CN109603539A - A kind of industrial smoke high temperature desulfurizing denitration dust removal system and its processing method - Google Patents
A kind of industrial smoke high temperature desulfurizing denitration dust removal system and its processing method Download PDFInfo
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- CN109603539A CN109603539A CN201910085786.4A CN201910085786A CN109603539A CN 109603539 A CN109603539 A CN 109603539A CN 201910085786 A CN201910085786 A CN 201910085786A CN 109603539 A CN109603539 A CN 109603539A
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- tower
- flue gas
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- 230000003009 desulfurizing effect Effects 0.000 title claims abstract description 114
- 239000000428 dust Substances 0.000 title claims abstract description 37
- 239000000779 smoke Substances 0.000 title claims abstract description 26
- 238000003672 processing method Methods 0.000 title claims abstract description 9
- 239000000919 ceramic Substances 0.000 claims abstract description 146
- 239000007789 gas Substances 0.000 claims abstract description 106
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 83
- 238000005496 tempering Methods 0.000 claims abstract description 79
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 60
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000003546 flue gas Substances 0.000 claims description 161
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 158
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 92
- 239000000920 calcium hydroxide Substances 0.000 claims description 91
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 91
- 238000006477 desulfuration reaction Methods 0.000 claims description 51
- 238000006243 chemical reaction Methods 0.000 claims description 46
- 230000023556 desulfurization Effects 0.000 claims description 46
- 239000003054 catalyst Substances 0.000 claims description 14
- 238000001914 filtration Methods 0.000 claims description 10
- 238000000034 method Methods 0.000 claims description 10
- 239000000126 substance Substances 0.000 claims description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 9
- 235000019504 cigarettes Nutrition 0.000 claims description 9
- 239000002699 waste material Substances 0.000 claims description 9
- 230000001351 cycling effect Effects 0.000 claims description 8
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 6
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 6
- 239000000835 fiber Substances 0.000 claims description 6
- 239000003517 fume Substances 0.000 claims description 6
- 239000004571 lime Substances 0.000 claims description 6
- 230000008569 process Effects 0.000 claims description 6
- 239000011575 calcium Substances 0.000 claims description 5
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 239000005864 Sulphur Substances 0.000 claims description 3
- 229910052573 porcelain Inorganic materials 0.000 claims description 3
- 239000002244 precipitate Substances 0.000 claims description 3
- 230000001939 inductive effect Effects 0.000 claims 1
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 claims 1
- 239000002918 waste heat Substances 0.000 abstract description 10
- 238000012545 processing Methods 0.000 abstract description 7
- 239000010419 fine particle Substances 0.000 abstract description 6
- 230000000903 blocking effect Effects 0.000 abstract description 4
- 235000011116 calcium hydroxide Nutrition 0.000 description 69
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 13
- 230000002378 acidificating effect Effects 0.000 description 12
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 12
- 230000003197 catalytic effect Effects 0.000 description 11
- 239000002245 particle Substances 0.000 description 10
- 239000000463 material Substances 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 229910052717 sulfur Inorganic materials 0.000 description 7
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 6
- 239000003344 environmental pollutant Substances 0.000 description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- 239000011593 sulfur Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 230000008859 change Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 5
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 229910052925 anhydrite Inorganic materials 0.000 description 4
- 239000001110 calcium chloride Substances 0.000 description 4
- 229910001628 calcium chloride Inorganic materials 0.000 description 4
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 4
- 238000006722 reduction reaction Methods 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 3
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 3
- 229910001634 calcium fluoride Inorganic materials 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 238000009792 diffusion process Methods 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000005530 etching Methods 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910052681 coesite Inorganic materials 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- 229910052906 cristobalite Inorganic materials 0.000 description 2
- 239000003500 flue dust Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 150000004767 nitrides Chemical class 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 238000005453 pelletization Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 229910052682 stishovite Inorganic materials 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 229910052905 tridymite Inorganic materials 0.000 description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 230000035568 catharsis Effects 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000005367 electrostatic precipitation Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- -1 flue gas alkali metal Chemical class 0.000 description 1
- 238000003682 fluorination reaction Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 210000004602 germ cell Anatomy 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- 238000002513 implantation Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000002075 main ingredient Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
Classifications
-
- 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
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- 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
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
-
- 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
- B01D53/76—Gas phase processes, e.g. by using aerosols
-
- 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
- B01D53/8603—Removing sulfur compounds
- B01D53/8609—Sulfur oxides
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
It further include by the sequentially connected desulfurizing tower of pipeline, whirlwind tower, quenched unit, ceramic integrated unit the invention discloses a kind of industrial smoke high temperature desulfurizing denitration dust removal system, including UTILIZATION OF VESIDUAL HEAT IN unit；Wherein, desulfurizing tower includes desulfurizing tower and the pipeline that is connected with desulfurizing tower；Whirlwind tower includes whirlwind tower and the pipeline that is connected with whirlwind tower；Quenched unit includes feeding tower, tempering tower, ammonia reservoir, water reservoir；Ceramic integrated unit includes multiple and ceramic catalytic reaction kettle even.This system integrates a variety of processing functions, and the concentration of SO2, NOX, fine particle can be effectively reduced；Invention also provides a kind of processing methods of industrial smoke high temperature desulfurizing denitration dust collecting can corrode to avoid the waste heat boiler of middle low-temperature zone, the blocking of pipeline, equipment etc. in conjunction with integrated apparatus of the invention, improve the service life and operation stability of device.The exhaust gas such as the good mutually standby realization desulphurization denitration dedusting of system are continuously uninterruptedly handled.
Description
Technical field
The present invention relates to environment protection fields, and in particular to a kind of industrial smoke high temperature desulfurizing denitration dust removal system and its processing side
Method.
Background technique
The concern of environmental protection was continuously improved in China in recent years, and respective standard is also being continuously improved.Some industrial productions
Discharge standard must be reached by, which discharging pollutants, can just discharge.Main ingredient is fine particle, SO in the flue gas of industrial discharge2、
NOXDeng, the industries kiln such as glass burning petroleum is burnt or the flue gas of other fossil fuel discharges have sulfur content it is high, containing fluorination
Object, pollutant are complicated and have the characteristics that stickum, cause environmental protection treatment to reach preferable purification standard extremely difficult.
It is traditional desulphurization denitration dust removal process technique that the processing of kiln gas, which experienced the first kind: the flue gas of kiln discharge
At 500 DEG C or more, temperature is quenched into tempering tower progress between 350-400 DEG C after progress level-one UTILIZATION OF VESIDUAL HEAT IN first, quenched
Afterwards enter electric precipitator in be dusted, temperature is down to 330-380 DEG C after dedusting, into SCR denitration tower carry out denitration, then into
Row second level Heat Treatment, the temperature after second level Heat Treatment are down to 200 DEG C or so, carry out desulfurization into desulfurizing tower, desulfurization is laggard
Enter bag filter to be dusted, chimney is finally introduced by air-introduced machine and is excluded, temperature when discharge is 50-70 DEG C.
Electrostatic precipitation is carried out in temperature higher stage in above-mentioned traditional process, and efficiency of dust collection is low, and flue dust is usually in 50-
100mg/m3More than, subsequent SCR, which can be blocked, containing the harmful substances such as alkali metal and other heavy metals in the flue dust of high concentration takes off
Nitre tower, at the same make denitrating catalyst be poisoned in various degree reduce denitration effect increase the escaping of ammonia, this makes the service life of catalyst
Only 1 to two years；There is no the exhaust gas of desulfurization to contain a large amount of SO2Equal highly acids etchant gas and the ammonia of escape form hydrogen sulfate
Ammonium causes waste heat boiler and system pipeline seriously corroded, so that boiler and pipeline service life is short is usually no more than 1 year, is safeguarded
At high cost, system is unable to safe and stable operation；Bag-type dust can only achieve 30-50mg/m3, and the service life of cloth bag is usual
No more than 2 years；Traditional processing unit takes up a large area, and the discharge of final desulphurization denitration is 400mg/m3Left and right, is not achieved
The higher environmental emission standard of country.
Second class is ceramic integration desulfurization denitration dust pelletizing system, and this system relies primarily on the progress of ceramic catalytic reaction kettle
Desulphurization denitration dedusting.It is quenched subsequently into tempering tower that flue gas in kiln carries out level-one UTILIZATION OF VESIDUAL HEAT IN first, subsequently into ceramics
The lime-ash of catalytic reaction kettle, dedusting, desulphurization and denitration in a kettle, collection is excluded in bottom, and flue gas enters second segment waste heat benefit
Chimney discharge is introduced by air-introduced machine with rear.
The processing mode of second class is only applicable to the fuel of the cleaning such as natural gas, and the original sulfur content in flue gas is less than
1000mg/m3, and because adsorbent utilization rate is low, operating cost is relatively high.
When the sulfureous in flue gas content of discharge is 2000 or more, how to handle complicated flue gas and reach country to the height of flue gas
Discharge standard is the problem for the urgent need to resolve that present enterprise faces.
Summary of the invention
To solve the above-mentioned problems, the present invention provides a kind of industrial smoke high temperature desulfurizing denitration dust removal system, this germlines
System integrates a variety of processing functions, and SO can be effectively reduced2、NOX, fine particle concentration, make SO2、NOXConcentration of emission is small
In 100mg/m3, the concentration of fine particle is less than 5mg/m3, realize high standard minimum discharge；Invention also provides a kind of works
Exhaust gas temperature may be implemented in conjunction with high temperature desulfurizing denitration dust removal system of the invention in the processing method of industry flue gas desulfurization denitration dust-removing
Degree reaches high standard purification in 300 degree or more completion desulphurization denitration dedustings, solves the blocking of middle-low temperature heat boiler and pipeline
And etching problem, the operation stability of entire environment friendly system is increased, the service life of device is improved and improves waste heat benefit
Use efficiency.
To achieve the above object, present invention employs the following technical solutions:
A kind of industrial smoke high temperature desulfurizing denitration dust removal system, including UTILIZATION OF VESIDUAL HEAT IN unit, for attracting smoke movement
Air-introduced machine and the chimney being connected with air-introduced machine for discharging clean flue gas, the UTILIZATION OF VESIDUAL HEAT IN unit include the first boiler,
Second boiler further includes by the sequentially connected desulfurizing tower of pipeline, whirlwind tower, quenched unit, ceramic integrated unit；
Wherein, the quenched unit includes feeding tower, tempering tower, ammonia reservoir, water reservoir；The ceramics integration is single
Member includes the ceramic catalytic reaction kettle of multiple parallel connections；
The flue gas emission mouth of first boiler is connected by pipeline with the desulfurizing tower gas inlet that desulfurizing tower lower part is arranged；
The desulfurizing tower exhanst gas outlet that desulfurizing tower top is arranged in is connected by pipeline with the whirlwind tower gas inlet on whirlwind tower top；Setting
Whirlwind tower exhanst gas outlet on whirlwind tower top is connected with the tempering tower gas inlet that tempering tower lower part is arranged in by pipeline,
The feeding tower for launching fresh calcium hydroxide is provided on pipeline between whirlwind tower and tempering tower；The top of the tempering tower is provided with
Tempering tower exhanst gas outlet is connected with ceramic integrated unit by pipeline, and ceramic integrated unit passes through pipeline and the second boiler
It is connected, second boiler flue gas outlet is communicated with air-introduced machine；
System further includes cycling element, and the cycling element includes flue gas recirculation pipeline and calcium hydroxide circulation line, institute
It states on the pipeline that one end of flue gas recirculation pipeline is arranged between air-introduced machine and chimney, the other end is connected to desulfurizing tower in desulfurizing tower
On, the calcium hydroxide circulation line is arranged between ceramic catalytic reaction kettle and desulfurizing tower.
A kind of processing method of desulfurizing industrial fume denitration dust collecting, includes the following steps:
The kiln original flue gas of S1: greater than 500 DEG C enters the first boiler by pipeline and carries out temperature adjustment, and temperature falls to 350-
The coconnected pipeline of 400 DEG C of outlets by the first boiler enters desulfurizing tower gas inlet；
S2: the useless ash comprising calcium hydroxide inside desulfurizing tower from the conveying of calcium hydroxide circulation line forms the shape of fluidized bed
Formula, high-temperature flue gas and calcium hydroxide haptoreaction complete first time desulfurization process, and the flue gas after first time desulfurization passes through desulfurizing tower cigarette
Gas outlet discharge desulfurizing tower；
S3: the flue gas being discharged from desulfurizing tower enters whirlwind tower gas inlet through piping and enters inside whirlwind tower, and flue gas is taken
Calcium hydroxide after the dust of band, stickum, reaction precipitates herein realizes dedusting, and makes the sulphur-containing substance and niter in flue gas
Second of desulfurization is realized in ash reaction, and whirlwind tower is discharged by whirlwind tower exhanst gas outlet in the flue gas after dedusting；
S4: the flue gas being discharged from whirlwind tower enters tempering tower by pipeline, on the pipeline between whirlwind tower and tempering tower
The feeding tower of setting delivers the fresh calcium hydroxide of 300-500 mesh according to the ratio that Ca:S is 2-5:1 to flue gas, and flue gas is in this segment pipe
It carries fresh calcium hydroxide and enters tempering tower gas inlet；
S5: flue gas is entered inside tempering tower by tempering tower gas inlet, and water is pumped into tune by water pump from water reservoir
Ammonia is pumped into tempering tower from ammonia reservoir and is uniformly mixed with exhaust gas by temperature adjustment in matter tower, ammonia pump, fresh calcium hydroxide
It is sufficiently mixed react with flue gas here and completes third time desulfurization, and realize the quenched of flue gas, complete to adjust in tempering tower
Temperature is reduced to 330-380 DEG C after temperature, and tempering tower is discharged by tempering tower exhanst gas outlet in flue gas, enters ceramic catalytic by pipeline
The reaction kettle gas inlet of reaction kettle；
S6: the exhaust air chamber of ceramic catalytic reaction kettle is entered by reaction kettle gas inlet flue gas, by ceramic filter
Absorption, filtering, catalysis complete the 4th desulphurization and denitration, dedusting, the inner cavity that purified flue gas enters ceramic filter passes through
The filter outlet of ceramic filter is discharged into air-purifying chamber, discharge this ceramic catalytic reaction kettle is exported by net gas, by ceramics one
The temperature of flue gas is 320-380 DEG C at this time after body unit；
S7: the flue gas being discharged from ceramic integrated unit enters the second boiler progress UTILIZATION OF VESIDUAL HEAT IN then will by air-introduced machine
The clean flue gas in part is introduced flue gas recirculation pipeline after chimney discharge or by air-introduced machine and is transmitted back to again by clean flue gas
Inside desulfurizing tower；
S8: being provided with discharger below each ceramic catalytic reaction kettle, collects the packet under ceramic integrated unit recoil
Useless ash containing calcium hydroxide is simultaneously transmitted back to desulfurizing tower by calcium hydroxide circulation line.
Former flue gas greater than 500 DEG C enters the first boiler after kiln discharge and carries out waste heat recycling, and temperature is reduced to 350-
400 DEG C, the former flue gas after the cooling of the first boiler enters desulfurizing tower from the lower section of desulfurizing tower by pipeline.Calcium hydroxide circulation pipe
Useless ash comprising calcium hydroxide is transported to inside desulfurizing tower by road outside desulfurizing tower, by former flue gas by the useless ash comprising calcium hydroxide
It blows afloat, the SO in former flue gasXIt comes into full contact with, is reacted with calcium hydroxide, so that the substance containing S is detached from former flue gas and realizes for the first time
Desulfurization.Former flue gas carries the useless ash comprising calcium hydroxide and enters whirlwind tower.Useless ash comprising calcium hydroxide is in the mistake flowed to whirlwind tower
Cheng Zhong, containing S material, the reaction was continued carries out second desulfurization with flue gas in whirlwind tower.It include imperfect combustion in former flue gas
Emplastic, particle and the useless ash Jing Guo desulfurization, be dusted in whirlwind tower, the reacted calcium hydroxide of a part,
Be adsorbed with the calcium hydroxide block of stickum, particle is discharged in the discharge valve of the bottom of whirlwind tower, by storehouse pump arranged
Enter in waste bin, the flue gas that another part is flowed is carried along into pipeline.The flue gas being discharged from whirlwind tower enters tune by pipeline
Matter tower is provided with feeding tower for launching calcium hydroxide between whirlwind tower and tempering tower, and wherein the ratio of Ca and S is 2-5:1.Newly
Fresh calcium hydroxide enters tempering tower from the lower part of tempering tower with flue gas, and the flue gas flowed up drives calcium hydroxide to flow up, and adjusts
Injection water carries out temperature adjustment in matter tower, sprays ammonia denitration, and flue gas is reacted with fresh calcium hydroxide completes third time in tempering tower
Desulfurization.The flue gas being discharged from tempering tower top will be disappeared into the lower part of ceramic catalytic reaction kettle by the filtering of ceramic filter
Lime, particle, dust isolation, react with the calcium hydroxide of ceramic filter adsorption when flue gas enters ceramic filter, realize
4th desulfurization.Ammonia reacts realization denitration with nitrogen to flue gas under the action of catalyst when by inside ceramic filter.It is filtered
Calcium hydroxide, particle, dust fall by blowback and collected and pumped and be discharged by storehouse by discharger and storehouse pump discharge, a part
Waste bin another part is discharged into desulfurizing tower again and is recycled.The flue gas given off from ceramic catalytic reaction kettle has reached
The standard of discharge, treated sulfide in flue gas, nitrogen oxides are respectively less than 100mg/m3, the content of fine particle is less than
5mg/m3, the temperature of flue gas is 320-380 DEG C, and flue gas carries out UTILIZATION OF VESIDUAL HEAT IN by the second boiler, and temperature is reduced, arranged through air-introduced machine
Enter chimney.
Compared with prior art, the present invention having the following beneficial effects:
1, the suitable high sulfur content of the present invention, high nitrogen-containing and the flue gas for having much complex harmful constituent, flue gas are being handled
Preceding sulfur content is generally in 2000-8000mg/m3, after cure object, nitrogen oxides are handled by present system and processing method
Respectively less than 100mg/m3, the content of fine particle is less than 5mg/m3, discharge index is much better than national standard.
2, the prior art is all made of low-temp desulfurization, (NH4)HSO3The table of pipeline, equipment is easily adhered to when being lower than 147 DEG C
Face is the maximum cause of corrosion.The present invention provides a kind of processing methods of desulfurizing industrial fume denitration dust collecting, in conjunction with the present invention
Integral system, may be implemented exhaust gas temperature 300 DEG C or more completion desulphurization denitration dedustings reach high standard purification, solve
Middle-low temperature heat boiler and pipeline (NH4)HSO3And blocking and the etching problem of sour corrosion substance, increase entire desulphurization denitration
The operation stability of dust pelletizing system improves the service life and utilization rate of waste heat of device.Service life can be used up to 10
Year or more, it further reduced operation expense.
3, environment protection device of the present invention has fully considered overhaul of the equipments needs, can ensure at 10 years or more continuous purifications
Flue gas is managed, to ensure that the kiln gas environmental protection of working continuously for many years such as glass is continuous uninterrupted up to standard.
Detailed description of the invention
Fig. 1 is flow chart of the present invention；
Fig. 2 is apparatus of the present invention connection schematic diagram；
Fig. 3 is ceramic catalytic reaction kettle structural schematic diagram of the present invention；
Fig. 4 is ceramic filter structure schematic diagram of the present invention；
Fig. 5 is the portion the A enlarged drawing of Fig. 4；
Fig. 6 is auxiliary smoke inlet pipe and Structure of Flue Gas Desulfuration Absorbing schematic diagram；
Fig. 7 is humidity, temperature to SO2The influence diagram of removing.
In figure, kiln 1, the first boiler 2, desulfurizing tower 3, whirlwind tower 4, feeding tower 5, tempering tower 6, the second boiler 7, ceramics are urged
Change reaction kettle 8, chimney 9, air-introduced machine 10, the first storehouse pump 11, supervisor 31, branch pipe 32, ammonia reservoir 61, water reservoir 62, ammonia pump
63, water pump 64, air-purifying chamber 81, exhaust air chamber 82, net gas outlet 83, discharger 84, waste residue outlet 85, reaction kettle gas inlet 86,
Ceramic filter 87, recoil mouth 88, branch pipe gas inlet 321, filter outlet 871, flue gas diffusion layer 875, surface stack layer
874, fibrous filter layer 873, inner cavity 872.
Specific embodiment
Below by specific embodiment, the present invention is described in further detail:
As shown in Figs 1-4, a kind of industrial smoke high temperature desulfurizing denitration dust removal system, including UTILIZATION OF VESIDUAL HEAT IN unit, for inhaling
The chimney 9 for drawing the air-introduced machine 10 of smoke movement and being connected with air-introduced machine 10 for discharging clean flue gas, the UTILIZATION OF VESIDUAL HEAT IN
Unit include the first boiler 2, the second boiler 7, further include by the sequentially connected desulfurizing tower 3 of pipeline, whirlwind tower 4, quenched unit,
Ceramic integrated unit；
Wherein, the quenched unit includes feeding tower 5, tempering tower 6, ammonia reservoir 61, water reservoir 62；Described ceramic one
Body unit includes ceramic catalytic reaction kettle 8；
The flue gas emission mouth of first boiler 2 passes through the desulfurizing tower gas inlet phase that pipeline is arranged with 3 lower part of desulfurizing tower
Even；The desulfurizing tower exhanst gas outlet that 3 top of desulfurizing tower is arranged in passes through the whirlwind tower gas inlet phase of pipeline and 4 top of whirlwind tower
Even；The whirlwind tower exhanst gas outlet that 4 top of whirlwind tower is arranged in and the tempering tower gas inlet that 6 lower part of tempering tower is arranged in pass through pipe
Road is connected, and the feeding tower 5 for launching fresh calcium hydroxide is provided on the pipeline between whirlwind tower 4 and tempering tower 6；The tempering tower
6 top is provided with tempering tower exhanst gas outlet and is connected with ceramic integrated unit by pipeline, and ceramic integrated unit passes through
Pipeline is connected with the second boiler 7, and 7 exhanst gas outlet of the second boiler is communicated with air-introduced machine 10；
System further includes cycling element, and the cycling element includes flue gas recirculation pipeline and calcium hydroxide circulation line, institute
It states on the pipeline that flue gas recirculation pipeline one end is arranged between air-introduced machine 10 and chimney 9, the other end is connected to the institute on desulfurizing tower 3
Calcium hydroxide circulation line is stated to be arranged between ceramic catalytic reaction kettle 8 and desulfurizing tower 3.
The upper one end of the ceramic catalytic reaction kettle 8 is provided with recoil mouth 88, and one end opposite with recoil mouth 88 is arranged
There is a net gas outlet 83, the lower part of ceramic catalytic reaction kettle 8 is provided with reaction kettle gas inlet 86, under ceramic catalytic reaction kettle 8
End is provided with waste residue outlet 85, and discharger 84 is provided in the waste residue outlet 85, is divided into exhaust gas inside ceramic catalytic reaction kettle 8
Room 82 and the air-purifying chamber 81 above exhaust air chamber 82, the exhaust air chamber 82 completely cut off with air-purifying chamber 81, reaction kettle gas inlet
86 are connected to exhaust air chamber 82, and the air-purifying chamber 81 is connected to recoil mouth 88, net gas outlet 83, in the ceramic catalytic reaction kettle 8
Portion is provided with the more ceramic filters 87 for desulphurization and denitration, dedusting.
The structure of the more ceramic filters 87 tubulose all the same that another end opening is closed in one end, is urged by load
The fibrous filter layer 873 of agent wraps up.
Second boiler 7 be connected to by pipeline with chimney 9, and air-introduced machine 10 be arranged the second boiler 7 and chimney 9 it
Between, the flue gas being discharged from the second boiler 7 can be entered chimney 9 by air-introduced machine 10.
The useless ash comprising calcium hydroxide for discharging ceramic catalytic reaction kettle 8 is provided on the calcium hydroxide circulation line
It is transmitted back to the conveying device of desulfurizing tower 3, the conveying device includes the first storehouse pump 11 or air compressor.
The ammonia reservoir 61 is connected with the ammonia pump 63 that ammonia is delivered to tempering tower 6, and the water reservoir 62 is connected with
Water is delivered to the water pump 64 of tempering tower 6.
A kind of processing method of desulfurizing industrial fume denitration dust collecting, includes the following steps:
The former flue gas of the kiln 1 of S1: greater than 500 DEG C enters the first boiler 2 by pipeline and carries out temperature adjustment, and temperature falls to 350-
400 DEG C enter desulfurizing tower gas inlet by the coconnected pipeline of outlet of the first boiler 2；
S2: the useless ash comprising calcium hydroxide inside desulfurizing tower 3 from the conveying of calcium hydroxide circulation line forms fluidized bed
Form, high-temperature flue gas and calcium hydroxide haptoreaction complete first time desulfurization process, and the flue gas after first time desulfurization passes through desulfurizing tower
Desulfurizing tower 3 is discharged in exhanst gas outlet；
S3: the flue gas being discharged from desulfurizing tower 3 enters whirlwind tower gas inlet through piping and enters inside whirlwind tower 4, flue gas
Calcium hydroxide after the dust of carrying, stickum, reaction precipitates herein realizes dedusting, and makes sulphur-containing substance in flue gas and disappear
Lime reaction realizes second of desulfurization, and whirlwind tower 4 is discharged by whirlwind tower exhanst gas outlet in the flue gas after dedusting；
S4: the flue gas being discharged from whirlwind tower 4 enters tempering tower 6 by pipeline, the pipe between whirlwind tower 4 and tempering tower 6
The feeding tower 5 of road setting delivers the fresh calcium hydroxide of 300-500 mesh according to the ratio that Ca:S is 2-5:1 to flue gas, and flue gas is herein
Segment pipe carries fresh calcium hydroxide and enters tempering tower gas inlet；
S5: flue gas is entered inside tempering tower 6 by tempering tower gas inlet, and water pump 64 pumps water from water reservoir 62
Enter temperature adjustment in tempering tower 6, ammonia is uniformly mixed with exhaust gas from being pumped into tempering tower 6 in ammonia reservoir 61 by ammonia pump 63, newly
Fresh calcium hydroxide, which is sufficiently mixed react here with flue gas, completes third time desulfurization, and realizes the quenched of flue gas, quenched
Temperature is reduced to 330-380 DEG C after completing temperature adjustment in tower 6, and flue gas is discharged tempering tower 6 by tempering tower exhanst gas outlet and passes through pipeline
Into the reaction kettle gas inlet 86 of ceramic catalytic reaction kettle 8；
S6: the exhaust air chamber 82 of ceramic catalytic reaction kettle 8 is entered by 86 flue gas of reaction kettle gas inlet, by ceramic mistake
The 4th desulphurization and denitration, dedusting are completed in absorption, filtering, the catalysis of filter 87, and purified flue gas enters ceramic filter 87
Inner cavity 872 is discharged into air-purifying chamber 81 by the filter outlet 871 of ceramic filter 87, this ceramics is discharged by net gas outlet 83 and urges
Change reaction kettle 8, the temperature of flue gas is 320-380 DEG C at this time after ceramic integrated unit；
S7: the flue gas being discharged from ceramic integrated unit, which enters the second boiler 7, to carry out UTILIZATION OF VESIDUAL HEAT IN and then passes through air-introduced machine
Clean flue gas is discharged through chimney 9 or is transmitted back to clean flue gas introducing flue gas recirculation pipeline again by air-introduced machine 10 by 10
Inside desulfurizing tower 3；
S8: the lower section of each ceramic catalytic reaction kettle 8 is provided with discharger 84, collects under ceramic integrated unit recoil
Useless ash comprising calcium hydroxide is transmitted back to desulfurizing tower 3 by calcium hydroxide circulation line.
A kind of industrial smoke high temperature desulfurizing denitration dust removal system, including UTILIZATION OF VESIDUAL HEAT IN unit, desulfurizing tower 3, whirlwind tower 4, tune
Matter unit, ceramic integrated unit, cycling element, wherein UTILIZATION OF VESIDUAL HEAT IN unit includes the first boiler 2, the second boiler 7.Original cigarette
Gas is discharged from kiln 1, and into the first boiler 2, second boiler 7 is connected with the chimney 9 that flue gas finally discharges, by second
It is discharged after secondary pre- recuperation of heat from chimney 9.It is set gradually between the first boiler 2 and the second boiler 7 according to the sequence of flow of flue gas
Have: desulfurizing tower 3, whirlwind tower 4, quenched unit, ceramic integrated unit, the cycling element include flue gas recirculation pipeline and disappear
Lime circulation line；
Wherein, the lower part of the desulfurizing tower 3 is provided with desulfurizing tower gas inlet, desulfurizing tower calcium hydroxide import, on desulfurizing tower 3
Portion is provided with desulfurizing tower exhanst gas outlet, and pipeline is communicated on the desulfurizing tower gas inlet, and the whirlwind tower 4 includes whirlwind tower 4
And the pipeline being connected with whirlwind tower 4；The quenched unit includes feeding tower 5, tempering tower 6, ammonia reservoir 61, water reservoir
62 and the pipeline that is connected with tempering tower 6；The ceramics integrated unit include the ceramic catalytic reaction kettle 8 of multiple parallel connections with
And the pipeline being connected with ceramic integrated unit；One end of the flue gas recirculation pipeline is arranged after air-introduced machine 10, another
The desulfurization fume entrance of desulfurizing tower 3 is arranged in end, so that flue gas is urged by desulfurizing tower 3, whirlwind tower 4, tempering tower 6, ceramics
The formation circulation of desulfurizing tower 3 is returned again after changing reaction kettle 8 and air-introduced machine 10；Drawing with setting one end of the calcium hydroxide circulation line
On pipeline between blower 10 and chimney 9, the other end is connected with desulfurizing tower 3.
Industrial original flue gas is discharged into pipeline from kiln 1, and 2 bypass pipe of the first boiler is provided on former smoke discharge pipe road
Road and valve, bypass line one end are connected between kiln 1 and the first boiler 2, and the other end is connected to the first boiler 2 and desulfurizing tower
Between 3, and it is provided with flue-gas temperature detection unit, bypass line valve can be passed through when the temperature of raw flue gas is greater than 400 DEG C
Opening size adjusts part or all of flue gas and enters the progress first time waste heat recycling of the first boiler 2, then passes through the first boiler 2
The coconnected pipeline of discharge outlet enters inside desulfurizing tower 3；When the temperature of raw flue gas is less than 400 DEG C, raw flue gas is directly logical
It crosses standard-sized sheet by-passing valve and enters desulfurizing tower 3.The gas inlet of first boiler 2 and outlet are designed with shut-off valve, and full pass shut-off valve can be right
The maintenance of first boiler 2 is without influencing whole system operation.
It is provided with desulfurizing tower calcium hydroxide import on desulfurizing tower 3, is connected to calcium hydroxide circulation line, calcium hydroxide circulation line
Other end setting pumps 11 for the useless ash comprising calcium hydroxide in ceramic integrated unit in ceramic integrated unit, by the first storehouse
It is transmitted back to inside desulfurizing tower 3.
Flue gas passes through the desulfurizing tower exhanst gas outlet of desulfurizing tower 3, into whirlwind tower 4.The top of whirlwind tower 4 is provided with whirlwind tower
Gas inlet, whirlwind tower exhanst gas outlet；Useless ash outlet is provided with below whirlwind tower 4.
Flue gas is discharged through whirlwind tower exhanst gas outlet, enters tempering tower 6 by pipeline.It is set between whirlwind tower 4 and tempering tower 6
It is equipped with feeding tower 5, brings fresh calcium hydroxide into pipeline between whirlwind tower 4 and tempering tower 6, the flue gas of flowing disappears fresh
Lime is brought into inside tempering tower 6.In lower part, tempering tower exhanst gas outlet is arranged upper for the tempering tower gas inlet setting of tempering tower 6
Portion, tempering tower 6 are internally provided with atomizer, and atomizer sprays water, the high settings such as in tempering tower 6.Have outside tempering tower 6
Ammonia reservoir 61, water reservoir 62, by ammonia pump 63, water pump 64, respectively by ammonia reservoir 61, water reservoir 62 ammonia and
Water is pumped into tempering tower 6, and water is quenched for cooling down, and ammonia is in back segment catalytic denitration.
Flue gas is discharged by the tempering tower exhanst gas outlet of tempering tower 6, and the ceramics of ceramic integrated unit are entered by pipeline
Catalytic reaction kettle 8.The ceramic catalytic reaction kettle 8 includes that shell and enclosure interior are mutually not attached to logical air-purifying chamber 81 and exhaust gas
Room 82 is provided with partition between the air-purifying chamber 81 and exhaust air chamber 82, multiple ceramic filters 87, institute are fixed at intervals on partition
Stating ceramic filter 87 is tubular structure closed at one end, and the open end is located in air-purifying chamber 81, and closed end is located at exhaust air chamber
In 82, the tube wall of the ceramic filter 87 is fibrous filter layer 873, and fibrous filter layer 873 is ceramic fibre, main component packet
Include Al2O3\SiO2, fibrous filter layer 873 with a thickness of 20mm, load has catalyst, the catalysis on fibrous filter layer 873
Agent is impregnated by nanometer to be combined on centrifugation technique load and fibrous filter layer 873.The reaction kettle flue gas of ceramic catalytic reaction kettle 8 into
The lower parts that ceramic catalytic reaction kettle 8 is arranged in mouth 86 are connected with exhaust air chamber 82, and net 83 setting of gas outlet is reacted in ceramic catalytic
The top of kettle 8 is connected with air-purifying chamber 81, and flue gas enters exhaust air chamber 82 and enters air-purifying chamber 81 after the filtering of ceramic filter 87
And it is discharged from net gas outlet 83.
Ceramic integrated unit has multiple ceramic catalytic reaction kettles 8 to be formed in parallel.Each ceramic catalytic reaction kettle 8 has multiple
Ceramic filter 87 is formed in parallel, and each ceramic catalytic reaction kettle 8 being capable of independent operating.It include being oppositely arranged on air-purifying chamber 81
Recoil mouth 88 and net gas outlet 83, interconnected each other by valve between each air-purifying chamber 81, Shuttoff Valve can be anti-to this
Answer kettle overhaul and other ceramic catalytic reaction kettles 8 work on, wherein the recoil mouth 88 on each reaction kettle air-purifying chamber 81 connects
Logical recoiling device, recoils to ceramic filter 87 included by this reaction kettle, other reaction kettle ceramic filters 87 are still
It can keep the work of desulphurization denitration dedusting.Multiple alternations of ceramic catalytic reaction kettle 8 have ensured that ceramic integrated unit can
Many years continuous work purified treatment flue gas.
Still up to 320-380 DEG C of the flue-gas temperature being discharged from ceramic integrated unit, flue gas is carried out into the second boiler 7
Second of UTILIZATION OF VESIDUAL HEAT IN after temperature reduces, introduces chimney 9 by air-introduced machine 10 and discharges, or enter flue gas recirculation pipeline, again
Into inside desulfurizing tower 3.Second boiler 7 is also equipped with bypass line and valve as the first boiler 2, closes 7 cigarette of the second boiler
Gas inlet and outlet valve, opening bypass line valve can make flue gas discharge to boiler maintenance, ensure entire gas cleaning system
System continuous operation.
The invention patent can complete flue gas desulfurization, denitration, dedusting in 300 DEG C of front end or more, and change existing skill
Art carries out the setting of desulfurization in low-temperature zone, and NH can be reduced by carrying out desulfurization in leading portion4HSO4With acidic materials to middle section, back segment pipe
The corrosiveness on road.Temperature of the flue gas in entire purification system is always held at 350 DEG C or so, this is because disappearing at 350 DEG C
Lime desulfurization effect is best, as shown in fig. 7, not being affected by humidity to the desulfurization of flue gas, at 330-370 DEG C so entirely
The temperature of system is controlled at 350 DEG C or so.
Containing SO in S material in original industrial smoke2It is relatively stable, and relatively active SO3With in system ammonia and water it is anti-
The NH with deep-etching effect should be generated4HSO4。NH4HSO4(1) equipment can be caused, which to block and corrode (2), causes catalyst to lose
It is living.It is maximum bottleneck in low-temp desulfurization.And SO3(1) aerosol itself can be caused to form plume (2) and form acidic materials corrosion
Pipeline and equipment (3) are that the precursor (3) of PM2.5 reduces boiler efficiency.The environment for keeping 350 DEG C in the present system, accelerates SO3's
Removing reduces NH4HSO4Generation, extend the service life of equipment.It is monitored by on-line monitoring equipment, desulfurizing tower 3, whirlwind tower 4
The SO of > 99% can be removed3。
SO3With NH3There is following reaction:
NH3+SO3+H2O=NH4HSO4(liquid)
2NH3+SO3+H2O=(NH4)2SO4(solid)
The reason of the escaping of ammonia includes: improper (2) flow of flue gas uneven distribution (3) low temperature of ratio of (1) ammonia Yu the substance containing N
(4) catalyst inactivation or catalyst reaction area are inadequate.320-400 DEG C of the reaction environment of this system and the pottery for invading profit catalyst
The high response area of porcelain filter screen nano size voids efficiently controls the escaping of ammonia, reduces NH4HSO4。
Inside desulfurizing tower 3, flue gas blows afloat the useless ash comprising calcium hydroxide, and useless ash both falls again by gravity and flows up and down shape
At fluidized bed.The fluidized bed bed that requires not collapse is formed inside desulfurizing tower 3 needs to keep the flow velocity and flow of certain flue gas, in order to
It ensures that exhaust gas volumn is stablized to need to attract the clean cigarette for having had reached discharge standard by flue gas recirculation pipeline after air-introduced machine 10
Gas recycling supplement.Need to maintain enough calcium hydroxides to reach desulfuration efficiency, calcium hydroxide circulation line is anti-by ceramic catalytic
It answers the useless ash comprising calcium hydroxide of 8 self-filtering of kettle to transport back desulfurizing tower 3, is the utilization in order to improve system calcium hydroxide with useless ash
Rate reduces cost.
Desulfurizing tower 3 is venturi fluidized beds empty tower structure, to Various Complex harmful exhaust and impurity in this desulfurizing tower 3
It carries out preliminary desulfurization depickling processing and first grade desulfurizing is realized to waste gas conditioning.Due to useless grey desulfurization so first grade desulfurizing is imitated herein
Rate is 50-70%.The main chemical reactions principle of Circulating Fluidized Bed Flue Gas Desulfurization Technology is as follows:
In the vertical Dual-Phrase Distribution of Gas olid system of nature, it can get at recirculating fluidized bed state (4~6m/s of gas velocity)
It is equivalent to the tens of gas-solid slip velocities to hundreds of times of individual particle slip velocity.Due to SO2Particle with calcium hydroxide is in recycle stream
Change the reaction process in bed, is that the chemical reaction process of external diffusion control is enhanced by slip velocity big between gas-solid
Mass transfer, rate of heat transfer and gas-solid mixing between gas-solid, to meet the condition requirement of sulfur dioxide and calcium hydroxide highly effective reaction.
Cause constantly to collide between particle by the fierce turbulence of particle, obtains the surface of calcium hydroxide constantly more
Newly and Desulphurization it is continuous recycled, to substantially increase the utilization rate of calcium hydroxide.
In recirculating fluidized bed, SO2With Ca (OH)2Reaction generate by-product CaSO3·1/2H2O, while and and SO3、HF
Corresponding by-product CaSO is generated with HCl reaction4·1/2H2O、CaF2、CaCl2Deng.Main chemical reactions equation is as follows:
Ca(OH)2+SO2=CaSO3·1/2H2O+1/2H2O
Ca(OH)2+SO3=CaSO4·1/2H2O+1/2H2O
CaSO3·1/2H2O+1/2O2=CaSO4·1/2H2O
Ca(OH)2+CO2=CaCO3+H2O
Ca(OH)2+ 2HCl=CaCl2·2H2O
2Ca(OH)2+ 2HCl=CaCl2·Ca(OH)2·2H2O
Ca(OH)2+ 2HF=CaF2+2H2O
In whirlwind tower 4, dust is carry into the flue gas in whirlwind tower 4, flue gas is downward, and because of centrifugal action,
Grain, dust encounter 4 inner wall of whirlwind tower, and particle, dust fall into bottom, from 4 bottom collection of whirlwind tower and are discharged into waste bin.In whirlwind
Inside tower 4, second of desulphurization reaction is carried out, while carrying out first time dedusting, and after the reaction of used first grade desulfurizing
The useless ash discharge in part, reduces the content of desulfurization product in systems, is conducive to the progress of desulphurization reaction, plays first quenched
Effect.Some stickums in systems also by most of discharge system, reduce the shadow to ceramic catalytic reaction kettle 8 herein
It rings.Secondary desulfuration efficiency is 30-50%.
Niter ash cellar is provided on feeding tower 5, the calcium hydroxide that granularity is narrower than 300-500 mesh in storehouse, which increases specific surface area, to be had
Conducive to quickening reaction.Internal system carries out 2-5 times of calcium sulfur ratio or more and sprays into fresh calcium hydroxide, it is ensured that the efficient of acidic components takes off
It removes, while substantially increasing the efficient utilization rate of adsorbent.
Ammonia inside tempering tower 6 is used to remove the substance containing N in flue gas, but denitration reaction needs catalyst, is adjusting
Ammonia and the ratio of the substance containing N are mainly adjusted inside matter tower 6 and are uniformly mixed, water primarily serves adjusting temperature, so that into
Flue gas is in optimum temperature range when next unit.Third level desulfurization and quenched is carried out before entering tempering tower 6 and in tower,
It mainly uses venturi principle, to flue gas, calcium hydroxide, atomization ammonia, is effectively mixed, it is ensured that extend and effectively connect
The time is touched, so that the acidic components improved effectively remove, and it is real to ensure that mixed uniformly flue gas enters ceramic catalytic reaction kettle 8
The efficient removal of existing multi-pollutant；Another function of tempering tower 6 is exactly event occur in the first Waste-heat boiler or desulfurizing tower 3
Hinder or safeguarded, implantation tempering tower 6 can carry out effective flue-gas temperature control to flue gas by sprayer unit, it is ensured that rear end
Lower than 400 DEG C safe operations of 8 catalytic denitration of ceramic catalytic reaction kettle reaction.Three-level desulfuration efficiency is 40-60%.
As shown in figure 5, after flue gas enters exhaust air chamber 82 from 8 gas inlet of ceramic catalytic reaction kettle, the calcium hydroxide meeting of carrying
Assemble the surface of ceramic filter 87, flue gas diffusion layer 875 surrounds ceramic filter 87, close to the surface of ceramic filter 87
When, because the surface of its fibrous filter layer 873 is the nano active factor, there is suction-operated, the surface to form calcium hydroxide can be adsorbed
Stack layer 874, and particle, calcium hydroxide are adsorbed on surface stack layer 874, play the role of dust removal by filtration and remove heavy metal, together
When sulfur-bearing S, hydrogen chloride HCl, react with calcium hydroxide when hydrogen fluoride HF gas passes through and play desulfurization deacidification, fiber
Load has catalyst on filter layer 873, has the function of that denitrification NOx, denitration, purified flue gas enter ceramic filter
The inner cavity 872 of device 87, and by filter outlet 871 enter air-purifying chamber 81 through air-purifying chamber 81 export discharge and it is in parallel with other
Ceramic integrated unit is discharged in the clean flue gas mixing that ceramic catalytic reaction kettle 8 is discharged.
The niter that recoil mouth 88 is used to be adsorbed on surface stack layer 874 is provided with above each ceramic catalytic reaction kettle 8
Into ash collecting box, unlatching discharger 84 is discharged ceramic catalytic reaction kettle 8 by waste residue outlet 85 and enters calcium hydroxide circulation for ash recoil
Pipeline.
The Base Material of ceramic filter 87 is ceramic fibre (Al2O3\SiO2), it is formed by centrifuging process.Ceramic filter
Device 87 is suitable for the gas cleaning of 200-1100 DEG C of temperature range, impregnates technology with nanometer and implements deeply to 87 tube body of ceramic filter
It spends SCR catalyst to impregnate deeply, being formed has high-effective dust-removing, desulfurization and NO_x Reduction by Effective in the ceramic catalytic filter of one, property
Can characteristic reaction mechanism be to containing nitride NOx and ammonium hydroxide NH3Flue gas be homogenized distribution, and penetrate nanometer scale ceramics mistake
Reduction reaction occurs for filtering layer and the high-efficiency activated factor direct collision of deep layer ceramic fibre surface SCR catalyst, has denitration efficiency
The features such as high low with the escaping of ammonia.
The principle of ceramic filter 87:
(1) dust in flue gas is removed by the tube surfaces of ceramic filter 87；
(2) slaked lime powder is used, SOx and acidic components are removed by the adsorption layer on ceramic pipe type filter.
SO2+Ca(OH)2=CaSO3+H2O
CaSO3+1/2O2=CaSO4
SO3+Ca(OH)2=CaSO4+H2O
2HCl+Ca(OH)2=CaCl2+2H2O
2HF+Ca(OH)2=CaF2+2H2O
(3) NH is used3Or urea realizes denitration as reducing agent when through the Catalytic Layer of 20mm, flue gas is passing through 20mm
Catalytic Layer when carry out denitration reaction, removal efficiency is high, and NH3Escapement ratio is low.
4NO+4NH3+O2=4N2+6H2O
2NO2+4NH3+O2=3N2+6H2O
The advantages of ceramic filter 87 includes:
(1) ceramic filter 87 can be in hot operation, the typical dedusting < 5mg/Nm of filtering material ontology3, ceramic filter
The validity of the desulfurization of component body superficial layer and other acidic components cooperation-removals；
(2) ceramic filter 87 including desulfurization, defluorinate, two is disliked in the high efficiency of high temperature catalytic denitration up to 95% or more
English and other acidic components efficient removals etc.；
Flue gas index after ceramic catalytic reaction kettle 8 is as follows:
Dirt < 5mg/Nm3；
Nitride NOx removal rate > 97%；
Sulfide SOx removal efficiency > 95%；
Acidic components HF, HCl, SO3And other acidic components removal efficiencies > 95%；
Dioxin removal efficiency is greater than 99%.
Discharge flue gas alkali metal content excessively high the defects of easily causing catalyst poisoning.Ceramic filter 87 disclosed by the invention
Product desulphurization and denitration, defluorinate, dust removal integrated control technology, feature show that system multi-pollutant cooperation-removal rate is high, runs
Expense is low and the advantages such as long service life, can be applied to boiler, waste incineration, ceramics, cement glass and other Industrial Stoves cigarettes
Gas purification techniques etc..Ceramic filter 87 uses wide in range 200-380 DEG C of Acclimation temperature range, and 330-380 DEG C of section multi-pollutant
Efficient removal；The national following environmental protection standard is promoted adaptable, it can be achieved that kiln gas multi-pollutant minimum discharge；Ceramics are urged
Agent tubular filter pipe cost performance with higher, service life are even up to 10 years or more, are had high-effective dust-removing, desulfurization, are taken off
Nitre and other acidic components are in the technical advantage of one；System footprint area is small, operational reliability is high, has lower running cost
With.
One of structure of desulfurizing tower 3 assists smoke inlet pipe road as shown in fig. 6, being arranged outside desulfurizing tower 3, described
Auxiliary smoke inlet pipe road is connected with flue gas recirculation pipeline, and auxiliary smoke inlet pipe road includes being arranged on supervisor 31 and supervisor 31
Multiple branch pipes 32, the supervisor 31 is arranged around desulfurizing tower 3, and one end of each branch pipe 32 is connected with being responsible for 31, the other end
It is extended to inside desulfurizing tower 3 for branch pipe gas inlet 321, the multiple branch pipe gas inlet 321 tilts upward setting.Assist cigarette
Be provided with air pressure pump in gas air inlet pipe, accelerate flue gas and spray into speed to form jet stream, jet strengthened calcium hydroxide and flue gas it is opposite
Sliding friction speed improves the desulfurization deacidification efficiency of fluidized bed.
System of the invention can purify sulfur content in 2000-8000mg/m3Between industrial smoke, by desulfurizing tower 3
First desulfurization, 4 secondary desulfuration of whirlwind tower, 8 four desulfurization, ceramic catalytic reaction kettle desulfurization, desulfurization effect are bright three times in tempering tower 6
Aobvious, whole system keeps high temperature at 350 DEG C or so, is conducive to react containing S material with calcium hydroxide, accelerates desulfurization effect.It recycles clean
Neat stress supplement holding system exhaust gas volumn stabilization prevents the bed that collapses.Calcium hydroxide circulation line recycles calcium hydroxide, and reduction disappears
The investment of lime, which improves utilization efficiency, reduces desulphurization cost.The high temperature desulfurizing depickling of this system front end, reduce acidic materials and
NH4HSO4 centering, back segment pipeline, equipment corrosiveness, improve the service life of whole system.Middle section dedusting, absorption viscosity
Substance, acidic materials, the blocking that poisons for reducing the ceramic catalytic reaction kettle 8 that back segment is arranged influence, further increase ceramics and urge
Change the catalytic effect of reaction kettle 8, NO_x Reduction by Effective reduces the escaping of ammonia, reduces NH4HSO4.Ceramic catalytic reaction kettle 8 passes through fiber
The long-pending desulphurization and denitration of the filtering and catalytic action of filter layer 873, dedusting further increase the catharsis of this system in one.This
The waste heat that the UTILIZATION OF VESIDUAL HEAT IN unit of system can make full use of industrial smoke can also play adjustment effect to the reaction temperature of system.
The 8 parallel configuration independent operating of ceramic catalytic reaction kettle of the waste heat boiler bypass line of this system and ceramic integrated unit is protected
System 10 years or more continuous operations are hindered.
System disclosed by the invention greatly reduces the discharge of dust, pernicious gas, realizes as an organic whole
The effect of high temperature desulfurizing, so that the fume indication of discharge is far superior to national standard.
Finally, it is stated that the above examples are only used to illustrate the technical scheme of the present invention and are not limiting, although referring to compared with
Good embodiment describes the invention in detail, those skilled in the art should understand that, it can be to skill of the invention
Art scheme is modified or replaced equivalently, and without departing from the objective and range of technical solution of the present invention, should all be covered at this
In the scope of the claims of invention.
Claims (7)
1. a kind of industrial smoke high temperature desulfurizing denitration dust removal system, including UTILIZATION OF VESIDUAL HEAT IN unit, for attracting drawing for smoke movement
Blower (10) and the chimney (9) being connected with air-introduced machine (10) for discharging clean flue gas, the UTILIZATION OF VESIDUAL HEAT IN unit include
First boiler (2), the second boiler (7), it is characterised in that: further include by the sequentially connected desulfurizing tower of pipeline (3), whirlwind tower
(4), quenched unit, ceramic integrated unit；
Wherein, the quenched unit includes feeding tower (5), tempering tower (6), ammonia reservoir (61), water reservoir (62)；The pottery
Porcelain integrated unit includes the ceramic catalytic reaction kettle (8) of multiple parallel connections；
The flue gas emission mouth of first boiler (2) passes through the desulfurizing tower gas inlet phase that pipeline is arranged with desulfurizing tower (3) lower part
Even；The whirlwind tower gas inlet that desulfurizing tower exhanst gas outlet on desulfurizing tower (3) top passes through pipeline and whirlwind tower (4) top is set
It is connected；Be arranged whirlwind tower (4) top whirlwind tower exhanst gas outlet and setting tempering tower (6) lower part tempering tower gas inlet
It is connected by pipeline, is provided with the feeding tower for launching fresh calcium hydroxide on the pipeline between whirlwind tower (4) and tempering tower (6)
(5)；The tempering tower exhanst gas outlet of the top setting of the tempering tower (6) is connected with ceramic integrated unit by pipeline, is made pottery
Porcelain integrated unit is connected by pipeline with the second boiler (7), and the second boiler (7) exhanst gas outlet is communicated with air-introduced machine
(10)；
System further includes cycling element, and the cycling element includes flue gas recirculation pipeline and calcium hydroxide circulation line, the cigarette
On the pipeline that gas circulation line one end is arranged between air-introduced machine (10) and chimney (9), the other end is connected on desulfurizing tower (3),
The calcium hydroxide circulation line is arranged between ceramic catalytic reaction kettle (8) and desulfurizing tower (3).
2. a kind of industrial smoke high temperature desulfurizing denitration dust removal system according to claim 1, it is characterised in that: the ceramics
The upper one end of catalytic reaction kettle (8) is provided with recoil mouth (88), and opposite one end is provided with net gas and exports with recoil mouth (88)
(83), the lower part of ceramic catalytic reaction kettle (8) is provided with reaction kettle gas inlet (86), the lower end of ceramic catalytic reaction kettle (8)
It is provided with waste residue outlet (85), is provided with discharger (84) on the waste residue outlet (85), ceramic catalytic reaction kettle (8) inner part
For exhaust air chamber (82) and the air-purifying chamber (81) being located above exhaust air chamber (82), the exhaust air chamber (82) and air-purifying chamber (81) every
Absolutely, reaction kettle gas inlet (86) is connected to exhaust air chamber (82), the air-purifying chamber (81) and recoil mouth (88), net gas outlet (83)
Connection, the ceramic catalytic reaction kettle (8) are internally provided with the more ceramic filters (87) for desulphurization and denitration, dedusting.
3. a kind of industrial smoke high temperature desulfurizing denitration dust removal system according to claim 2, it is characterised in that: described more
The structure of ceramic filter (87) tubulose all the same that another end opening is closed in one end, is there is the fiber filter of catalyst by load
Layer (873) wraps up.
4. a kind of industrial smoke high temperature desulfurizing denitration dust removal system according to claim 1, it is characterised in that: described second
Boiler (7) is connected to by pipeline with chimney (9), and air-introduced machine (10) is arranged between the second boiler (7) and chimney (9), air inducing
The flue gas being discharged from the second boiler (7) can be entered chimney (9) by machine (10).
5. a kind of industrial smoke high temperature desulfurizing denitration dust removal system according to claim 4, it is characterised in that: the niter
It is provided with the useless ash comprising calcium hydroxide for discharging ceramic catalytic reaction kettle (8) on grey circulation line and is transmitted back to desulfurizing tower
(3) conveying device, the conveying device include the first storehouse pump (11) or air compressor.
6. a kind of industrial smoke high temperature desulfurizing denitration dust removal system according to claim 1, it is characterised in that: the ammonia storage
Storage (61) is connected with the ammonia pump (63) that ammonia is delivered to tempering tower (6), and the water reservoir (62), which is connected with, conveys water
To the water pump (64) of tempering tower (6).
7. a kind of processing method of desulfurizing industrial fume denitration dust collecting, characterized by the following steps:
The former flue gas of the kiln (1) of S1: greater than 500 DEG C enters the first boiler (2) by pipeline and carries out temperature adjustment, and temperature falls to 350-
400 DEG C enter desulfurizing tower gas inlet by the coconnected pipeline of outlet of the first boiler (2)；
S2: the shape of fluidized bed is formed in the internal useless ash comprising calcium hydroxide from the conveying of calcium hydroxide circulation line of desulfurizing tower (3)
Formula, high-temperature flue gas and calcium hydroxide haptoreaction complete first time desulfurization process, and the flue gas after first time desulfurization passes through desulfurizing tower cigarette
Gas outlet discharge desulfurizing tower (3)；
S3: the flue gas being discharged from desulfurizing tower (3) enters whirlwind tower gas inlet through piping and enters whirlwind tower (4) inside, flue gas
Calcium hydroxide after the dust of carrying, stickum, reaction precipitates herein realizes dedusting, and makes sulphur-containing substance in flue gas and disappear
Lime reaction realizes second of desulfurization, and the flue gas after dedusting passes through whirlwind tower exhanst gas outlet discharge whirlwind tower (4)；
S4: the flue gas being discharged from whirlwind tower (4) enters tempering tower (6) by pipeline, between whirlwind tower (4) and tempering tower (6)
Pipeline on the feeding tower (5) that is arranged to flue gas deliver the fresh calcium hydroxide of 300-500 mesh, cigarette according to the ratio that Ca:S is 2-5:1
Gas carries fresh calcium hydroxide in this segment pipe and enters tempering tower gas inlet；
S5: flue gas enters tempering tower (6) inside by tempering tower gas inlet, and water pump (64) is by water from water reservoir (62)
It is pumped into tempering tower (6) interior temperature adjustment, ammonia is pumped into tempering tower (6) from ammonia reservoir (61) and mixes with exhaust gas by ammonia pump (63)
It closes uniformly, fresh calcium hydroxide, which is sufficiently mixed react here with flue gas, completes third time desulfurization, and realizes the tune of flue gas
Matter, temperature is reduced to 330-380 DEG C after temperature adjustment is completed in tempering tower (6), and flue gas is discharged quenched by tempering tower exhanst gas outlet
Tower (6) enters the reaction kettle gas inlet (86) of ceramic catalytic reaction kettle (8) by pipeline；
S6: the exhaust air chamber (82) of ceramic catalytic reaction kettle (8) is entered by reaction kettle gas inlet (86) flue gas, by ceramics
The 4th desulphurization and denitration, dedusting are completed in absorption, filtering, the catalysis of filter (87), and purified flue gas enters ceramic filter
(87) inner cavity (872) is discharged into air-purifying chamber (81) by the filter outlet (871) of ceramic filter (87), is exported by net gas
(83) this ceramic catalytic reaction kettle (8) are discharged, the temperature of flue gas is 320-380 DEG C at this time after ceramic integrated unit；
S7: the flue gas being discharged from ceramic integrated unit, which enters the second boiler (7), to carry out UTILIZATION OF VESIDUAL HEAT IN and then passes through air-introduced machine
(10) the clean flue gas in part is introduced into flue gas recirculation pipe after being discharged through chimney (9) by clean flue gas or pass through air-introduced machine (10)
It is internal that road is transmitted back to desulfurizing tower (3) again；
S8: being provided with discharger (84) below each ceramic catalytic reaction kettle (8), collects under ceramic integrated unit recoil
Useless ash comprising calcium hydroxide is transmitted back to desulfurizing tower (3) by calcium hydroxide circulation line.
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| CN110960973A (en) * | 2019-12-30 | 2020-04-07 | 山东瀚江环保科技有限公司 | Industrial flue gas purification process |
| CN111249881A (en) * | 2020-02-25 | 2020-06-09 | 四川美富特环境治理有限责任公司 | Glass kiln flue gas treatment method and system |
| CN113446865A (en) * | 2021-06-15 | 2021-09-28 | 台玻咸阳玻璃有限公司 | Ceramic catalyst desulfurization, denitrification and dust removal integrated process |
| CN116272357A (en) * | 2023-05-06 | 2023-06-23 | 凤阳凯盛硅材料有限公司 | Low-temperature treatment method for flue gas denitration |
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