CN116764436B - Cement kiln flue gas treatment equipment and treatment process - Google Patents
Cement kiln flue gas treatment equipment and treatment process Download PDFInfo
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- CN116764436B CN116764436B CN202310759927.2A CN202310759927A CN116764436B CN 116764436 B CN116764436 B CN 116764436B CN 202310759927 A CN202310759927 A CN 202310759927A CN 116764436 B CN116764436 B CN 116764436B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 111
- 239000003546 flue gas Substances 0.000 title claims abstract description 96
- 239000004568 cement Substances 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 14
- 230000008569 process Effects 0.000 title claims abstract description 11
- 239000000428 dust Substances 0.000 claims abstract description 125
- 239000003054 catalyst Substances 0.000 claims abstract description 68
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- 239000004071 soot Substances 0.000 claims abstract description 25
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 20
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 20
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 20
- 238000002347 injection Methods 0.000 claims abstract description 9
- 239000007924 injection Substances 0.000 claims abstract description 9
- 238000010531 catalytic reduction reaction Methods 0.000 claims abstract 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 78
- 239000002245 particle Substances 0.000 claims description 43
- 238000007664 blowing Methods 0.000 claims description 30
- 239000000779 smoke Substances 0.000 claims description 29
- 238000009826 distribution Methods 0.000 claims description 17
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 14
- 230000009471 action Effects 0.000 claims description 12
- 239000004480 active ingredient Substances 0.000 claims description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 10
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 claims description 10
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical compound O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 claims description 8
- 239000012752 auxiliary agent Substances 0.000 claims description 8
- 239000002808 molecular sieve Substances 0.000 claims description 8
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 8
- 229910000420 cerium oxide Inorganic materials 0.000 claims description 7
- 239000004615 ingredient Substances 0.000 claims description 7
- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 claims description 7
- 229910000831 Steel Inorganic materials 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 6
- 239000010959 steel Substances 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 claims description 4
- 229910001928 zirconium oxide Inorganic materials 0.000 claims description 4
- 239000011230 binding agent Substances 0.000 claims description 3
- 230000007062 hydrolysis Effects 0.000 claims description 3
- 238000006460 hydrolysis reaction Methods 0.000 claims description 3
- 238000002955 isolation Methods 0.000 claims description 3
- 238000000197 pyrolysis Methods 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 239000003623 enhancer Substances 0.000 claims 1
- 229910021529 ammonia Inorganic materials 0.000 abstract description 6
- 239000002956 ash Substances 0.000 description 31
- 230000000694 effects Effects 0.000 description 14
- 230000005684 electric field Effects 0.000 description 9
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 7
- 239000002585 base Substances 0.000 description 6
- 230000000903 blocking effect Effects 0.000 description 5
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 5
- 239000000292 calcium oxide Substances 0.000 description 5
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 229910052748 manganese Inorganic materials 0.000 description 4
- 239000011572 manganese Substances 0.000 description 4
- 230000002035 prolonged effect Effects 0.000 description 4
- 238000005245 sintering Methods 0.000 description 4
- 238000005299 abrasion Methods 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
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- 230000009467 reduction Effects 0.000 description 3
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- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 229910052684 Cerium Inorganic materials 0.000 description 2
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Chemical compound O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- VASIZKWUTCETSD-UHFFFAOYSA-N oxomanganese Chemical compound [Mn]=O VASIZKWUTCETSD-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 238000006479 redox reaction Methods 0.000 description 2
- 239000012744 reinforcing agent Substances 0.000 description 2
- 238000009991 scouring Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 229910052726 zirconium Inorganic materials 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- 206010008428 Chemical poisoning Diseases 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229940037003 alum Drugs 0.000 description 1
- CSDREXVUYHZDNP-UHFFFAOYSA-N alumanylidynesilicon Chemical compound [Al].[Si] CSDREXVUYHZDNP-UHFFFAOYSA-N 0.000 description 1
- RGKMZNDDOBAZGW-UHFFFAOYSA-N aluminum calcium Chemical compound [Al].[Ca] RGKMZNDDOBAZGW-UHFFFAOYSA-N 0.000 description 1
- 230000001147 anti-toxic effect Effects 0.000 description 1
- 239000000729 antidote Substances 0.000 description 1
- 229910052586 apatite Inorganic materials 0.000 description 1
- 238000010009 beating Methods 0.000 description 1
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- 230000002308 calcification Effects 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
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- 150000002500 ions Chemical class 0.000 description 1
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- LQKOJSSIKZIEJC-UHFFFAOYSA-N manganese(2+) oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[O-2].[Mn+2].[Mn+2].[Mn+2].[Mn+2] LQKOJSSIKZIEJC-UHFFFAOYSA-N 0.000 description 1
- TYTHZVVGVFAQHF-UHFFFAOYSA-N manganese(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Mn+3].[Mn+3] TYTHZVVGVFAQHF-UHFFFAOYSA-N 0.000 description 1
- GEYXPJBPASPPLI-UHFFFAOYSA-N manganese(III) oxide Inorganic materials O=[Mn]O[Mn]=O GEYXPJBPASPPLI-UHFFFAOYSA-N 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
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- 238000012544 monitoring process Methods 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- VSIIXMUUUJUKCM-UHFFFAOYSA-D pentacalcium;fluoride;triphosphate Chemical compound [F-].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O VSIIXMUUUJUKCM-UHFFFAOYSA-D 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The invention discloses a cement kiln flue gas treatment device and a treatment process, wherein the cement kiln flue gas treatment device comprises a controller, a dust remover and an SCR (selective catalytic reduction) reactor, the dust remover comprises a dust removal base shell and a pulse power supply, two sides of the dust removal base shell are respectively provided with an air inlet channel and an air outlet channel, the air outlet channel is connected with a reaction inlet of the SCR reactor, a cathode line and an anode plate are arranged between the air inlet channel and the air outlet channel, the cathode line and the anode plate are both electrically connected with an output end of the pulse power supply, one side of the anode plate is provided with an anode rapping device, the bottom of the dust removal base shell is provided with a dust removing ash bucket, at least one layer of catalyst and a soot blower arranged on one side of the catalyst are arranged in the SCR reactor, one side of the SCR reactor close to the air outlet channel is provided with an ammonia water injection device, the SCR reactor is provided with a reaction outlet and a dust collecting bucket, and the controller is respectively electrically connected with the pulse power supply, the anode rapping device, the soot blower and the ammonia injection device. The invention can efficiently treat the flue gas generated by the cement kiln and remarkably prolong the service life of equipment.
Description
Technical Field
The invention relates to the technical field of cement kiln flue gas treatment, in particular to cement kiln flue gas treatment equipment and a cement kiln flue gas treatment process.
Background
With the continuous development of industry, the pollution problem of ozone and fine particles caused by pollutants such as nitrogen oxides is increasingly prominent, the physical health is seriously threatened, the pollution problem is an environmental problem which needs to be solved currently urgently, and the emission reduction of the nitrogen oxides is an important point of pollution control and emission reduction in the next stage.
China is a large country for cement manufacture and use, and in recent years, the annual yield of cement is 23-24 hundred million tons. Coal is used as fuel in the novel dry cement production process, the discharged flue gas has large dust content and complex components, and SO 2、SO3、NOx、CO2, CO and fly ash are harmful to the environment. Wherein, NO x has the greatest harm to human body and seriously pollutes the environment. The emission of nitrogen oxides is the third-row amplifying household after thermal power generation and automobile exhaust emission, and the percentage of the emission of nitrogen oxides in the whole country is as high as 12% -15%.
The SCR denitration technology is used as the most widely and efficiently applied nitrogen oxide removal technology worldwide, and is one of the most ideal technical routes for treating nitrogen oxides in the cement industry. However, the special cement kiln has high dust concentration, and the particles of the cement kiln are irregular burrs, have small particle size and poor fluidity, are easy to form bridging, cause blocking of catalyst pore channels and micropores, cause unsmooth flue gas flow in the SCR reactor, reduce the temperature of the reactor, can not reach the reaction temperature of the catalyst, continuously reduce the temperature of the reactor along with the increase of the debugging time, particularly the long-time ash accumulation blocking, reduce the activity of the catalyst, reduce the denitration efficiency, and increase the ammonia spraying amount without obvious change; meanwhile, the high-content dust contains alkali (earth) metals, heavy metals and the like, which are easy to cause chemical poisoning of the catalyst.
Disclosure of Invention
In order to solve the problems, the technical scheme provided by the invention is as follows:
The utility model provides a cement kiln flue gas treatment facility, includes controller, dust remover and SCR reactor, the dust remover includes dust removal basal shell and pulse power supply, one side of dust removal basal shell is provided with the inlet channel, the opposite side of dust removal basal shell is provided with the passageway of giving vent to anger, give vent to anger the passageway with the reaction entry linkage of SCR reactor, the inlet channel with cathode line and anode plate between the passageway of giving vent to anger, the cathode line with the anode plate all with pulse power supply's output electricity is connected, one side of anode plate is provided with the positive pole rapping device, the bottom of dust removal basal shell is equipped with the dust hopper, be provided with at least one deck catalyst and set up in the SCR reactor soot blower of catalyst one side, the SCR reactor is close to one side of giving vent to anger the passageway is provided with ammonia water injection device, the SCR reactor is equipped with reaction outlet and collects the ash hopper, the controller respectively with pulse power supply the positive pole rapping device with ammonia water injection device electricity is connected.
The invention is further arranged that the pulse power supply is electrically connected with the high-voltage isolation switch box, the voltage output by the pulse power supply comprises a basic direct-current voltage V a and a peak pulse voltage V p, the average value of the basic direct-current voltage V a is adjustable, and the frequency and the peak value of the peak pulse voltage V p are adjustable.
The invention further provides that a smoke flow direction is arranged between the air inlet channel and the air outlet channel, the cathode line is perpendicular to the smoke flow direction, and the anode plate is parallel to the smoke flow direction.
The invention is further characterized in that a blowing ash removing device is further arranged in the dust removing base shell, the blowing ash removing device is connected with an external air compressor, the blowing direction of the blowing ash removing device is from top to bottom, and the input end of the blowing ash removing device is connected with the output end of the controller.
The invention further provides that the air inlet channel is a trapezoid supporting section steel, a distribution plate is arranged in the trapezoid supporting section steel, the diameter of an opening of the distribution plate is 65-90 mm, the aperture ratio of the distribution plate is 40-50%, a guide plate is arranged on the distribution plate, and guide vanes are arranged on the guide plate.
The invention further provides that the dust-removing ash bucket and the ash collecting bucket are both boat-shaped ash buckets, a dust-removing heater and a first thermocouple are arranged in the dust-removing ash bucket, and an insulating layer is laid on the outer layer of the dust-removing ash bucket; one side of the ash collecting hopper is provided with a steam heating pipe and a second thermocouple, and the steam heating pipe is arranged between the catalyst and the reaction outlet; the output end of the first thermocouple and the output end of the second thermocouple are both connected with the input end of the controller, and the output end of the controller is respectively connected with the input end of the dust removal heater and the input end of the steam heating pipe.
The invention further provides that a carbon monoxide detector and a dust specific resistance tester are arranged in the air inlet channel, a nitrogen oxide concentration detector, a third thermocouple and a gas pressure detector are arranged at the reaction inlet and the reaction outlet, a smoke parameter detector is arranged at the reaction outlet, a catalyst pressure detector is arranged in the SCR reactor, and the output ends of the carbon monoxide detector, the dust specific resistance tester, the nitrogen oxide concentration detector, the third thermocouple, the gas pressure detector, the smoke parameter detector and the catalyst pressure detector are all connected with the input end of the controller.
The invention is further arranged that the bottom of the dust-removing ash bucket and the bottom of the ash collecting bucket are both provided with a discharger, and a scraper is arranged below the discharger; the sootblowers include rake and sonic sootblowers.
The invention further provides that the catalyst comprises a carrier, an active ingredient, an auxiliary agent and an auxiliary ingredient; the weight percentage of the carrier is 75% -80%, the weight percentage of the active ingredient is 5% -8%, the weight percentage of the auxiliary agent is 3% -5%, and the weight percentage of the auxiliary ingredient is 10% -14%; the carrier comprises a molecular sieve; the active ingredients comprise manganese oxide and cerium oxide; the auxiliary agent comprises aluminum phosphate and zirconium oxide; the auxiliary components comprise a binder and a reinforcing agent.
The cement kiln flue gas treatment process adopts the cement kiln flue gas treatment equipment, and comprises the following steps:
Introducing cement kiln flue gas into an air inlet channel of a dust remover, mechanically removing dust from the cement kiln flue gas through a distribution plate, enabling part of flue gas particles to fall into a dust removing ash bucket along the air inlet channel, and enabling the rest of flue gas particles to uniformly enter a discharge area;
The controller drives the pulse power supply to discharge the anode plate and the cathode wire, residual smoke particles carry negative charges under the ionization action of the cathode wire, and the smoke particles carrying the negative charges are adsorbed by the anode plate; the controller periodically drives the anode rapping device and the blowing ash removing device to alternately rap and blow the anode plate, so that flue gas particles on the anode plate fall into the dust removing hopper;
The flue gas continuously enters a reaction inlet of the SCR reactor, the controller controls the ammonia water injection device to spray the flue gas, ammonia water is subjected to hydrolysis and pyrolysis reaction to generate ammonia gas, and the ammonia gas reduces nitrogen oxides in the flue gas under the action of a catalyst to generate nitrogen and water; the controller regularly operates the rake soot blower and the acoustic wave soot blower to soot the particles on the surface of the catalyst, so that the flue gas particles fall into the dust collecting hopper; the purified gas is discharged from a reaction outlet;
The controller adjusts the basic direct current voltage V a and the peak pulse voltage V p of the pulse power supply according to the dust specific resistance information fed back by the dust specific resistance tester; the controller drives the dust removal heater to work according to the temperature information fed back by the first thermocouple; the controller drives the steam heating pipe to work according to the temperature information fed back by the second thermocouple; the controller adjusts the running state of the ammonia water spraying device according to the nitrogen oxide concentration information fed back by the nitrogen oxide concentration detector; the controller controls the running state of the whole equipment according to the temperature information fed back by the third thermocouple, the pressure information fed back by the air pressure detector and the pressure information fed back by the SCR reactor inlet and outlet pressure difference information fed back by the carbon monoxide detector, the carbon monoxide concentration information fed back by the smoke parameter detector, the smoke parameter information fed back by the smoke parameter detector and the pressure information fed back by the catalyst pressure detector; the controller periodically operates the discharger to collect the flue gas particles onto the scraper.
Compared with the prior art, the technical scheme provided by the invention has the following beneficial effects:
According to the technical scheme, the cement kiln flue gas treatment equipment firstly carries out flow rate reduction and large particle blocking on cement kiln flue gas, so that the subsequent residence time of the flue gas in the equipment and the flue gas particles are smaller, and abrasion caused by scouring of the flue gas particles to cathode lines and anode plates is also reduced; the pulse power supply discharges to the cathode wire and the anode plate, so that the smoke particles are attached with negative charges under the ionization of the cathode wire, the smoke particles carrying the negative charges are attracted and captured by the anode plate, and the captured smoke particles are beaten into the ash bucket in a vibrating and blowing mode, so that main dust removal work is realized. The pulse power supply can be output and adjusted according to different flue gas conditions so as to improve the dust removal efficiency and the dust removal effect.
According to the technical scheme, the cement kiln flue gas treatment equipment continuously treats flue gas entering the SCR reactor, ammonia water is sprayed on the flue gas firstly, ammonia water is decomposed into ammonia gas at the internal high temperature, oxidation reduction reaction is carried out on the ammonia gas and nitrogen oxides in the flue gas under the action of the catalyst, nitrogen and water are generated, and in order to ensure the active contact area of the catalyst, sound waves and air blowing dust removal treatment are carried out on the catalyst regularly, so that the treatment effect on the nitrogen oxides is ensured.
The technical scheme realizes stable, efficient and safe operation of equipment through an automatic control system, and a specific operation mechanism is described in the following embodiment.
Drawings
Fig. 1 is a schematic diagram of a flue gas treatment device for a cement kiln according to an embodiment of the invention.
Fig. 2 is a schematic view of a dust collector according to an embodiment of the invention.
Fig. 3 is a schematic view of an air intake passage according to an embodiment of the present invention.
Fig. 4 is a schematic diagram of an SCR reactor according to an embodiment of the present invention.
FIG. 5 is a block diagram of an automated control system for a cement kiln flue gas treatment apparatus according to an embodiment of the present invention.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Example 1
Referring to fig. 1 to 5, the technical scheme of the invention is a cement kiln flue gas treatment device, which comprises a controller 3, a dust remover 1 and an SCR reactor 2, wherein the dust remover 1 comprises a dust removing base shell 11 and a pulse power supply 12, one side of the dust removing base shell 11 is provided with an air inlet channel 13, the other side of the dust removing base shell 11 is provided with an air outlet channel 14, the air outlet channel 14 is connected with a reaction inlet 22 of the SCR reactor 2, a cathode line 15 and an anode plate 16 are arranged between the air inlet channel 13 and the air outlet channel 14, the cathode line 15 and the anode plate 16 are electrically connected with an output end of the pulse power supply 12, one side of the anode plate 16 is provided with an anode rapping device 111, the bottom of the dust removing base shell 11 is provided with a dust hopper 112, at least one layer of catalyst 23 and a device 24 arranged on one side of the catalyst 23, one side of the SCR reactor 2 close to the air outlet channel 14 is provided with an ammonia spraying device 25, the SCR reactor 2 is provided with a reaction outlet 26 and a dust collecting hopper 27, and the controller 3, the dust hopper and the pulse power supply 111 are respectively connected with the dust-blowing device and the dust-blowing device 25.
In the above embodiment, the cement kiln flue gas treatment device includes two parts of dust removal and denitration: the physical mechanical dust removal and corona adsorption dust removal are adopted, wherein the physical mechanical dust removal utilizes the air inlet channel 13 to intercept large particles in the flue gas of the cement kiln, the large particles fall into the dust removal ash bucket 112 along the inclined guide surface of the air inlet channel 13, and meanwhile, the flow rate of the flue gas is reduced, which means that under the condition that the flue gas amount and the electric field length are unchanged, the treatment time of the flue gas in the electric field is prolonged, the abrasion caused by the scouring of the large particles in the flue gas to the cathode line 115 and the anode plate 116 is also reduced (the service life of an electric dust removal accessory is prolonged, the abrasion is particularly important under the working condition of high-concentration dust), the flue gas is ionized by the cathode line to be attached with negative charge after entering the electric field, the flue gas particles carrying the negative charge are attracted and captured by the anode plate, and the particles on the anode plate 116 are cleaned regularly by utilizing the anode vibration beating mode, so that the dust removal efficiency is greatly improved; the denitration adopts the catalyst 23 and ammonia to reduce nitrogen oxides in the flue gas, ammonia water is decomposed into ammonia at high temperature, oxidation reduction reaction is carried out on the ammonia and the nitrogen oxides in the flue gas under the action of the catalyst, nitrogen and water are generated, in order to ensure the active contact area of the catalyst, the catalyst is subjected to sound wave and blowing dust removal treatment regularly, the treatment effect on the nitrogen oxides is ensured, the flue gas particles entering the SCR reactor 2 are continuously collected by the ash collecting hopper 27, and the pollution of the gas at the discharge position to the environment is further reduced.
In the above embodiment, the controller 3 is a Programmable Logic Controller (PLC); in further embodiments, a Microcontroller (MCU) is also possible.
In the above embodiment, the ammonia water spraying device 25 is connected to an external ammonia water tank.
In this embodiment, the pulse power supply 12 is electrically connected to the high-voltage isolation switch box 121, the voltage output by the pulse power supply 12 includes a basic dc voltage V a and a peak pulse voltage V p, the average value of the basic dc voltage V a is adjustable, and the frequency and peak value of the peak pulse voltage V p are adjustable.
In the above embodiment, the output voltage of the pulse power supply 12 adopts the mode of superposition of the basic dc voltage Va and the peak pulse voltage Vp, which can enhance the spark discharge level, and is not easy to generate flashover, the pulse width of the pulse power supply 12 is only tens of microseconds, the peak time is extremely short, and is far less than the time of the charge transferred from the discharge electrode to the dust collecting electrode, so that a very high voltage can be generated instantaneously, and the flashover phenomenon is not easy to occur; the adjustability of the basic direct-current voltage V a and the peak pulse voltage V p can be well adapted to different working conditions of different coals, in the production process, the process working conditions are changed frequently, including the change of dust recycling rate, the change of the coals, the temperature and humidity, the dust concentration and the dust specific resistance are all changed continuously, which means that the average voltage and the peak voltage of the pulse power supply 12 are required to be adjusted continuously correspondingly to ensure that the emission standard is unchanged, the V a and the V p of the pulse power supply are independently controlled by two independent power supply systems, the sizes of the V a、Vp and the frequency f can be independently adjusted, and different V a、Vp and f are used for combining the operation parameters adapted to the current working conditions, for example, when the specific resistance is high, back corona is easy to appear, at the moment, the basic direct-current voltage V a can be reduced, the peak voltage V p is suppressed to back corona, and the working frequency f is increased to output power by increasing; when the concentration of flue gas dust is higher, the electric field is easy to generate flashover, at this time, the basic direct current voltage V a can be reduced, the working frequency f is reduced, the flashover limit can be effectively broken through by adjusting the peak pulse voltage V p, the flashover is reduced, the excellent adjusting capability of the pulse power supply 12 can adapt to the continuously-changing external environment, and the dust removal effect is ensured.
In the above embodiment, the pulse power supply 12 can avoid back corona, for the dc power supply, the output voltage is increased to improve the dust removal efficiency, however, for the final stage and the penultimate stage electric fields, the particle size of the dust is smaller, the specific resistance is higher, the dust is easy to be adsorbed on the dust collection plate, the dust removal effect is poorer and poorer along with the increase of the adsorbed dust, the back corona is caused, the voltage increase can cause poorer dust removal effect, and the pulse-type power supply mode can effectively avoid back corona, the output peak voltage is higher, and the dust removal effect is better; the pulse power supply 12 can improve the collection capability of dust with medium-high specific resistance, for dust with medium-low specific resistance, the corona current can be improved by improving the secondary current density in the direct current power supply, but the power consumption is increased greatly, a large part of current is wasted in an electric field, for dust with medium-high specific resistance, the back corona is easily caused to reduce the dust removal efficiency by improving the charge effect by increasing the secondary output power in the direct current power supply, the back corona can be avoided by intermittent or charging specific power supply (pulse power supply), but the basic direct current voltage V a is greatly reduced, the peak pulse voltage V p is unchanged, the dust removal efficiency is improved to be limited, the pulse power supply adopts a special excitation pulse power supply to greatly improve the pulse energy, the charge time is improved to be microsecond from millisecond level, and the peak pulse voltage V p is greatly improved on the premise of not reducing the basic direct current voltage V a, so that the dust removal effect of dust with high specific resistance is greatly improved. Studies have shown that: the pulse power supply has an enhanced dust trapping capacity of 17 times or more for PM10 or less, and is particularly suitable for a dust specific resistance section of 10 11～1013.
In this embodiment, a smoke flow direction is located between the air inlet channel 13 and the air outlet channel 14, the cathode line 15 is perpendicular to the smoke flow direction, and the anode plate 16 is parallel to the smoke flow direction.
In the above embodiment, the flue gas particles of the cement kiln are adsorbed on the anode plate 116, the anode plate 116 is parallel to the flow direction of the flue gas, so that the capturing capability of the flue gas particles can be greatly improved, and if the anode plate 116 is vertically arranged, the flue gas flows reversely and the dust collection efficiency is low.
In this embodiment, a blowing ash removing device 113 is further disposed in the dust removing base shell 11, the blowing ash removing device 113 is connected to an external air compressor, a blowing direction of the blowing ash removing device 113 is from top to bottom, and an input end of the blowing ash removing device 113 is connected to an output end of the controller 3.
In the above embodiment, in the electric field dust collecting area, the blowing ash removing device 113 is further provided, and the cleaning blind area is avoided in a single soot blowing mode by cleaning the flue gas particles in the area through the blowing ash removing device 113 and the anode rapping device 111.
In this embodiment, the air inlet channel 13 is a trapezoidal support section steel, a distribution plate 131 is disposed in the trapezoidal support section steel, the diameter of the opening of the distribution plate 131 is 65-90 mm, the aperture ratio of the distribution plate 131 is 40-50%, a guide plate 132 is mounted on the distribution plate 131, and guide vanes 133 are disposed on the guide plate 132.
In the above embodiment, the air inlet channel 13 is provided with the form of the distributing plate 131 and the guide plate 132, so that the flue gas flows through the electric field uniformly and smoothly, and is not easy to be blocked, and the two sides of the distributing plate 131 are provided with the folded edges, so that the rigidity of the air inlet channel is greatly enhanced, the air inlet channel is not deformed even under the action of quite strong vortex, and the phenomenon of air flow overflowing along the non-vertical direction of the distributing plate surface is effectively eliminated; the guide vane 133 is suspended on the guide plate 132, so that the on-site adjustment of the air flow distribution is convenient, the holes do not need to be formed in the distribution plate, and the purpose can be achieved by only changing the suspension position of the guide vane.
In this embodiment, the dust-removing hopper 112 and the dust-collecting hopper 27 are both ship-shaped hoppers, a dust-removing heater 114 and a first thermocouple 115 are disposed in the dust-removing hopper 112, and an insulation layer 116 is laid on the outer layer of the dust-removing hopper 112; a steam heating pipe 271 and a second thermocouple 272 are arranged at one side of the ash collecting hopper 27, and the steam heating pipe 271 is arranged between the catalyst 23 and the reaction outlet 22; the output end of the first thermocouple 115 and the output end of the second thermocouple 272 are both connected with the input end of the controller 3, and the output end of the controller 3 is respectively connected with the input end of the dust removal heater 114 and the input end of the steam heating pipe 271.
In the above embodiment, in order to avoid blocking caused by caking and solidification of the flue gas in the electric field, the first thermocouple 115 is disposed on the dust hopper 112 to collect the real-time temperature of the dust hopper 112, and when the temperature is lower than the preset value, the controller 3 controls the dust removal heater 114 to operate to raise the temperature of the dust hopper 112, specifically, the preset value is 5-10 ℃ higher than the dew point temperature of the flue gas.
In the above embodiment, the side of the dust hopper 112 is also provided with a manual hole and a vibrating anvil for the treatment tool of ash blocking of the hopper in an abnormal state.
In the above embodiment, in order to avoid the condensation of the flue gas particles in the SCR reactor 2, a steam heating pipe 271 and a second thermocouple 272 are disposed at one side of the ash collecting hopper 27, and when the second thermocouple 272 collects that the temperature in the SCR reactor 2 is lower than the preset value, the controller 3 controls the steam heating pipe 271 to operate to raise the temperature of the SCR reactor 2.
In this embodiment, a carbon monoxide detector 134 and a dust specific resistance detector 135 are disposed in the air intake channel 13, the reaction inlet 21 and the reaction outlet 22 are both provided with a nitrogen oxide concentration detector 211, a third thermocouple 212 and a gas pressure detector 213, the reaction outlet 22 is provided with a flue gas parameter detector 221, a catalyst pressure detector 222 is disposed in the SCR reactor 2, and the output ends of the carbon monoxide detector 134, the dust specific resistance detector 135, the nitrogen oxide concentration detector 211, the third thermocouple 212, the gas pressure detector 213, the flue gas parameter detector 221 and the catalyst pressure detector 222 are all connected with the input end of the controller 3.
In the above embodiment, the warning value of the carbon monoxide concentration is preset, and when the carbon monoxide detector 134 detects that the carbon monoxide concentration exceeds the warning value, the equipment is shut down; the controller adjusts the output voltage of the pulse power supply 12 (refer to the adjustment mode of the pulse power supply) according to the dust specific resistance information fed back by the dust specific resistance measuring instrument 135, so as to improve the dust removal efficiency; presetting a differential pressure warning value of a reaction inlet and outlet of the SCR reactor 2, wherein the change of the differential pressure is an important parameter for judging whether the catalyst deposits ash or not, determining whether a soot blowing system needs to be used or not, and stopping the device to carry out soot cleaning maintenance or catalyst replacement treatment on the inside of the SCR when the differential pressure fed back by the air pressure detector 213 exceeds the differential pressure warning value; and presetting an exhaust smoke warning value, and overhauling and maintaining the dust remover 1 and a dust removing mechanism inside the SCR reactor when the parameters fed back by the smoke parameter detector 221 exceed the exhaust smoke warning value.
In this embodiment, the bottom of the dust hopper 112 and the bottom of the dust collecting hopper 27 are both provided with a discharger 4, and a scraper 5 is provided below the discharger 4.
In the above embodiment, when the dust in the dust hopper 112 and the collecting hopper 27 is collected to a certain amount, the controller 3 opens the corresponding discharger 4 to transfer.
In this embodiment, the sootblowers include a rake sootblower 24 and a sonic sootblower 26.
In this embodiment, the catalyst includes a support, an active ingredient, an auxiliary agent, and an auxiliary ingredient; the weight percentage of the carrier is 75% -80%, the weight percentage of the active ingredient is 5% -8%, the weight percentage of the auxiliary agent is 3% -5%, and the weight percentage of the auxiliary ingredient is 10% -14%; the carrier comprises a molecular sieve; the active ingredients comprise manganese oxide and cerium oxide; the auxiliary agent comprises aluminum phosphate and zirconium oxide; the auxiliary components comprise a binder and a reinforcing agent.
In the above embodiment, the molar ratio of manganese element to cerium element in the active ingredient is 1:1.5-1.9; the manganese oxide is at least one of manganese monoxide, manganese dioxide, manganese sesquioxide and manganese tetraoxide; the cerium oxide is at least one of cerium oxide and cerium oxide; the molecular sieve is at least two of a ZMS-5 molecular sieve, a ZSM-11 molecular sieve and a 13X molecular sieve, and the silicon-aluminum ratio of the molecular sieve is not less than 400:1.
In the embodiment, the catalyst is added with the manganese oxide and the cerium oxide serving as active ingredients, wherein the addition of the manganese element can improve the activity, poisoning resistance, sintering resistance and shedding resistance of the catalyst, so that the denitration efficiency and the service life of the denitration catalyst are improved, ceO 2 has good oxygen storage and release capacities, and the addition of the cerium element can improve the concentration of oxygen on the surface of the catalyst and the thermal stability of the carrier, so that the acidification of the active ingredients of the catalyst is effectively inhibited.
In the embodiment, aluminum phosphate and zirconium oxide are added into the catalyst, wherein zirconium element can improve the thermal stability and corrosion resistance of the catalyst, and meanwhile, the zirconium element and manganese element are synergistic to improve the activity, the poisoning resistance and the sintering resistance of the catalyst; the aluminum phosphate can inhibit the contact between CaO and active sites on the catalyst, specifically, the aluminum phosphate can form high-melting-point compound apatite (Ca 3(PO4)2) with calcification, and the aluminum phosphate can combine with calcium ions in calcium oxide to form insoluble aluminum-calcium alum (CaAl 2O4) and other compounds, so that the calcium oxide is prevented from further corroding the surface of the denitration catalyst, and the service life and the calcium resistance of the catalyst are prolonged. In addition, the aluminum phosphate can also form a layer of protective film on the surface of the denitration catalyst, so that calcium oxide is prevented from further corroding the surface of the catalyst, and the stability and the calcium resistance of the catalyst are improved.
In the above examples, the activity of the catalyst was improved: manganese can increase the number of active sites of the denitration catalyst and improve the catalytic activity of the catalyst; antidote: manganese can reduce the poisoning effect of hardness ions such as calcium oxide on the denitration catalyst, so that the antitoxic performance of the catalyst is improved; anti-sintering: the manganese can promote the uniform dispersion of active components in the denitration catalyst and prevent the catalyst from sintering, thereby prolonging the service life of the catalyst; anti-falling: the manganese can enhance the mechanical strength of the denitration catalyst, prevent the catalyst from falling off and improve the stability of the catalyst.
In the embodiment, in order to better study the influence of the deposition hardening of the fly ash on the surface of the catalyst on the formation of strong scale, the conventional soot blowing technology is improved, and finally, the acoustic wave soot blower and rake soot blower combined technology is innovatively used aiming at the characteristics of the cement dust kiln, and the compressed air for soot blowing is heated to more than 150 ℃, so that the soot blowing effect is good, and the project running time is effectively prolonged.
In the embodiment, the control system can complete all the functions of measurement, monitoring, operation, automatic control, alarm, protection, linkage, recording and the like in the whole denitration device. According to the NO x concentration at the inlet and the outlet of the SCR reactor, the denitration efficiency and other requirements, the automatic control of ammonia water supply and the operation of the SCR reactor is realized, and key parameters are monitored.
Example 2
The technical scheme of the invention is a cement kiln flue gas treatment process, which adopts the cement kiln flue gas treatment equipment described in the embodiment 1 and comprises the following steps:
Introducing cement kiln flue gas into an air inlet channel of a dust remover, mechanically removing dust from the cement kiln flue gas through a distribution plate, enabling part of flue gas particles to fall into a dust removing ash bucket along the air inlet channel, and enabling the rest of flue gas particles to uniformly enter a discharge area;
The controller drives the pulse power supply to discharge the anode plate and the cathode wire, residual smoke particles carry negative charges under the ionization action of the cathode wire, and the smoke particles carrying the negative charges are adsorbed by the anode plate; the controller periodically drives the anode rapping device and the blowing ash removing device to alternately rap and blow the anode plate, so that flue gas particles on the anode plate fall into the dust removing hopper;
The flue gas continuously enters a reaction inlet of the SCR reactor, the controller controls the ammonia water injection device to spray the flue gas, ammonia water is subjected to hydrolysis and pyrolysis reaction to generate ammonia gas, and the ammonia gas reduces nitrogen oxides in the flue gas under the action of a catalyst to generate nitrogen and water; the controller regularly operates the rake soot blower and the acoustic wave soot blower to soot the particles on the surface of the catalyst, so that the flue gas particles fall into the dust collecting hopper; the purified gas is discharged from a reaction outlet;
The controller adjusts the basic direct current voltage V a and the peak pulse voltage V p of the pulse power supply according to the dust specific resistance information fed back by the dust specific resistance tester; the controller drives the dust removal heater to work according to the temperature information fed back by the first thermocouple; the controller drives the steam heating pipe to work according to the temperature information fed back by the second thermocouple; the controller adjusts the running state of the ammonia water spraying device according to the nitrogen oxide concentration information fed back by the nitrogen oxide concentration detector; the controller controls the running state of the whole equipment according to the temperature information fed back by the third thermocouple, the pressure information fed back by the air pressure detector and the pressure information fed back by the SCR reactor inlet and outlet pressure difference information fed back by the carbon monoxide detector, the carbon monoxide concentration information fed back by the smoke parameter detector, the smoke parameter information fed back by the smoke parameter detector and the pressure information fed back by the catalyst pressure detector; the controller periodically operates the discharger to collect the flue gas particles onto the scraper.
It should also be noted that in this specification, relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising one … …" does not exclude the presence of other like elements in a process, method, article, or apparatus that comprises the element.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (9)
1. The cement kiln flue gas treatment equipment is characterized by comprising a controller, a dust remover and an SCR (selective catalytic reduction) reactor, wherein the dust remover comprises a dust removal base shell and a pulse power supply, one side of the dust removal base shell is provided with an air inlet channel, the other side of the dust removal base shell is provided with an air outlet channel, the air outlet channel is connected with a reaction inlet of the SCR reactor, a cathode wire and an anode plate are arranged between the air inlet channel and the air outlet channel, the cathode wire and the anode plate are both electrically connected with an output end of the pulse power supply, one side of the anode plate is provided with an anode rapping device, the bottom of the dust removal base shell is provided with a dust removal hopper, at least one layer of catalyst and a soot blower arranged on one side of the catalyst are arranged in the SCR reactor, and the catalyst comprises a carrier, an active ingredient, an auxiliary ingredient and an auxiliary ingredient; the weight percentage of the carrier is 75% -80%, the weight percentage of the active ingredient is 5% -8%, the weight percentage of the auxiliary agent is 3% -5%, and the weight percentage of the auxiliary ingredient is 10% -14%; the carrier comprises a molecular sieve; the active ingredients comprise manganese oxide and cerium oxide; the auxiliary agent comprises aluminum phosphate and zirconium oxide; the auxiliary components comprise a binder and an enhancer, an ammonia water injection device is arranged on one side, close to the air outlet channel, of the SCR reactor, a reaction outlet and an ash collecting hopper are arranged on the SCR reactor, and the controller is respectively and electrically connected with the pulse power supply, the anode rapping device, the soot blower and the ammonia water injection device.
2. The cement kiln flue gas treatment device according to claim 1, wherein the pulse power supply is electrically connected with the high-voltage isolation switch box, the voltage output by the pulse power supply comprises a basic direct-current voltage V a and a peak pulse voltage V p, the average value of the basic direct-current voltage V a is adjustable, and the frequency and the peak value of the peak pulse voltage V p are adjustable.
3. A cement kiln flue gas treatment device according to claim 2, wherein a flue gas flow direction is between the inlet channel and the outlet channel, the cathode line is perpendicular to the flue gas flow direction, and the anode plate is parallel to the flue gas flow direction.
4. The cement kiln flue gas treatment device according to claim 3, wherein a blowing ash removing device is further arranged in the dust removing base shell, the blowing ash removing device is connected with an external air compressor, the blowing direction of the blowing ash removing device is from top to bottom, and the input end of the blowing ash removing device is connected with the output end of the controller.
5. The cement kiln flue gas treatment device according to claim 4, wherein the air inlet channel is a trapezoid support section steel, a distribution plate is arranged in the trapezoid support section steel, the diameter of an opening of the distribution plate is 65-90 mm, the aperture ratio of the distribution plate is 40-50%, a guide plate is arranged on the distribution plate, and guide vanes are arranged on the guide plate.
6. The cement kiln flue gas treatment device according to claim 5, wherein the dust-removing ash bucket and the ash collecting bucket are both ship-shaped ash buckets, a dust-removing heater and a first thermocouple are arranged in the dust-removing ash bucket, and an insulating layer is coated on the outer layer of the dust-removing ash bucket; one side of the ash collecting hopper is provided with a steam heating pipe and a second thermocouple, and the steam heating pipe is arranged between the catalyst and the reaction outlet; the output end of the first thermocouple and the output end of the second thermocouple are both connected with the input end of the controller, and the output end of the controller is respectively connected with the input end of the dust removal heater and the input end of the steam heating pipe.
7. The cement kiln flue gas treatment device according to claim 6, wherein a carbon monoxide detector and a dust specific resistance detector are arranged in the air inlet channel, a nitrogen oxide concentration detector, a third thermocouple and a gas pressure detector are arranged at the reaction inlet and the reaction outlet, a flue gas parameter detector is arranged at the reaction outlet, a catalyst pressure detector is arranged in the SCR reactor, and the output ends of the carbon monoxide detector, the dust specific resistance detector, the nitrogen oxide concentration detector, the third thermocouple, the gas pressure detector, the flue gas parameter detector and the catalyst pressure detector are all connected with the input end of the controller.
8. The cement kiln flue gas treatment device according to claim 7, wherein the bottom of the dust removal hopper and the bottom of the dust collection hopper are both provided with a discharger, a scraper is arranged below the discharger, an input end of the discharger is connected with an output end of the controller, and the soot blower comprises a rake soot blower and a sonic soot blower.
9. A cement kiln flue gas treatment process, characterized in that the cement kiln flue gas treatment device according to claim 8 is adopted, comprising:
Introducing cement kiln flue gas into an air inlet channel of a dust remover, mechanically removing dust from the cement kiln flue gas through a distribution plate, enabling part of flue gas particles to fall into a dust removing ash bucket along the air inlet channel, and enabling the rest of flue gas particles to uniformly enter a discharge area;
The controller drives the pulse power supply to discharge the anode plate and the cathode wire, residual smoke particles carry negative charges under the ionization action of the cathode wire, and the smoke particles carrying the negative charges are adsorbed by the anode plate; the controller periodically drives the anode rapping device and the blowing ash removing device to alternately rap and blow the anode plate, so that flue gas particles on the anode plate fall into the dust removing hopper;
The flue gas continuously enters a reaction inlet of the SCR reactor, the controller controls the ammonia water injection device to spray the flue gas, ammonia water is subjected to hydrolysis and pyrolysis reaction to generate ammonia gas, and the ammonia gas reduces nitrogen oxides in the flue gas under the action of a catalyst to generate nitrogen and water; the controller regularly operates the rake soot blower and the acoustic wave soot blower to soot the particles on the surface of the catalyst, so that the flue gas particles fall into the dust collecting hopper; the purified gas is discharged from a reaction outlet;
The controller adjusts the basic direct current voltage V a and the peak pulse voltage V p of the pulse power supply according to the dust specific resistance information fed back by the dust specific resistance tester; the controller drives the dust removal heater to work according to the temperature information fed back by the first thermocouple; the controller drives the steam heating pipe to work according to the temperature information fed back by the second thermocouple; the controller adjusts the running state of the ammonia water spraying device according to the nitrogen oxide concentration information fed back by the nitrogen oxide concentration detector; the controller controls the running state of the whole equipment according to the temperature information fed back by the third thermocouple, the pressure information fed back by the air pressure detector and the pressure information fed back by the SCR reactor inlet and outlet pressure difference information fed back by the carbon monoxide detector, the carbon monoxide concentration information fed back by the smoke parameter detector, the smoke parameter information fed back by the smoke parameter detector and the pressure information fed back by the catalyst pressure detector; the controller periodically operates the discharger to collect the flue gas particles onto the scraper.
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