Picture, graphic picture and rod figure can be the orders according to operator according to format print report predetermined, the printing of report
Or predefined time interval carries out automatically, system to events and its times such as alarm, interlocking, the variations of operational order, as
Historical data is stored.
The present invention can carry out fume treatment to the sintering machine of twin flue, and be carried out by PLC controller to flue gas emission
Automatically control, under the premise of flue gas emission meets the discharge standard of national regulation, saved energy consumption, reduce operation at
This.
Claims (7)
- The white integral control system 1. a kind of sintering machine desulfuration denitration disappears, the control system are based on sintering machine desulfuration denitration and disappear white one Body system is realized；The sintering machine desulfuration denitration white integral system that disappears includes the middle and back wind that sintering machine large flue is arranged in For reducing the SO in flue gas at case2The SDS dry desulfurization device (3) of concentration is arranged at SDS dry desulfurization device (3) rear For removing the electrostatic precipitator (4) of dust in flue gas, being arranged at electrostatic precipitator (4) rear for further decreasing SO2It is dense The SDA semidry process desulfurizer (7) of degree is arranged at SDA semidry process desulfurizer (7) rear for reducing the cloth bag of dust concentration Deduster (8) is arranged at bag filter (8) rear for reducing NO in flue gasXThe SCR denitration device of concentration and for controlling Make the control system of above-mentioned each device work；The SDS dry desulfurization device (3), SDA semidry process desulfurizer (7) and SCR are de- The controlled end of nitre device is separately connected the output end of control system；The SCR denitration device includes for improving flue-gas temperature Burner (11), the GGH heat exchanger (10) for recycling high-temperature flue gas heat, the SCR reacted for denitrating flue gas take off Nitre reactor (12) and reducing agent NH is prepared for storage3Reducing agent store preparing device, the output of GGH heat exchanger (10) cold end End is connected to the input terminals of burner (11) by pipeline, and it is anti-that the output end of burner (11) by pipeline is connected to SCR denitration The input terminal of device (12) is answered, the output end of SCR denitration reaction device (12) connects the input in GGH heat exchanger (10) hot end by pipeline The output end at end, reducing agent storage preparing device is connected on the pipeline between burner (11) and SCR denitration reaction device (12)；Its It is characterized in that:The control system includes the SDS control subsystem for carrying out flue gas desulfurization for controlling SDS dry desulfurization device (3), uses In control SDA semidry process desulfurizer (7) carry out flue gas desulfurization SDA control subsystem, for control bag filter (8) into The bag-type dust control subsystem of row flue gas ash removal, SCR control that denitrating flue gas is carried out for controlling SCR denitration reaction device System and the PLC controller being electrically connected respectively with each control subsystem.
- The white integral control system 2. a kind of sintering machine desulfuration denitration according to claim 1 disappears, it is characterised in that: described It is separately provided on the pipeline that electrostatic precipitator (4) is connect with SDA semidry process desulfurizer (7) by cigarette in bag filter The first main exhauster (5) and the second main exhauster (6) of gas extraction, are arranged on the pipeline at the first main exhauster (5) rear useful It is set on the first flue gas flow sensor (L1) of flue gas flow in monitoring 1# pipeline, the pipeline at the second main exhauster (6) rear Be equipped with the second flue gas flow sensor (L2) for monitoring flue gas flow in 2# pipeline, the first flue gas flow sensor (L1) and The output end of second flue gas flow sensor (L2) is separately connected the input terminal of PLC controller, the output end difference of PLC controller Connect the controlled end of the first main exhauster (5) and the second main exhauster (6).
- The white integral control system 3. a kind of sintering machine desulfuration denitration according to claim 1 disappears, it is characterised in that: described The rear of SCR denitration device is provided with the booster fan (13) for flue gas to be discharged, on the pipeline at booster fan (13) rear It is provided with the third flue gas flow sensor (L3) for monitoring flue gas flow, the output end of third flue gas flow sensor (L3) Connect the input terminal of PLC controller, the controlled end of output end connection booster fan (13) of PLC controller.
- The white integral control system 4. a kind of sintering machine desulfuration denitration according to claim 1 disappears, it is characterised in that: described SDS control subsystem includes being separately positioned in two flue bellows for monitoring SO in flue2First SO of concentration2Concentration passes Sensor (N1) and the 2nd SO2Concentration sensor (N2), setting are de- for monitoring SDS dry method inside SDS dry desulfurization device (3) SO in sulphur device23rd SO of concentration2Concentration sensor (N3) and setting are used to open in SDS dry desulfurization device power input Close the first switch valve (K1) of SDS dry desulfurization device, the first SO2Concentration sensor (N1), the 2nd SO2Concentration sensor (N2) With the 3rd SO2The output end of concentration sensor (N3) is separately connected the input terminal of PLC controller, and the output end of PLC controller connects Connect the controlled end of first switch valve (K1).
- The white integral control system 5. a kind of sintering machine desulfuration denitration according to claim 1 disappears, it is characterised in that: described SDA control subsystem includes being arranged inside SDA semidry process desulfurizer for monitoring SO in SDA semidry process desulfurizer2It is dense 4th SO of degree2Concentration sensor (N4) and setting are used to open and close SDA semi-dry desulphurization in SDA semidry process desulfurizer output end The second switch valve (K2) of device outlet, the 4th SO2The input terminal of the output end connection PLC controller of concentration sensor (N4), The controlled end of output end connection second switch valve (K2) of PLC controller.
- The white integral control system 6. a kind of sintering machine desulfuration denitration according to claim 1 disappears, it is characterised in that: described Bag-type dust control subsystem includes being arranged at bag filter air-out passage for monitoring powder at bag filter air outlet The sensor of dust concentration (N5) of dust concentration is arranged in the injection tube inside bag filter for controlling injection tube jet pressure The pressure valve of power and the bottom that bag filter is arranged in are used to control the third switch valve (K3) of discharge dust, and dust concentration passes The input terminal of the output end connection PLC controller of sensor (N5), the output end of PLC controller is separately connected pressure valve and third is opened Close the controlled end of valve (K3).
- The white integral control system 7. a kind of sintering machine desulfuration denitration according to claim 1 disappears, it is characterised in that: described SCR control subsystem includes that GGH heat exchanger cold end is arranged in pass for detecting the first temperature of GGH heat exchanger cold end flue-gas temperature Sensor (W1) is arranged in burner for detecting the second temperature sensor (W2) of the fuel gas temperature after burner heats, setting It sets in SCR denitration reaction device exit for detecting NOXThe NO of concentrationXConcentration sensor (N6) and setting are in GGH exchanger heat Hold the third temperature sensor (W3) for detecting GGH heat exchanger hot end flue-gas temperature, the first temperature sensor (W1), the second temperature Spend sensor (W2), third temperature sensor (W3) and NOXThe output end of concentration sensor (N6) is separately connected PLC controller Input terminal, the output end of PLC controller are separately connected GGH heat exchanger (10), burner (11) and SCR denitration reaction device (12) Controlled end.
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| CN110433633B (en) | 2024-07-23 |
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