CN102166471B - Heterogeneous-Photo-Fenton-based integrated smoke gas purification system - Google Patents
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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 the 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 for the Single Pollution thing for removing target, remove when generally can't realize flue gas multiple pollutant.For example, use at present more flue gas desulfurization and denitrification technology and be mainly wet method limestone-gypsum method flue gas desulfurization technology (Ca-WFGD) and ammine selectivity catalytic reduction method (NH
3-SCR), although these two kinds of techniques can be distinguished independent desulphurization denitration, all can't in a reactor, realize removing simultaneously.Although the stack of uniting of two kinds of techniques is used and can be realized simultaneously desulphurization denitration, also causes whole system complicated simultaneously, floor space is large, 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 for the laws and regulations of mercury in flue gas emission control, use but also there is at present a kind of cost-effective flue gas demercuration technology to obtain large-scale commercial applications.If at existing Ca-WFGD and NH
3-SCR system for desulfuration and denitration afterbody increases independent flue gas mercury removal system again, then certainly will will cause the initial outlay of whole system and operating cost further sharply to increase, and finally is difficult to obtain large-scale commercial applications in developing country and uses.
In sum, if can in a reactor, oxysulfide, nitrogen oxide and mercury be realized removing simultaneously, then can greatly reduce complexity and the floor space of system, and then reduce 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 the characteristics such as multi-pollutant removes simultaneously, it is a kind of flue gases purification that the development and application prospect is extremely arranged, but the progress of traditional wet type flue gas desulphurization technology is always relatively slow, 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 then chemical reaction could occur be fixed in the absorption liquid, and NO and Hg
0The characteristic of indissoluble is so that its absorption resistance to mass tranfer in liquid phase increases greatly, and only the method by regulation and control absorption liquid pH and temperature is difficult to significantly improve NO and Hg
0In the solubility of liquid phase, this characteristic has caused traditional wet desulphurization denitration demercuration technology ubiquity desulfuration efficiency high, 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
0Rapid conversion is that the effective ways of easy molten form are one of keys that addresses this problem.
Summary of the invention
The invention discloses a kind of integrated fume cleaning system based on heterogeneous Photo-Fenton, namely utilize heterogeneous Photo-Fenton (ultraviolet light, hydrogen peroxide, solid catalyst advanced oxidation processes) to produce the hydroxyl radical free radical (OH) with strong oxidizing property, with the SO in the flue gas
2, NO
xAnd Hg
0Be oxidized to respectively H
2SO
4, HNO
3And Hg
2+Be fixed in the solution, the solid catalyst after the reaction in the solution can be by realizing recycling after the simple precipitate and separate, the Hg in the solution
2+Can be by adding the sulfidion S of equimolar ratio
2-Generate the HgS of indissoluble, then recycle through realizing after the precipitate and separate, 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 a kind of flue gases purification that application prospect is extremely arranged.
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 consist of, burner combustion produces comprises SO
2, NO
xAnd Hg
0Flue gas through after the heat exchanger cooling, the nozzle that arranges from the bubble tower bottom passes into bubble tower, the heterogeneous Fenton reagent that contains hydrogen peroxide and solid catalyst adds to add behind the liquid tower by the first circulating pump and also passes into 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, again passed into 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 the second-order separation tower, by add the sulfidion S of equimolar ratio to the second-order separation tower
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
3Referred to 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 circumference 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 entrance, liquid-gas ratio is 5L/m
3-50L/m
3, and smoke gas flow is 0.5s-20s through the time of staying of bubbling column reactor.
The sulfidion S that adds in the second-order separation 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 flue gas of burner discharging
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, then cycling and reutilization 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, then recycle through after the precipitate and separate:
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 easily various pollutants 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 photochemical advanced oxygenation the time: 201012096592.5) with (a kind of flue gas mercury removal system based on photochemical advanced oxidation: 201012096592.8) compare, the present invention has following obvious advantage:
(1) along with people's improving constantly environmental requirement, laws and regulations for the mercury in flue gas emission control 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 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 further improve by adding callable high-performance solid catalyst the removal efficiency of pollutant, and dosage that can also the decrease hydrogen peroxide under the same terms, and then use cost that can the decrease hydrogen peroxide.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 a kind of Novel fume cleaning technology that application prospect is extremely arranged.
Description of drawings
Fig. 1 is 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, then pass into the liquid phase reactor district from the nozzle 3 of bubbling bed 4 bottoms and participate in the Gas-Liquid Absorption reaction; Heterogeneous Fenton reagent at first adds and adds liquid tower 12, then adds bubbling bed 4 interior liquid phase reactor districts to from the top of bubble tower 4 by the first circulating pump 7 and participates in the Gas-Liquid Absorption reaction; Cover has the uviol lamp 6 of quartz socket tube 5 to excite decomposition heterogeneous Fenton reagent to discharge the hydroxyl radical free radical OH with strong oxidizing property, and rapidly with the SO in the flue gas
2, NO
xAnd Hg
0Be oxidized to respectively H
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, it is recycling that the partially mixed solution that reaction generates needs to add liquid tower 12 by 8 suction of the second circulating pump, remaining mixed solution is then by the 3rd circulating pump 9 suction one-level knockout towers 10, solid catalyst is sent into regenerator 14 by the 4th circulating pump 11 and is realized regeneration activatings after the simple precipitate and separate of one-level knockout tower 10 interior processes, the solid catalyst after the regeneration is again passed into 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 is then by the 6th circulating pump 15 suction the second-order separation towers 16, then by adding the sulfidion S of equimolar ratio
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 passes into 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 passed into bubble tower, high-temperature flue gas need to carry out effective cooling by heat exchanger, therefore the bubble tower entrance flue gas temperature generally should be controlled between 15-75 ℃.
Owing to containing 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 to 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 to be than the external diameter of uviol lamp large 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 large, then the flow resistance of flue gas will increase in the reactor, cause 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 decomposed to produce the hydroxyl radical free radical OH oxidation removal pollutant of sufficient amount if ultraviolet light irradiation intensity is too little, if but ultraviolet light irradiation intensity is too large, and then the energy consumption of system will significantly increase.Therefore, ultraviolet ray intensity need to remain on 5W/m
3-200W/m
3, the W/m of unit wherein
3Referred to 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 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 large, then the specific area of catalyst can descend, if bring very large 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 strict control criterion need to be arranged, 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 second-order separation tower abundant not, Hg
2+Capture rate low.Therefore, in the practical application, add S
2-Mole should with Hg solution
2+Mole keep to equate, namely need to keep n (S
2-): n (Hg
2+)=1: 1.
Because separating when reclaiming, the liquid phase mix products need to 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 to arrange solution part recirculating system, and it is recycling that the mixed solution that namely produces after the reaction generally need to have 20-40% to be added the liquid tower by suction again, in order to 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 respectively 92.1%, 80.9% and 98.8%.
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 respectively 100%, 92.2% and 100%.
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 respectively 89.2%, 83.2% and 100%.
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 respectively 85.8%, 70.8% and 93.7%.
In sum, embodiment 2 has best integration desulfurization denitration demercuration effect, can be used as most preferred embodiment and consults and uses.
Claims (1)
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 consist of, burner combustion produces comprises SO
2, NO
xAnd Hg
0Flue gas through after the heat exchanger cooling, the nozzle that arranges from the bubble tower bottom passes into bubble tower, the heterogeneous Fenton reagent that contains hydrogen peroxide and solid catalyst adds to add behind the liquid tower by the first circulating pump and also passes into 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, again passed into 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 the second-order separation tower, by add the sulfidion S of equimolar ratio to the second-order separation tower
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;
Said 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
3Referred to 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 circumference with ultraviolet lamp tube concentric circles alternate intervals uniform, and places on the diameter line of two ultraviolet lamp tube central angle half-angles;
Said 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 said bubble tower entrance, liquid-gas ratio is 5L/m
3-50L/m
3, and smoke gas flow is 0.5s-20s through the time of staying of bubbling column reactor,
The sulfidion S that adds in the said the second-order separation tower
2-Mole and Hg solution
2+Mole equate i.e. n (S
2-): n (Hg
2+)=1:1.
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|---|---|---|---|
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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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