CN110523158A - The system and method that the comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas is administered - Google Patents
The system and method that the comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas is administered Download PDFInfo
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- CN110523158A CN110523158A CN201910832048.1A CN201910832048A CN110523158A CN 110523158 A CN110523158 A CN 110523158A CN 201910832048 A CN201910832048 A CN 201910832048A CN 110523158 A CN110523158 A CN 110523158A
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- flue gas
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- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 238000000034 method Methods 0.000 title claims abstract description 51
- 239000004408 titanium dioxide Substances 0.000 title claims abstract description 39
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 105
- 239000003546 flue gas Substances 0.000 claims abstract description 104
- 239000007789 gas Substances 0.000 claims abstract description 89
- 239000002253 acid Substances 0.000 claims abstract description 72
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 49
- 230000023556 desulfurization Effects 0.000 claims abstract description 48
- 238000001354 calcination Methods 0.000 claims abstract description 30
- 239000000428 dust Substances 0.000 claims abstract description 26
- 239000000779 smoke Substances 0.000 claims abstract description 23
- 239000003595 mist Substances 0.000 claims abstract description 18
- 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 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 69
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 57
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 28
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 claims description 25
- 239000000498 cooling water Substances 0.000 claims description 24
- 238000011084 recovery Methods 0.000 claims description 12
- 239000003795 chemical substances by application Substances 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 10
- 239000007921 spray Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 239000002699 waste material Substances 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 6
- 235000021110 pickles Nutrition 0.000 claims description 6
- 235000019504 cigarettes Nutrition 0.000 claims description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 4
- 239000005864 Sulphur Substances 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 239000000835 fiber Substances 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 3
- 238000006722 reduction reaction Methods 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 238000006555 catalytic reaction Methods 0.000 claims description 2
- 239000010936 titanium Substances 0.000 claims description 2
- 229910052719 titanium Inorganic materials 0.000 claims description 2
- 239000003344 environmental pollutant Substances 0.000 abstract description 6
- 231100000719 pollutant Toxicity 0.000 abstract description 6
- 235000010215 titanium dioxide Nutrition 0.000 description 31
- 238000004519 manufacturing process Methods 0.000 description 13
- 230000008569 process Effects 0.000 description 13
- 241000196324 Embryophyta Species 0.000 description 8
- 230000003009 desulfurizing effect Effects 0.000 description 6
- 239000010440 gypsum Substances 0.000 description 6
- 229910052602 gypsum Inorganic materials 0.000 description 6
- 239000002918 waste heat Substances 0.000 description 6
- 239000001038 titanium pigment Substances 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 4
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 238000007710 freezing Methods 0.000 description 3
- 230000008014 freezing Effects 0.000 description 3
- 239000000395 magnesium oxide Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 238000005201 scrubbing Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical group O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 239000010439 graphite Substances 0.000 description 2
- 229910002804 graphite Inorganic materials 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 2
- -1 papermaking Substances 0.000 description 2
- 238000004094 preconcentration Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 238000003303 reheating Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000011800 void material Substances 0.000 description 2
- 239000005997 Calcium carbide Substances 0.000 description 1
- 241001070941 Castanea Species 0.000 description 1
- 235000014036 Castanea Nutrition 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 229910002089 NOx Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000004378 air conditioning Methods 0.000 description 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 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
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- YYRMJZQKEFZXMX-UHFFFAOYSA-N calcium;phosphoric acid Chemical compound [Ca+2].OP(O)(O)=O.OP(O)(O)=O YYRMJZQKEFZXMX-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229940063774 carbon dioxide 5 % Drugs 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
- 235000013312 flour Nutrition 0.000 description 1
- 229920002313 fluoropolymer Polymers 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 1
- 229910010271 silicon carbide Inorganic materials 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000012463 white pigment Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
- B01D46/06—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material with means keeping the working surfaces flat
-
- 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
- B01D53/38—Removing components of undefined structure
- B01D53/40—Acidic components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
- B01D53/70—Organic halogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8628—Processes characterised by a specific catalyst
-
- 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
- B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
-
- 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
- B01D2251/602—Oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/206—Organic halogen compounds
- B01D2257/2064—Chlorine
-
- 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
The present invention discloses a kind of system and method that the comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas is administered, it includes house-bag duster for high temperature, calcining exhaust pipe is circumscribed on the house-bag duster for high temperature side wall, the house-bag duster for high temperature is connected with gas cooler by pipeline, it is connected at the top of the gas cooler and venturi acid solution inspissator, the venturi acid solution inspissator bottom is provided with preconcentrator acid solution basin；The preconcentrator acid solution basin side wall is connected with flue gas desulfurization first stage tower and flue gas desulfurization second level tower in turn by pipeline；The flue gas desulfurization second level tower, which is connected with to be arranged side by side by pipeline, flue gas condenser, demister and smoke re-heater；The smoke re-heater is connected with low temperature SCR denitration reactor and chimney in turn by pipeline.The present invention can be realized acid mist, SO in titanium dioxide calcining tail gas3、SO2, dust, NOx, the qualified discharge of the pollutants such as dioxin.
Description
Technical field
The present invention relates to calcining the field of tail gas treatment, and in particular to a kind of comprehensive cooperate with of titanium dioxide calcined by rotary kiln tail gas is controlled
The system and method for reason.
Background technique
Titanium dioxide is now widely used most important white pigment, is widely used in the neck such as coating, papermaking, ink
Proportional relationship is presented in domain, demand and GDP.Whole world titanium dioxide annual capacity is at 5,000,000 tons or more at present, domestic titanium dioxide year
For production capacity at 2,000,000 tons or more, price is about 15000-22000 yuan/ton.In production method, the country is used except a small amount of factory
Outside chloridising, remaining most of factory is produced using sulfuric acid process.Present in current sulfate process titanium dioxide production process
One comparison distinct issues is environmental protection and energy conservation.
During calcining in rotary kiln, a large amount of calcining tail gas can be generated, the exhaust temperature is high, water capacity
Greatly, main component is carbon dioxide, nitrogen, vapor, oxygen etc., and more typical volume group becomes carbon dioxide 5%, nitrogen
Gas 58%, vapor 30%, oxygen 7%, separately there is acid mist, SO2、SO3、NOx, the pollutants such as titanium dioxide dust, calcine exhaust temperature
Up to 300 DEG C -400 DEG C, usually contain acid mist 1000-2000mg/Nm3, SO3About 10000mg/Nm3, S02Concentration about 5000mg/
Nm3, titanium valve dust concentration about 10000mg/Nm3。
Improvement for titanium dioxide calcined by rotary kiln tail gas, domestic also someone carried out some researchs, were formed some special
Benefit, main conditions are as follows:
1. application No. is 200610039260.5 Chinese invention patents to disclose a kind of sulfuric acid method titanium pigment production process
The method of middle rotary kiln calcining tail gas and dilute sulfuric acid comprehensive utilization, this method forge the dilute sulfuric acid generated in titanium white production and rotary kiln
It burns tail gas contact and carries out heat exchange, after obtained pre-concentration sulfuric acid heat preservation settlement, carry out medium temperature concentration using its own temperature,
Carry out vacuum and crystallisation by cooling again, then with 98% sulfuric acid respectively be configured to production titanium dioxide or normal superphosphate needed for it is dense
Degree.This method is the problem is that utilization rate of waste heat is low, but also wants auxiliary construction pigment waste acid concentrator, and pre-concentration sulfuric acid
It also needs to keep the temperature.
It is generated 2. being disclosed in a kind of production process of titanium pigment application No. is 200410041226.2 Chinese invention patent
Waste Sulfuric Acid, exhaust gas recovery method, be sent into " titanium white including the calcining tail gas that will be generated in production process of titanium pigment and Waste Sulfuric Acid
Powder stove calcines tail gas concentrate alkene sulfuric acid Graphite Tower " in mixing, gas-liquid contact, concentration, by acid and the wherein divided titanium dioxide that contains
From, by inorganic salts crystallization, separation in acid solution, and further acid solution is sent into silicon carbide evaporator, and is steamed under negative pressure state
Hair removes partial moisture, makes acid concentration up to 80~90%.This method is the problem is that factory has to equipped with a set of concentrate
The Graphite Tower of alkene sulfuric acid, and it is easy to appear equipment fault.
3. application No. is 200710030100.9 Chinese invention patents to disclose a kind of exhaust heat refrigerating energy conservation discharge reducing technology,
Recirculated water is converted into heat source water by heat exchanger by rotary kiln calcination waste heat first, then heat source water is input to non-electric air conditioner and is set
For freezing in standby, after by non-electric air conditioner equipment refrigeration using in the process for freezing and crystallizing in production process of titanium pigment, by non-
The cold water generated after electric air-conditioning equipment refrigeration is recycled.This method is the problem is that the thermal efficiency using low, needs list
Solely configuration non-electric air conditioner equipment, and repeated with existing freezing equipment, increase investment.
4. application No. is 201010278103.6 Chinese invention patents to disclose a kind of time for automatically controlling fan delivery
Rotary kiln flue gas processing device is related to the fume treatment auxiliary of rotary kiln used in titanium white production.Primary structure is: one cyclonic
Deduster connects rotary kiln, and one cyclonic deduster connects second cyclone dust extractor, and second cyclone dust extractor connection Venturi tube removes
Dirt device, venturi scrubber connect acid mist scrubbing tower, and acid mist scrubbing tower connects chimney by exhaust pipe, is equipped on exhaust pipe
Air-introduced machine is equipped with frequency converter on air-introduced machine；In the spray thrower and wash spray device point of venturi scrubber and acid mist scrubbing tower
Not Lian Jie feed pipe, feed pipe connects the water supply chestnut of cooling sedimentation basin, the pond of venturi scrubber and acid mist wash tower bottoms
Return pipe is connected, return pipe connects cooling sedimentation basin.This method is not the problem is that carry out recuperation of heat.
It is returned 5. being disclosed in a kind of production of sulfuric acid method titanium pigment application No. is 201110036997.2 Chinese invention patent
The method that rotary kiln calcining smoke heat energy utilizes, in terms of it includes following three:
1. the calcining tail gas generated in rotary calciner is purified by electric precipitation, dry method is gathered dust, and the product of recycling returns
Rotary kiln is calcined again；
2. purified high-temperature flue gas a part is sprayed with the spent acid of the concentration 20% generated in production process, passed
Matter heat transfer, evaporates moisture content in spent acid, and acid-spending strength is improved to 30%, 70-80 DEG C of low temperature calcination tail gas after waste acid concentration
It is purified again through electric demister system, calcines tail gas standard discharge；
3. purified another part calcining tail gas returns again to rotary calciner reuse, additional heat adjusts kiln temperature
Gradient.For this method the problem is that hot waste gas heat loss during spent acid sprays is larger, utilization rate of waste heat is low, and forges
After harmful void gas in burning tail gas returns to stove, calcination process is adversely affected；
6. document " titanium dioxide calcines tail gas treatment process improvement and the research of UTILIZATION OF VESIDUAL HEAT IN " (inorganic chemicals industry, 2009
4th phase) and document " Processing tecchnics of simple analysis titanium dioxide calcining tail gas " (China Chemical Industry trade, the 9th phase in 2011) describe
A kind of method that simplified titanium dioxide calcines vent gas treatment process, improves calcining exhaust emissions effect, by the way that secondary wash water to be used as
Tail gas shower water is calcined, a wash water is made in shower water reuse, using calcining waste heat from tail gas, reduces the consumption of steam.But this method
It is lower using the efficiency of waste heat by way of spray.
Currently, there is part titanium dioxide factory auxiliary construction environment treating facility, these environment treating facilities are all
It is the aspect for being conceived to UTILIZATION OF VESIDUAL HEAT IN, treating flour dust, acid mist and sulfur dioxide removal, common process includes cyclone dust collection, Wen Qiu
In spray system, water scrubber, electric demisting, chimney etc., there are problems for this conventional method:
1. calcining waste heat from tail gas does not make full use of,
2. items pollutant described above is still difficult to qualified discharge,
3. with stepping up for environmental protection standard, dust, acid mist, SO2And SO3Emission request it is increasingly stringent, original skill
Art means can no longer meet the requirement of new standard,
4. new environmental protection standard is to NOxDischarge, wet plume, dioxin discharge be proposed requirement, and this three refer to
It is marked in original technological means and does not include.
Summary of the invention
The present invention provides the system and method that a kind of comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas is administered, the system is comprehensive
Close the row up to standard for solving the pollutants such as acid mist, sulfur dioxide, sulfur trioxide, NOx, dust, dioxin in titanium dioxide calcining tail gas
The problem of putting can also solve the important topics such as wet smoke plume emission and problem.
To achieve the above object, what a kind of comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas designed by the present invention was administered is
System, the system comprises house-bag duster for high temperature, is circumscribed with calcining exhaust pipe on the house-bag duster for high temperature side wall, described
House-bag duster for high temperature is connected with gas cooler by pipeline, connects at the top of the gas cooler and venturi acid solution inspissator
Logical, the venturi acid solution inspissator side wall is connect by being connected with acid solution pipe with external plant area's acid solution, the venturi acid solution
Inspissator bottom is provided with preconcentrator acid solution basin, and the preconcentrator acid solution basin side wall is returned by recovery tube and plant area's acid
Receiving apparatus connection；The preconcentrator acid solution basin side wall is connected with flue gas desulfurization first stage tower and flue gas desulfurization in turn by pipeline
Second level tower；The flue gas desulfurization second level tower, which is connected with to be arranged side by side by pipeline, flue gas condenser, demister and flue gas reheat
Device；The flue gas condenser is equipped with cooling water low temperature side ducts and cooling water high temperature side ducts form cooling water recirculation system；Institute
It states and is equipped with heat medium water low temperature side ducts and heat medium water high temperature side ducts formation heat medium water between gas cooler and smoke re-heater
The circulatory system；The smoke re-heater is connected with low temperature SCR denitration reactor and chimney in turn by pipeline.
Further, dilute sulfuric acid recovery pump is provided on the recovery tube.
Still further, being provided with air-introduced machine on the pipeline of the low temperature SCR denitration reactor and chimney.
Still further, being provided with heating agent water-circulating pump in the heat medium water low temperature side ducts.
Still further, the house-bag duster for high temperature is internally provided with chimney filter, the chimney filter is ceramic fibre or metal
Chimney filter, single chimney filter outer diameter are 130~155mm, and internal diameter is 100~120mm, and length is 2.5~5m, the temperature model that chimney filter uses
Enclose is 200~600 DEG C.
Titanium dioxide calcined by rotary kiln tail gas dirt, sulphur, nitre, dioxin are carried out using above-mentioned apparatus the present invention also provides a kind of
And the method that the comprehensive collaboration of wet plume is administered, comprising the following steps:
1) high-temperature bag dust removal by filtration: the titanium dioxide that temperature is 200-450 DEG C is calcined tail gas and is entered by calcining exhaust pipe
House-bag duster for high temperature removes the dust and dioxin in tail gas, and dust is less than 5mg/Nm after filtering3, dioxin
Removal rate is up to 99%；
2) flue gas is cooling:
A. enter gas cooler by the flue gas of high-temperature bag filter collector, flue-gas temperature is reduced by 400~420 DEG C
To 300~330 DEG C；The water at low temperature of heat medium water low temperature side ducts carries out heat source with high-temperature flue gas and exchanges to form high-temperature water, high-temperature water
Enter smoke re-heater by heat medium water high temperature side ducts；Heating agent water flow and temperature are determined according to system heat balance situation；(cigarette
Gas Cooler, heat medium water low temperature side ducts, heat medium water high temperature side ducts and smoke re-heater form heating agent water circulation system, flue gas
Air water changes thermogenetic heat medium water as the heat source of hot fume again after desulfurization in cooler, and the flue-gas temperature after desulfurization is promoted to
Needed for meeting SCR denitration system, that is, the heat of raw flue gas is utilized, the temperature requirement of denitration, still further aspect are on the one hand reached
Wet plume is eliminated, without adding other heat sources, improves the energy utilization rate of full factory).
3) acid pickle is concentrated: by the flue gas of gas cooler, spraying into venturi acid solution inspissator and acid solution pipe
Sulfuric acid solution contact, flue-gas temperature is reduced to saturation state, i.e., 60~80 DEG C, while the moisture in acid pickle is evaporated, and gives up
Aqueous concentration is concentrated into 30% by original 20% and enters preconcentrator acid solution basin 4, is delivered to plant area's acid by sulfuric acid circulating pump
Reuse is carried out in recyclable device；
4) flue gas desulfurization: the tail gas after waste acid concentration (contains more sulfur dioxide, sulfur trioxide and a small amount of
Sulfuric acid mist), sulfur dioxide in tail gas, sulfur trioxide and sulfuric acid mist when by flue gas desulfurization first stage tower and flue gas desulfurization second level tower
It is removed, wherein in the tail gas of desulfurization, sulfur dioxide concentration≤35mg/Nm3, sulfur trioxide removal rate >=95%；
5) flue gas condensing: the cooling water that flue gas condenser, cooling water low temperature side ducts and cooling water high temperature side ducts are formed
The circulatory system；The system uses temperature for 0~40 DEG C of recirculated cooling water, by flue gas condenser by desulfurizing tower exiting flue gas temperature
Degree is down to 55 DEG C by 80 DEG C, while reducing the moisture content in flue gas, then enters to flue gas after level-one flat defogger
Reheater；Enter smoke re-heater by the high-temperature water of heat medium water high temperature side ducts to carry out heat source and exchange to form water at low temperature and by desulfurization
Flue gas afterwards is warming up to 220 DEG C again, and water at low temperature enters gas cooler by heat medium water low temperature side ducts；
6) denitrating flue gas: the flue gas after desulfurization, which enters in continuous operation low temperature SCR denitration reactor, carries out selective catalysis
Reduction reaction carries out denitration,
7) discharge: the flue gas after denitration enters after air-introduced machine pressurization by smoke stack emission.
Preferably, in the step 1), titanium dioxide calcine tail gas in titanium dioxide dust content be 10000~
15000mg/m3, the temperature of house-bag duster for high temperature is 450 DEG C, and pressure is ± 6kPa.
Preferably, in the step 6), denitration temperature is 200 DEG C, and removal efficiency is to reach 90% or more.
The principle of the present invention:
ND steel, 2205 two-phases can be used in the water-borne formula heat exchanger that gas cooler is selected in present system, the heat exchanger
The materials such as stainless steel, fluoroplastics, plastic-steel.
Flue gas desulfurization first stage tower and flue gas desulfurization second level tower use 1 grade or 2 grades of wet desulfuration tower (wet processes in present system
Sulfur removal technology uses desulfurization method of limestone-gypsum, lime-gypsum method desulfurization, acetylene sludge-gypsum process desulphurization, magnesium oxide method desulfurization
Etc. various wet desulfurizing process), desulfurizing tower is spray void tower, is followed successively by tower reactor slurry pool, flue gas even distribution device, spray in tower
Lime stone, lime, carbide slag, magnesia etc. can be used in layer, demister etc., desulfurizing agent.
Wet desulfurizing process uses desulfurization method of limestone-gypsum, lime-gypsum method desulfurization, calcium carbide in method of the invention
The various wet desulfurizing process such as slag-gypsum desulfurization, magnesium oxide method desulfurization.
Method of the invention condenses the flue gas after wet desulphurization using flue gas condensing technique, and condensation method can be used
Water-borne formula heat exchanger carries out cooling condensation, cooling water can also be used directly sprays and carry out cooling condensation, and purpose is all after making desulfurization
Saturated flue gas temperature reduce, so that moisture therein be precipitated.
The present invention carries out heat temperature raising to condensed flue gas using flue gas reheat technique, flue-gas temperature is at least raised to full
The reaction temperature of sufficient SCR denitration.Reheating method can be used water-borne formula heat exchanger and heat up, and heat medium water may be derived from cooler
Hot water, reheating method also use other heat sources such as steam heating.
The SCR denitration process that denitration of the present invention uses, denitrating system are arranged in desulphurization system, condenser system and reheat system
Later, catalyst selects low temperature catalyst.Air-introduced machine is mounted on after denitrating system, and the cigarette of environmental emission standard is reached through handling
Gas can be directly entered chimney after air-introduced machine is pressurized, to be emitted into atmosphere.
Beneficial effects of the present invention:
1) present invention can be realized acid mist, SO in titanium dioxide calcining tail gas3、SO2, dust, NOx, the pollutants such as dioxin
Qualified discharge.
2) the first dedusting of the present invention, then desulfurization and denitration, can effectively avoid dust and sulfur trioxide to denitrating catalyst
Service life influence, a large amount of ammonium sulfate crystallizations can also be generated to avoid denitrating system and dedusting, desulfurization and heat exchanger are impacted.
3) air-introduced machine postposition of the present invention is it is possible to prevente effectively from abrasion and corrosion of the calcining tail gas to the impeller of air-introduced machine.
4) present invention can effectively solve the problems, such as the coloured plume of current hot topic.
5) present invention can be effectively using the heat of calcining tail gas, and a part is used to be concentrated dilute sulfuric acid, and another part is used
To heat flue gas, abjection pollutant etc..
6) present invention can recycle the moisture contained in calcining tail gas, reduce the whole water consume of titanium white production unit, section
About use water.
Detailed description of the invention
Fig. 1 is the schematic diagram for the system that the comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas is administered；
In figure, house-bag duster for high temperature 1, calcining exhaust pipe 1.1, gas cooler 2, venturi acid solution inspissator 3, acid
Liquid pipe 3.1, preconcentrator acid solution basin 4, recovery tube 4.1, dilute sulfuric acid recovery pump 5, flue gas desulfurization first stage tower 6, flue gas desulfurization two
Grade tower 7, flue gas condenser 8, cooling water low temperature side ducts 8.1, cooling water high temperature side ducts 8.2, demister 9, smoke re-heater
10, low temperature SCR denitration reactor 11, air-introduced machine 12, chimney 13, heat medium water low temperature side ducts 14, heating agent water-circulating pump 14.1, heat
Matchmaker's water high temperature side ducts 15.
Specific embodiment
The present invention is described in further detail combined with specific embodiments below, so as to those skilled in the art understand that.
The system that the comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas as shown in Figure 1 is administered, system includes that high-temperature bag removes
Dirt device 1, house-bag duster for high temperature 1 are internally provided with chimney filter, and chimney filter is ceramic fibre or metal filter candle, and single chimney filter outer diameter is
130~155mm, internal diameter are 100~120mm, and length is 2.5~5m, and the temperature range that chimney filter uses is 200~600 DEG C.
Calcining exhaust pipe 1.1 is circumscribed on 1 side wall of house-bag duster for high temperature, house-bag duster for high temperature 1 is connected by pipeline
It is connected to gas cooler 2, is connected at the top of gas cooler 2 and venturi acid solution inspissator 3,3 side wall of venturi acid solution inspissator
It is connect by being connected with acid solution pipe 3.1 with external plant area's acid solution, 3 bottom of venturi acid solution inspissator is provided with preconcentrator acid solution
Basin 4,4 side wall of preconcentrator acid solution basin are connect by recovery tube 4.1 with plant area acid-restoring plant；It is arranged on recovery tube 4.1
There is dilute sulfuric acid recovery pump 5；
4 side wall of preconcentrator acid solution basin is connected with flue gas desulfurization first stage tower 6 and flue gas desulfurization second level in turn by pipeline
Tower 7；Flue gas desulfurization second level tower 7, which is connected with to be arranged side by side by pipeline, flue gas condenser 8, demister 9 and smoke re-heater 10；
Flue gas condenser 8 is equipped with cooling water low temperature side ducts 8.1 and cooling water high temperature side ducts 8.2 form cooling water recirculation system；Cigarette
It is equipped with heat medium water low temperature side ducts 14 between Gas Cooler 2 and smoke re-heater 10 and heat medium water high temperature side ducts 15 form heating agent
Water circulation system；Heating agent water-circulating pump 14.1 is provided in heat medium water low temperature side ducts 14；Smoke re-heater 10 by pipeline according to
It is secondary to be connected with low temperature SCR denitration reactor 11 and chimney 13；It is provided on the pipeline of low temperature SCR denitration reactor 11 and chimney 13
Air-introduced machine 12.
The comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas dirt, sulphur, nitre, dioxin and wet plume is carried out using above-mentioned apparatus to control
The method of reason, comprising the following steps:
1) high-temperature bag dust removal by filtration: temperature be 200-450 DEG C titanium dioxide calcine tail gas by calcining exhaust pipe 1.1 into
Entering temperature is 450 DEG C, and pressure is that the house-bag duster for high temperature 1 of ± 6kPa removes dust and dioxin in tail gas, cigarette after filtering
Dust concentration is less than 5mg/Nm in gas3, dioxin removal rate is up to 99%；Wherein, titanium dioxide calcining tail gas Gas Parameters are as follows
Shown in table 1:
1 Gas Parameters table of table
| Serial number | Title | Unit | Quantity | |
| 1 | Raw flue gas volume flow | m3/h | 310000 | |
| 2 | Raw flue gas standard state volume flow | Nm3/h | 121559 | |
| 3 | Industry benchmark oxygen content | % | 7 | |
| 4 | Flue gas initial pressure | KPa | 100.825 | |
| 5 | Local average atmospheric pressure | KPa | 101.325 | |
| 6 | Raw flue gas temperature | ℃ | 420 | |
| 7 | Flue gas CO2Content | Vol% | 5 | |
| 8 | Flue gas H2O content | Vol% | 30.00 | |
| 9 | Flue gas N2Content | Vol% | 58 | |
| 10 | Flue gas O2Content | Vol% | 7 | |
| 11 | Flue gas SO2Content | mg/Nm3 | 5000 | |
| 12 | Flue gas SO3Content | mg/Nm3 | 8000 | |
| 13 | Flue gas NOxContent | mg/Nm3 | 300 | |
| 14 | Flue gas sulphuric acid mist content | mg/Nm3 | 2000 | |
| 15 | Exhaust gas dust content | mg/Nm3 | 10000 | Dust TiO2 |
2) flue gas is cooling:
A. enter gas cooler 2 by the flue gas of high-temperature bag filter collector 1, flue-gas temperature is dropped by 400~420 DEG C
Down to 300~330 DEG C；The water at low temperature of heat medium water low temperature side ducts 14 carries out heat source with high-temperature flue gas and exchanges to form high-temperature water, high
Warm water enters smoke re-heater 10 by heat medium water high temperature side ducts 15；Heating agent water flow and temperature according to system heat balance situation come
It determines；
3) acid pickle is concentrated: by the flue gas of gas cooler 2, spraying into venturi acid solution inspissator 3 and acid solution pipe 3.1
The sulfuric acid solution of leaching contacts, and flue-gas temperature is reduced to saturation state, i.e., 60~80 DEG C, while the moisture in acid pickle is steamed
Hair, exhausted water concentration are concentrated into 30% by original 20% and enter preconcentrator acid solution basin 4, is delivered to by sulfuric acid circulating pump 5
Reuse is carried out in plant area's acid-restoring plant；
4) flue gas desulfurization: the tail gas after waste acid concentration (contains more sulfur dioxide, sulfur trioxide and a small amount of
Sulfuric acid mist), sulfur dioxide in tail gas, sulfur trioxide and sulfuric acid when by flue gas desulfurization first stage tower 6 and flue gas desulfurization second level tower 7
Mist is removed, wherein in the tail gas of desulfurization, sulfur dioxide concentration≤35mg/Nm3, sulfur trioxide removal rate >=95%；
5) flue gas condensing: what flue gas condenser 8, cooling water low temperature side ducts 8.1 and cooling water high temperature side ducts 8.2 were formed
Cooling water recirculation system；The system uses the recirculated cooling water of certain temperature (0~40 DEG C), by flue gas condenser 8 by desulfurization
Tower exit gas temperature is down to 55 DEG C by 80 DEG C, while reducing the moisture content in flue gas, then passes through level-one flat defogger 9
After enter to smoke re-heater 10, by the high-temperature water of heat medium water high temperature side ducts 15 enter smoke re-heater 10 carry out heat source exchange
It forms water at low temperature and the flue gas after desulfurization is warming up to 220 DEG C again, water at low temperature is cold into flue gas by heat medium water low temperature side ducts 14
But device 2；
6) denitrating flue gas: the flue gas after desulfurization, which enters in continuous operation low temperature SCR denitration reactor 11, carries out selective urge
Change reduction reaction and carry out denitration, wherein denitration temperature is 200 DEG C, and removal efficiency reaches 90% or more；
7) discharge: the flue gas after denitration enters after air-introduced machine 12 is pressurized to be discharged by chimney 13, wherein 13 scheme heel row of chimney
It puts flue gas and reaches following technical indicator:
| Serial number | Index subjet | Unit | Index value |
| 1 | Final discharge SO2Concentration | mg/Nm3 | 35 |
| 2 | Final discharge NOxConcentration | mg/Nm3 | 50 |
| 3 | Final discharge acid mist concentration | mg/Nm3 | 10 |
| 4 | Final discharge dust concentration | mg/Nm3 | 5 |
| 5 | Exhaust gas temperature | ℃ | 180 |
Other unspecified parts are the prior art.Although above-described embodiment is made that the present invention and retouches in detail
State, but it is only a part of the embodiment of the present invention, rather than whole embodiments, people can also according to the present embodiment without
Other embodiments are obtained under the premise of creativeness, these embodiments belong to the scope of the present invention.
Claims (8)
1. the system that a kind of comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas is administered, it is characterised in that: the system comprises high temperature
Sack cleaner (1) is circumscribed with calcining exhaust pipe (1.1), the high-temperature bag on house-bag duster for high temperature (1) side wall
Deduster (1) is connected with gas cooler (2) by pipeline, and the gas cooler (2) and venturi acid solution inspissator (3) push up
Portion's connection, venturi acid solution inspissator (3) side wall are connect by being connected with acid solution pipe (3.1) with external plant area's acid solution, institute
It states venturi acid solution inspissator (3) bottom and is provided with preconcentrator acid solution basin (4), preconcentrator acid solution basin (4) side
Wall is connect by recovery tube (4.1) with plant area acid-restoring plant；Preconcentrator acid solution basin (4) side wall passes through pipeline successively
It is connected with flue gas desulfurization first stage tower (6) and flue gas desulfurization second level tower (7)；The flue gas desulfurization second level tower (7) is connected by pipeline
Have to be arranged side by side and has flue gas condenser (8), demister (9) and smoke re-heater (10)；The flue gas condenser (8) is equipped with cooling
Water low temperature side ducts (8.1) and cooling water high temperature side ducts (8.2) form cooling water recirculation system；The gas cooler (2)
It is equipped with heat medium water low temperature side ducts (14) between smoke re-heater (10) and heat medium water high temperature side ducts (15) form heat medium water
The circulatory system；The smoke re-heater (10) is connected with low temperature SCR denitration reactor (11) and chimney (13) in turn by pipeline.
2. the system that the comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas is administered according to claim 1, it is characterised in that: described
Dilute sulfuric acid recovery pump (5) are provided on recovery tube (4.1).
3. the system that the comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas is administered according to claim 1, it is characterised in that: described
Air-introduced machine (12) is provided on the pipeline of low temperature SCR denitration reactor (11) and chimney (13).
4. the system that the comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas is administered according to claim 1, it is characterised in that: described
Heating agent water-circulating pump (14.1) are provided in heat medium water low temperature side ducts (14).
5. the system that the comprehensive collaboration of titanium dioxide calcined by rotary kiln tail gas is administered according to claim 1, it is characterised in that: described
House-bag duster for high temperature (1) is internally provided with chimney filter, and the chimney filter is ceramic fibre or metal filter candle, and single chimney filter outer diameter is
130~155mm, internal diameter are 100~120mm, and length is 2.5~5m, and the temperature range that chimney filter uses is 200~600 DEG C.
6. a kind of carry out titanium dioxide calcined by rotary kiln tail gas dirt, sulphur, nitre, dioxin and wet cigarette using claim 1 described device
The method that the comprehensive collaboration of plumage is administered, it is characterised in that: the following steps are included:
1) high-temperature bag dust removal by filtration: the titanium dioxide that temperature is 200-450 DEG C is calcined tail gas and is entered by calcining exhaust pipe (1.1)
House-bag duster for high temperature (1) removes the dust and dioxin in tail gas, and dust is less than 5mg/Nm after filtering3, two
It dislikes English removal rate and is up to 99%；
2) flue gas is cooling:
A. enter gas cooler (2) by the flue gas of high-temperature bag filter collector (1), flue-gas temperature is dropped by 400~420 DEG C
Down to 300~330 DEG C；The water at low temperature of heat medium water low temperature side ducts (14) carries out heat source with high-temperature flue gas and exchanges to form high-temperature water,
High-temperature water enters smoke re-heater (10) by heat medium water high temperature side ducts (15)；Heating agent water flow and temperature are according to system heat balance
Situation determines；
3) acid pickle is concentrated: passing through the flue gas of gas cooler (2), into venturi acid solution inspissator (3) and acid solution pipe (3.1)
The sulfuric acid solution of spray contacts, and flue-gas temperature is reduced to saturation state, i.e., 60~80 DEG C, while the moisture in acid pickle is steamed
Hair, exhausted water concentration is concentrated into 30% by original 20% and enters preconcentrator acid solution basin (4), defeated by sulfuric acid circulating pump (5)
It send and carries out reuse into plant area's acid-restoring plant；
4) flue gas desulfurization: the tail gas after waste acid concentration is passing through flue gas desulfurization first stage tower (6) and flue gas desulfurization second level tower
(7) sulfur dioxide in tail gas, sulfur trioxide and sulfuric acid mist are removed when, wherein in the tail gas of desulfurization, sulfur dioxide concentration≤
35mg/Nm3, sulfur trioxide removal rate >=95%；
5) flue gas condensing: flue gas condenser (8), cooling water low temperature side ducts (8.1) and cooling water high temperature side ducts (8.2) formation
Cooling water recirculation system；The system uses temperature for 0~40 DEG C of recirculated cooling water, by flue gas condenser (8) by desulfurization
Tower exit gas temperature is down to 55 DEG C by 80 DEG C, while reducing the moisture content in flue gas, then passes through level-one flat defogger
(9) smoke re-heater (10) are entered to after；By the high-temperature water of heat medium water high temperature side ducts (15) enter smoke re-heater (10) into
Row heat source exchanges to form water at low temperature and the flue gas after desulfurization is warming up to 220 DEG C again, and water at low temperature is by heat medium water low temperature side ducts
(14) enter gas cooler (2)；
6) denitrating flue gas: the flue gas after desulfurization, which enters, carries out selective catalysis in continuous operation low temperature SCR denitration reactor (11)
Reduction reaction carries out denitration；
7) discharge: the flue gas after denitration is discharged after entering air-introduced machine (12) pressurization by chimney (13).
7. according to the method described in claim 1, it is characterized by: titanium dioxide calcines titanium dioxide in tail gas in the step 1)
Titanium valve dust content is 10000~15000mg/m3, the temperature of house-bag duster for high temperature (1) is 450 DEG C, and pressure is ± 6kPa.
8. according to the method described in claim 1, it is characterized by: denitration temperature is 200 DEG C, and removing is imitated in the step 6)
Rate reaches 90% or more.
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| 陈章水: "《水泥工业大气污染物排放标准达标实用技术及实例》", 30 April 2014, 中国建材工业出版社, pages: 148 * |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112076624A (en) * | 2020-09-15 | 2020-12-15 | 山东电力研究院 | SCR denitration device inlet smoke temperature adjusting system and method |
| CN112619372A (en) * | 2020-12-17 | 2021-04-09 | 襄阳龙蟒钛业有限公司 | Novel calcination tail gas desulfurization method |
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