CN104815538A - Photolytic peroxide up and down counter spray atomizing bed desulfurization and denitrification method - Google Patents
Photolytic peroxide up and down counter spray atomizing bed desulfurization and denitrification method Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention relates to a photolytic peroxide up and down counter spray atomizing bed desulfurization and denitrification method. The method mainly comprises an emission source, a fan, a dust remover, a gas cooler, an up and down counter spray atomizing bed, a circulating pump I, a circulating pump II, a filling layer, an ultraviolet tube, atomizing nozzles, a demister, a liquid storage tank and a product after-processing system. SO2 and NO from the emission source react with sulfate radicals and hydroxyl radicals generated by decomposing peroxides through ultraviolet to produce sulfuric acid and nitric acid solutions applicable to resource utilization. The photolytic peroxide up and down counter spray atomizing bed desulfurization and denitrification method can effectively remove the SO2 and NO in flue gas and avoid secondary pollution during removal, and achieve a novel flue gas purification system having a broad application prospect.
Description
Technical field
The present invention relates to Air Pollution Control field, be specifically related to a kind of photodissociation peroxide up and down to atomization bed desulfurization denitration method.
Background technology
The SO produced in combustion process
2﹑ NO
xand Hg can cause Suan Yu ﹑ photochemical fog and the serious atmosphere polluting problem such as carcinogenic, the healthy and ecological balance of harm humans.In the past few decades, although be developed a large amount of flue gas desulfurization and denitrification demercuration technology, existing various desulfurization denitration demercuration technology research and development originally only for Single Pollution thing for removing target, remove while cannot multi-pollutant being realized.
Such as, the more flue gas desulfurization and denitrification technology of application is mainly wet desulfurization of flue gas by limestone-gypsum method technology and ammine selectivity catalytic reduction method at present.Though these two kinds of methods can desulphurization denitration separately, cannot remove realizing in atomization bed about one simultaneously.Although two kinds of technique superpositions use and can realize simultaneous SO_2 and NO removal, cause whole system complicated, floor space is large, investment and the high deficiency of operating cost.In addition, along with the mankind's improving constantly environmental requirement, the laws and regulations for mercury in flue gas emission control are also put into effect gradually, but also do not have a kind of cost-effective flue gas demercuration technology to obtain large-scale commercial applications application at present.If again increase independent flue gas mercury removal system in existing desulfurization and denitrating system afterbody, then the initial cost and operating cost that cause whole system certainly will be increased further, final being difficult to is applied to obtain large-scale commercial applications in developing country.
In sum, if can about one in atomization bed by SO
2﹑ NO
x﹑ Hg removes simultaneously, be then expected to the complexity and the floor space that greatly reduce system, and then reduces investment and the operating cost of system.Therefore, the effective sulphur/nitrogen of exploiting economy/mercury simultaneously removing sulfuldioxide is the current hot issue in this field.
Summary of the invention
The present invention relates to a kind of photodissociation peroxide up and down to atomization bed desulfurization denitration method.From the SO of emission source
2﹑ NO and Hg
0first in flue is SO by ozone pre-oxidation
3﹑ NO
2and Hg
2+.Uviol lamp ultraviolet light radiation excites peroxide to produce sulfate radical and hydroxyl radical free radical is oxidized SO further
2﹑ NO ﹑ Hg
0and by SO that ozone oxidation produces
3and NO
2, product mainly resourcebility utilize Liu Suan ﹑ nitric acid and dimercurion.This system can SO in efficient removal flue gas
2﹑ NO and Hg
0, and subtractive process non-secondary pollution, be a kind of Novel fume cleaning system with broad prospect of application.
The present invention record method based on principle and course of reaction as follows:
1 ﹑ as shown in Figure 1, adopts electron spin resonance (ESR) instrument can be measured in system and creates potentiometric titrations and hydroxyl radical free radical.Therefore, first light radiation peroxide is release the potentiometric titrations and hydroxyl radical free radical with strong oxidizing property, and detailed process can represent with following chemical reaction (1)-(5):
H
2O
2+UV→2·OH (1)
O
3+UV→·O+O
2(3)
·O+H
2O
2→·OH+HO
2· (6)
Sulphur/nitrogen/mercury oxidation in flue gas can remove by potentiometric titrations and the hydroxyl radical free radical of the strong oxidizing property 2, produced:
a·OH+bSO
2→cSO
3++other products (7)
a·OH+bNO→cNO
2++other products (8)
3, react the sulphur acid ﹑ nitric acid mixed solution produced and can be used as raw material of industry recycling (such as, recycling with rear generation ammonium sulfate and ammonium nitrate agricultural fertilizer by adding in ammonia).This system can SO in efficient removal flue gas
2and NO, and subtractive process non-secondary pollution, be a kind of Novel fume cleaning system with broad prospect of application.
For realizing the object of desulphurization denitration, based on above-mentioned principle, the technical solution used in the present invention is as follows:
A kind of photodissociation peroxide up and down to atomization bed desulfurization denitration method, the flue gas of emission source introduces deduster through blower fan, gas cooler is entered after deduster dedusting, after gas cooler cooling, enter up and down to atomization bed by bottom, be 20-70 DEG C to the smoke inlet temperature of atomization bed up and down, effective liquid-gas ratio is 0.1-5.0L/m
3, liquid reserve tank sprays into up and down to atomization bed after being atomized by atomizer by the peroxide solutions in liquid reserve tank by circulating pump one, reacted peroxide solutions is introduced liquid reserve tank through circulating pump two and is recycled, the concentration of peroxide is between 0.1mol/L-3.5mol/L, the pH of solution is between 1.0-9.5, solution temperature is 20-70 DEG C, described is oppositely arranged the atomizer of atomization bed up and down, the peroxide solutions of atomization sprays and clashes into, ultraviolet lamp tube is provided with in the middle of the described atomizer be oppositely arranged, the ultraviolet light that uviol lamp is launched intensifies peroxide and produces hydroxyl radical free radical, SO in oxidation flue gas
2and NO, the Net long wave radiation intensity of ultraviolet light is 10 μ W/cm
2-400 μ W/cm
2, ultraviolet EWL is 150nm-365nm, pass through the flue gas of purification by discharging the top exhanst gas outlet of atomization bed up and down, the product produced after reaction is by passing into product postprocessing system to the product exit d of atomization bed up and down, and in flue gas, the content of SO2 and NO is not respectively higher than 10000ppm and 2000ppm.
The too high meeting of smoke inlet temperature causes peroxide that the waste of selfdecomposition in advance occurs, if but smoke inlet temperature is too low, and can reduce chemical reaction rate, thus reduce the removal efficiency of pollutant.20-70 DEG C is that inventor is according to orthogonal experiment and the comprehensive best smoke inlet temperature analyzing rear acquisition, smoke inlet temperature more than 70 DEG C after the decomposition rate of peroxide increase considerably, but smoke inlet temperature then significantly reduces lower than chemical reaction rate when 20 DEG C, the removal efficiency of pollutant is caused significantly to decline.Therefore, be 20-70 DEG C to the best smoke inlet temperature of atomization bed up and down.
Liquid-gas ratio is too low, and the removal efficiency of pollutant is too low, cannot meet environmental requirement, but liquid-gas ratio setting is too high, and the power of circulating pump is crossed conference and caused the energy consumption of system greatly to increase.Inventor finds through the experiment of system and theoretical research, and effective liquid-gas ratio is 0.1-5.0L/m
3.The too low free-radical oxidation that cannot discharge abundance of peroxide concentrations removes pollutant, but the peroxide once throwing in too high concentration can cause extra selfdecomposition and side reaction, selfdecomposition can cause peroxide oxidant consumption serious, increase operating cost, side reaction can cause producing various harmful components in product, affects recycling of end product.Through experiment and the discovery after detecting analysis of inventor, the optium concentration of peroxide is 0.1mol/L-3.5mol/L.
The too high meeting of pH of peroxide solutions causes peroxide accelerate selfdecomposition and consume, and increases application cost, but chemical absorbing can be suppressed when pH is too low to balance, cause pollutant removing efficiency to remain on low-level, cannot meet environmental protection index.Inventor through the reality of system test grind study carefully ﹑ theoretical research and detect analyze after find, solution Optimal pH is between 1.0-9.5.The too high meeting of solution temperature causes peroxide that the expensive oxidant of the waste of selfdecomposition in advance occurs, if but solution temperature is too low, and can reduce chemical reaction rate, thus reduce pollutant removing efficiency.Solution temperature more than 70 DEG C after the decomposition rate of peroxide increase considerably, but solution temperature then significantly reduces lower than chemical reaction rate when 20 DEG C, causes the removal efficiency of pollutant significantly to decline.Therefore, be 20-70 DEG C to the best solution temperature of atomization bed up and down.
Inventor finds after adopting electronic self-rotary resonant technology to detect, the too low free-radical oxidation that cannot generate enough concentration that ultraviolet light Net long wave radiation intensity is arranged removes pollutant, but the too high energy consumption of system that will cause of ultraviolet radiation intensity increases substantially, reduce the economy of system.Therefore, ultraviolet light Net long wave radiation intensity is 10 μ W/cm
2-400 μ W/cm
2if ultraviolet EWL is selected too short, then the propagation distance of ultraviolet light in reactor is too short, pollutant treating capacity under unit power reduces greatly, basic processing requirements cannot be met, if but ultraviolet wavelength select oversize, the energy of ultraviolet photon will obviously reduce, low-energy ultraviolet photon cannot destroy the molecular link of peroxide, thus the free-radical oxidation that cannot produce enough concentration removes pollutant.Find after comprehensive detection is analyzed, ultraviolet EWL is 150nm-365nm.
Inventor is through the experiment of system and find after detecting analysis, SO in flue gas
2﹑ NO
xthe too high removal efficiency that will cause of content significantly decline, the unabsorbed middle SO of afterbody
2﹑ NO
xescape amount increases considerably, and easily causes serious secondary pollution, therefore finds after research, SO in flue gas
2distinguish not higher than 10000ppm and 2000ppm with the content of NO.
Preferred technical parameter, the SO in flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm; Be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, ammonium persulfate concentrations is 3.0mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 82 μ W/cm
2, ultraviolet EWL is 254nm.Adopt above-mentioned parameter, pilot run is, SO in flue gas
2100% and 100% can be reached respectively with removal efficiency while NO.
Described peroxide comprises one or both the mixing in hydrogen peroxide and ammonium persulfate.Described emission source comprises one or more the combination in Ran coal Guo Lu ﹑ Nei Ran Ji ﹑ Gong industry Yao Lu ﹑ smelting/coking Wei Qi ﹑ incinerator and petrochemical equipment tail gas.
Described a kind of photodissociation peroxide up and down to atomization bed desulfurization denitration method based on device be provided with emission source, blower fan, deduster, gas cooler, up and down to atomization bed, circulating pump one and circulating pump two, liquid reserve tank and product postprocessing system; Describedly up and down exhanst gas outlet, demister, atomizer, ultraviolet lamp tube, packing layer and outlet at bottom are provided with successively from top to bottom to atomization bed; Emission source connects deduster entrance by flue, the outlet of deduster connects the entrance of gas cooler, the outlet of described gas cooler connects up and down to the bottom of atomization bed, described liquid reserve tank enters up and down in atomization bed by pipeline, and described pipeline is provided with at least one group of laterally zygomorphic atomizer; Described up and down to being provided with ultraviolet lamp tube row between atomizer laterally zygomorphic in atomization bed.
Described liquid reserve tank enters the circulating pump one up and down pipeline of atomization bed being provided with to the atomization bed introduced by peroxide solutions; Describedly up and down the taphole of atomization bed is provided with to the circulating pump two peroxide solutions being introduced liquid reserve tank.
Up and down to the cross section of atomization bed be square or rectangle, inside is provided with the ultraviolet lamp tube row of more than a group, often organize ultraviolet lamp tube row and be equipped with atomizer up and down, the atomizer on ultraviolet lamp tube row top sprays solution downwards, and the atomizer of ultraviolet lamp tube row bottom upwards sprays solution.Distance A between two adjacent groups ultraviolet lamp tube row is between 10cm-50cm.In ultraviolet lamp tube row, the spacing B of adjacent two ultraviolet lamp tubes is between 3cm-30cm, to reach best light radiation effect.Ultraviolet lamp tube one end (right-hand member) is fixed on up and down in atomization bed wall after inserting, and the other end (left end) is changed and maintenance through being convenient to ultraviolet lamp tube to more than 1cm reserved after atomization bed wall up and down.Often organizing the upper best ultraviolet lamp tube number arranged of ultraviolet lamp tube row's vertical direction (above-below direction) is that 5-10 follows, and the best ultraviolet lamp tube number that horizontal direction is arranged can by determining the sectional area of atomization bed and the ultraviolet lamp tube distance computation of selection up and down.
It is significant to note that: the above various Optimal Parameters selected are all that inventor passes through just to obtain after a large amount of Zong conjunction Shi Yan ﹑ theory calculate is analyzed with detection.Because each operating parameter also can be subject to combined influence or the interference of other one or more parameter usually, therefore cannot be obtained by simple on-the-spot experiment of single factor or document contrast.Optimal Parameters provided by the invention determines after Comprehensive Correlation on mini-plant and the equipment after amplifying in addition, considered equipment amplification process issuable " enlarge-effect ", therefore field technician is not by obtaining safe and reliable Optimal Parameters to inferring after existing equipment simple analysis.
Advantage of the present invention and remarkable result:
Chinese patent 201010296492.5 proposes a kind of simultaneous SO_2 and NO removal system utilizing light radiation hydrogen peroxide to produce free radical, but what this removing process described in this patent adopted is the bubbling column reactor that mass transfer rate is very low and market application potential is little, and the bed accessory of spraying up and down that the present invention proposes has better mass transfer rate and removal efficiency, thus increase substantially the removal efficiency of pollutant.Such as, present system can realize SO
2namely demonstrate this system with 100% removal efficiency of NO two kinds of pollutants to have and outstanding remove performance.
Accompanying drawing explanation
Fig. 1. photodissociation peroxide is up and down to the electron spin resonance figure of atomization bed.
Fig. 2 is the process chart of system of the present invention.
Fig. 3 is up and down to atomization bed structure figure.
Fig. 4 is up and down to cross section and the fluorescent tube layout drawing of atomization bed.
Fig. 5 is product postprocessing system of the present invention.
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is further described.
As shown in Figure 2, the present invention relates to a kind of photodissociation peroxide up and down to the method for atomization bed desulphurization denitration institute based on device, be mainly provided with emission source 1, blower fan 2, deduster 3, gas cooler 4, up and down to atomization bed 6, circulating pump 1 and circulating pump 28, packing layer 13, ultraviolet lamp tube 12, atomizer 11, demister, 10 liquid reserve tanks 9 and product postprocessing system 5.Describedly up and down exhanst gas outlet c, demister 10, atomizer 11, ultraviolet lamp tube 12, packing layer 13 and outlet at bottom d are provided with successively to atomization bed 6 from top to bottom; Emission source 1 connects deduster 3 entrance by flue, is provided with blower fan 2 between emission source 1 and deduster 3; The outlet of deduster 3 connects the entrance of gas cooler 4, the outlet of described gas cooler 4 connects up and down to the bottom of atomization bed 6, described liquid reserve tank 9 connects up and down to the atomizer 11 in atomization bed 6 by pipeline, and described pipeline is provided with at least one group of laterally zygomorphic atomizer 11; Described up and down to being provided with the ultraviolet lamp tube row be made up of uviol lamp 12 between atomizer 11 laterally zygomorphic in atomization bed 6.
As shown in Figure 3 and Figure 4, up and down to the cross section of atomization bed 6 be square or rectangle, inside be provided with more than one group ultraviolet lamp tube row, often organize ultraviolet lamp tube row be equipped with atomizer 11 up and down; The atomizer 11 on ultraviolet lamp tube row top sprays solution downwards, and the atomizer 11 of ultraviolet lamp tube row bottom upwards sprays solution.
Distance A between two adjacent groups ultraviolet lamp tube row is between 10cm-50cm; In ultraviolet lamp tube row, the spacing B of adjacent two ultraviolet lamp tubes is between 3cm-30cm.
As shown in Figure 5, the product postprocessing system of the method, product postprocessing system 5 with up and down the product exit d bottom atomization bed 6 is connected, product postprocessing system 5 is provided with solution circulation pump 14, described product postprocessing system 5 connects neutralizing tower 15 and evaporating and crystallizing tower 16 successively, and evaporating and crystallizing tower 16 adopts fume afterheat system 17 to heat; In neutralizing tower 14 by adding in ammonia and, enter evaporative crystallization in evaporating and crystallizing tower 16 after neutralization, finally produce ammonium sulfate and ammonium nitrate agricultural fertilizer is recycled.
Course of reaction is as follows: the flue gas from emission source 1 is drawn by blower fan 2, after deduster 3 dedusting and gas cooler 4 are lowered the temperature, then enters up and down to atomization bed 6 by after packing layer 13 cloth wind.Peroxide solutions from liquid reserve tank 9 is aspirated by circulating pump 1, and sprays into up and down to atomization bed 6 after being atomized by atomizer 11.Uviol lamp 12 ultraviolet light radiation excites peroxide to produce sulfate radical and hydroxyl radical free radical oxidation SO
2sulfuric acid and the salpeter solution of resourcebility utilization is produced with NO.Up and down to atomization bed 6 top fall after rise sulfuric acid and salpeter solution by exporting b, through circulating pump 28 again sucks liquid reserve tank 9 circulating atomization spray.Product realizes resourcebility utilization by passing into product postprocessing system 5 to the product exit d of atomization bed 6 up and down.
SO in embodiment 1. flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm, and be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 40 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas
2100% and 70.2% can be reached respectively with removal efficiency while NO.
SO in embodiment 2. flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm, and be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, ammonium persulfate concentrations is 1.0mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 40 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas
2100% and 67.4% can be reached respectively with removal efficiency while NO.
SO in embodiment 3. flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm, and be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 40 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas
2100% and 79.9% can be reached respectively with removal efficiency while NO.
SO in embodiment 4. flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm, and be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, ammonium persulfate concentrations is 1.5mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 40 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas
2100% and 76.5% can be reached respectively with removal efficiency while NO.
SO in embodiment 5. flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm, and be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 82 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas
2100% and 88.3% can be reached respectively with removal efficiency while NO.
SO in embodiment 6. flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm, and be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, ammonium persulfate concentrations is 1.5mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 82 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas
2100% and 86.3% can be reached respectively with removal efficiency while NO.
SO in embodiment 7. flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm, and be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, hydrogen peroxide concentration is 2.0mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 82 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas
2100% and 95.7% can be reached respectively with removal efficiency while NO.
SO in embodiment 8. flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm, and be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, ammonium persulfate concentrations is 2.0mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 82 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas
2100% and 93.9% can be reached respectively with removal efficiency while NO.
SO in embodiment 9. flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm, and be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, hydrogen peroxide concentration is 3.0mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 82 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas
2100% and 100% can be reached respectively with removal efficiency while NO.
SO in embodiment 10. flue gas
2﹑ NO concentration is respectively 3000ppm, 400ppm, and be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, ammonium persulfate concentrations is 3.0mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 82 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas
2100% and 100% can be reached respectively with removal efficiency while NO.
Comprehensive Correlation through above embodiment is known, and embodiment 9 and 10 has best simultaneous SO_2 and NO removal effect, can be used as most preferred embodiment and consults and uses.
Claims (5)
1. a photodissociation peroxide up and down to atomization bed desulfurization denitration method, it is characterized in that, the flue gas of emission source introduces deduster through blower fan, gas cooler is entered after deduster dedusting, after gas cooler cooling, enter up and down to atomization bed by bottom, be 20-70 DEG C to the smoke inlet temperature of atomization bed up and down, effective liquid-gas ratio is 0.1-5.0L/m
3, liquid reserve tank sprays into up and down to atomization bed after being atomized by atomizer by the peroxide solutions in liquid reserve tank by circulating pump one, reacted peroxide solutions is introduced liquid reserve tank through circulating pump two and is recycled, the concentration of peroxide is between 0.1mol/L-3.5mol/L, the pH of solution is between 1.0-9.5, solution temperature is 20-70 DEG C, described is oppositely arranged the atomizer of atomization bed up and down, the peroxide solutions of atomization sprays and clashes into, ultraviolet lamp tube is provided with in the middle of the described atomizer be oppositely arranged, the ultraviolet light that uviol lamp is launched intensifies peroxide and produces hydroxyl radical free radical, SO in oxidation flue gas
2and NO, the Net long wave radiation intensity of ultraviolet light is 10 μ W/cm
2-400 μ W/cm
2, ultraviolet EWL is 150nm-365nm, pass through the flue gas of purification by discharging the top exhanst gas outlet of atomization bed up and down, the product produced after reaction is by passing into product postprocessing system to the product exit d of atomization bed up and down.
2. a kind of photodissociation peroxide according to claim 1 up and down to atomization bed desulfurization denitration method, it is characterized in that, in flue gas, the content of SO2 and NO is not respectively higher than 10000ppm and 2000ppm.
3. a kind of photodissociation peroxide according to claim 2 up and down to atomization bed desulfurization denitration method, it is characterized in that, be 55 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.0L/m
3, ammonium persulfate concentrations is 3.0mol/L, and pH value of solution is 3.5, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 82 μ W/cm
2, ultraviolet EWL is 254nm.
4. a kind of photodissociation peroxide according to claim 1 and 2 up and down to atomization bed desulfurization denitration method, it is characterized in that: described peroxide comprises one or both the mixing in hydrogen peroxide and ammonium persulfate.
5. a kind of photodissociation peroxide according to claim 1 and 2 up and down to atomization bed desulfurization denitration method, it is characterized in that: described emission source comprises one or more the combination in Ran coal Guo Lu ﹑ Nei Ran Ji ﹑ Gong industry Yao Lu ﹑ smelting/coking Wei Qi ﹑ incinerator and petrochemical equipment tail gas.
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| CN110090538A (en) * | 2019-04-17 | 2019-08-06 | 安徽节源环保科技有限公司 | A kind of oxyradical wet process of FGD method of denitration |
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| CN109224654A (en) * | 2018-11-03 | 2019-01-18 | 郭绍华 | System for cleaning fume |
| CN110090538A (en) * | 2019-04-17 | 2019-08-06 | 安徽节源环保科技有限公司 | A kind of oxyradical wet process of FGD method of denitration |
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