CN110433633B - Desulfurization, denitrification and whitening integrated control system of sintering machine - Google Patents
Desulfurization, denitrification and whitening integrated control system of sintering machine Download PDFInfo
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- CN110433633B CN110433633B CN201910830659.2A CN201910830659A CN110433633B CN 110433633 B CN110433633 B CN 110433633B CN 201910830659 A CN201910830659 A CN 201910830659A CN 110433633 B CN110433633 B CN 110433633B
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 99
- 230000023556 desulfurization Effects 0.000 title claims abstract description 99
- 238000005245 sintering Methods 0.000 title claims abstract description 41
- 230000002087 whitening effect Effects 0.000 title claims abstract description 18
- 239000000428 dust Substances 0.000 claims abstract description 79
- 238000003860 storage Methods 0.000 claims abstract description 16
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 15
- 239000012717 electrostatic precipitator Substances 0.000 claims abstract description 10
- 238000002360 preparation method Methods 0.000 claims abstract description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 133
- 239000003546 flue gas Substances 0.000 claims description 133
- 238000012544 monitoring process Methods 0.000 claims description 22
- 239000004744 fabric Substances 0.000 claims description 16
- 238000000034 method Methods 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 8
- 238000007664 blowing Methods 0.000 claims description 6
- 238000002347 injection Methods 0.000 claims description 4
- 239000007924 injection Substances 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 3
- 239000000779 smoke Substances 0.000 abstract description 22
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000003054 catalyst Substances 0.000 description 12
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 11
- 235000011114 ammonium hydroxide Nutrition 0.000 description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- 239000000446 fuel Substances 0.000 description 6
- 230000010354 integration Effects 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 239000000843 powder Substances 0.000 description 5
- 238000005507 spraying Methods 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 239000004071 soot Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 206010022000 influenza Diseases 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000000306 component Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000008358 core component Substances 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 210000003746 feather Anatomy 0.000 description 1
- 238000009851 ferrous metallurgy Methods 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 238000004519 manufacturing process 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
- 238000012545 processing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000004092 self-diagnosis Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000012719 wet electrostatic precipitator Substances 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
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- 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
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- 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
The invention discloses a desulfurization, denitrification and whitening integrated control system of a sintering machine, which is realized based on the desulfurization, denitrification and whitening integrated system of the sintering machine; the sintering machine desulfurization, denitrification and whitening integrated system comprises an SDS dry desulfurization device, an electrostatic precipitator, an SDA semi-dry desulfurization device, a bag-type dust remover, an SCR denitrification device and a control system; controlled ends of the SDS dry desulfurization device, the SDA semi-dry desulfurization device and the SCR denitration device are respectively connected with an output end of the control system; the SCR denitration device comprises a combustor, a GGH heat exchanger, an SCR denitration reactor and a reducing agent storage preparation device; the control system comprises an SDS control subsystem, an SDA control subsystem, a bag-type dust removal control subsystem, an SCR control subsystem and a PLC controller which is respectively and electrically connected with the control subsystems. On the premise that the smoke emission meets the national emission standard, the invention saves energy consumption and reduces the operation cost.
Description
Technical Field
The invention relates to the technical field of flue gas treatment of sintering machines, in particular to a desulfurization, denitrification and whitening integrated control system of a sintering machine.
Background
The sintering machine is used in sintering operation of large-scale ferrous metallurgy sintering plant, and is main equipment used in exhausting sintering process, and can sinter concentrate powder and rich ore powder with different components and different granularity into blocks and eliminate harmful impurities, such as sulfur, phosphorus, etc. contained in ore.
The existing sintering machine is provided with relevant environmental protection facilities such as a nose electrostatic precipitator, a limestone-gypsum desulfurization method, a wet electrostatic precipitator and the like, but with the gradual severity of environmental protection forms, the emission index requirements of various pollutants are stricter, and manufacturers using the sintering machine are required to perform flue gas denitration and whitening treatment on the sintering machine so as to meet the requirements of national specified emission standards.
Chinese patent CN108704463a discloses a comprehensive treatment system and process for desulfurization and denitration of sintered flue gas and whitening of flue gas, which realizes the purpose of denitration of flue gas and whitening of flue gas, and meets the requirements of national specified emission standard. However, there are several problems in this patent: 1) The patent adopts wet desulfurization, the desulfurization reaction speed is high, but the temperature of the flue gas after desulfurization is relatively low, which is not beneficial to exhaust diffusion of the flue gas, and the desulfurization method has the problems that the wastewater is required to be treated in the later stage, the equipment investment is large, and the operation cost is high; 2) The technical scheme provided by the patent is only aimed at a sintering machine with a single flue structure, and because the existing sintering machine is of a double flue structure, if the scheme in the patent is used for desulfurizing, denitrating and whitening feather, processing equipment is required to be added, the implementation is complicated, and the cost is high; 3) In this patent in carrying out flue gas treatment's in-process, need the manual work to control the operation and the stop of each device according to flue gas treatment's degree, intelligent degree is low.
Disclosure of Invention
The invention aims to solve the technical problem of providing a desulfurization, denitrification and whitening integrated control system of a sintering machine, which can automatically control the operation and stop of a device according to the flue gas treatment degree, improve the flue gas treatment effect and reduce the operation cost.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows.
The control system is realized based on the sintering machine desulfurization, denitrification and whitening integrated system; the sintering machine desulfurization, denitrification and whitening integrated system comprises an SDS dry desulfurization device, an electrostatic precipitator, an SDA semi-dry desulfurization device, a cloth bag dust remover, an SCR denitration device and a control system, wherein the SDS dry desulfurization device is arranged at the middle rear part of a large flue of a sintering machine and is used for reducing the concentration of SO 2 in flue gas; controlled ends of the SDS dry desulfurization device, the SDA semi-dry desulfurization device and the SCR denitration device are respectively connected with an output end of the control system; the SCR denitration device comprises a combustor for improving the temperature of flue gas, a GGH heat exchanger for recycling the heat of high-temperature flue gas, an SCR denitration reactor for flue gas denitration reaction and a reducing agent storage preparation device for storing and preparing reducing agent NH 3, wherein the output end of the cold end of the GGH heat exchanger is connected with the input end of the combustor through a pipeline, the output end of the combustor is connected with the input end of the SCR denitration reactor through a pipeline, the output end of the SCR denitration reactor is connected with the input end of the hot end of the GGH heat exchanger through a pipeline, and the output end of the reducing agent storage preparation device is connected with a pipeline between the combustor and the SCR denitration reactor; the control system comprises an SDS control subsystem for controlling the SDS dry desulfurization device to carry out flue gas desulfurization, an SDA control subsystem for controlling the SDA semi-dry desulfurization device to carry out flue gas desulfurization, a bag dust removal control subsystem for controlling the bag dust remover to carry out flue gas dust removal, an SCR control subsystem for controlling the SCR denitration reaction device to carry out flue gas denitration and a PLC (programmable logic controller) electrically connected with each control subsystem respectively.
Above-mentioned sintering machine desulfurization denitration white integration control system that disappears, be provided with first main air exhauster and the second main air exhauster that is used for taking out the interior flue gas of sack cleaner on the pipeline that electrostatic precipitator and SDA semi-dry desulfurization device are connected respectively, be provided with the first flue gas flow sensor that is used for monitoring the interior flue gas flow of 1# pipeline on the pipeline at first main air exhauster rear, be provided with the second flue gas flow sensor that is used for monitoring the interior flue gas flow of 2# pipeline on the pipeline at second main air exhauster rear, the input of PLC controller is connected respectively to first flue gas flow sensor and second flue gas flow sensor's output, the controlled end of first main air exhauster and second main air exhauster is connected respectively to the output of PLC controller.
Above-mentioned sintering machine SOx/NOx control white integration control system that disappears, SCR denitrification facility's rear is provided with the booster fan that is used for with flue gas exhaust, is provided with the third flue gas flow sensor that is used for monitoring flue gas flow on the pipeline at booster fan rear, and the input of PLC controller is connected to the output of third flue gas flow sensor, and the controlled end of booster fan is connected to the output of PLC controller.
Above-mentioned sintering machine SOx/NOx control removes white integration control system, SDS control subsystem is including setting up respectively in two flue bellows be used for monitoring the first SO 2 concentration sensor and the second SO 2 concentration sensor of in flue SO 2 concentration, the setting is inside to be used for monitoring the third SO 2 concentration sensor of SO 2 concentration in the SDS dry desulfurization device and the setting is used for opening and close the first ooff valve of SDS dry desulfurization device power input at the SDS dry desulfurization device, the input of PLC controller is connected respectively to first SO 2 concentration sensor, second SO 2 concentration sensor and third SO 2 concentration sensor's output, the controlled end of first ooff valve is connected to the output of PLC controller.
Above-mentioned sintering machine SOx/NOx control white integration control system that disappears, SDA control subsystem is including setting up at the inside fourth SO 2 concentration sensor that is used for monitoring the SO 2 concentration in the SDA semi-dry desulfurization device of SDA semi-dry desulfurization device and setting up the second ooff valve that is used for opening and close the SDA semi-dry desulfurization device and give vent to anger at SDA semi-dry desulfurization device output, and the input of PLC controller is connected to the output of fourth SO 2 concentration sensor, and the controlled end of second ooff valve is connected to the output of PLC controller.
Above-mentioned sintering machine SOx/NOx control and remove white integration control system, sack cleaner control subsystem is including setting up the dust concentration sensor that is used for monitoring sack cleaner air outlet department dust concentration in sack cleaner air-out passageway department, set up the pressure valve that is used for controlling jetting pipe injection pressure on the inside jetting pipe of sack cleaner and set up the third ooff valve that is used for controlling the exhaust dust in the bottom of sack cleaner, the input of PLC controller is connected to dust concentration sensor's output, the controlled end of pressure valve and third ooff valve is connected respectively to the output of PLC controller.
Above-mentioned sintering machine SOx/NOx control removes white integration control system, SCR control subsystem is including setting up at the first temperature sensor that GGH heat exchanger cold junction was used for detecting GGH heat exchanger cold junction flue gas temperature, the second temperature sensor that sets up in the combustor and is used for detecting the gas temperature after the combustor heats, the setting is used for detecting NO X concentration sensor of NO X concentration in SCR denitration reactor exit and the setting is used for detecting the third temperature sensor of GGH heat exchanger hot junction flue gas temperature at GGH heat exchanger hot junction, the input of PLC controller is connected respectively to first temperature sensor, second temperature sensor, third temperature sensor and NO X concentration sensor, the controlled end of GGH heat exchanger, combustor and SCR denitration reactor is connected respectively to the output of PLC controller.
By adopting the technical scheme, the invention has the following technical progress.
The invention can treat the flue gas of the sintering machine with double flues, and automatically control the flue gas emission through the PLC, thereby saving energy consumption and reducing operation cost on the premise that the flue gas emission meets the national specified emission standard.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
Wherein: a # 1 flue, a # 2 flue, a # 3.SDS dry desulfurization device, a # 4 electrostatic precipitator, a # 5 first main exhaust fan, a # 6 second main exhaust fan, a # 7.SDA semi-dry desulfurization device, a # 8 bag-type dust collector, a # 9 concentrated ash bin, a # 10.GGH heat exchanger, a # 11 burner, a # 12.SCR denitration reactor, a # 13 booster fan, a # 14 chimney, a # 1 first flue gas flow sensor, a # 2 second flue gas flow sensor, a # 3 third flue gas flow sensor, a N1. first SO 2 concentration sensor, a # 2 second SO 2 concentration sensor, a # N3. third SO 2 concentration sensor, a # 4 fourth SO 2 concentration sensor, a # N5. dust concentration sensor, a # 6 first NO X concentration sensor, a # K1. first switching valve, a # K2. second switching valve, a # K3. third switching valve, a # 1 first temperature sensor, a # 2 second temperature sensor, and a # W3. temperature sensor.
Detailed Description
The invention will be described in further detail with reference to the drawings and the specific embodiments.
The integrated control system for desulfurization, denitrification and whitening of the sintering machine is shown in fig. 1, and structurally comprises an SDS dry desulfurization device 3, an electrostatic precipitator 4, a first main exhaust fan 5, a second main exhaust fan 6, an SDA semi-dry desulfurization device 7, a bag-type dust collector 8, a concentrated ash bin 9, an SCR denitrification device, a booster fan 13, a chimney 14 and a control system. The SDS dry desulfurization device 3 is arranged at the middle and rear parts of the 1# flue 1 and the 2# flue 2 of the sintering machine and is used for reducing the concentration of SO 2 in the flue gas; the electrostatic dust collectors 4 are arranged in two and are respectively arranged on a pipeline behind the SDS dry desulfurization device 3 for removing dust in the flue gas; the first main exhaust fan 5 and the second main exhaust fan 6 are respectively arranged behind the two electrostatic dust collectors 4 and are used for extracting the flue gas in the two flues of the sintering machine; the SDA semi-dry desulfurization device 7 is arranged behind the first main exhaust fan 5 and the second main exhaust fan 6 and is used for further reducing the concentration of SO 2 in the flue gas; the cloth bag dust remover 8 is arranged at the rear of the SDA semi-dry desulfurization device 7 and is used for reducing dust concentration; the concentrated ash bin 9 is arranged at the outlet end of the bag-type dust collector 8 and is used for collecting dust; the SCR denitration device is arranged at the rear of the bag-type dust collector 8 and is used for reducing the concentration of NO X in the flue gas; the booster fan 13 is arranged at the rear of the SCR denitration device and is used for discharging the flue gas; the chimney 14 is arranged behind the booster fan 13 and is used for exhausting; the control system is used for controlling the operation of the devices, and the controlled ends of the SDS dry desulfurization device 3, the SDA semi-dry desulfurization device 7 and the SCR denitration device are respectively connected with the output end of the control system.
The SCR denitration device comprises a combustor 11, a GGH heat exchanger 10, an SCR denitration reactor 12 and a reducing agent storage preparation device. The combustor 11 is used for increasing the flue gas temperature, the GGH heat exchanger 10 is used for recycling high-temperature flue gas heat, the SCR denitration reactor 12 is used for flue gas denitration reaction, and the reducing agent storage and preparation device is used for storing and preparing the reducing agent NH 3. The output end of the cold end of the GGH heat exchanger 10 is connected with the input end of the burner 11 through a pipeline, the output end of the burner 11 is connected with the input end of the SCR denitration reactor 12 through a pipeline, the output end of the SCR denitration reactor 12 is connected with the input end of the hot end of the GGH heat exchanger 10 through a pipeline, and the output end of the reducing agent storage preparation device is connected with the pipeline between the burner 11 and the SCR denitration reactor 12.
The burner 11 generates a certain amount of high temperature flue gas by burning coke oven gas, and then directly mixes with the sintering flue gas before entering the denitration, thereby raising the temperature of the boiler flue gas entering the denitration system. The GGH heat exchanger 10 adopts a rotary gas-gas heat exchanger, and indirectly exchanges heat to transfer heat of high-temperature flue gas at a denitration outlet to inlet low-temperature flue gas, so that fuel consumption of a hot blast stove system of the denitration system can be greatly reduced, and running cost is reduced.
The SCR denitration reactor 12 is a core component of a denitration device, and mainly comprises an inlet flue, a reactor body, a denitration catalyst bed layer and a sound soot blower. The inlet flue is arranged above the reactor body, and an ammonia spraying grid is arranged in the inlet flue to ensure that the flue gas and sprayed NH 3 are uniformly mixed. The reactor body is used for reaction denitration, and the channel inlets are all provided with rectification grids, so that uniformity of a flow field in the channel is ensured. The denitration catalyst bed layer is arranged in the reactor body and is used for realizing flue gas denitration, and the middle and high temperature honeycomb catalyst is selected to realize the denitration of the sintering flue gas by combining the sintering flue gas temperature, the dust content, the SO 2 concentration and the whole process flow in the project, SO that the concentration of NO X is ensured to be less than 50mg/Nm 3. The sound wave soot blower is arranged at the upper part of the denitration catalyst bed layer, compressed air is converted into high-power sound waves and is transmitted in space in a form of dense waves, so that deposited ash attached to the surface of the catalyst is separated due to fatigue loosening under the repeated action of the dense waves alternately changed at a certain frequency, and is taken away along with smoke air flow, the ash removal effect is achieved, a reverberation effect can be generated in the reactor through reasonable layout design, and no dead angle in the space is ensured; in addition, the sound wave generated by the sound wave soot blower has long wavelength, large amplitude, slow energy attenuation, strong diffraction capacity and large action range, can not damage a catalyst, can adjust the operation period and each operation time of the sound wave soot blower according to operation requirements, has multiple safety alarms during on-line operation, and can realize unattended automatic control.
The reducing agent in the reducing agent storage preparation device is prepared by using NH 3 through evaporation of outsourced 20% concentration ammonia water. Ammonia water is conveyed to an ammonia water storage tank through a pipeline for centralized storage, cofferdams are arranged around the ammonia water storage tank area, a ceiling and a spraying device are arranged at the top of the ammonia water storage tank area, and a water collecting tank and a wastewater pump are arranged in the cofferdams and used for collecting wastewater and sending the wastewater out periodically; the ammonia water storage tank is matched with a desalting water tank, is placed outside the cofferdam and is used for absorbing gas ammonia discharged by the ammonia water storage tank, and ammonia water in the ammonia water storage tank is delivered into the ammonia water evaporation tank for evaporation through 2 ammonia water delivery pumps.
Because the temperature of the flue gas from the bag-type dust collector cannot meet the temperature requirement of denitration, the flue gas is required to be heated, and the temperature is raised by adopting a burner temperature raising mode; in order to reduce the fuel consumption of the combustor heating system, GGH heat exchangers are arranged at the inlet and the outlet of the denitration system, and the fuel consumption of the combustor heating system can be greatly reduced by recovering the heat of high-temperature flue gas at the denitration outlet and transmitting the heat to low-temperature flue gas at the denitration inlet. After passing through a GGH heat exchanger and a burner, the temperature of the flue gas entering the SCR denitration device reaches about 280 ℃, a diluted reducing agent (NH 3) is sprayed into a flue through an ammonia spraying grid before entering the denitration catalyst, the flue gas enters the denitration catalyst after passing through an airflow uniformly-distributing device, and under the action of the catalyst, NO X and NH 3 in the flue gas undergo selective catalytic reduction reaction to generate N 2 and H 2 O, and the concentration of NO X at a denitration outlet is ensured to be less than 50mg/Nm 3 from the surface.
The control system comprises an SDS control subsystem, an SDA control subsystem, a bag-type dust removal control subsystem, an SCR control subsystem and a PLC controller. The SDS control subsystem is used for controlling the SDS dry desulfurization device 3 to carry out flue gas desulfurization, the SDA control subsystem is used for controlling the SDA semi-dry desulfurization device 7 to carry out flue gas desulfurization, the bag dust removal control subsystem is used for controlling the bag dust remover 8 to carry out flue gas dust removal, the SCR control subsystem is used for controlling the SCR denitration reaction device to carry out flue gas denitration, the PLC controller is used for controlling each control subsystem to work, and the SDS control subsystem, the SDA control subsystem, the bag dust removal control subsystem and the SCR control subsystem are respectively electrically connected with the PLC controller.
The SDS control subsystem comprises a first SO 2 concentration sensor N1, a second SO 2 concentration sensor N2, a third SO 2 concentration sensor N3 and a first switch valve K1. The first SO 2 concentration sensor N1 and the second SO 2 concentration sensor N2 are respectively arranged in the windboxes of the 1# flue 1 and the 2# flue 2 of the sintering machine and are used for monitoring the SO 2 concentration in the 1# flue 1 and the 2# flue 2; the third SO 2 concentration sensor N3 is arranged in the SDS dry desulfurization device 3 and is used for monitoring the concentration of SO 2 in the SDS dry desulfurization device; the first switching valve K1 is provided at a power input terminal of the SDS dry desulfurization device 3 for switching on and off the SDS dry desulfurization device 3. The output ends of the first SO 2 concentration sensor N1, the second SO 2 concentration sensor N2 and the third SO 2 concentration sensor N3 are respectively connected with the input end of the PLC, and the output end of the PLC is connected with the controlled end of the first switch valve K1.
The first SO 2 concentration sensor N1 and the second SO 2 concentration sensor N2 respectively monitor the concentration of SO 2 in the 1# flue 1 and the 2# flue 2, when the monitored concentration of SO 2 exceeds a set value, the PLC controller controls the first switch valve K1 to automatically start the SDS dry desulfurization device 3, by spraying ultrafine powder NaHCO 3 particles into the flue, the powder is decomposed at the flue gas temperature and reacts with SO 2 in the flue gas, SO that the concentration of SO 2 in the flue gas is reduced, when the third SO 2 concentration sensor N3 monitors that the concentration of SO 2 is lower than the set value, the PLC controller controls the first switch valve K1 to be closed to close the SDS dry desulfurization device 3, and when the first SO 2 concentration sensor N1 and the second SO 2 concentration sensor N2 respectively monitor that the concentration of SO 2 in the 1# flue 1 and the 2# flue 2 is lower than the set value, the SDS dry desulfurization device 3 is not required to be started at the moment.
A first smoke flow sensor L1 is arranged on the 1# pipeline behind the first main exhaust fan 5 and is used for monitoring the smoke flow in the 1# pipeline; and a second smoke flow sensor L2 is arranged on the 2# pipeline behind the second main exhaust fan 6 and is used for monitoring the smoke flow in the 2# pipeline. The output ends of the first smoke flow sensor L1 and the second smoke flow sensor L2 are respectively connected with the input end of the PLC, the output end of the PLC is respectively connected with the controlled ends of the first main exhaust fan 5 and the second main exhaust fan 6, and when the smoke flow monitored by the first smoke flow sensor L1 and the second smoke flow sensor L2 is smaller than a set value, the PLC increases the exhaust pressure of the first main exhaust fan 5 and the second main exhaust fan 6, improves the smoke flow, and ensures that the smoke can smoothly enter the SDA semi-dry desulfurization device.
The SDA control subsystem comprises a fourth SO 2 concentration sensor N4 and a second switch valve K2, wherein the fourth SO 2 concentration sensor N4 is arranged in the SDA semi-dry desulfurization device and is used for monitoring the concentration of SO 2 in the SDA semi-dry desulfurization device; the second switch valve K2 is arranged at the output end of the SDA semi-dry desulfurization device and is used for opening and closing the air outlet of the SDA semi-dry desulfurization device. The output end of the fourth SO 2 concentration sensor N4 is connected with the input end of the PLC, and the output end of the PLC is connected with the controlled end of the second switch valve K2.
The flue gas coming out of the first main exhaust fan and the second main exhaust fan of the sintering machine is converged and then enters an SDA semi-dry desulfurization device, ca (OH) 2 slurry is fully atomized into small fog drops through an atomizer rotating at a high speed, the specific surface area is greatly improved, the Ca (OH) 2 slurry is fully contacted with the flue gas and reacts, the flue gas is gradually evaporated in the reaction process, and the final desulfurization product is solid dry powder. The fourth SO 2 concentration sensor N4 monitors the concentration of SO 2 in the SDA semi-dry desulfurization device, and when the concentration of SO 2 is more than 35mg/Nm 3, the PLC controller closes the second switch valve, and the flue gas is desulfurized in the SDA semi-dry desulfurization device; when the concentration of SO 2 is less than 35mg/Nm 3, the PLC controller opens the second switch valve K2, the air outlet end of the SDA semi-dry desulfurization device is opened, and the flue gas is output through a pipeline and enters the bag-type dust collector.
The cloth bag dust removal control subsystem comprises a dust concentration sensor N5, a pressure valve and a third switch valve K3, wherein the dust concentration sensor N5 is arranged at an air outlet channel of the cloth bag dust remover 8 and used for monitoring dust concentration at an air outlet of the cloth bag dust remover, the pressure valve is arranged on a blowing pipe in the cloth bag dust remover and used for controlling the blowing pipe to spray pressure, and the third switch valve K3 is arranged at the bottom of the cloth bag dust remover and used for controlling the cloth bag dust remover to remove dust. The output end of the dust concentration sensor N5 is connected with the input end of the PLC, and the output end of the PLC is respectively connected with the controlled ends of the pressure valve and the third switch valve K3.
The desulfurized flue gas from the SDA semi-dry desulfurization device contains solid desulfurization products, the solid desulfurization products need to enter a bag-type dust remover for dust removal, the desulfurized dust-containing flue gas enters a flue gas air inlet channel from an air inlet of the dust remover, enters the lower part of a filter chamber through an ash bucket, large particle dust in the flue gas inlet channel is settled in advance and falls into the ash bucket, finer dust enters the filter chamber upwards to be adsorbed and intercepted on the outer surface of the filter bag, clean gas enters a gas purifying chamber through the filter bag and enters an air outlet channel through each off-line valve, and the clean gas is discharged into the atmosphere through a fan. Along with the progress of filtering work, when the dust on the surface of the filter bag is continuously increased, the resistance of the dust remover is increased, a ash removal control device presses a difference set value or a time set value, compressed air is sprayed from an airflow distributor to a cloth bag through a pulse valve and a nozzle on a blowing pipe in sequence, the pressure in the filter bag is rapidly increased during blowing, the filter bag is rapidly expanded outwards, when the wall of the filter bag is expanded to a limit position, the filter bag is subjected to strong impact vibration and obtains maximum reverse acceleration by great tension, so that the filter bag starts to shrink inwards, a dust layer attached to the surface of the filter bag is not acted by tension, falls off from the filter bag and is settled to an ash bucket due to the action of inertia force, and accumulated ash on other filter bags is cleared. Dust in the ash bucket is discharged by ash conveying equipment.
When the dust concentration sensor N5 monitors that the dust concentration is more than 10mg/Nm 3, the PLC controls the pressure valve, so that the pressure of injection of the injection pipe is increased, and the dust filtration is accelerated; when the dust concentration sensor N5 monitors that the dust concentration is less than 10mg/Nm 3, the pressure valve is reduced, and the dust-removed flue gas is discharged from the air outlet of the bag-type dust collector to enter the subsequent process. The PLC controller opens the third switch valve K3 at regular time according to the set time, so that dust at the bottom of the bag-type dust collector falls into the concentrated dust bin below, and dust accumulation in the bag-type dust collector is avoided.
The SCR control subsystem includes a first temperature sensor W1, a second temperature sensor W2, a third temperature sensor W3, and a NO X concentration sensor N6. The first temperature sensor W1 is arranged at the cold end of the GGH heat exchanger 10 and used for detecting the smoke temperature at the cold end of the GGH heat exchanger, the second temperature sensor W2 is arranged inside the burner 11 and used for detecting the smoke temperature heated by the burner, the third temperature sensor W3 is arranged at the hot end of the GGH heat exchanger and used for detecting the smoke temperature at the hot end of the GGH heat exchanger, and the NO X concentration sensor N6 is arranged at the outlet of the SCR denitration reactor 12 and used for detecting the concentration of NO X after smoke denitration. The output ends of the first temperature sensor W1, the second temperature sensor W2, the third temperature sensor W3 and the NO X concentration sensor N6 are respectively connected with the input end of a PLC (programmable logic controller), and the output end of the PLC is respectively connected with the controlled ends of the GGH heat exchanger 10, the burner 11 and the SCR denitration reactor 12.
The flue gas after desulfurization and dust removal firstly enters the cold end of the GGH heat exchanger 10, and after passing through the GGH heat exchanger, the flue gas temperature is increased, and the fuel consumption of the burner 11 is reduced. After the flue gas of GGH heat exchanger cold junction after heat transfer intensification gets into combustor 11 intensification system, through burning intensification, further improve flue gas temperature to around 280 ℃, satisfied SCR denitration reactor's temperature requirement. Before entering the denitration catalyst, the flue gas qualified by temperature rise is sprayed with a diluted reducing agent NH 3 into a flue through an ammonia spraying grid and then enters the SCR denitration reactor 12. After the flue gas containing NH 3 enters the SCR denitration reactor, the flue gas uniformly passes through a catalyst bed layer, and under the action of a catalyst, NO X in the flue gas and NH 3 undergo selective catalytic reduction reaction to generate N 2 and H 2 O, and the concentration of NO X at a denitration outlet is ensured to be less than 50mg/Nm 3 from the surface. The high-temperature flue gas after denitration enters the hot end of the GGH heat exchanger again, and heat is transferred to the low-temperature flue gas of the denitration inlet through heat exchange, so that most of heat is recovered while the temperature of the discharged flue gas is reduced, and the fuel loss of the burner is reduced.
The first temperature sensor W1 and the third temperature sensor W3 respectively detect the temperature of the cold end and the hot end of the GGH heat exchanger, and when the first temperature sensor W1 detects that the smoke temperature is lower than the smoke temperature detected by the third temperature sensor W3, the PLC controller starts the GGH heat exchanger, the GGH heat exchanger starts to work, and the heat of the cold end and the hot end of the GGH heat exchanger is exchanged. The second temperature sensor W2 detects the flue gas temperature after the combustor heats, and when the second temperature sensor W2 detects that the flue gas temperature is less than 280 ℃, the PLC controller starts the combustor, the combustor promotes the flue gas temperature through burning, and when the detected flue gas temperature reaches 280 ℃, the PLC controller controls the combustor to stop working, so that the fuel loss of the combustor is reduced. NO X concentration sensor N6 detects NO X concentration in SCR denitration reactor exit, when detecting NO X concentration > 50mg/Nm 3, the PLC controller starts SCR denitration reactor work, carries out flue gas denitration, when detecting NO X concentration <50mg/Nm 3, the PLC controller controls SCR denitration reactor to stop working, flue gas after denitration enters the hot end of GGH heat exchanger, and flue gas after heat exchange is discharged through booster fan.
As the desulfurization, dust removal and denitration technology and the flue gas pipe network are added in the whole system, the resistance of the flue gas is greatly increased, and the tail end of the whole system is provided with the booster fan 13, so that the flue gas resistance is overcome, the normal operation of the whole system is ensured, and the smooth discharge of the flue gas after the purification treatment is realized.
A third smoke flow sensor L3 is arranged on the pipeline behind the booster fan 13 and used for monitoring the smoke flow after the booster fan is boosted, the output end of the third smoke flow sensor L3 is connected with the input end of the PLC, and the output end of the PLC is connected with the controlled end of the booster fan. And when the flue gas flow is increased, the PLC controls the booster fan to reduce the pressure of the booster fan, reduce the flow of the flue gas, and finally ensure that the flue gas is smoothly discharged on the premise of saving energy.
The PLC controller is based on a microprocessor, is used for centralized monitoring and management, is provided with a self-diagnosis function, and improves the reliability and the dispersion danger of the system. The system has rich functional software, can directly receive or process various input and output signals, analog quantity input, analog quantity output, digital quantity input, digital quantity output and pulse input, and the process controller can realize continuous control, discrete control and sequential control functions, and the picture of the PLC provides a display window for operators to know the production process, so that the following pictures are supported: the system can print reports according to a predefined format, wherein the printing of the reports is automatically performed according to the command of an operator or a predefined time interval, and events such as alarm, interlocking, change of an operation command and the like and time thereof are stored as historical data.
The invention can treat the flue gas of the sintering machine with double flues, and automatically control the flue gas emission through the PLC, thereby saving energy consumption and reducing operation cost on the premise that the flue gas emission meets the national specified emission standard.
Claims (3)
1. The control system is realized based on the sintering machine desulfurization, denitrification and whitening integrated system; the sintering machine desulfurization, denitrification and whitening integrated system comprises an SDS dry desulfurization device (3) arranged at a middle rear part bellows of a large flue of a sintering machine and used for reducing the concentration of SO 2 in flue gas, an electrostatic precipitator (4) arranged behind the SDS dry desulfurization device (3) and used for removing dust in the flue gas, an SDA semi-dry desulfurization device (7) arranged behind the electrostatic precipitator (4) and used for further reducing the concentration of SO 2, a cloth bag dust remover (8) arranged behind the SDA semi-dry desulfurization device (7) and used for reducing the concentration of dust, an SCR denitrification device arranged behind the cloth bag dust remover (8) and used for reducing the concentration of NO X in the flue gas, and a control system used for controlling the operation of the devices; the controlled ends of the SDS dry desulfurization device (3), the SDA semi-dry desulfurization device (7) and the SCR denitration device are respectively connected with the output end of the control system; the SCR denitration device comprises a combustor (11) for improving the temperature of flue gas, a GGH heat exchanger (10) for recycling the heat of high-temperature flue gas, an SCR denitration reactor (12) for flue gas denitration reaction and a reducing agent storage preparation device for storing and preparing a reducing agent NH 3, wherein the output end of the cold end of the GGH heat exchanger (10) is connected with the input end of the combustor (11) through a pipeline, the output end of the combustor (11) is connected with the input end of the SCR denitration reactor (12) through a pipeline, the output end of the SCR denitration reactor (12) is connected with the input end of the hot end of the GGH heat exchanger (10) through a pipeline, and the output end of the reducing agent storage preparation device is connected on the pipeline between the combustor (11) and the SCR denitration reactor (12); the method is characterized in that:
The control system comprises an SDS control subsystem for controlling the SDS dry desulfurization device (3) to carry out flue gas desulfurization, an SDA control subsystem for controlling the SDA semi-dry desulfurization device (7) to carry out flue gas desulfurization, a bag dust removal control subsystem for controlling the bag dust remover (8) to carry out flue gas dust removal, an SCR control subsystem for controlling the SCR denitration reaction device to carry out flue gas denitration and a PLC (programmable logic controller) electrically connected with each control subsystem respectively;
The SDS control subsystem comprises a first SO 2 concentration sensor (N1) and a second SO 2 concentration sensor (N2) which are respectively arranged in two flue bellows and used for monitoring the concentration of SO 2 in a flue, a third SO 2 concentration sensor (N3) which is arranged in a SDS dry desulfurization device (3) and used for monitoring the concentration of SO 2 in the SDS dry desulfurization device, and a first switch valve (K1) which is arranged at the power input end of the SDS dry desulfurization device and used for opening and closing the SDS dry desulfurization device, wherein the output ends of the first SO 2 concentration sensor (N1), the second SO 2 concentration sensor (N2) and the third SO 2 concentration sensor (N3) are respectively connected with the input end of a PLC (programmable logic controller), and the output end of the PLC is connected with the controlled end of the first switch valve (K1);
The SDA control subsystem comprises a fourth SO 2 concentration sensor (N4) which is arranged in the SDA semi-dry desulfurization device and used for monitoring the concentration of SO 2 in the SDA semi-dry desulfurization device, and a second switch valve (K2) which is arranged at the output end of the SDA semi-dry desulfurization device and used for opening and closing the outlet of the SDA semi-dry desulfurization device, wherein the output end of the fourth SO 2 concentration sensor (N4) is connected with the input end of a PLC (programmable logic controller), and the output end of the PLC is connected with the controlled end of the second switch valve (K2);
The cloth bag dust removal control subsystem comprises a dust concentration sensor (N5) arranged at an air outlet channel of the cloth bag dust remover and used for monitoring dust concentration at an air outlet of the cloth bag dust remover, a pressure valve arranged on a blowing pipe in the cloth bag dust remover and used for controlling the injection pressure of the blowing pipe, and a third switch valve (K3) arranged at the bottom of the cloth bag dust remover and used for controlling dust discharge, wherein the output end of the dust concentration sensor (N5) is connected with the input end of a PLC (programmable logic controller), and the output end of the PLC is respectively connected with the controlled ends of the pressure valve and the third switch valve (K3);
The SCR control subsystem comprises a first temperature sensor (W1) arranged at the cold end of the GGH heat exchanger and used for detecting the temperature of flue gas at the cold end of the GGH heat exchanger, a second temperature sensor (W2) arranged in the burner and used for detecting the temperature of the gas heated by the burner, an NO X concentration sensor (N6) arranged at the outlet of the SCR denitration reactor and used for detecting the concentration of NO X, and a third temperature sensor (W3) arranged at the hot end of the GGH heat exchanger and used for detecting the temperature of flue gas at the hot end of the GGH heat exchanger, wherein the output ends of the first temperature sensor (W1), the second temperature sensor (W2), the third temperature sensor (W3) and the NO X concentration sensor (N6) are respectively connected with the input end of the PLC, and the output end of the PLC is respectively connected with the controlled ends of the GGH heat exchanger (10), the burner (11) and the SCR denitration reactor (12).
2. The integrated desulfurization, denitrification and whitening control system of a sintering machine according to claim 1, which is characterized in that: the utility model discloses a flue gas desulfurization device, including electrostatic precipitator (4), SDA semi-dry desulfurization device (7), be provided with first main air exhauster (5) and second main air exhauster (6) that are used for taking out the interior flue gas of sack cleaner on the pipeline that electrostatic precipitator (4) and SDA semi-dry desulfurization device (7) are connected respectively, be provided with first flue gas flow sensor (L1) that is used for monitoring the interior flue gas flow of 1# pipeline on the pipeline at first main air exhauster (5) rear, be provided with second flue gas flow sensor (L2) that is used for monitoring the interior flue gas flow of 2# pipeline on the pipeline at second main air exhauster (6) rear, the input of PLC controller is connected respectively to the output of first flue gas flow sensor (L1) and second flue gas flow sensor (L2), the controlled end of first main air exhauster (5) and second main air exhauster (6) is connected respectively to the output of PLC controller.
3. The integrated desulfurization, denitrification and whitening control system of a sintering machine according to claim 1, which is characterized in that: the rear of SCR denitrification facility is provided with and is used for with flue gas exhaust booster fan (13), is provided with third flue gas flow sensor (L3) that are used for monitoring flue gas flow on the pipeline at booster fan (13) rear, and the input of PLC controller is connected to the output of third flue gas flow sensor (L3), and the controlled end of booster fan (13) is connected to the output of PLC controller.
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| CN111151108A (en) * | 2020-02-21 | 2020-05-15 | 中冶大地工程咨询有限公司 | Sintering machine head flue gas desulfurization and denitrification treatment device and treatment method thereof |
| CN112426860A (en) * | 2020-11-03 | 2021-03-02 | 福建龙兰环保科技有限公司 | Pulse bag type desulfurization and denitrification dust remover system convenient for deashing |
| CN112807978A (en) * | 2021-01-13 | 2021-05-18 | 西安热工研究院有限公司 | Pressure control system and method for wet desulphurization booster fan of thermal power generating unit |
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