CN110201512A - A kind of method and apparatus of flue gas desulfurization and denitrification - Google Patents
A kind of method and apparatus of flue gas desulfurization and denitrification Download PDFInfo
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- CN110201512A CN110201512A CN201910535373.1A CN201910535373A CN110201512A CN 110201512 A CN110201512 A CN 110201512A CN 201910535373 A CN201910535373 A CN 201910535373A CN 110201512 A CN110201512 A CN 110201512A
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- flue gas
- slurries
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- red mud
- slurry
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- 239000003546 flue gas Substances 0.000 title claims abstract description 156
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 150
- 238000000034 method Methods 0.000 title claims abstract description 72
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 51
- 230000023556 desulfurization Effects 0.000 title claims abstract description 45
- 239000002002 slurry Substances 0.000 claims abstract description 255
- 238000001556 precipitation Methods 0.000 claims abstract description 52
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 47
- 230000008569 process Effects 0.000 claims abstract description 42
- 239000006228 supernatant Substances 0.000 claims abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- 239000007921 spray Substances 0.000 claims description 159
- 239000007789 gas Substances 0.000 claims description 40
- 239000007788 liquid Substances 0.000 claims description 28
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 20
- 229910010293 ceramic material Inorganic materials 0.000 claims description 17
- 239000002994 raw material Substances 0.000 claims description 11
- 229910052742 iron Inorganic materials 0.000 claims description 10
- 210000002966 serum Anatomy 0.000 claims description 10
- 235000019504 cigarettes Nutrition 0.000 claims description 8
- 238000007254 oxidation reaction Methods 0.000 claims description 8
- 238000003756 stirring Methods 0.000 claims 2
- 238000002156 mixing Methods 0.000 abstract description 11
- 230000000694 effects Effects 0.000 abstract description 10
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 abstract description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 239000003517 fume Substances 0.000 abstract description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 11
- 238000004064 recycling Methods 0.000 description 11
- 230000008901 benefit Effects 0.000 description 8
- 239000000463 material Substances 0.000 description 8
- 238000004131 Bayer process Methods 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- 238000000247 postprecipitation Methods 0.000 description 6
- 239000008235 industrial water Substances 0.000 description 5
- 230000001376 precipitating effect Effects 0.000 description 5
- 239000000779 smoke Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 230000001502 supplementing effect Effects 0.000 description 5
- 230000008676 import Effects 0.000 description 4
- 239000004615 ingredient Substances 0.000 description 4
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 4
- KKCBUQHMOMHUOY-UHFFFAOYSA-N Na2O Inorganic materials [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 3
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 3
- 239000000292 calcium oxide Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 3
- 229910052593 corundum Inorganic materials 0.000 description 3
- 229910001845 yogo sapphire Inorganic materials 0.000 description 3
- 229910001051 Magnalium Inorganic materials 0.000 description 2
- 238000000498 ball milling Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 229910052681 coesite Inorganic materials 0.000 description 2
- 229910052906 cristobalite Inorganic materials 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 229910052682 stishovite Inorganic materials 0.000 description 2
- 229910052905 tridymite Inorganic materials 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000007605 air drying Methods 0.000 description 1
- 229910001570 bauxite Inorganic materials 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- JESHZQPNPCJVNG-UHFFFAOYSA-L magnesium;sulfite Chemical compound [Mg+2].[O-]S([O-])=O JESHZQPNPCJVNG-UHFFFAOYSA-L 0.000 description 1
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 229910052573 porcelain Inorganic materials 0.000 description 1
- 239000012286 potassium permanganate Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 229910001948 sodium oxide Inorganic materials 0.000 description 1
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 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
- B01D53/46—Removing components of defined structure
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen 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
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/76—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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Dispersion Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention relates to fume treatment technical fields, and in particular to a kind of method and apparatus of flue gas desulfurization and denitrification.The present invention provides a kind of methods of flue gas desulfurization and denitrification, the present invention carries out the processing of first time desulphurization denitration to flue gas to be processed after first mixing part red mud with water, then the first slurries of gained carry out precipitation process after reacting, obtained supernatant is mixed with remaining red mud, it is handled for second of desulphurization denitration, while improving desulfurization off sulfide effect, the utilization rate of red mud is improved, production cost is reduced；It is mixed by the flue gas that first time desulphurization denitration is handled with ozone, the NO for being insoluble in water is oxidized to NO soluble easily in water using ozone2And N2O5, then second of desulphurization denitration is carried out, desulfurization off sulfide effect is effectively increased, total desulfurization effect is up to 95% or more, and total denitration efficiency is 60~80%.
Description
Technical field
The present invention relates to fume treatment technical fields, and in particular to a kind of method and apparatus of flue gas desulfurization and denitrification.
Background technique
Red mud is a kind of using bauxite as the waste residue emitted in raw material production alumina process, it is estimated that, every production
1t aluminium oxide output about 1~1.5t red mud, generates nearly 1.2 hundred million tons of red muds every year, and global red mud accumulation discharge in 2017 reaches about
3900000000 tons.Currently, the mode of disposition red mud is mostly outdoor stockpiling, since the granularity of red mud is thinner, alkalinity it is strong (pH value is 10~
13) it is drifted after, air-drying and easily causes atmosphere pollution in air, Soil Surrounding alkalization can be made by meeting rainwater, and then penetrate into underground
In water, security risk is brought to the growth of animals and plants, therefore, realizes the recycling to red mud increasingly by the pass of researcher
Note.
It is well known that the SO industrially generated2、NOxPhotochemical fog and acid rain phenomenon can be caused, is to cause atmosphere
The principal element of pollution removes SO in flue gas about using red mud in the prior art2Report, but on the basis of desulfurization simultaneously
Realize that denitration is rarely reported.A kind of method that Chinese patent CN109224820A describes boiler smoke oxidizing and denitrating ozone, but
This method needs to provide the absorbing liquid of magnesium sulfite, potassium permanganate composition, increases cost, and this method can only be realized to cigarette
The denitration of gas, desulfurization effect be not good enough.
Summary of the invention
The purpose of the present invention is to provide a kind of method and apparatus of flue gas desulfurization and denitrification, the present invention utilizes red mud and ozone
Combination not only increases the denitrification efficiency of flue gas, also achieves the recycling to red mud, reduces production cost,
With preferably economical and environmentally friendly benefit.
In order to achieve the above-mentioned object of the invention, the present invention the following technical schemes are provided:
The present invention provides a kind of methods of flue gas desulfurization and denitrification, comprising the following steps:
Part red mud is mixed with water, obtains initial slurry；
The initial slurry is mixed with flue gas to be processed, the processing of first time desulphurization denitration is carried out, obtains the first slurry
Liquid and the first flue gas；
First slurries are subjected to precipitation process, obtain supernatant；
The supernatant is mixed with remaining red mud, obtains the second slurries；
First flue gas is mixed with ozone, oxidation reaction occurs, obtains the second flue gas；
Second slurries are mixed with second flue gas, carry out second of desulphurization denitration processing, by gained the
Three flue gas emissions.
Preferably, the mass ratio of the part red mud and water is 1:(10~40).
Preferably, the granularity of the part red mud and the remaining red mud independently is 100~300 mesh.
Preferably, the liquid-gas ratio of the initial slurry and flue gas to be processed is 1~10L/m3。
Preferably, the time of the precipitation process is 6~10h.
Preferably, the molar ratio of the NO in first flue gas and ozone is 1:(1~1.8).
Preferably, the liquid-gas ratio of second slurries and second flue gas is 1~6L/m3
Preferably, first slurries also obtain lower layer's slurries after carrying out precipitation process；Using lower layer's slurries as system
The raw material of standby ceramic material；
Third slurries are also obtained after second of desulphurization denitration processing, are recycled in the third slurries using magnetic method
Iron obtains red mud slurry；Using the red mud slurry as the raw material for preparing ceramic material.
The present invention provides a kind of devices of flue gas desulfurization and denitrification, including
Slurry tank 9；
The first spray column 2 being connected to the discharge port of the slurry tank 9；
The precipitation tank 8 being connected to the first serum outlet of first spray column 2；
The recycle slurry liquid bath 12 being connected to the water outlet of the precipitation tank 8；
The second spray column 11 being connected to the discharge port of the recycle slurry liquid bath 12；
Second spray column 11 is connected with the first exhanst gas outlet of first spray column 2；
Ozone generator 10 is provided between first spray column 2 and second spray column 11；
Cigarette between the ozone outlet of the ozone generator 10 and first spray column 2 and second spray column 11
Feed channel is connected.
It preferably, further include the first agitating device 3-1 and the second agitating device 3-2, the first agitating device 3-1 setting
Bottom inside first spray column 2；The second agitating device 3-2 is set to the bottom inside second spray column 11
Portion.
The present invention provides a kind of methods of flue gas desulfurization and denitrification, comprising the following steps: mixes part red mud with water
It closes, obtains initial slurry；The initial slurry is mixed with flue gas to be processed, the processing of first time desulphurization denitration is carried out, obtains
To the first slurries and the first flue gas；First slurries are subjected to precipitation process, obtain supernatant；By the supernatant and residue
Red mud is mixed, and the second slurries are obtained；First flue gas is mixed with ozone, oxidation reaction occurs, obtains second
Flue gas；Second slurries are mixed with second flue gas, second of desulphurization denitration processing is carried out, obtains third slurries
With third flue gas, by gained third flue gas emission.The present invention carries out the to flue gas to be processed after first mixing part red mud with water
Once desulfurization denitration process, the first slurries of gained carry out precipitation process, obtained supernatant and remaining red mud after then reacting
Mixing while improving desulfurization off sulfide effect, improves the utilization rate of red mud, reduces for second of desulphurization denitration processing
Production cost；It mixes by the flue gas that first time desulphurization denitration is handled with ozone, is aoxidized the NO for being insoluble in water using ozone
At NO soluble easily in water2And N2O5, then second of desulphurization denitration is carried out, effectively increase desulfurization off sulfide effect, total desulfurization effect
Up to 95% or more, total denitration efficiency is 60~80%.In addition, the first slurries carry out gained lower layer after precipitation process in the present invention
Slurries and third slurries can be used for preparing ceramic material after treatment, realize maximally utilizing for resource, have important
Environment protection significance.
The present invention provides a kind of device of flue gas desulfurization and denitrification, device each processing unit configuration provided by the invention is closed
Reason, stable, high degree of automation, desulfurization off sulfide effect is good, and scale is suitble to handle flue gas.
Detailed description of the invention
Fig. 1 is the apparatus structure schematic diagram of flue gas desulfurization and denitrification provided by the invention, in figure, 1- gas inlet to be processed,
The first spray column of 2-, the first agitating device of 3-1-, the second agitating device of 3-2-, the first spray equipment of 4-1-, 4-2- second are sprayed
Device, 5-1- first circulation pump, 5-2- second circulation pump, 5-3- third circulating pump, the second gas inlet of 6-, 7-1- third spray
Device, the 4th spray equipment of 7-2-, 8- precipitation tank, 9- slurry tank, 10- ozone generator, the second spray column of 11-, 12- recycle slurry
Liquid bath.
Specific embodiment
The present invention provides a kind of methods of flue gas desulfurization and denitrification, comprising the following steps:
Part red mud is mixed with water, obtains initial slurry；
The initial slurry is mixed with flue gas to be processed, the processing of first time desulphurization denitration is carried out, obtains the first slurry
Liquid and the first flue gas；
First slurries are subjected to precipitation process, obtain supernatant；
The supernatant is mixed with remaining red mud, obtains the second slurries；
First flue gas is mixed with ozone, oxidation reaction occurs, obtains the second flue gas；
Second slurries are mixed with second flue gas, second of desulphurization denitration processing is carried out, obtains third
Slurries and third flue gas, by gained third flue gas emission.
The present invention mixes part red mud with water, obtains initial slurry.In the present invention, the red mud is preferably made a living
The waste residue generated in alumina process is produced, the Bayer process red mud preferably produced in a specific embodiment of the present invention using magnalium factory.
In the present invention, the granularity of the red mud is preferably 100~300 mesh, more preferably 200~300 mesh.In specific reality of the invention
It applies in mode, if the partial size of commercially available red mud is excessive, is preferably reused after ball milling obtains the suitable red mud of partial size.The present invention is preferred
Commercially available red mud progress ball milling is first obtained into the suitable red mud of partial size, then takes part red mud for first time desulphurization denitration, it is remaining
Red mud is used for subsequent second of desulphurization denitration.The present invention does not have special limit to the mass ratio of the part red mud and remaining red mud
It is fixed, it is advisable with obtaining the initial slurry for meeting pH value requirement and the second slurries.
The present invention does not have special restriction to the source of the water, it is preferred to use industrial water.The present invention is to the part
The hybrid mode of red mud and water does not have special restriction, using the hybrid mode of this field routine.In the present invention, described
The mass ratio of part red mud and water is preferably 1:(10~40), more preferably 1:20.
After obtaining initial slurry, the present invention mixes the initial slurry with flue gas to be processed, carries out de- for the first time
Sulphur denitration process obtains the first slurries and the first flue gas.In the present invention, the liquid-gas ratio of the initial slurry and flue gas to be processed
Preferably 1~10L/m3, more preferably 6L/m3.The present invention increases gas liquid interfacial area, can promote just by improving liquid-gas ratio
Beginning, slurries were to SO2、NOxAbsorption.In the present invention, the flue gas to be processed is preferably calcining petroleum coke flue gas, described to be processed
The temperature of flue gas is preferably 150 DEG C~200 DEG C, more preferably 160 DEG C；The flow of the flue gas to be processed is preferably 1.8~
2.5m3/ h, more preferably 2.2m3/h；SO in the flue gas to be processed2Concentration be preferably 1500~3500mg/m3, more excellent
It is selected as 3000mg/m3；The concentration of NO is preferably 200~500mg/m3, more preferably 400mg/m3。
In the present invention, the mixed mode preferably sprays the initial slurry onto the flue gas to be processed,
The contact area of initial slurry and flue gas is improved, and then improves denitrification efficiency.
The present invention carries out first time desulphurization denitration during the first time desulphurization denitration is handled, to flue gas to be processed
Processing, the reaction of generation specifically include that
SO2+H2O→H2SO3；
Al2O3+3H2SO3→Al2(SO3)3+3H2O；
Na2O+H2SO3→Na2SO3+H2O；
CaO+H2SO3→CaSO3+H2O；
3NO2+H2O→2HNO3+NO。
Wherein, aluminium oxide, sodium oxide molybdena and calcium oxide are all from red mud.The present invention is handled in the first time desulphurization denitration
In the process, the pH value of gained slurries can decline, when the pH value of gained slurries drops to 5 or less, the preferred discharge part of the present invention
Slurries carry out post precipitation processing as the first slurries, while supplementing the initial slurry of same volume.In the present invention, described
First slurries preferably account for the 30~60% of first time desulphurization denitration processing gained slurries total volume.
First slurries are carried out precipitation process by the present invention, obtain supernatant.In the present invention, the precipitation process
Mode preferably staticly settles, and the temperature of the precipitation process is preferably 60 DEG C；The time of the precipitation process is preferably 6~
10h。
After obtaining supernatant, the present invention mixes the supernatant with remaining red mud, obtains the second slurries.The present invention
It is used to be mixed with remaining red mud it is preferred that being rounded the 20~40% of a slurry volume, remaining supernatant still remains in precipitation process
In obtained solid precipitating, lower layer's slurries are formed, ceramic material is used to prepare.
The present invention does not have special requirement to the mass ratio of the supernatant and remaining red mud, to obtain that pH value is 7
Two slurries are advisable.The present invention recycles the supernatant in first slurries, is used for subsequent second of desulphurization denitration, not only subtracts
Lack production cost, also improves desulphurization denitration ability.
After obtaining the first flue gas, the present invention mixes first flue gas with ozone, and oxidation reaction occurs, and obtains the
Two flue gases.In the present invention, the molar ratio of the NO in first flue gas and ozone is preferably 1:(1~1.8).In the present invention
In, the time of the oxidation reaction is preferably 1.2~1.5s.The present invention utilizes in the mixed process of the first flue gas and ozone
The NO for being insoluble in water is oxidized to NO soluble easily in water by ozone2And N2O5, subsequent second of desulphurization denitration is then carried out again,
Desulfurization off sulfide effect can be effectively improved.
After obtaining the second slurries and the second flue gas, the present invention mixes second slurries with second flue gas,
Second of desulphurization denitration processing is carried out, third slurries and third flue gas are obtained.In the present invention, second slurries and described the
The liquid-gas ratio of two flue gases is preferably 1~6L/m3, more preferably 5L/m3.In the present invention, the mixed mode is preferably by institute
It states on the second slurries spray to second flue gas, improves the contact area of the second slurries and flue gas, and then improve desulphurization denitration
Efficiency.
The present invention carries out at second of desulphurization denitration the second flue gas during second of desulphurization denitration is handled
Reason, the reaction of generation specifically include that
SO2+H2O→2H++SO3 2-；
N2O5+H2O→2HNO3；
The present invention utilizes SO contained in supernatant during second of desulphurization denitration is handled3 2-、HSO3 -With
Fe3+, mixed with red mud, Fe3+Liquid phase catalytic oxidation SO2And NOxIt is dissolved in liquid phase, forms S6+Compound enhances desulphurization denitration
Efficiency.The total desulfuration efficiency of third flue gas being discharged after second of desulphurization denitration is handled is up to 95% or more, total denitration efficiency
Reach 60~80%, meets standard limit of smog release, it can be with direct emission.In the present invention, the pH value of the third slurries is preferred
It is 4.
After obtaining third slurries, present invention preferably employs the iron in magnetic method recycling third slurries, obtain red mud slurry.?
In the present invention, preferably using the red mud slurry as the raw material for preparing ceramic material, or preferably with the first slurries described previously
The lower layer's slurries obtained after precipitation process mixing is carried out, obtained mixed material is as the raw material for preparing ceramic material.In this hair
In bright, the mixed material main component is Al2O3、SiO2Deng, have production ceramic material primary condition, and pass through magnetic
After selecting method to recycle the iron in slurries, influence of the iron to porcelain body whiteness, transparency is avoided, therefore, at desulphurization denitration
The mixed material obtained after reason can be used for preparing ceramic material, while to red mud recycling and reusing, so that red mud becomes useless
For treasured, have high economic benefit and environmental benefit.
The present invention provides a kind of devices of flue gas desulfurization and denitrification, including
Slurry tank 9；
The first spray column 2 being connected to the discharge port of the slurry tank 9；
The precipitation tank 8 being connected to the first serum outlet of first spray column 2；
The recycle slurry liquid bath 12 being connected to the water outlet of the precipitation tank 8；
The second spray column 11 being connected to the discharge port of the recycle slurry liquid bath 12；
Second spray column 11 is connected with the first exhanst gas outlet of first spray column 2；
Ozone generator 10 is provided between first spray column 2 and second spray column 11；
Cigarette between the ozone outlet of the ozone generator 10 and first spray column 2 and second spray column 11
Feed channel is connected.
Flue gas desulfurization and denitrification device provided by the invention includes slurry tank 9.In the present invention, the slurry tank 9 is for mixing
Close the part red mud and water；The present invention restriction not special for the slurry tank 9, can guarantee that the mixed process is suitable
Benefit carries out.
Flue gas desulfurization and denitrification device provided by the invention includes the first spray column being connected to the discharge port of the slurry tank 9
2.In the present invention, first spray column 2 is for carrying out the first time desulphurization denitration processing；The present invention is to first spray
The not special restriction of tower 2 is drenched, can guarantee that the first time desulphurization denitration processing is gone on smoothly.
As an embodiment of the present invention, first spray column 2 include gas inlet 1 to be processed, initial slurry into
Mouth, the first exhanst gas outlet and the first serum outlet.As an embodiment of the present invention, first exhanst gas outlet is set to institute
The top of the first spray column 2 is stated, for the first flue gas to be discharged；First serum outlet is set to first spray column 2
Bottom, for the first slurries to be discharged.
As an embodiment of the present invention, the gas inlet to be processed 1 and initial slurry import be provided independently from
The side of first spray column 2.
As an embodiment of the present invention, the flue gas desulfurization and denitrification device further includes the first spray equipment 4-1 and
Two spray equipment 4-2, the first spray equipment 4-1 and the second spray equipment 4-2 are provided independently from first spray column 2
Internal top, is connected with the initial slurry import.As one embodiment of invention, the first spray equipment 4-1
With the second spray equipment 4-2 in setting up and down.In the present invention, initial slurry enters the first spray equipment through initial slurry import
In 4-1 and the second spray equipment 4-2, spray into flue gas to be processed.
As an embodiment of the present invention, the height of the gas inlet to be processed 1 is lower than first spray equipment
The height of 4-1 and the second spray equipment 4-2.In the present invention, the initial slurry enters the first spray through initial slurry import
In device 4-1 and the second spray equipment 4-2, the flue gas to be processed enters in the first spray column 2 through gas inlet 1 to be processed,
Initial slurry flows from above to below, and flue gas to be processed flows from bottom to top, is conducive to the contact surface for improving initial slurry and flue gas
Product keeps the first time desulphurization denitration processing more abundant.
As an embodiment of the present invention, the flue gas desulfurization and denitrification device further includes first circulation pump 5-1, the present invention
The slurries for passing through desulphurization denitration processing in the first spray column 2 are sent into the first spray equipment 4-1 and the using first circulation pump 5-1
In two spray equipment 4-2, utilize gained serum recycle.The present invention does not have special want to the recycling number of the slurries
It asks, is advisable when dropping to 5 or less with the pH value of gained slurries, be conducive to be used to prepare through post precipitation processing gained lower layer slurries
Ceramic material.
As an embodiment of the present invention, the flue gas desulfurization and denitrification device further includes the first agitating device 3-1, described
First agitating device 3-1 is set to the bottom inside first spray column 2.The present invention can prevent red mud by agitating device
Particle deposit buildup in the first spray column 2, it is ensured that the first slurries can be uniformly delivered in precipitation tank.
Flue gas desulfurization and denitrification device provided by the invention includes being connected to the first serum outlet of first spray column 2
Precipitation tank 8.In the present invention, the precipitation tank 8 is used for the precipitation process；The present invention is not special for the precipitation tank 8
Restriction, can guarantee that the precipitation process is gone on smoothly.
As an embodiment of the present invention, the flue gas desulfurization and denitrification device further includes second circulation pump 5-2, and described the
Two circulating pump 5-2 are set between first spray column 2 and the precipitation tank 8, for will be discharged in the first spray column 2
One slurries are delivered in precipitation tank 8.
Flue gas desulfurization and denitrification device provided by the invention includes the recycle slurry liquid bath being connected to the water outlet of the precipitation tank 8
12.In the present invention, the recycle slurry liquid bath 12 is for mixing the remaining red mud and supernatant；The present invention is for the circulation
The not special restriction of slurry tank 12 can guarantee that the mixed process is gone on smoothly.
Flue gas desulfurization and denitrification device provided by the invention includes second be connected to the discharge port of the recycle slurry liquid bath 12
Spray column 11.In the present invention, second spray column 11 is for carrying out second of desulphurization denitration processing；The present invention is to institute
The not special restriction of the second spray column 11 is stated, can guarantee that second of desulphurization denitration processing is gone on smoothly.
As an embodiment of the present invention, second spray column 11 include the second gas inlet 6, the second slurries into
Mouth, third exhanst gas outlet and third serum outlet.As an embodiment of the present invention, the third exhanst gas outlet is set to institute
The top for stating the second spray column 11, for third flue gas to be discharged；The third serum outlet is set to second spray column 11
Bottom, for third slurries to be discharged.
As an embodiment of the present invention, second gas inlet 6 and the second slurry inlet are provided independently from institute
State the side of the second spray column 11.
As an embodiment of the present invention, the flue gas desulfurization and denitrification device further includes third spray equipment 7-1 and
Four spray equipment 7-2, the third spray equipment 7-1 and the 4th spray equipment 7-2 are provided independently from second spray column
Top inside 11 is connected with second slurry inlet.As one embodiment of invention, the third spray equipment 7-
1 and the 4th spray equipment 7-2 in setting up and down.In the present invention, the second slurries are through the second slurry inlet third spray equipment 7-1
In the 4th spray equipment 7-2, spray into the second flue gas.
As an embodiment of the present invention, the height of second gas inlet 6 is lower than the third spray equipment 7-1
With the height of the 4th spray equipment 7-2.In the present invention, second slurries enter third spray equipment through the second slurry inlet
In 7-1 and the 4th spray equipment 7-2, second flue gas enters in the second spray column 11 through the second gas inlet 6, the second slurries
It flows from above to below, the second flue gas flows from bottom to top, is conducive to the contact area for improving the second slurries and the second flue gas, makes institute
Second of desulphurization denitration processing is stated sufficiently to carry out.
As an embodiment of the present invention, the flue gas desulfurization and denitrification device further includes third circulating pump 5-3, the present invention
Using third circulating pump 5-3 by the second spray column 11 pass through desulphurization denitration processing slurries be sent into third spray equipment 7-1 and
In 4th spray equipment 7-2, utilize gained serum recycle.It is special that the present invention does not have the recycling number of the slurries
It is required that dropping to 4 with the pH value of gained slurries is advisable, is conducive to gained third slurries and is used to prepare ceramic material.
As an embodiment of the present invention, the flue gas desulfurization and denitrification device further includes the second agitating device 3-2, described
Second agitating device 3-2 is set to the bottom inside second spray column 11.The present invention can prevent red by agitating device
Mud particle deposit buildup in the second spray column 11, it is ensured that third slurries are smoothly discharged.
In the present invention, second spray column 11 is connected with the first exhanst gas outlet of first spray column 2.At this
In invention, the first flue gas that first spray column 2 is discharged, which enters, carries out secondary desulfuration denitration process in the second spray column 11, mentions
High desulfurization off sulfide effect.
Flue gas desulfurization and denitrification device provided by the invention includes ozone generator 10, and the ozone generator 10 is set to institute
State between the first spray column 2 and the second spray column 11, the ozone outlet of the ozone generator 10 and first spray column 2 and
Flue between second spray column 11 is connected.In the present invention, ozone generator 10 generates ozone into first
It in flue between spray column 2 and second spray column 11, is mixed in the duct with the first flue gas, and by first
NO in flue gas is oxidized to NO soluble easily in water2And N2O5, and then improve denitration efficiency.
Below with reference to Fig. 1, to the specific steps for carrying out fume treatment using flue gas desulfurization and denitrification device provided by the invention
It is illustrated: part red mud slurries being added in slurry tank 9 with water and are mixed, initial slurry is obtained；By the initial slurry
It is sent into the first spray column 2 with flue gas to be processed, carries out the processing of first time desulphurization denitration, obtain the first slurries and the first flue gas；
First slurries, which enter, carries out precipitation process in precipitation tank 8, obtain supernatant and lower layer's slurries；By the supernatant and residue
Red mud is added in recycle slurry liquid bath 12 and is mixed, and obtains the second slurries；First flue gas is generated with ozone generator 10
Ozone mixing, occur oxidation reaction, obtain the second flue gas；Second slurries and the second flue gas are sent into the second spray column 11
In, second of desulphurization denitration processing is carried out, third slurries and third flue gas are obtained；Using in magnetic method recycling third slurries
Iron obtains red mud slurry, and the lower layer's slurries obtained after the red mud slurry is carried out precipitation process with the first slurries mix, and obtains
Mixed material be used to prepare ceramic material；The third flue gas is discharged through chimney.
Below in conjunction with the embodiment in the present invention, the technical solution in the present invention is clearly and completely described.It is aobvious
So, described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.Based on the reality in the present invention
Example is applied, every other embodiment obtained by those of ordinary skill in the art without making creative efforts all belongs to
In the scope of protection of the invention.
Embodiment 1
The Bayer process red mud that the present embodiment is produced using Ningxia magnalium factory, by mass percentage, the Bayer process is red
The composition of mud are as follows: CaO 24.7%, Al2O323.9%, SiO222.38%, Na2O 13.12%, Fe2O39.14%,
TiO23.57% and inevitable impurity.
Above-mentioned Bayer process red mud is milled to 100 mesh~200 mesh, by the red mud of milled and industrial water according to solid-to-liquid ratio 1:
35 mass ratio is added in slurry tank 9 and is mixed, and obtains initial slurry, and the initial slurry enters in the first spray column 2
It is sprayed through the first spray equipment 4-1 and the second spray equipment 4-2, with the SO in flue gas to be processed2、NOxIt is de- to carry out first time desulfurization
Nitre processing, obtains the first flue gas, and gained slurries are delivered to the spray of the first spray equipment 4-1 and second through first circulation pump 5-1 and fill
It sets in 4-2 and recycles, when the pH value of gained slurries drops to 5 or less, the slurries of discharge 30%~40% are as the first slurry
Liquid carries out post precipitation processing, while supplementing the initial slurry of same volume into the first spray column 2 from slurry tank 9；Wherein, to
Handle SO in flue gas2Concentration be 3000mg/m3, NO concentration be 400mg/m3, the flow of flue gas to be processed is 2.2m3/ h, temperature
Degree is 160 DEG C, and the liquid-gas ratio of initial slurry and industrial smoke is 6L/m3；
The precipitation process that in precipitation tank 8 first slurries of discharge carried out with 7h takes out 30% supernatant and milled
Remaining red mud is added in recycle slurry liquid bath 12 and is mixed, and obtains the second slurries that pH value is 7；Remaining supernatant still remains in
In precipitation process obtained solid precipitating, lower layer's slurries are formed；
The ozone that ozone generator 10 generates enters the flue between the first spray column 2 and second spray column 11
In, with the first flue gas mixing 1.2s, the NO in the first flue gas is oxidized to NO2And N2O5, obtain the second flue gas；Wherein ozone
The molar ratio of NO is 1 in the ozone and the first flue gas that generator 10 generates；
Above-mentioned second slurries enter in the second spray column 11 to be sprayed through third spray equipment 7-1 and the 4th spray equipment 7-2,
Second of desulphurization denitration processing is carried out with the second flue gas, obtains third slurries and third flue gas, wherein the second slurries and the second cigarette
The liquid-gas ratio of gas is 5L/m3；
Gained slurries are delivered in third spray equipment 7-1 and the 4th spray equipment 7-2 through third circulating pump 5-3 and recycle benefit
With, until the pH value of slurries is 4, discharge third slurries obtain red mud slurry using the iron in magnetic method recycling third slurries,
The lower layer's slurries obtained after the red mud slurry is carried out precipitation process with the first slurries mix, and obtained mixed material is as system
The raw material of standby ceramic material.
The ingredient of third flue gas is detected, as the result is shown: SO2Concentration be 126mg/m3, NOxConcentration be
156mg/m3, desulfuration efficiency 95.8%, denitration efficiency 61%.
Embodiment 2
Above-mentioned Bayer process red mud is milled to 200 mesh~300 mesh, by the red mud of milled and industrial water according to solid-to-liquid ratio 1:
25 mass ratio is added in slurry tank 9 and is mixed, and obtains initial slurry, and the initial slurry enters in the first spray column 2
It is sprayed through the first spray equipment 4-1 and the second spray equipment 4-2, with the SO in flue gas to be processed2、NOxIt is de- to carry out first time desulfurization
Nitre processing, obtains the first flue gas, and gained slurries are delivered to the spray of the first spray equipment 4-1 and second through first circulation pump 5-1 and fill
It sets in 4-2 and recycles, when the pH value of gained slurries drops to 5 or less, the slurries of discharge 40%~60% are as the first slurry
Liquid carries out post precipitation processing, while supplementing the initial slurry of same volume into the first spray column 2 from slurry tank 9；Wherein, to
Handle SO in flue gas2Concentration be 3000mg/m3, NO concentration be 400mg/m3, the flow of flue gas to be processed is 2.2m3/ h, temperature
Degree is 160 DEG C, and the liquid-gas ratio of initial slurry and industrial smoke is 6L/m3；
The precipitation process that in precipitation tank 8 first slurries of discharge carried out with 7h takes out 30% supernatant and milled
Remaining red mud is added in recycle slurry liquid bath 12 and is mixed, and obtains the second slurries that pH value is 7；Remaining supernatant still remains in
In precipitation process obtained solid precipitating, lower layer's slurries are formed；
The ozone that ozone generator 10 generates enters the flue between the first spray column 2 and second spray column 11
In, with the first flue gas mixing 1.2s, the NO in the first flue gas is oxidized to NO2And N2O5, obtain the second flue gas；Wherein ozone
The molar ratio of NO is 1 in the ozone and the first flue gas that generator 10 generates；
Above-mentioned second slurries enter in the second spray column 11 to be sprayed through third spray equipment 7-1 and the 4th spray equipment 7-2,
Second of desulphurization denitration processing is carried out with the second flue gas, obtains third slurries and third flue gas, wherein the second slurries and the second cigarette
The liquid-gas ratio of gas is 5L/m3；
Gained slurries are delivered in third spray equipment 7-1 and the 4th spray equipment 7-2 through third circulating pump 5-3 and recycle benefit
With, until the pH value of slurries is 4, discharge third slurries obtain red mud slurry using the iron in magnetic method recycling third slurries,
The lower layer's slurries obtained after the red mud slurry is carried out precipitation process with the first slurries mix, and obtained mixed material is as system
The raw material of standby ceramic material.
The ingredient of third flue gas is detected, as the result is shown: SO2Concentration be 84mg/m3, NOxConcentration be 137mg/
m3, desulfuration efficiency 97.2%, denitration efficiency 65.75%.
Embodiment 3
Above-mentioned Bayer process red mud is milled to 200 mesh~300 mesh, by the red mud of milled and industrial water according to solid-to-liquid ratio 1:
25 mass ratio is added in slurry tank 9 and is mixed, and obtains initial slurry, and the initial slurry enters in the first spray column 2
It is sprayed through the first spray equipment 4-1 and the second spray equipment 4-2, with the SO in flue gas to be processed2、NOxIt is de- to carry out first time desulfurization
Nitre processing, obtains the first flue gas, and gained slurries are delivered to the spray of the first spray equipment 4-1 and second through first circulation pump 5-1 and fill
It sets in 4-2 and recycles, when the pH value of gained slurries drops to 5 or less, the slurries of discharge 30%~40% are as the first slurry
Liquid carries out post precipitation processing, while supplementing the initial slurry of same volume into the first spray column 2 from slurry tank 9；Wherein, to
Handle SO in flue gas2Concentration be 3000mg/m3, NO concentration be 400mg/m3, the flow of flue gas to be processed is 2.2m3/ h, temperature
Degree is 160 DEG C, and the liquid-gas ratio of initial slurry and industrial smoke is 6L/m3；
The precipitation process that in precipitation tank 8 first slurries of discharge carried out with 7h takes out 30% supernatant and milled
Remaining red mud is added in recycle slurry liquid bath 12 and is mixed, and obtains the second slurries that pH value is 7；Remaining supernatant still remains in
In precipitation process obtained solid precipitating, lower layer's slurries are formed；
The ozone that ozone generator 10 generates enters the flue between the first spray column 2 and second spray column 11
In, with the first flue gas mixing 1.2s, the NO in the first flue gas is oxidized to NO2And N2O5, obtain the second flue gas；Wherein ozone
The molar ratio of NO is 1.5:1 in the ozone and the first flue gas that generator 10 generates；
Above-mentioned second slurries enter in the second spray column 11 to be sprayed through third spray equipment 7-1 and the 4th spray equipment 7-2,
Second of desulphurization denitration processing is carried out with the second flue gas, obtains third slurries and third flue gas, wherein the second slurries and the second cigarette
The liquid-gas ratio of gas is 5L/m3；
Gained slurries are delivered in third spray equipment 7-1 and the 4th spray equipment 7-2 through third circulating pump 5-3 and recycle benefit
With, until the pH value of slurries is 4, discharge third slurries obtain red mud slurry using the iron in magnetic method recycling third slurries,
The lower layer's slurries obtained after the red mud slurry is carried out precipitation process with the first slurries mix, and obtained mixed material is as system
The raw material of standby ceramic material.
The ingredient of third flue gas is detected, as the result is shown: SO2Concentration be 69mg/m3, NOxConcentration be 106mg/
m3, desulfuration efficiency 97.7%, denitration efficiency 73.5%.
Embodiment 4
Above-mentioned Bayer process red mud is milled to 200 mesh~300 mesh, by the red mud of milled and industrial water according to solid-to-liquid ratio 1:
15 mass ratio is added in slurry tank 9 and is mixed, and obtains initial slurry, and the initial slurry enters in the first spray column 2
It is sprayed through the first spray equipment 4-1 and the second spray equipment 4-2, with the SO in flue gas to be processed2、NOxIt is de- to carry out first time desulfurization
Nitre processing, obtains the first flue gas, and gained slurries are delivered to the spray of the first spray equipment 4-1 and second through first circulation pump 5-1 and fill
It sets in 4-2 and recycles, when the pH value of gained slurries drops to 5 or less, the slurries of discharge 30%~40% are as the first slurry
Liquid carries out post precipitation processing, while supplementing the initial slurry of same volume into the first spray column 2 from slurry tank 9；Wherein, to
Handle SO in flue gas2Concentration be 3000mg/m3, NO concentration be 400mg/m3, the flow of flue gas to be processed is 2.2m3/ h, temperature
Degree is 160 DEG C, and the liquid-gas ratio of initial slurry and industrial smoke is 6L/m3；
The precipitation process that in precipitation tank 8 first slurries of discharge carried out with 7h takes out 30% supernatant and milled
Remaining red mud is added in recycle slurry liquid bath 12 and is mixed, and obtains the second slurries that pH value is 7；Remaining supernatant still remains in
In precipitation process obtained solid precipitating, lower layer's slurries are formed；
The ozone that ozone generator 10 generates enters the flue between the first spray column 2 and second spray column 11
In, with the first flue gas mixing 1.2s, the NO in the first flue gas is oxidized to NO2And N2O5, obtain the second flue gas；Wherein ozone
The molar ratio of NO is 1.8:1 in the ozone and the first flue gas that generator 10 generates；
Above-mentioned second slurries enter in the second spray column 11 to be sprayed through third spray equipment 7-1 and the 4th spray equipment 7-2,
Second of desulphurization denitration processing is carried out with the second flue gas, obtains third slurries and third flue gas, wherein the second slurries and the second cigarette
The liquid-gas ratio of gas is 5L/m3；
Gained slurries are delivered in third spray equipment 7-1 and the 4th spray equipment 7-2 through third circulating pump 5-3 and recycle benefit
With, until the pH value of slurries is 4, discharge third slurries obtain red mud slurry using the iron in magnetic method recycling third slurries,
The lower layer's slurries obtained after the red mud slurry is carried out precipitation process with the first slurries mix, and obtained mixed material is as system
The raw material of standby ceramic material.
The ingredient of third flue gas is detected, as the result is shown: SO2Concentration be 57mg/m3, NOxConcentration be 76mg/
m3, desulfuration efficiency 98.1%, denitration efficiency 81%.
The above is only a preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
For member, various improvements and modifications may be made without departing from the principle of the present invention, these improvements and modifications are also answered
It is considered as protection scope of the present invention.
Claims (10)
1. a kind of method of flue gas desulfurization and denitrification, which comprises the following steps:
Part red mud is mixed with water, obtains initial slurry；
The initial slurry is mixed with flue gas to be processed, carry out the processing of first time desulphurization denitration, obtain the first slurries and
First flue gas；
First slurries are subjected to precipitation process, obtain supernatant；
The supernatant is mixed with remaining red mud, obtains the second slurries；
First flue gas is mixed with ozone, oxidation reaction occurs, obtains the second flue gas；
Second slurries are mixed with second flue gas, second of desulphurization denitration processing are carried out, by gained third cigarette
Gas discharge.
2. the method according to claim 1, wherein the mass ratio of the part red mud and water be 1:(10~
40)。
3. method according to claim 1 or 2, which is characterized in that the granularity of the part red mud and the remaining red mud
It independently is 100~300 mesh.
4. the method according to claim 1, wherein the liquid-gas ratio of the initial slurry and flue gas to be processed is 1
~10L/m3。
5. the method according to claim 1, wherein the time of the precipitation process is 6~10h.
6. the method according to claim 1, wherein the molar ratio of NO and ozone in first flue gas are 1:
(1~1.8).
7. method according to claim 1 or 6, which is characterized in that the liquid gas of second slurries and second flue gas
Than for 1~6L/m3。
8. the method according to claim 1, wherein first slurries also obtain lower layer after carrying out precipitation process
Slurries；Using lower layer's slurries as the raw material for preparing ceramic material；
Third slurries are also obtained after second of desulphurization denitration processing, the iron in the third slurries is recycled using magnetic method,
Obtain red mud slurry；Using the red mud slurry as the raw material for preparing ceramic material.
9. a kind of device of flue gas desulfurization and denitrification, which is characterized in that including
Slurry tank (9)；
The first spray column (2) being connected to the discharge port of the slurry tank (9)；
The precipitation tank (8) being connected to the first serum outlet of first spray column (2)；
The recycle slurry liquid bath (12) being connected to the water outlet of the precipitation tank (8)；
The second spray column (11) being connected to the discharge port of the recycle slurry liquid bath (12)；
Second spray column (11) is connected with the first exhanst gas outlet of first spray column (2)；
Ozone generator (10) are provided between first spray column (2) and second spray column (11)；
Flue gas between the ozone outlet and first spray column (2) and the second spray column (11) of the ozone generator (10)
Pipeline is connected.
10. device according to claim 9, which is characterized in that further include the first agitating device (3-1) and the second stirring dress
It sets (3-2), first agitating device (3-1) is set to the internal bottom of first spray column (2)；The second stirring dress
It sets (3-2) and is set to the internal bottom of second spray column (11).
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| CN112675692A (en) * | 2020-12-29 | 2021-04-20 | 西安交通大学 | Red mud harmless treatment system based on circulating fluidized bed boiler and working method thereof |
| CN114146556A (en) * | 2021-12-02 | 2022-03-08 | 昆明理工大学 | Method and device for improving desulfurization and denitrification effects of red mud |
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Application publication date: 20190906 |