CN104028103A - Method for catalyzing and oxidizing boiler smoke gas through chlorine dioxide and simultaneously desulfurizing and denitrating boiler smoke gas - Google Patents
Method for catalyzing and oxidizing boiler smoke gas through chlorine dioxide and simultaneously desulfurizing and denitrating boiler smoke gas Download PDFInfo
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- CN104028103A CN104028103A CN201410246700.9A CN201410246700A CN104028103A CN 104028103 A CN104028103 A CN 104028103A CN 201410246700 A CN201410246700 A CN 201410246700A CN 104028103 A CN104028103 A CN 104028103A
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Abstract
The invention discloses a method for catalyzing and oxidizing boiler smoke gas through chlorine dioxide and simultaneously desulfurizing and denitrating boiler smoke gas. The method comprises the following steps: injecting an absorption solution from the top of an absorption tower, introducing the smoke gas from the bottom of the absorption tower, and filling the absorption tower with a carrier loaded with a catalyst, wherein the absorption solution contains the chlorine dioxide with the concentration being 0.0015-0.015mol/L, the pH value of the absorption solution is 2-8,the temperature of the absorption solution is 20 DEG C-80 DEG C, the flow rate of the smoke gas is 0.05m/s-5m/s and a liquid-gas ratio between the absorption solution and the smoke gas is controlled to be 10-40L/m<3>. By virtue of the method for catalyzing and oxidizing boiler smoke gas through chlorine dioxide and simultaneously desulfurizing and denitrating boiler smoke gas, the pH value of the absorption solution is adjusted, meanwhile, the catalyst is used for activating, active radicals with a certain concentration are quickly generated on the surface of the catalyst, thus the desulfurizing rate and the denitrating rate are greatly improved, therefore the problem that the denitrating rate is not increased by increasing the use amount of the chlorine dioxide is solved; the method is free of complex device, low-cost chlorine dioxide is adopted, the parameters are controlled, and good effects of desulfurizing and denitrating are achieved, the maximum denitrating rate can reach 95%, and the maximum desulfurizing rate can reach 100%.
Description
Technical field
The present invention relates to industrial waste gas process field, relate in particular to a kind of boiler smoke ClO 2 catalyzed oxidation desulfurization denitration method simultaneously.
Background technology
Atmosphere is the most basic vital principle that the mankind depend on for existence, yet produces sulfur dioxide (SO while utilizing the fossil energy work by combustion such as coal, oil
2), oxynitrides (NO
x) and particle, SO
2and NO
xbeing topmost two kinds of atmosphere pollutions, is the main cause place of causing acid rain.While NO
xalso be a kind of material that causes the environmental problems such as depletion of the ozone layer and photochemical fog.The key factor that these have become restriction social and economic development, has caused the people of various countries' extensive concern.
Various countries scientist and commercial undertaking are devoted to the technical research of desulphurization denitration always.More than global sulfur method of researching and developing is existing hundreds of, method of denitration also has tens kinds more than, and these methods generally can be divided into dry method and wet method by technique.Utilizing state can be divided into absorption method and abandoning method by product; By absorption pattern, can be divided into Physical Absorption and chemical absorbing.
Existing denitration technology is mainly divided into two large classes: Combustion Process Control and burning post processing.Burning post processing comprises again: SNCR method (SNCR), selective catalytic reduction (SCR), thermal decomposition method, catalytic decomposition, gas scrubbing method, plasma improvement technology, liquid absorption method, the processing of oxidation absorption process etc.
Current global desulphurization and denitration carries out substantially in different ways, be that desulfurization separates processing with denitration, or desulfuration in furnace and the outer denitration mode of stove, or wet type desulfurizing and dry method denitration phase mode etc., although these methods can reach the requirement of environment protection emission in desulphurization and denitration effect, infrastructure investment is high, system floor space is large, operation is complicated, and operation and maintenance cost is very high, and enterprise has to bear high investment cost and operating cost.
The Chinese patent literature that for example publication number is CN101745305A discloses a kind of method that removes various gaseous pollutants in smoke gas, controls the limitation problem of improvement technology for solving flue gas multi-pollutant.It utilizes an absorption tower to SO in flue gas
2, NO
x, mercury vapour and CO
2remove comprehensively, bottom, described absorption tower arranges absorption slurry pool, and middle part arranges shower, top is provided with oxidant pipe, and absorption tower is longitudinally provided with dividing plate, dividing plate both sides are respectively desulfurization active section and denitration decarburization active section, the zoneofoxidation of top, absorption tower for being communicated with; Flue gas enters desulfurization active section by absorption tower import, completes SO
2with removing of HCl; Flue gas continues upwards to enter zoneofoxidation, at zoneofoxidation NO
xafter changing into high valence state oxide soluble in water, enter denitration decarburization active section, complete NO
x, mercury vapour and CO
2remove.
Through long research and development, successfully develop several flue gas and desulfurizing and denitrifying technology.The Chinese patent literature that is CN102500207A as publication number discloses a kind of coal-fired flue-gas while desulfurizing and denitrifying process of low temperature plasma oxidation bonding ammonia process wet absorption, this technique comprises low temperature plasma oxidation and two processes of ammonia process wet absorption, first pending coal-fired flue-gas enters reaction of low temperature plasma device by flue, makes in flue gas 40%～50% NO be oxidized to NO
2, the flue gas after processing enters desulphurization denitration spray column simultaneously, fully contacts with ammonia absorption liquid the SO removing in flue gas
2and NO
xrear discharge; The absorption liquid of while desulphurization denitration spray column bottom is again sent into spraying layer through absorption liquid circulating pump and is recycled, and constantly the ammoniacal liquor in ammonia vessel is supplemented into spray column by aqua ammonia pump, simultaneously by mother liquor delivery pump discharge unit mother liquor.
Day active carbon Absorption Desulfurization denitration synchronous process of the present invention, active carbon absorption technique is to utilize active carbon to have larger specific area to carry out flue gas and desulfurizing and denitrifying.SO
2be the micro-porous adsorption effect by active carbon, be stored in the micropore of active carbon, then regenerate by heat, generate the SO of high concentration
2gas, forms the byproducts such as high-purity sulphur, the concentrated sulfuric acid through reforming unit; NO
xthat catalytic action generation water and the nitrogen through active carbon enters atmosphere under the condition of ammonification, the advantage of this method is non-secondary pollution, desulfuration efficiency can reach 90% left and right, shortcoming be active carbon kind very little, the high operation expense that causes of purchase cost is too high, although denitration efficiency can reach 65% left and right simultaneously, along with the also decline thereupon of decay denitration efficiency of active carbon activity, stable not.
China is used the maximum country of Industrial Boiler, in the end of the year 2011, with coal-burned industrial boiler, is being 62.03 ten thousand, consumes every year approximately 6.4 hundred million tons, raw coal, the SO of generation
2and NO
xaccount for respectively 22.2% and 15% of national total release.SO
2, NO
xand the secondary pollution forming not only damages ecological environment and affect health, also directly cause huge economic loss.At present, China's coal-burned industrial boiler has a large capacity and a wide range, and pollution intensity is disperseed greatly.
A large amount of coal-burned industrial boiler flue gas desulfurization and denitrification facilities are unsound, the situation that has facility not move is very general, and main cause is that existing flue gas desulfurization and denitration method treatment effect is not good, and high cost, the actual requirement of Industrial Boiler can not be met, the approval of enterprise can not be obtained.Therefore, the desulphurization denitration technology of the low-cost high-efficiency of the applicable coal-burned industrial boiler of research is extremely urgent.
Summary of the invention
The invention provides a kind of boiler smoke ClO 2 catalyzed oxidation desulfurization denitration method simultaneously, denitrification efficiency is high, and processing cost is lower.
The technical scheme that the present invention deals with problems is:
Boiler smoke ClO 2 catalyzed oxidation is a desulfurization denitration method simultaneously, comprises absorption liquid is sprayed into from top, absorption tower, and flue gas imports from bottom, absorption tower,
In described absorption tower, being filled with load has the carrier of catalyst, contains the chlorine dioxide that concentration is 0.0015～0.015mol/L in described absorption liquid, and the pH value of absorption liquid is 2～8, and the temperature of absorption liquid is 20 ℃～80 ℃;
Flue gas flow rate is 0.05m/s～5m/s, and the liquid-gas ratio of controlling between absorption liquid and flue gas is 10～40L/m
3.
Principle of the present invention is:
Absorption liquid main component chlorine dioxide (ClO
2) there is very strong oxidability, can with sulfur dioxide in flue gas (SO
2) and nitrogen oxide (NO
x, more than 95% be NO) occur may react as follows:
5SO
2+2ClO
2+6H
2O→5H
2SO
4+2HCl (1)
5NO+2ClO
2+H
2O→5NO
2+2HCl (2)
5NO
2+ClO
2+3H
2O→5HNO
3+HCl (3)
In addition, in the preparation process of absorption liquid, chlorine dioxide (ClO
2) water-soluble, there is the chlorition (ClO that disproportionated reaction generates
2 -), hypochlorite ion (ClO
-), chlorine (Cl
2) and chloranion (ClO
3 -) also there is strong oxidability, can with flue gas in sulfur dioxide (SO
2) reaction generation sulfate ion (SO4
2-), with the nitrogen oxide (NO in flue gas
x) reaction generation nitrate ion (NO
3 -), thereby remove sulfur dioxide in flue gas and nitrogen oxide.
Under certain pH value and temperature conditions, chlorition and chlorine (Cl
2) existence and the oxidability of absorbent solution is improved greatly.The reaction of this series of complex is all conducive to the carrying out of desulfurization and denitrification reaction and the raising of efficiency simultaneously.
With chlorine dioxide, adopt prior art desulphurization denitration simultaneously, even if the consumption of chlorine dioxide increases, but denitration rate is difficult to improve.The present invention is by regulating pH value to make absorption liquid produce appropriate chlorition, hypochlorite ion and chlorine (Cl
2) isoreactivity material, add and can produce synergistic catalyst, can make desulfurization degree and denitration rate increase substantially.
The pH value of absorption liquid can produce a certain amount of active material to improve desulfurization degree and denitration rate at 2～8 o'clock, and especially take the pH value of absorption liquid, be 4～6 o'clock, and the active material of generation is maximum, the most obvious to the effect of raising desulfurization degree and denitration rate.
As preferably, the pH value of described absorption liquid is 4～6.
As preferably, in described absorption liquid, contain the chlorine dioxide that concentration is 0.003～0.015mol/L.Under this concentration, desulphurization denitration rate is higher.
Unilaterally changing the parameters such as chlorine dioxide concentration, flue gas flow rate and gas liquid ratio that contain in change pH values, absorption liquid all can exert an influence to desulfurization degree and denitration rate, just the effect of each parameter generating varies in size, when every kind of parameter all reaches optimum and each parameter matching, desulfurization degree and denitration rate are the highest, preferably, the pH value of described absorption liquid is 4～6, in described absorption liquid, contain concentration and be 0.003～0.015 chlorine dioxide, flue gas flow rate is 0.5～0.7m/s, the liquid-gas ratio 13～16L/m between absorption liquid and flue gas
3.
In described absorption tower, filled carrier, on carrier load corresponding catalyst.General absorption tower, for liquid is evenly distributed in tower, can arrange filler in absorption tower, to increase solution-air contact-making surface, it is mixed strongly.
And go back load on carrier of the present invention, there is catalyst, when improving the contact area of gas-liquid-solid three-phase, also the chlorine dioxide in absorption liquid is activated.
As preferably, described carrier is cellular ceramic substrate.Described cellular ceramic substrate can make the gas or the liquid distribution that flow through even, and the structure of its porous can increase the contact area of catalyst and gas or liquid, increases catalyst effecting reaction area.The optional ceramic honey comb of described cellular ceramic substrate, ceramic honey comb surface area is larger, and gas-liquid-solid three-phase contact area is larger.
As preferably, described catalyst is transition metal oxide, inert metal or inert metal oxides, and this catalyst is acidproof catalyst.
Due to invention, processing waste gas is to carry out under acidity or slant acidity condition, and catalyst must be acidproof catalyst, otherwise catalyst can inactivation.Transition metal oxide, inert metal or inert metal oxides all can, V for example
2o
5, CrO
3, TiO
2, MnO
2or Pt etc.
As preferably, described catalyst is TiO
2or MnO
2.
Chlorine dioxide can be at TiO
2or MnO
2surface disintegration produces free radical, and further with water, reaction generates a certain amount of hydroxyl radical free radical, has changed chemistry route, is conducive to the raising of desulphurization denitration rate.These two kinds of catalyst are under acid condition, and stability is better.
Described chlorine dioxide is produced by chlorine dioxide generator, more water-soluble dilution formation absorption liquid, and with hydrochloric acid and NaOH water, regulates the pH value of absorption liquid.In a series of processes of dissolving, dilution, adjust pH etc., all can produce a small amount of chlorition, chlorine (Cl
2), hypochlorite ion and chloranion.
Chlorition wherein, chlorine (Cl
2), hypochlorite ion and chloranion can improve desulphurization denitration rate, especially larger to the contribution of denitration rate.
SO in absorption liquid of the present invention and flue gas
2and NO
xchemical reaction occurs and generate harmless product, last absorption liquid is processed after circulation absorbs, and after processing method can be discharged circulation fluid and react with ammoniacal liquor, obtains the mixture of ammonium sulfate, ammonium nitrate and ammonium chloride through condensing crystallizing.
Beneficial effect of the present invention is: by regulating the pH value of absorption liquid, make it produce a small amount of hypochlorite ion and chlorition etc., and make absorption liquid by load, have the filler of catalyst, at catalyst surface, can produce rapidly certain density hydroxyl radical free radical, desulfurization degree and denitration rate are increased substantially, and having overcome Chlorine increases the difficult point that still denitration rate does not increase.
The present invention does not need complicated equipment, adopts cheap chlorine dioxide as absorbing medium and control each parameter to reach good desulfurization off sulfide effect, and flue gas desulphuization rate reaches as high as 100%, and denitration rate reaches as high as 95%.
The specific embodiment
Below in conjunction with specific embodiment, the invention will be further described.
The common preparation process of chlorine dioxide absorption liquid is as follows: by chlorine dioxide generator, produced the materials such as chlorine dioxide and be dissolved in water again, be stored in fresh absorption liquid storage tank after being then diluted to finite concentration.
The preparation method that specifically can adopt has several as follows:
(1) electrolytic saltwater: finite concentration or saturated saline solution are added to electrolyzer anode chamber, clear water is added to electric tank cathode chamber simultaneously, connect 12V dc source and start electrolysis, can produce ClO
2, Cl
2, H
2o
2deng hybrid oxidant, by the negative pressure of jet pump, gas is sucked in water and makes ClO after dissolving
2the aqueous solution for main oxidant.The absorption liquid that electrolysis makes, except containing the chlorine-bearing compounds such as chlorine dioxide, also contains H
2o
2.
(2) chemical reaction method that sodium chlorate is raw material: utilize sodium chlorate and hydrochloric acid reaction to make chlorine dioxide and chlorine gas, be then dissolved in the water and make.Can also utilize in addition sodium chlorate and sulfuric acid and hydrogen peroxide to react under the effect of composite catalyst and produce chlorine dioxide and oxygen, be dissolved in water and make absorption liquid.
(3) chemical reaction method that sodium chlorite is raw material: utilize sodium chlorite and hydrochloric acid reaction to make highly purified chlorine dioxide, be then dissolved in the water and make.
In flue gas desulfurization and denitrification process, flue gas enters from bottom, absorption tower, and absorption liquid sprays into absorption tower from top, absorption tower, filled honeycomb type or other macroporous solid catalysts in absorption tower, after sulfur dioxide in flue gas and nitrogen oxide are absorbed, the gas of purification is from absorption tower top discharge.
Absorption liquid in use, automatically adds fresh absorption liquid according to the needs of while desulphurization denitration and enters absorption liquid circulating slot, makes the sulfur dioxide that will remove in chlorine dioxide and flue gas in absorption liquid and the amount maintenance balance of nitrogen oxide.According to SO in flue gas
2, NO
xconcentration and flue gas flow rate, calculate the speed that roughly consumes chlorine dioxide in absorption liquid, this wear rate is exactly the speed of automatically adding chlorine dioxide.In circulating absorption solution, sulfate and nitrate reaches after finite concentration, draws absorption tower and carries out harmless treatment.
Embodiment 1
According to above-mentioned either method, prepare absorption liquid, the concentration of chlorine dioxide is 0.003mol/L, and wherein chlorition concentration is 0.0002～0.0005mol/L, and hypochlorite ion's concentration is 8 * 10
-5～12 * 10
-5mol/L, the concentration of chloranion is 0.0002～0.0005mol/L;
With hydrochloric acid, regulate the pH value to 4 of absorption liquid;
Load is had to catalyst TiO
2ceramic honey comb be seated in absorption tower;
Above-mentioned absorption liquid is packed in the circulation reservoir on absorption tower, and enter absorption tower from absorption tower top spray, flue gas is imported from bottom, absorption tower, control flue gas flow rate 0.7m/s, liquid-gas ratio 15L/m
3, keep 40 ℃ of absorbent solution constant temperature.
The test of desulphurization denitration rate:
Take initial concentration as 600mg/m
3nO and initial concentration be 1300mg/m
3sO
2as simulated flue gas, process.After processing, with flue gas analyzer, measure sulfur dioxide and the nitrous oxides concentration that enters front and back, absorption tower, comparative analysis show that desulfurization degree reaches 99%, and denitration rate reaches more than 90%.
Embodiment 2
According to above-mentioned either method, prepare absorption liquid, the concentration of chlorine dioxide is 0.0015mol/L, and wherein the concentration containing chlorition is 0.0001～0.0004mol/L, and hypochlorite ion's concentration is 5 * 10
-5～7 * 10
-5mol/L, the concentration of chloranion is 0.0001～0.0004mol/L;
With hydrochloric acid, regulate the pH value to 5 of absorption liquid;
Load is had to catalyst TiO
2ceramic honey comb be seated in absorption tower;
Above-mentioned absorption liquid is packed in the circulation reservoir on absorption tower, and enter absorption tower from absorption tower top spray, flue gas is imported from bottom, absorption tower, control flue gas flow rate 0.7m/s, liquid-gas ratio 16L/m
3, keep 40 ℃ of absorbent solution constant temperature.
The test of desulphurization denitration rate:
Take initial concentration as 600mg/m
3nO and initial concentration be 1300mg/m
3sO
2as simulated flue gas, process.After processing, with flue gas analyzer, measure sulfur dioxide and the nitrous oxides concentration that enters front and back, absorption tower, comparative analysis show that denitration rate reaches more than 78%, and desulfurization degree reaches 100%.
Embodiment 3
According to above-mentioned either method, prepare absorption liquid, the concentration of chlorine dioxide is 0.003mol/L, and wherein the concentration containing chlorition is 0.0002～0.0005mol/L, and hypochlorite ion's concentration is 7 * 10
-5～9 * 10
-5mol/L, chloranion concentration be 0.0002～0.0005mol/L;
With hydrochloric acid, regulate the pH value to 5 of absorption liquid;
Load is had to catalyst TiO
2ceramic honey comb be seated in absorption tower;
Above-mentioned absorption liquid is packed in the circulation reservoir on absorption tower, and enter absorption tower from absorption tower top spray, flue gas is imported from bottom, absorption tower, control flue gas flow rate 0.5m/s, liquid-gas ratio 13L/m
3, keep 40 ℃ of absorbent solution constant temperature.
The test of desulphurization denitration rate:
Take initial concentration as 500mg/m
3nO and initial concentration be 1500mg/m
3sO
2as simulated flue gas, process.After processing, with flue gas analyzer, measure sulfur dioxide and the nitrous oxides concentration that enters front and back, absorption tower, comparative analysis show that denitration rate reaches more than 80%, and desulfurization degree reaches 100%.
Embodiment 4
According to above-mentioned either method, prepare absorption liquid, the concentration of chlorine dioxide is 0.006mol/L, containing chlorition concentration, be wherein 0.0004～0.0007mol/L, hypochlorite ion's concentration is 0.00015～0.0003mol/L, and the concentration of chloranion is 0.0005～0.001mol/L;
With NaOH and hydrochloric acid, regulate absorption liquid pH value to 7;
Load is had to catalyst TiO
2ceramic honey comb be seated in absorption tower;
Above-mentioned absorption liquid is packed in the circulation reservoir on absorption tower, and enter absorption tower from absorption tower top spray, flue gas is imported from bottom, absorption tower, control flue gas flow rate 0.5m/s, liquid-gas ratio 18L/m
3, keep 40 ℃ of absorbent solution constant temperature.
The test of desulphurization denitration rate:
Take initial concentration as 1200mg/m
3nO and initial concentration be 1500mg/m
3sO
2as simulated flue gas, process.After processing, with flue gas analyzer, measure sulfur dioxide and the nitrous oxides concentration that enters front and back, absorption tower, comparative analysis show that denitration rate reaches more than 80%, and desulfurization degree reaches 100%.
Embodiment 5
According to above-mentioned either method, prepare absorption liquid, the concentration of chlorine dioxide is 0.015mol/L, wherein, containing the concentration 0.001～0.003mol/L of chlorition, hypochlorite ion's concentration is 0.0002～0.0008mol/L, and the concentration of chloranion is 0.001～0.003mol/L;
With NaOH, regulate the pH value to 8 of absorption liquid;
Load is had to catalyst TiO
2ceramic honey comb be seated in absorption tower;
Above-mentioned absorption liquid is packed in the circulation reservoir on absorption tower, and enter absorption tower from absorption tower top spray, flue gas is imported from bottom, absorption tower, control flue gas flow rate 4m/s, liquid-gas ratio 25～30L/m
3, keep 60 ℃ of absorbent solution constant temperature.
The test of desulphurization denitration rate:
Take initial concentration as 1000mg/m
3nO and initial concentration be 1500mg/m
3sO
2as simulated flue gas, process.After processing, with flue gas analyzer, measure sulfur dioxide and the nitrous oxides concentration that enters front and back, absorption tower, comparative analysis show that denitration rate reaches more than 86%, and desulfurization degree reaches 100%.
Embodiment 6
According to above-mentioned either method, prepare absorption liquid, the concentration of chlorine dioxide is 0.015mol/L, concentration 0.0007mol/L～the 0.003mol/L of chlorition wherein, hypochlorite ion's concentration is 0.0002～0.0007mol/L, and the concentration of chloranion is 0.0005mol/L～0.002mol/L;
With hydrochloric acid, regulate absorption liquid pH value to 5;
Load is had to catalyst TiO
2ceramic honey comb be seated in absorption tower;
Above-mentioned absorption liquid is packed in the circulation reservoir on absorption tower, and enter absorption tower from absorption tower top spray, flue gas is imported from bottom, absorption tower, control flue gas flow rate 5m/s, liquid-gas ratio 26～30L/m
3, keep 50 ℃ of absorbent solution constant temperature.
The test of desulphurization denitration rate:
Take initial concentration as 1200mg/m
3nO and initial concentration be 2000mg/m
3sO
2as simulated flue gas, process.After processing, with flue gas analyzer, measure sulfur dioxide and the nitrous oxides concentration that enters front and back, absorption tower, comparative analysis show that denitration rate reaches more than 75%, and desulfurization degree reaches 100%.
Claims (7)
1. a boiler smoke ClO 2 catalyzed oxidation while desulfurization denitration method, comprises absorption liquid is sprayed into from the top on absorption tower, and flue gas imports from bottom, absorption tower, it is characterized in that:
In described absorption tower, fill load and had the carrier of catalyst;
In described absorption liquid, contain the chlorine dioxide that concentration is 0.0015～0.015mol/L, the pH value of absorption liquid is 2～8, and the temperature of absorption liquid is 20 ℃～80 ℃;
Flue gas flow rate is 0.05m/s～5m/s, and the liquid-gas ratio of controlling between absorption liquid and flue gas is 10～40L/m
3.
2. boiler smoke ClO 2 catalyzed oxidation while desulfurization denitration method as claimed in claim 1, is characterized in that: the pH value of described absorption liquid is 4～6.
3. boiler smoke ClO 2 catalyzed oxidation while desulfurization denitration method as claimed in claim 1 or 2, is characterized in that: in described absorption liquid, contain the chlorine dioxide that concentration is 0.003～0.015mol/L.
4. boiler smoke ClO 2 catalyzed oxidation as claimed in claim 1 desulfurization denitration method simultaneously, it is characterized in that: the pH value of described absorption liquid is 4～6, in described absorption liquid, contain concentration and be 0.003～0.015 chlorine dioxide, flue gas flow rate is 0.5～0.7m/s, the liquid-gas ratio 13～16L/m between absorption liquid and flue gas
3.
5. boiler smoke ClO 2 catalyzed oxidation while desulfurization denitration method as claimed in claim 1, is characterized in that: described carrier is cellular ceramic substrate.
6. boiler smoke ClO 2 catalyzed oxidation while desulfurization denitration method as claimed in claim 1, it is characterized in that: described catalyst is transition metal oxide, inert metal or inert metal oxides, and this catalyst is acidproof catalyst.
7. the while of the boiler smoke ClO 2 catalyzed oxidation as described in claim 1 or 6 desulfurization denitration method, is characterized in that: described catalyst is TiO
2or MnO
2.
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|---|---|---|---|
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| CN110624385A (en) * | 2019-10-17 | 2019-12-31 | 中瑞工程设计院有限公司 | Low-temperature denitration system and method for sodium chlorite solution |
| CN111282417A (en) * | 2020-03-11 | 2020-06-16 | 山东师范大学 | Method for denitration of flue gas by using chlorine dioxide |
| CN111644063A (en) * | 2020-07-03 | 2020-09-11 | 中国环境科学研究院 | Based on ClO2Denitration liquid regeneration system and method for flue gas denitration |
| CN112933875A (en) * | 2021-02-25 | 2021-06-11 | 滨州中科催化技术有限公司 | Desulfurization and denitrification tower and desulfurization and denitrification method |
| CN113117486A (en) * | 2019-12-30 | 2021-07-16 | 中晶环境科技股份有限公司 | Integrated treatment method for flue gas desulfurization and denitrification and cementing material preparation |
| CN113447614A (en) * | 2021-06-21 | 2021-09-28 | 中国原子能科学研究院 | Method for measuring denitration rate in radioactive waste liquid calcination process |
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| CN102553428A (en) * | 2012-01-10 | 2012-07-11 | 华北电力大学（保定） | Absorption tower for desulfurization and denitrification combined with oxidant in forward-flow and back-flow spraying and method |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110624385A (en) * | 2019-10-17 | 2019-12-31 | 中瑞工程设计院有限公司 | Low-temperature denitration system and method for sodium chlorite solution |
| CN113117486A (en) * | 2019-12-30 | 2021-07-16 | 中晶环境科技股份有限公司 | Integrated treatment method for flue gas desulfurization and denitrification and cementing material preparation |
| CN111282417A (en) * | 2020-03-11 | 2020-06-16 | 山东师范大学 | Method for denitration of flue gas by using chlorine dioxide |
| CN111282417B (en) * | 2020-03-11 | 2024-05-24 | 山东师范大学 | Method for flue gas denitration by using chlorine dioxide |
| CN111644063A (en) * | 2020-07-03 | 2020-09-11 | 中国环境科学研究院 | Based on ClO2Denitration liquid regeneration system and method for flue gas denitration |
| CN112933875A (en) * | 2021-02-25 | 2021-06-11 | 滨州中科催化技术有限公司 | Desulfurization and denitrification tower and desulfurization and denitrification method |
| CN112933875B (en) * | 2021-02-25 | 2023-01-17 | 滨州中科催化技术有限公司 | Desulfurization and denitrification tower and desulfurization and denitrification method |
| CN113447614A (en) * | 2021-06-21 | 2021-09-28 | 中国原子能科学研究院 | Method for measuring denitration rate in radioactive waste liquid calcination process |
| CN113447614B (en) * | 2021-06-21 | 2022-08-09 | 中国原子能科学研究院 | Method for measuring denitration rate in radioactive waste liquid calcination process |
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