CN204637945U - A kind of ozone is in conjunction with the desulfurization denitration demercuration system of light radiation peroxide - Google Patents

Abstract

The utility model relates to the desulfurization denitration demercuration system of a kind of ozone in conjunction with light radiation peroxide, described system be mainly provided with emission source, blower fan, deduster, gas cooler, ozone generator, up and down to atomization bed, circulating pump one and two, packing layer, ultraviolet lamp tube, atomizer, demister, liquid reserve tank and product postprocessing system.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.

Description

A kind of ozone is in conjunction with the desulfurization denitration demercuration system of light radiation peroxide

Technical field

The utility model relates to Air Pollution Control field, is specifically related to the desulfurization denitration demercuration system of a kind of ozone in conjunction with light radiation peroxide.

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 utility model relates to the desulfurization denitration demercuration system of a kind of ozone in conjunction with light radiation peroxide.Described system be mainly provided with emission source, blower fan, deduster, gas cooler, ozone generator, up and down to atomization bed, circulating pump one and two, packing layer, ultraviolet lamp tube, atomizer, demister, liquid reserve tank and product postprocessing system.

The course of reaction principle of the utility model system:

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 ozone be release the potentiometric titrations and hydroxyl radical free radical with strong oxidizing property in conjunction with light radiation peroxide, and detailed process can represent with following chemical reaction (1)-(6):

H ₂O ₂+UV 2×OH (1)

$\begin{array}{cc}{S}_2{O}_8^{2-}+\mathrm{UV}& 2S{O}_4^{-}\×\end{array}---\left(2\right)$

O ₃+UV ×O+O ₂(3)

$\begin{array}{cc}{H}_2{O}_2& {\mathrm{HO}}_2^{-}+H^{+}---\left(4\right)\end{array}$

$\begin{array}{cc}{O}_3+{\mathrm{HO}}_2^{-}& \×\mathrm{OH}+O_2^{-}+O_2---\left(5\right)\end{array}$

×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 ₂cH ₂SO ₄+other products

(7)

a×OH+bSO ₂cSO ₃++other products

(8)

a×OH+bNO cNO ₂++other products

(9)

a×OH+bNO cHNO ₃+other products

(10)

a×OH+bHg ⁰cHgO+other products

(11)

$\begin{array}{cc}a{\mathrm{SO}}_4^{-}\×+b{\mathrm{SO}}_2& {\mathrm{cH}}_2{\mathrm{SO}}_4+\mathrm{other\; products}\end{array}---\left(12\right)$

$\begin{array}{cc}a{\mathrm{SO}}_4^{-}\×+b{\mathrm{SO}}_2& c{\mathrm{SO}}_4+\mathrm{other\; products}\end{array}---\left(13\right)$

$\begin{array}{cc}a{\mathrm{SO}}_4^{-}\×+\mathrm{bNO}& c{\mathrm{NO}}_4+\mathrm{other\; products}\end{array}---\left(14\right)$

$\begin{array}{cc}a{\mathrm{SO}}_4^{-}\×+\mathrm{bNO}& \mathrm{cH}{\mathrm{NO}}_4+\mathrm{other\; products}\end{array}---\left(15\right)$

$\begin{array}{cc}a{\mathrm{SO}}_4^{-}\×+b{\mathrm{Hg}}^0& \mathrm{cHgO}+\mathrm{other\; products}\end{array}$

$\left(16\right)$

3, the Liu Suan ﹑ nitric acid of reaction generation and the mixed solution of mercury can be used as raw material of industry recycling (such as, by add sulfidion and bivalent mercury react produce mercuric sulphide precipitate and separate after recycle, remaining sulfuric acid and salpeter solution add again in ammonia with rear generation ammonium sulfate and the recycling of ammonium nitrate agricultural fertilizer.) 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.

For realizing above object, according to above-mentioned principle, the technical solution adopted in the utility model is as follows:

A kind of ozone is in conjunction with the desulfurization denitration demercuration system of light radiation peroxide.Described system be provided with emission source, blower fan, deduster, gas cooler, ozone generator, 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, ozone generator is connected to gas cooler with in the connecting pipe up and down to atomization bed by pipeline, 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 be provided with more than one group ultraviolet lamp tube row, often organize ultraviolet lamp tube row 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.

Up and down to the cross section of atomization bed 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 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.Ultraviolet lamp tube one end (right-hand member) is fixed on up and down in atomization bed wall after inserting, and should seal, and prevents from flue gas from flowing through from the gap between uviol lamp top and reactor wall causing pipe to arrange other local smoke distribution uneven.The other end (left end) through up and down should at more than 1cm to length in reserve C after atomization bed wall so that the ultraviolet lamp tube later stage is changed and maintenance.Often organizing the upper best ultraviolet lamp tube number arranged of ultraviolet lamp tube row's vertical direction (above-below direction) is 5-10 root, and the best ultraviolet lamp tube number arranged of horizontal direction can by determining the cross-sectional area of atomization bed and ultraviolet lamp tube distance computation up and down.

Course of reaction is as follows: the flue gas from emission source is drawn by blower fan, after deduster dedusting and gas cooler cooling, then enters up and down to atomization bed by after packing layer cloth wind.The ozone that ozone generator produces is imported in flue gas by entrance e, and first to the SO in flue gas in flue ₂﹑ NO _xand Hg ⁰carry out pre-oxidation.Peroxide solutions from liquid reserve tank is aspirated by circulating pump one, and sprays into after being atomized by atomizer up and down to atomization bed.Uviol lamp ultraviolet light radiation excites peroxide to produce sulfate radical and hydroxyl radical free radical is oxidized SO further ₂﹑ NO _x﹑ Hg ⁰and by SO that ozone oxidation produces ₃and NO ₂.From up and down to atomization bed top fall after rise solution by exporting b, again suck liquid reserve tank circulated sprinkling through circulating pump two.Product realizes resourcebility utilization by passing into product postprocessing system to the product exit d of atomization bed up and down.Such as, by add sulfidion and bivalent mercury react produce mercuric sulphide precipitate and separate after recycle, remaining sulfuric acid and salpeter solution add again in ammonia with rear generation ammonium sulfate and the recycling of ammonium nitrate agricultural fertilizer

Flue is provided with the SO in ozonizer generates ozone pre-oxidation flue gas ₂﹑ NO and Hg ⁰.In order to avoid ozone at high temperature selfdecomposition, after ozone generator is positioned at gas cooler and up and down to before atomization bed entrance, best ozone entrance concentration is 20ppm-1000ppm.Be 20-70 DEG C to the best smoke inlet temperature of atomization bed up and down, effective liquid-gas ratio is 0.1-5.0L/m ³, the optium concentration of peroxide is between 0.1mol/L-3.5mol/L, and the pH of solution is between 1.0-9.5, and best solution temperature is 20-70 DEG C.Ultraviolet light Net long wave radiation intensity is 10 μ W/cm ²-400 μ W/cm ², ultraviolet EWL is 150nm-365nm.SO in flue gas ₂﹑ NO and Hg ⁰content respectively not higher than 10000ppm ﹑ 2000ppm and 800 μ g/m ³.

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.

Advantage of the present utility model and remarkable result:

(1) Chinese patent 201310683135.8 proposes a kind of photoactivation persulfate simultaneous SO_2 and NO removal demercuration system based on spray, but because the removal efficiency of independent photoactivation persulfate system is lower, strict environmental requirement cannot be met, and system described in the utility model adopts the pre-oxidation of flue injection of ozone, and then the two-stage oxidizing method of pollutant is removed in conjunction with photoactivation peroxide deep oxidation, there is higher removal efficiency.Such as, native system can realize SO ₂﹑ NO _xnamely 100% removal efficiency of ﹑ Hg tri-kinds of pollutants proves that this system has outstanding multi-pollutant and removes performance simultaneously.

(2) 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 this system can only simultaneous SO_2 and NO removal, demercuration cannot be realized, and the utility model can realizing SO in atomization bed up and down ₂﹑ NO _xremove while ﹑ Hg tri-kinds of pollutants, thus can reduce initial cost and the operating cost of system.Along with the mankind's improving constantly environmental requirement, this advantage of the present utility model will be highlighted gradually.In addition, what the 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 utility model proposes has better mass transfer rate and absorption efficiency, thus removal efficiency while can pollutant being increased substantially.Such as, native system can realize SO ₂﹑ NO _xnamely 100% removal efficiency of ﹑ Hg tri-kinds of pollutants demonstrates this system has outstanding multi-pollutant and removes performance simultaneously.

Accompanying drawing explanation

Fig. 1 is electron spin resonance (ESR) the light general figure of a kind of ozone in conjunction with light radiation peroxide.

Fig. 2 is the process chart of system described in the utility model.

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 utility model.

Detailed description of the invention

Below in conjunction with accompanying drawing, detailed description of the invention of the present utility model is further described.

As described in Figure 2, a kind of ozone in conjunction with light radiation peroxide desulfurization denitration demercuration method based on device be mainly provided with emission source 1, blower fan 2, deduster 3, gas cooler 4, ozone generator 5, 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 tank 9 and product postprocessing system 18.

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, and emission source 1 is provided with blower fan 2 with the flue of 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, ozone generator 5 is connected to gas cooler 4 with in the connecting pipe up and down to atomization bed 6 by pipeline, described liquid reserve tank 9 enters up and down 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 ultraviolet lamp tube 12 between atomizer 11 laterally zygomorphic in atomization bed 6.

Described liquid reserve tank 9 enter up and down to the pipeline of atomization bed 6 be provided with by peroxide solutions introduce up and down to the circulating pump 1 of atomization bed 6; Describedly up and down the taphole b of atomization bed 6 is provided with to the circulating pump 28 peroxide solutions being introduced liquid reserve tank 9.

As shown in Figure 3 and Figure 4, up and down to the cross section of atomization bed 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 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 between 10cm-50cm, to reach best light radiation effect.In ultraviolet lamp tube row, the spacing B of adjacent two ultraviolet lamp tubes is between 3cm-30cm, to reach best shock and atomization coverage effect.Ultraviolet lamp tube one end is fixed on up and down in atomization bed wall after inserting, and should seal, and prevents from flue gas from flowing through from the gap between uviol lamp top and reactor wall causing pipe to arrange other local smoke distribution uneven.The other end through up and down should at more than 1cm to length in reserve C after atomization bed wall so that the ultraviolet lamp tube later stage is changed and maintenance.Often organizing the upper best ultraviolet lamp tube number arranged of ultraviolet lamp tube row's vertical direction (above-below direction) is 5-10 root, and the best ultraviolet lamp tube number arranged of horizontal direction can by determining the cross-sectional area of atomization bed and ultraviolet lamp tube distance computation up and down.

As shown in Figure 5, product postprocessing system 18 with up and down the product exit d of the bottom of atomization bed is connected, reacted product introduces mercury knockout tower by solution circulation pump 19, then to introduce in neutralizing tower 15 ammonification and after, enter evaporating and crystallizing tower 16, the heat that evaporating and crystallizing tower 16 provides is provided by smoke waste heat utilization system 17, and product is solid-state ammonium sulfate and ammonium nitrate.

Course of reaction is: 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.The ozone that ozone generator 5 produces is imported in flue gas by entrance e, and first to the SO in flue gas in flue ₂﹑ NO _xand Hg ⁰carry out pre-oxidation.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.Ultraviolet lamp tube 12 ultraviolet light radiation excites peroxide to produce sulfate radical and hydroxyl radical free radical is oxidized SO further ₂﹑ NO _x﹑ Hg ⁰and by SO that ozone oxidation produces ₃and NO ₂.From up and down to atomization bed 6 top fall after rise solution by exporting b, again suck liquid reserve tank 9 circulated sprinkling through circulating pump 28.Product realizes resourcebility utilization by passing into product postprocessing system 18 to the product exit d of atomization bed 6 up and down.Such as, by add sulfidion and bivalent mercury react produce mercuric sulphide precipitate and separate after recycle, remaining sulfuric acid and salpeter solution add again in ammonia with rear generation ammonium sulfate and the recycling of ammonium nitrate agricultural fertilizer.

SO in embodiment 1. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 800ppm and 60 μ g/m ³, be 60 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 0.5L/m ³, hydrogen peroxide concentration is 0.5mol/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 25 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 50.6% and 63.2% respectively.

SO in embodiment 2. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 800ppm and 60 μ g/m ³, be 60 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 0.5L/m ³, ammonium persulfate concentrations is 0.5mol/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 25 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 45.7% and 58.1% respectively.

SO in embodiment 3. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 400ppm and 50 μ g/m ³, be 60 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 0.5L/m ³, hydrogen peroxide concentration is 0.5mol/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 25 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 71.5% and 83.3% respectively.

SO in embodiment 4. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 400ppm and 50 μ g/m ³, be 60 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 0.5L/m ³, ammonium persulfate concentrations is 0.5mol/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 25 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 67.9% and 77.7% respectively.

SO in embodiment 5. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 400ppm and 50 μ g/m ³, be 60 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 0.5L/m ³, hydrogen peroxide concentration is 0.5mol/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 55 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 78.8% and 89.8% respectively.

SO in embodiment 6. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 400ppm and 50 μ g/m ³, be 60 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 0.5L/m ³, ammonium persulfate concentrations is 0.5mol/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 55 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 73.1% and 84.9% respectively.

SO in embodiment 7. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 400ppm and 50 μ g/m ³, be 60 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 0.5mol/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 55 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 89.2% and 93.0% respectively.

SO in embodiment 8. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 400ppm and 50 μ g/m ³, be 60 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 0.5mol/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 55 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 86.3% and 90.0% respectively.

SO in embodiment 9. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 400ppm and 50 μ g/m ³, be 60 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.5L/m ³, hydrogen peroxide concentration is 0.5mol/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 80 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 95.9% and 100.0% respectively.

SO in embodiment 10. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 400ppm and 50 μ g/m ³, be 60 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 1.5L/m ³, hydrogen peroxide concentration is 0.5mol/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 80 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 93.8% and 100.0% respectively.

SO in embodiment 11. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 400ppm and 50 μ g/m ³, be 60 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 2.0L/m ³, hydrogen peroxide concentration is 0.5mol/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 150 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 100.0% and 100.0% respectively.

SO in embodiment 12. flue gas ₂﹑ NO _xwith Hg ⁰concentration is respectively 6000ppm, 400ppm and 50 μ g/m ³, be 60 DEG C to the smoke inlet temperature of atomization bed up and down, liquid-gas ratio is 2.0L/m ³, hydrogen peroxide concentration is 0.5mol/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 150 μ W/cm ², ultraviolet EWL is 254nm.Pilot run is: SO in flue gas ₂﹑ NO _xwith Hg ⁰while removal efficiency can reach 100%, 100.0% and 100.0% respectively.

Comprehensive Correlation through above embodiment is known, and embodiment 11 and 12 has best simultaneous SO_2 and NO removal demercuration effect, can be used as most preferred embodiment and consults and uses.

Claims (4)

1. ozone is in conjunction with a desulfurization denitration demercuration system for light radiation peroxide, it is characterized in that: described system be provided with emission source, blower fan, deduster, gas cooler, ozone generator, 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, ozone generator is connected to gas cooler with in the connecting pipe up and down to atomization bed by pipeline, 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.

2. a kind of ozone, in conjunction with the desulfurization denitration demercuration system of light radiation peroxide, is characterized in that according to claim 1: 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.

3. according to claim 1 a kind of ozone in conjunction with the desulfurization denitration demercuration system of light radiation peroxide, it is characterized in that: be square or rectangle to the cross section of atomization bed up and down, inside is provided with the ultraviolet lamp tube row of more than a group, often organizes ultraviolet lamp tube row and is 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.

4. a kind of ozone, in conjunction with the desulfurization denitration demercuration system of light radiation peroxide, is characterized in that according to claim 1: the 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.