CN102166471A - Heterogeneous-Photo-Fenton-based integrated smoke gas purification system - Google Patents
Heterogeneous-Photo-Fenton-based integrated smoke gas purification system Download PDFInfo
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Abstract
The invention discloses a heterogeneous-Photo-Fenton-based integrated smoke gas purification system. The smoke gas purification system generates a hydroxyl radical (.OH) with strong oxidizability by using heterogeneous Photo-Fenton to oxidize SO2, NO and Hg0 in the smoke gas into H2SO4, HNO3 and Hg2<+> respectively, wherein the H2SO4, the HNO3 and the Hg2<+> are fixed in solution; after reaction, a solid catalyst in mixed solution can be recycled through simple primary precipitation separation; a small amount of Hg2<+> in the solution can be generated into insoluble HgS by adding the same mole ratio of S2<->, and then the HgS is recycled through secondary precipitation separation; and the remaining sulfuric acid and nitric acid solution can be used as an industrial raw material to be further recycled. The whole integrated desulfuration, denitration and demercuration processes generate no secondary pollution, so the heterogeneous-Photo-Fenton-based integrated smoke gas purification system has a very good application prospect.
Description
Technical field
The present invention relates to the control of smoke emissioning pollution thing in the combustion process, relate in particular to a kind of integrated fume cleaning system based on heterogeneous Photo-Fenton.
Background technology
The oxysulfide that produces in the combustion process, nitrogen oxide and mercury can cause acid rain, photochemical fog and serious harms such as carcinogenic and teratogenesis.Therefore, researching and developing effective flue gas desulfurization and denitrification demercuration method is one of vital task of various countries' environmental protection scientific and technical personnel.In the last few years, although people have developed a large amount of flue gas desulfurization and denitrification demercuration technology, but because human cognitive process's limitation and scientific technological advance is gradual, existing various desulfurization denitration demercuration technology research and development originally only at single pollutant for removing target, remove when generally can't realize flue gas multiple pollutant.For example, use more flue gas desulfurization and denitrification technology at present and be mainly wet method limestone-gypsum method flue gas desulfurization technology (Ca-WFGD) and ammine selectivity catalytic reduction method (NH
3-SCR),, all can't in a reactor, realize removing simultaneously though these two kinds of technologies can be distinguished independent desulphurization denitration.Though the stack of uniting of two kinds of technologies is used and can be realized desulphurization denitration simultaneously, also causes the whole system complexity simultaneously, floor space is big, investment and the high deficiency of operating cost.In addition, along with the mankind to the improving constantly of environmental requirement, also put into effect gradually at the laws and regulations of mercury emissions control in the flue gas, use but also there is a kind of cost-effective flue gas demercuration technology to obtain large-scale commercial applications at present.If at existing C a-WFGD and NH
3-SCR system for desulfuration and denitration afterbody increases independent flue gas demercuration system once more, then certainly will will cause the initial outlay of whole system and operating cost further sharply to increase, and finally is difficult in developing country's acquisition large-scale commercial applications and uses.
In sum, if can in a reactor, oxysulfide, nitrogen oxide and mercury be realized removing simultaneously, then can reduce the complexity and the floor space of system greatly, and then reduce the initial cost and the operating cost of system.The wet type flue gas desulphurization technology is a kind of traditional flue gas treatment technology, have that initial cost is little, technological process is simple and is easy to realize characteristics such as multi-pollutant removes simultaneously, it is the flue gases purification that a kind of extremely has the development and application prospect, but traditional wet type flue gas desulphurization Study on Technology progress is slow relatively always, and its main cause just is to contain respectively in nitrogen oxide and the mercury element NO of 90% above indissoluble and the Hg of 40-80% indissoluble
0By double-film theory as can be known, gas molecule in space must at first dissolve in liquid phase by gaseous state through mass transfer and diffusion process, and chemical reaction could take place then to be fixed in the absorption liquid, and NO and Hg
0The characteristic of indissoluble makes its absorption resistance to mass tranfer in liquid phase increase greatly, only is difficult to significantly improve NO and Hg by regulation and control absorption liquid pH and method of temperature
0In the solubility of liquid phase, this characteristic has caused traditional wet desulphurization denitration demercuration technology ubiquity desulfuration efficiency height, but the low deficiency that waits of denitration and demercuration efficient, in fact can't realize desulfurization denitration demercuration real the time.Therefore, searching can be with NO and Hg
0Being converted into easy molten effective morphological fast is one of key that addresses this problem.
Summary of the invention
The invention discloses a kind of integrated fume cleaning system based on heterogeneous Photo-Fenton, promptly utilize heterogeneous Photo-Fenton (ultraviolet light, hydrogen peroxide, solid catalyst advanced oxidation processes) to produce hydroxyl radical free radical (OH), with the SO in the flue gas with strong oxidizing property
2, NO
xAnd Hg
0Be oxidized to H respectively
2SO
4, HNO
3And Hg
2+Be fixed in the solution, the solid catalyst in the solution of reaction back can be by realizing recycling after the simple precipitate and separate, the Hg in the solution
2+Can be by the sulfidion S of mol ratios such as interpolation
2-Generate the HgS of indissoluble, recycle through realizing after the precipitate and separate then, further recycle and remaining sulfuric acid and salpeter solution can be used as the raw material of industry, whole integration desulfurization denitration demercuration process non-secondary pollution is the flue gases purification that a kind of extremely has application prospect.
For realizing above purpose, the embodiment that the present invention adopts is: a kind of integrated fume cleaning system based on heterogeneous Photo-Fenton, it is characterized in that: the burning and the exhaust system that be provided with burner, heat exchanger, bubble tower, add the liquid tower, two-stage knockout tower, regenerator, air-introduced machine and chimney constitute, burner combustion produces comprises SO
2, NO
xAnd Hg
0Flue gas through after the heat exchanger cooling, the nozzle that is provided with from the bubble tower bottom feeds bubble tower, the heterogeneous Fenton reagent that contains hydrogen peroxide and solid catalyst adds to add behind the liquid tower by first circulating pump and also feeds bubble tower from the top of bubble tower, be provided with ultraviolet lamp tube in the bubble tower, flue gas and heterogeneous Fenton reagent produce the Gas-Liquid Absorption reaction in bubble tower, ultraviolet excitation decomposes heterogeneous Fenton reagent and discharges the hydroxyl radical free radical (OH) with strong oxidizing property, with the SO in the flue gas
2, NO
xAnd Hg
0Be oxidized to H
2SO
4, HNO
3And Hg
2+And be fixed in the solution, it is recycling that general's 20-40% mixed solution wherein adds the liquid tower by the second circulating pump suction, remaining mixed solution is then by sending into regenerator by the 4th circulating pump after the 3rd circulating pump suction one-level knockout tower precipitate and separate, fed once more by the 5th circulating pump behind the solid catalyst regeneration in the mixed solution and adds the liquid tower and recycle; Through the Hg that contains after the one-level separation
2+Solution is by the 6th circulating pump suction secondary knockout tower, by the sulfidion S to mol ratios such as secondary knockout tower interpolations
2-Reaction generates the HgS of indissoluble, and through realizing the recycling of mercuric sulphide after the precipitate and separate, remaining high-concentration sulfuric acid and salpeter solution are recycled as the raw material of industry, and the flue gas after the washing passes through air-introduced machine suction smoke stack emission by the bubble tower top.
Ultraviolet lamp tube is vertical with the bubble tower bottom surface, and unit volume ultraviolet radiation power is 5W/m in the bubble tower
3-200W/m
3, the W/m of unit
3Be meant bubble tower before uviol lamp is not installed, the needed ultraviolet radiation power of unit volume when bubble tower is void tower, ultraviolet wavelength is 120nm-360nm.When many ultraviolet lamp tubes were set, many ultraviolet lamp tubes were the concentric circles setting, and distance is identical between the neighboring concentric circle, many ultraviolet lamp tubes are distributed on the circumference of different-diameter, along same diameter line setting, the central angle between each adjacent two diameter line is identical, and circle centre position is provided with ultraviolet lamp tube; Nozzle is arranged on the concentric circumferences with ultraviolet lamp tube concentric circles alternate intervals uniform, and places on the diameter line of two ultraviolet lamp tube central angle half-angles,
Solid catalyst is Fe
2O
3, MnO
2, CuO or TiO
2In a kind of, solid catalyst in regenerator by high-temperature calcination means activating and regenerating, its calcining heat is in 300 ℃ of-600 ℃ of scopes, the mass concentration that solid catalyst adds is in the 0.5g/L-5.0g/L scope, the particle diameter of solid catalyst is between 80 orders-200 order, and the molar concentration that hydrogen peroxide adds is at 0.1mol/L-2.5mol/L.
15 ℃-75 ℃ of the flue-gas temperatures of bubble tower inlet, liquid-gas ratio is 5L/m
3-50L/m
3, and flow through time of staying of bubbling column reactor of flue gas be 0.5s-20s.
The sulfidion S that adds in the secondary knockout tower
2-Mole and Hg solution
2+Mole equate i.e. n (S
2-): n (Hg
2+)=1: 1.
System response process of the present invention:
1, heterogeneous Photo-Fenton advanced oxidation processes discharges the hydroxyl radical free radical (OH) with strong oxidizing property:
Fe
2+-S+H
2O
2-S→Fe
3+-S+·OH-S+OH
--S (1)
Fe
3+-S+H
2O
2-S→Fe
3+(HO
2)
2+-S+H
+-S (2)
FeOH
2+-S+H
2O
2-S→Fe
3+(OH)(HO
2)
+-S+H
+-S (3)
Fe
3+(HO
2)
2+-S+hv-S→Fe
2+-S+·HO
2-S (4)
Fe
3+(OH)(HO
2)
+-S+hv-S→Fe
2+-S+·HO
2-S+OH
--S (5)
2, the SO in the burner discharged flue gas
2, NO
xAnd Hg
0Generated H by hydroxyl radical free radical (OH) oxidation
2SO
4, HNO
3And Hg
2+Mixed solution:
NO-S+·OH-S→HNO
2-S (6)
NO
2-S+·OH-S→HNO
3-S (7)
SO
2-S+·OH-S→HSO
3-S (8)
HSO
3-S+·OH-S→H
2SO
4-S (9)
Hg
0-S+·OH-S→HgO-S+·H-S (10)
Hg
0-S+·OH-S→Hg(OH)
2-S (11)
3, solid catalyst can be sent into regenerator activating and regenerating, cycling and reutilization then after precipitate and separate in the one-level knockout tower;
4, the Hg of reaction generation
2+The S that can be added
2+Absorb and react the HgS sediment that generates indissoluble, recycle through after the precipitate and separate then:
Hg
2++S
2-→HgS↓ (12)
5, after the heavy metal Hg element is hunted down recovery, the sulfuric acid and the nitric acid mixed solution that only are left high concentration in the solution can be used as raw material of industry recycling, whole integration desulfurization denitration demercuration process non-secondary pollution.
Advantage of the present invention and remarkable result: heterogeneous Photo-Fenton advanced oxidation processes can discharge the hydroxyl radical free radical (OH) with extremely strong oxidability, and the reaction rate constant of OH and most organic is up to 10
6-10
10Mol/Ls can attack all contaminations easily and it is degraded to harmless product, and the solid catalyst in the course of reaction is easy to separate and regeneration cycle is used, and is that a kind of oxidability is strong, the advanced oxidation removing process of clean environmental protection and non-selectivity.With the applicant (a kind of system for desulfuration and denitration based on the photochemistry advanced oxidation time: 201012096592.5) with (a kind of flue gas demercuration system based on the effect of photochemistry advanced oxidation: 201012096592.8) compare, the present invention has following remarkable advantages:
(1) along with people's improving constantly to environmental requirement, laws and regulations at mercury emissions control in the flue gas are also put into effect gradually, the present invention can realize removing in three kinds of pollutants such as oxysulfide, nitrogen oxide and heavy metal element mercury in a reactor, thereby can further reduce the initial outlay and the operating cost of system.Along with the mankind to the improving constantly of environmental requirement, this advantage of the present invention will be highlighted gradually, and 201012096592.5 and 201012096592.8 all can't realize removing in three kinds of pollutants in same reactor.
(2) the present invention can be by adding the removal efficiency that callable high-performance solid catalyst further improves pollutant, and the same terms can also reduce the dosage of hydrogen peroxide down significantly, and then can reduce the use cost of hydrogen peroxide significantly.In addition, solid catalyst can be realized the regeneration cycle use among the present invention after the simple precipitate and separate of process, whole subtractive process non-secondary pollution, thereby be the novel flue gases purification that a kind of extremely has application prospect.
Description of drawings
Fig. 1 is a system flow chart of the present invention;
Fig. 2 is the fitting arrangement of system of the present invention bubbling bed inner nozzle and ultraviolet lamp tube.
The specific embodiment
Referring to Fig. 1,2, from containing finite concentration SO in the burner (boiler) 1
2, NO
xAnd Hg
0Flue gas at first be cooled to suitable temperature through heat exchanger, feed the liquid phase reactor districts from the nozzle 3 of bubbling bed 4 bottoms then and participate in the Gas-Liquid Absorption reaction; Heterogeneous Fenton reagent at first adds and adds liquid tower 12, is added from the top of bubble tower 4 by first circulating pump 7 then to the liquid phase reactor districts participate in the Gas-Liquid Absorption reaction in the bubbling bed 4; The uviol lamp 6 that is with quartz socket tube 5 excites and decomposes the hydroxyl radical free radical OH that heterogeneous Fenton reagent release has strong oxidizing property, and rapidly with the SO in the flue gas
2, NO
xAnd Hg
0Be oxidized to H respectively
2SO
4, HNO
3And Hg
2+Solution; For sulfuric acid and the salpeter solution of producing high concentration, reduce the processing cost of liquid product, the partially mixed solution that reaction generates needs recycling by second circulating pump 8 suction the adding liquid tower 12, remaining mixed solution is then by the 3rd circulating pump 9 suction one-level knockout towers 10, solid catalyst is realized regeneration activatings through sending into regenerator 14 by the 4th circulating pump 11 after the simple precipitate and separate in one-level knockout tower 10, the solid catalyst after the regeneration is fed once more by the 5th circulating pump 13 and adds liquid tower 12 and recycle; Through the Hg that contains after the one-level separation
2+Solution passes through the sulfidion S of mol ratios such as interpolation then then by the 6th circulating pump 15 suction secondary knockout towers 16
2-Reaction generates the HgS of indissoluble, and through realizing the recycling of mercury element mercuric sulphide after the precipitate and separate, last remaining high-concentration sulfuric acid and salpeter solution then can be used as the raw material of industry and recycle; Enter atmosphere from bubble tower 4 tops after by air-introduced machine 17 suction chimneys 18 through the flue gas after the washing.
In the said system:
Because flue-gas temperature is higher, if high-temperature flue gas directly feeds bubble tower liquid phase reactor district, then the solubility of vapor phase contaminants will descend, and causes the removal efficiency of target contaminant to descend.In addition, high temperature also can cause hydrogen peroxide directly to be decomposed into oxygen, and utilization rate descends.Therefore, before flue gas fed bubble tower, high-temperature flue gas need effectively cool off by heat exchanger, so the bubble tower entrance flue gas temperature generally should be controlled between 15-75 ℃.
Owing to contain fine particle in the flue gas, if uviol lamp is directly exposed in the flue gas, then uviol lamp is easy to wash away because of the high speed of particle and damages.Therefore, uviol lamp need put the quartz socket tube of being made by the quartz material of high-penetration light rate at outer surface, the internal diameter of quartz socket tube need be than the external diameter of uviol lamp big 2-4mm, length keeps equating with uviol lamp or is close.In order to maximally utilise luminous energy, improve ultraviolet radiation intensity, the uviol lamp in the reactor must keep vertical with the bubble tower bottom surface when mounted.In addition, even in order to keep in the reactor ultraviolet radiation, increase the luminous energy effective rate of utilization, it is equal that the spacing b between the uviol lamp must keep, and central angle a also must keep equating.Simultaneously, if the layout density of uviol lamp in reactor is too big, then the flow resistance of flue gas will increase in the reactor, cause the operating load and the energy consumption of system to increase, if but uviol lamp arranges that density is too little in the reactor, then be difficult to the light radiation intensity that reaches enough, thereby cause the pollutant removing index not reach environmental requirement.Therefore, the optimum range of uviol lamp spacing b and central angle a generally is respectively 2cm-30cm and 10-40 degree.The uv light irradiation strength relationship is to the size of quantum yield or the productive rate of hydroxyl radical free radical OH.Be difficult to fully excite ozone to decompose the hydroxyl radical free radical OH oxidation removal pollutant that produces sufficient amount if ultraviolet light irradiation intensity is too little, but if ultraviolet light irradiation intensity is too big, then the energy consumption of system will significantly increase.Therefore, ultraviolet ray intensity need remain on 5W/m
3-200W/m
3, the W/m of unit wherein
3Be meant reactor before uviol lamp is not installed, the needed ultraviolet radiation power of unit volume when reactor is void tower.When ultraviolet wavelength more in short-term, the photon excitation of ultraviolet light can increase relatively, but this moment ultraviolet light propagation distance shorter, the pollutant disposal ability that shows as the unit power ultraviolet light is lower.When ultraviolet wavelength is longer, although the propagation distance of ultraviolet light can increase, but this moment, the excitation energy of ultraviolet light photons significantly reduced, cause ultraviolet light photons to excite and decompose the energy shortage that heterogeneous Fenton reagent discharges hydroxyl radical free radical OH, finally cause the removal efficiency of pollutant to be difficult to satisfy environmental requirement.Therefore, the EWL of ultraviolet light should remain in the 160nm-360nm scope.
The effective mass concentration that solid catalyst adds should remain in the 0.5g/L-5.0g/L scope, and effective molar concentration that hydrogen peroxide adds should remain on 0.1mol/L-2.5mol/L.If dosage is too high, then will cause application cost to rise, otherwise then the removal efficiency of pollutant is difficult to reach requirement.In addition, the particle diameter of the solid catalyst that adds also has strict requirement, if the particle diameter that adds is too big, then the specific area of catalyst can descend, if bring very big difficulty can for the one-level precipitate and separate but the solid catalyst particle diameter is too little, increases the post processing cost.Therefore, the particle diameter of solid catalyst generally should remain between 80 orders-200 order.
The sulfidion S that adds in the Gas-Liquid Absorption tower
2-Amount need strict control criterion, if excessive interpolation S
2-Will cause secondary pollution and application cost to increase, but S
2-Addition is too little then can to cause the MODEL OF CHEMICAL ABSORPTION PROCESS in the secondary knockout tower abundant inadequately, Hg
2+Capture rate low.Therefore, in the practical application, add S
2-Mole should with Hg solution
2+Mole keep to equate, promptly need to keep n (S
2-): n (Hg
2+)=1: 1.
Because separating when reclaiming, the liquid phase mix products need pass through after-treatment.Therefore, if mixed solution concentration is too rare, then certainly will the after-treatment expense will be increased.Therefore, the whole system that removes need be provided with solution part recirculating system, and promptly the mixed solution that produces of reaction back generally needs 20-40% to be added the liquid tower by suction again recycling, so that increase solution concentration, and then reduces the post processing cost of product.
SO in embodiment 1. flue gases
2, NO and Hg
0Concentration is respectively 2000ppm, 500ppm and 100ug/m
3, solid catalyst is Fe
2O
3Particle (mass concentration is 1.0g/L, and particle diameter is 100 orders), flue-gas temperature is 25 ℃, and ultraviolet wavelength is 254nm, and the UV radiation intensity is 100W/m
3, the hydrogen peroxide molar concentration is 1.0mol/L, liquid-gas ratio is 20L/m
3, the effect time of staying is 10s, uviol lamp spacing b and central angle a are respectively 10cm and 25 when spending, SO in the flue gas
2, NO and Hg
0Integrated removal efficiency can reach 92.1%, 80.9% and 98.8% respectively.
SO in embodiment 2. flue gases
2, NO and Hg
0Concentration is respectively 2000ppm, 500ppm and 100ug/m
3, solid catalyst is Fe
2O
3Particle (mass concentration is 1.0g/L, and particle diameter is 100 orders), flue-gas temperature is 25 ℃, and ultraviolet wavelength is 254nm, and the UV radiation intensity is 150W/m
3, the hydrogen peroxide molar concentration is 1.0mol/L, liquid-gas ratio is 20L/m
3, the effect time of staying is 10s, uviol lamp spacing b and central angle a are respectively 10cm and 25 when spending, SO in the flue gas
2, NO and Hg
0Integrated removal efficiency can reach 100%, 92.2% and 100% respectively.
SO in embodiment 3. flue gases
2, NO and Hg
0Concentration is respectively 2000ppm, 500ppm and 100ug/m
3, solid catalyst is Fe
2O
3Particle (mass concentration is 1.0g/L, and particle diameter is 100 orders), flue-gas temperature is 25 ℃, and ultraviolet wavelength is 254nm, and the UV radiation intensity is 100W/m
3, the hydrogen peroxide molar concentration is 1.0mol/L, liquid-gas ratio is 20L/m
3, the effect time of staying is 10s, uviol lamp spacing b and central angle a are respectively 10cm and 25 when spending, SO in the flue gas
2, NO and Hg
0Integrated removal efficiency can reach 89.2%, 83.2% and 100% respectively.
SO in embodiment 4. flue gases
2, NO and Hg
0Concentration is respectively 2000ppm, 500ppm and 100ug/m
3, solid catalyst is Fe
2O
3Particle (mass concentration is 1.0g/L, and particle diameter is 100 orders), flue-gas temperature is 25 ℃, and ultraviolet wavelength is 254nm, and the UV radiation intensity is 50W/m
3, the hydrogen peroxide molar concentration is 1.0mol/L, liquid-gas ratio is 15L/m
3, the effect time of staying is 10s, uviol lamp spacing b and central angle a are respectively 10cm and 25 when spending, SO in the flue gas
2, NO and Hg
0Integrated removal efficiency can reach 85.8%, 70.8% and 93.7% respectively.
In sum, embodiment 2 has best integration desulfurization denitration demercuration effect, can be used as most preferred embodiment and consults and uses.
Claims (6)
1. integrated fume cleaning system based on heterogeneous Photo-Fenton, it is characterized in that: the burning and the exhaust system that be provided with burner, heat exchanger, bubble tower, add the liquid tower, two-stage knockout tower, regenerator, air-introduced machine and chimney constitute, burner combustion produces comprises SO
2﹑ NO
xAnd Hg
0Flue gas through after the heat exchanger cooling, the nozzle that is provided with from the bubble tower bottom feeds bubble tower, the heterogeneous Fenton reagent that contains hydrogen peroxide and solid catalyst adds to add behind the liquid tower by first circulating pump and also feeds bubble tower from the top of bubble tower, be provided with ultraviolet lamp tube in the bubble tower, flue gas and heterogeneous Fenton reagent produce the Gas-Liquid Absorption reaction in bubble tower, ultraviolet excitation decomposes heterogeneous Fenton reagent and discharges the hydroxyl radical free radical (OH) with strong oxidizing property, with the SO in the flue gas
2﹑ NO
xAnd Hg
0Be oxidized to H
2SO
4﹑ HNO
3And Hg
2+And be fixed in the solution, it is recycling that general's 20-40% mixed solution wherein adds the liquid tower by the second circulating pump suction, remaining mixed solution is then by sending into regenerator by the 4th circulating pump after the 3rd circulating pump suction one-level knockout tower precipitate and separate, fed once more by the 5th circulating pump behind the solid catalyst regeneration in the mixed solution and adds the liquid tower and recycle; Through the Hg that contains after the one-level separation
2+Solution is by the 6th circulating pump suction secondary knockout tower, by the sulfidion S to mol ratios such as secondary knockout tower interpolations
2-Reaction generates the HgS of indissoluble, and through realizing the recycling of mercuric sulphide after the precipitate and separate, remaining high-concentration sulfuric acid and salpeter solution are recycled as the raw material of industry, and the flue gas after the washing passes through air-introduced machine suction smoke stack emission by the bubble tower top.
2. the integrated fume cleaning system based on heterogeneous Photo-Fenton according to claim 1, it is characterized in that: ultraviolet lamp tube is vertical with the bubble tower bottom surface, and unit volume ultraviolet radiation power is 5W/m in the bubble tower
3-200W/m
3, the W/m of unit
3Be meant bubble tower before uviol lamp is not installed, the needed ultraviolet radiation power of unit volume when bubble tower is void tower, ultraviolet wavelength is 120nm-360nm.
3. the integrated fume cleaning system based on heterogeneous Photo-Fenton according to claim 2, it is characterized in that: when many ultraviolet lamp tubes are set, many ultraviolet lamp tubes are the concentric circles setting, distance is identical between the neighboring concentric circle, many ultraviolet lamp tubes are distributed on the circumference of different-diameter, along same diameter line setting, the central angle between each adjacent two diameter line is identical, and circle centre position is provided with ultraviolet lamp tube; Nozzle is arranged on the concentric circumferences with ultraviolet lamp tube concentric circles alternate intervals uniform, and places on the diameter line of two ultraviolet lamp tube central angle half-angles.
4. according to claim 1 or 2 or 3 described integrated fume cleaning systems, it is characterized in that solid catalyst is Fe based on heterogeneous Photo-Fenton
2O
3﹑ MnO
2﹑ CuO or TiO
2In a kind of, solid catalyst in regenerator by high-temperature calcination means activating and regenerating, its calcining heat is in 300 ℃ of-600 ℃ of scopes, the mass concentration that solid catalyst adds is in the 0.5g/L-5.0g/L scope, the particle diameter of solid catalyst is between 80 orders-200 order, and the molar concentration that hydrogen peroxide adds is at 0.1mol/L-2.5mol/L.
5. according to claim 1 or 2 or 3 described integrated fume cleaning systems, it is characterized in that based on heterogeneous Photo-Fenton, 15 ℃-75 ℃ of the flue-gas temperatures of bubble tower inlet, liquid-gas ratio is 5L/m
3-50 L/m
3, and flow through time of staying of bubbling column reactor of flue gas be 0.5s-20s.
6. according to claim 1 or 2 or 3 described integrated fume cleaning systems, it is characterized in that: the sulfidion S that adds in the secondary knockout tower based on heterogeneous Photo-Fenton
2-Mole and Hg solution
2+Mole equate i.e. n (S
2-): n (Hg
2+)=1:1.
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| CN103007753A (en) * | 2012-12-31 | 2013-04-03 | 上海电气石川岛电站环保工程有限公司 | Heterogeneous Fenton reagent and preparation method and application thereof |
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| CN103706238A (en) * | 2013-12-20 | 2014-04-09 | 华中科技大学 | System and method for removing SO2, NO and Hg in smoke on the basis of heterogeneous Fenton |
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| CN104043325A (en) * | 2014-05-30 | 2014-09-17 | 江苏大学 | Method for purifying flue gas through activating persulfate by ozone, and apparatus thereof |
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| CN106861392A (en) * | 2017-02-21 | 2017-06-20 | 华北电力大学 | A kind of nitrogen oxide removal process based on catalytic oxidation of hydrogen peroxide |
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| CN109499363A (en) * | 2019-01-14 | 2019-03-22 | 重庆工商大学 | A kind of combined padding and drying system waste gas purification technique |
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