CN104923049A - Simultaneous desulfurization, denitrification and demercuration optical radiation method for ozone and hydrogen peroxide - Google Patents

Simultaneous desulfurization, denitrification and demercuration optical radiation method for ozone and hydrogen peroxide Download PDF

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CN104923049A
CN104923049A CN201510191175.XA CN201510191175A CN104923049A CN 104923049 A CN104923049 A CN 104923049A CN 201510191175 A CN201510191175 A CN 201510191175A CN 104923049 A CN104923049 A CN 104923049A
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hydrogen peroxide
ozone
flue gas
solution
bed
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CN201510191175.XA
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CN104923049B (en
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刘杨先
王燕
邵霞
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江苏大学
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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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Abstract

The invention relates to a simultaneous desulfurization, denitrification and demercuration optical radiation method for ozone and hydrogen peroxide. The method adopts ultraviolet light in combination with ozone and hydrogen peroxide generating hydroxyl radicals with high oxidizing property to oxidatively remove SO2, NOx and HgO in an impact bed. One part of flue gas from a boiler is injected into the impact bed by one impactor after being mixed with one part of ozone and hydrogen peroxide, the other part of glue gas is injected into the impact bed by the other impactor coaxially arranged in the opposite direction after being mixed with the other part of ozone and hydrogen peroxide, and the two airflows are impacted and mixed in the impact bed. The hydroxyl radicals with high oxidizing property are generated through ultraviolet light radiation decomposition of ozone and hydrogen peroxide oxidizing SO2, NOx and HgO to generate divalent mercury, sulfuric acid and nitric acid for resource utilization. The system can realize integrated removal of sulfur, nitrogen and mercury, is free of secondary pollution, and has wide market application prospect.

Description

A kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method
Technical field
The present invention relates to the Pollutant Control Technology field of air environmental protection, be specifically related to a kind of method of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration.
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 realize removing in a reactor 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 by SO in a reactor 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 light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration system, described system is the hydroxyl radical free radical oxidation removal SO in shock bed adopting ultraviolet light associating ozone/hydrogen peroxide solution to produce strong oxidizing property 2﹑ NO xand Hg 0.
Method provided by the present invention based on principle and course of reaction:
1, as shown in Figure 1, adopt electron spin resonance (ESR) kaleidophon to be measured in reaction system and create hydroxyl radical free radical.Therefore, first this system is release the 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(2)
·O+H 2O 2→·OH+HO 2·(5)
The hydroxyl radical free radical of the strong oxidizing property 2, produced can by the SO in flue gas 2﹑ NO xand Hg 0oxidation generates Er Jia Gong ﹑ sulfuric acid and nitric acid mixed solution.Detailed process can represent with following reaction (6)-(8):
a·OH+bSO 2→cH 2SO 4+other products (6)
a·OH+bNO→cHNO 3+other products (7)
a·OH+bHg 0→cHgO+other products (8)
3, the Er Jia Gong ﹑ sulfuric acid produced and nitric acid separated recovery in the product postprocessing system of afterbody is oxidized.Such as, bivalent mercury first can produce mercuric sulphide sediment separation and recovery by adding sulfidion reaction, and remaining sulfuric acid and nitric acid mixed solution generate ammonium sulfate and ammonium nitrate agricultural fertilizer by adding ammonium.This system can realize the integration of Liu ﹑ Dan ﹑ mercury and remove, and product resourcebility utilizes, and has wide market application foreground.
For realizing above object, the embodiment that the present invention adopts is as follows:
A kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method, the flue gas of discharge enters cooler after deduster dedusting.Ultraviolet light associating ozone/hydrogen peroxide solution produces hydroxyl radical free radical oxidation removal SO in shock bed of strong oxidizing property 2﹑ NO xand Hg 0, Er Jia Gong ﹑ sulfuric acid and nitric acid.
Cause ozone and hydrogen peroxide that the expensive oxidant of the waste of selfdecomposition in advance occurs owing to clashing into the too high meeting of smoke inlet temperature of bed, if but the too low chemical reaction rate that will cause again of temperature reduce, and then affect removal efficiency.The research of inventor finds, flue gas is 30-75 DEG C to the best inlet temperature of shock bed.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 best liquid-gas ratio is 0.2-3.5L/m 3.
Gas-liquid mixture is formed after the flue gas of cooling mixes with ozone, hydrogen peroxide.The too low free-radical oxidation that cannot discharge abundance of ozone, hydrogen peroxide concentration removes pollutant, but once throw in the ozone of too high concentration, hydrogen peroxide can cause extra selfdecomposition and side reaction, selfdecomposition can cause ozone, hydrogen 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 best entrance concentration of ozone is 20ppm-500ppm, and it is between 0.2mol/L-2.5mol/L that the best of hydrogen peroxide drops into concentration.
The ram that gas-liquid mixture is arranged by coaxial subtend respectively sprays into shock bed, and two strands of air-flows, in shock bed, impingement mix occur.The research of inventor finds, when the shock equalization point of the gas-liquid mixture of described two bursts of atomizations is positioned on the vertical center line of shock bed, in reactor, gas-liquid mixture can reach best impact strength (now mass transfer rate is the highest) and best mixed effect, and the removal efficiency of pollutant is the highest.On the contrary, when described two strands of gas-liquid mixtures clash into generation deflection (time not on vertical center line), in reactor, gas-liquid mixture cannot realize uniform mixing, and mass transfer rate reduces greatly, pollutant removing efficiency obviously declines, and cannot meet environmental protection index.Therefore, the shock equalization point of described gas-liquid mixture should be positioned on the center line of shock bed.
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, effective ultraviolet radiation intensity of clashing in bed is 20 μ W/cm 2-500 μ W/cm 2.If 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 selection is oversize, the energy of ultraviolet photon will obviously reduce, and 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 160nm-365nm.
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, the Optimal pH of solution is between 1.0-7.5.The too high meeting of solution temperature causes peroxide that selfdecomposition in advance occurs, if but temperature is too low, and can reduce chemical reaction rate, thus reduce pollutant removing efficiency.20-65 DEG C is that inventor is according to orthogonal experiment and the comprehensive best solution temperature analyzing rear acquisition, solution temperature more than 65 DEG C after the decomposition rate of ozone and hydrogen peroxide increase considerably, but reduce lower than chemical reaction rate after 20 DEG C, cause the removal efficiency of pollutant significantly to decline.Therefore, best solution temperature is 20-65 DEG C.
Inventor is through the experiment of system and find after detecting analysis, SO in flue gas 2﹑ NO x﹑ Hg 0the too high removal efficiency that will cause of content significantly decline, the unabsorbed middle SO of afterbody 2﹑ NO x﹑ Hg 0escape amount increases considerably, and easily causes serious secondary pollution, therefore finds after research, SO in flue gas 2﹑ NO x﹑ Hg 0content respectively not higher than 8000ppm ﹑ 2000ppm ﹑ 300 μ g/m 3.
Described ram is made up of solution conduit and gas accelerating tube, and described solution conduit one end is with hydrogen peroxide solution entrance, and the other end is provided with atomizer; Flue gas from boiler enters the flue gas accelerating tube of ram after deduster dedusting and cooler cooling; Ozone gas from ozone generator also enters the flue gas accelerating tube of ram; Streams of ozone and flue gas are pre-mixed in the flue gas accelerating tube of ram; Atomized drop is produced after the atomizer atomization of hydrogen peroxide through solution conduit top; The atomized drop carrying hydrogen peroxide after ozone mixes with flue gas after flue gas accelerating tube accelerates enters high speed nozzle.
Preferred technical parameter, the SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m 3, hydrogen peroxide concentration is 0.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.
Preferred technical parameter, the SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m 3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.
Preferred technical parameter, the SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.5L/m 3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.
Preferred technical parameter, the SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 2.5L/m 3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.
Preferred technical parameter, the SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 50 DEG C, and liquid-gas ratio is 2.5L/m 3, hydrogen peroxide concentration is 2.5mol/L, and pH value of solution is 3.1, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.
Described solution is not more than 15 microns from the atomization droplets diameter that nozzle sprays; The flue gas flow rate that flue gas flows out from conduit outlet is between 5m/s-30m/s.Described removal methods based on system be provided with pot stove ﹑ and clash into device ﹑ smelly oxygen and send out device ﹑ raw clash into bed ﹑ uviol lamp except warm device ﹑ falls in dirt device ﹑ and quartzy sleeve pipe ﹑ stores up liquid tank ﹑ chimney and product postprocessing system etc. except mist device ﹑ follows ring pump ﹑.
Clash into the ram in bed and ultraviolet lamp tube employing multi-stage cross layout.Ram layout alternate with ultraviolet lamp tube, and adjacent ram and ultraviolet lamp tube adopt cocurrent and parallel to arrange.Vertical interval A between ultraviolet lamp tube adjacent two layers between 5cm-60cm, to reach best light radiation effect.Distance B between two ram tops (distances between two atomizers) positioned opposite between 20cm-350cm, to reach best atomizing effect.Ram is arranged in the central spot between adjacent two layers ultraviolet lamp tube.Adjacent two-stage ram adopts 90 degree of arranged crosswise staggered, and the ultraviolet lamp tube of adjacent two-stage adopts 90 degree of arranged crosswise staggered equally, to reach best impingement mix effect.
Ram is made up of solution conduit and gas accelerating tube.Solution conduit one end is with hydrogen peroxide solution entrance, and the other end is provided with atomizer.Gas accelerating tube is with ozone entrance and smoke inlet, and ozone entrance and smoke inlet adopt coaxially positioned opposite.The optimum length C of solution conduit is between 60cm-150cm, and the optimum length D of flue gas accelerating tube is between 50cm-130cm.The diameter of solution conduit is relevant with liquid inventory, but will ensure that solution is not more than 15 microns from the atomization droplets diameter that nozzle sprays.The diameter of flue gas accelerating tube is relevant with flue gas flow, but will ensure that flue gas flow rate that flue gas flows out from conduit outlet is between 5m/s-30m/s.
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 (with prior art or Patent Reference):
(1) according to internationally famous chemical industry expert Danckwerts [1]find with the research of Zhang Chengfang professor [2], for fast chemical reaction system, the rate-determining steps of whole pollutant removing mainly concentrates on mass transfer link, if the mass transfer rate of the necessary preferential consolidation system of the removal efficiency namely wanting to increase substantially pollutant.Because the mass transfer rate of traditional bubble tower and spray column is lower, the high-speed chemical reaction system that free radical causes cannot be met.In addition, the research that the famous scholar Wu Yuan of China teaches shows [2], under the same terms, the mass transfer rate clashing into bed, than more than bubbling bed and spray height of bed order of magnitude, has high mass transfer rate, is very suitable for the fast chemical reaction system that free radical causes.Native system achieve 100% pollutant removing efficiency and provable shock bed be a kind of superior gas-liquid reactor, be suitable for the Quickly react system of free yl induction.Therefore, inventor proposes shock bed to combine for removing the hydrogen sulfide in flue gas with free radical Quickly react system first, has obvious novelty and practical value, also has good development potentiality and market prospects.
(bibliography [1] Danckwerts, P.V.Gas-Liquid Reactions.New York:McGraw-Hill, 1970. [2] Zhang Chengfang. gas liquid reaction and reactor [M]. Beijing: Chemical Industry Press, 1985. [3] Wu Yuan. percussion flow-principle character application [M]. Beijing: Chemical Industry Press, 2005.)
(2) patent No. be 201310683135.8 Chinese patent propose a kind of photoactivation persulfate simultaneous SO_2 and NO removal demercuration system based on spray column, but because the mass transfer rate of spray column is low, the fast reaction that free radical causes cannot be met, cause pollutant removing efficiency not high, and the photochemistry shock bed accessory that the present invention proposes has extremely strong mass transfer rate, can mass transfer rate be significantly improved, thus increase substantially the removal efficiency of pollutant.System of the present invention can realize SO 2﹑ NO x100% removal efficiency of ﹑ Hg tri-kinds of pollutants namely demonstrate this system outstanding remove performance.
(3) patent No. be 201010296492.5 Chinese patent propose a kind of light radiation hydrogen peroxide that utilizes and produce the simultaneous SO_2 and NO removal system of free radical, but this system can only simultaneous SO_2 and NO removal, demercuration cannot be realized, and the present invention can realize SO in a reactor 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 invention will be highlighted gradually.In addition, what the removal methods described in this patent and technique adopted is the bubbling column reactor that mass transfer rate is very low and market application potential is little, and the photochemistry shock bed accessory that the present invention proposes has extremely strong mass transfer rate, can mass transfer rate be significantly improved, thus increase substantially the removal efficiency of pollutant.
Accompanying drawing explanation
The general figure of hydroxyl radical free radical ESR light caught in a kind of light radiation of Fig. 1 ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration system.
Fig. 2 is technological process and the structure chart of present system.
Fig. 3 is product postprocessing device and the flow chart of present system.
Fig. 4 is the structural representation that an inner impact device and ultraviolet lamp tube two adjacent groups layout are clashed in the present invention.
Fig. 5 is the structural representation of ram.
Fig. 6 is the critical size mark schematic diagram of ram.
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, light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method based on a system, be provided with boiler 1 ﹑ deduster 2 ﹑ cooler 3 ﹑ ram 11 ﹑ ozone generator 4 ﹑ and clash into bed 5 ﹑ uviol lamp 13 and quartz socket tube 14 ﹑ demister 9 ﹑ circulating pump 1 ﹑ circulating pump 28, fluid reservoir 6 ﹑ chimney 10 and product postprocessing system 15.
Hydrogen peroxide enters fluid reservoir 6 from the entrance c of fluid reservoir 6, then aspirates by circulating pump 1 or circulating pump 28 the solution conduit 11-1 sending into ram 11; Flue gas from boiler 1 enters the flue gas accelerating tube 11-2 of ram 11 after deduster 2 dedusting and cooler 3 are lowered the temperature.Ozone gas from ozone generator 4 also enters the flue gas accelerating tube 11-2 of ram 11; Streams of ozone and flue gas are pre-mixed in the flue gas accelerating tube 11-2 of ram 11.
As shown in Figure 5 and Figure 6, ram 11 is made up of solution conduit 11-1, flue gas accelerating tube 11-2 and atomizer 12, and solution conduit 11-1 one end is with hydrogen peroxide solution entrance m, and the other end is provided with atomizer 12.Flue gas accelerating tube is with ozone entrance n and smoke inlet p, and ozone entrance n and smoke inlet p adopts coaxially positioned opposite.The optimum length C of solution conduit between 60cm-150cm, between the length 50cm-130cm of flue gas accelerating tube D.The diameter of solution conduit is relevant with liquid inventory, but will ensure that solution is not more than 15 microns from the atomization droplets diameter that nozzle sprays.The diameter of flue gas accelerating tube is relevant with flue gas flow, but will ensure that flue gas flow rate that flue gas flows out from conduit outlet is between 5m/s-30m/s.
Atomized drop is produced after the atomizer 12 of hydrogen peroxide through solution conduit 11-1 top is atomized.After flue gas accelerating tube accelerates, carry the same air-flow of atomized drop and opposite after ozone mixes with flue gas mutually clash into.The hydroxyl radical free radical that ultraviolet radiation ozone/hydrogen peroxide solution produces strong oxidizing property SO in oxidation removal flue gas in shock bed 2﹑ NO xand Hg 0generate Er Jia Gong ﹑ sulfuric acid and the nitric acid of resourcebility utilization.The two valency mercury ﹑ sulfuric acid produced and nitric acid mixed solution send into afterproduct treatment system 15 by exporting a, and the flue gas of cleaning enters chimney by clashing into bed outlet d and enters air.
As shown in Figure 3, product postprocessing system 15 is by mercury knockout tower 16, and neutralizing tower 17 and evaporating and crystallizing tower 18 form, and evaporating and crystallizing tower 18 utilizes the heat of smoke waste heat utilization system 19.In mercury knockout tower 16, bivalent mercury first produces mercuric sulphide sediment separation and recovery by adding sulfidion reaction, and remaining sulfuric acid and nitric acid mixed solution in neutralizing tower 17 by adding in ammonium and, then enter evaporating and crystallizing tower 18 and heat and generate ammonium sulfate and ammonium nitrate agricultural fertilizer.
As shown in Figure 5, the ram 11 in shock bed 5 and ultraviolet lamp tube 13 adopt multi-stage cross to arrange.Ultraviolet lamp tube 13 is provided with quartz socket tube 14, and quartz socket tube 14 pairs of ultraviolet lamp tubes 13 play a protective role.Ram 11 layout alternate with ultraviolet lamp tube 13, and adjacent ram 11 and ultraviolet lamp tube 13 adopt cocurrent and parallel to arrange.Vertical interval A between ultraviolet lamp tube 13 adjacent two layers is between 5cm-60cm.Distance B between two ram 11 tops (distances between two atomizers 12) positioned opposite is between 20cm-350cm.
Ram 11 is arranged in the central spot between adjacent two layers ultraviolet lamp tube.Adjacent two-stage ram 11 adopts 90 degree of arranged crosswise staggered, and the ultraviolet lamp tube of adjacent two-stage adopts 90 degree of arranged crosswise staggered equally.
Course of reaction is as follows: the flue gas that boiler 1 discharges enters cooler 3, SO in flue gas after deduster 2 dedusting 2﹑ NO x﹑ Hg 0content respectively not higher than 8000ppm ﹑ 2000ppm ﹑ 300 μ g/m 3.After cooling, flue gas is 30-75 DEG C to the inlet temperature of shock bed 5; After the flue gas of cooling mixes with ozone, hydrogen peroxide, form gas-liquid mixture, the entrance concentration of ozone is 20ppm-500ppm, and the concentration of hydrogen peroxide is between 0.2mol/L-2.5mol/L, and effective liquid-gas ratio is 0.2-3.5L/m3; The ram 11 that gas-liquid mixture is arranged by coaxial subtend respectively sprays into shock bed 5, two strands of air-flows, in shock bed, impingement mix occurs, and the shock equalization point of described gas-liquid mixture is positioned on the center line of shock bed; The uviol lamp clashed in bed launches ultraviolet light, and ultraviolet light Net long wave radiation intensity is 20-500, and ultraviolet EWL is 160nm-365nm; Ultraviolet light associating ozone/hydrogen peroxide solution produces hydroxyl radical free radical oxidation removal SO2 ﹑ NOx and Hg0 in shock bed of strong oxidizing property, Er Jia Gong ﹑ sulfuric acid and nitric acid.
The length of embodiment 1. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m 3, hydrogen peroxide concentration is 0.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas 2﹑ NO xwith Hg 0while removal efficiency can reach 89.2%, 65.7% and 73.5% respectively.
The length of embodiment 2. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m 3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.Pilot run is: SO in flue gas 2﹑ NO xwith Hg 0while removal efficiency can reach 96.8%, 75.1% and 83.7% respectively.
The length of embodiment 3. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.5L/m 3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 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%, 85.9% and 93.8% respectively.
The length of embodiment 4. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 2.5L/m 3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 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%, 94.1% and 100% respectively.
The length of embodiment 5. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 50 DEG C, and liquid-gas ratio is 2.5L/m 3, hydrogen peroxide concentration is 2.5mol/L, and pH value of solution is 3.1, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 30 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% and 100% respectively.
Comprehensive Correlation through above embodiment is known, and embodiment 5 has best removal effect, SO 2﹑ NO xwith Hg 0removal efficiency all reaches 100%, can be used as most preferred embodiment and consults and uses.

Claims (9)

1. a light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method, is characterized in that: the flue gas of discharge enters cooler after deduster dedusting, and after cooling, flue gas is 30-75 DEG C to the inlet temperature of shock bed; After the flue gas of cooling mixes with ozone, hydrogen peroxide, form gas-liquid mixture, the entrance concentration of ozone is 20ppm-500ppm, and the concentration of hydrogen peroxide is between 0.2mol/L-2.5mol/L, and effective liquid-gas ratio is 0.2-3.5L/m 3; The ram that gas-liquid mixture is arranged by coaxial subtend respectively sprays into shock bed, and two strands of air-flows, in shock bed, impingement mix occur, and the shock equalization point of described gas-liquid mixture is positioned on the center line of shock bed; The uviol lamp clashed in bed launches ultraviolet light, and ultraviolet light Net long wave radiation intensity is 20 μ W/cm 2-500 μ W/cm 2, ultraviolet EWL is 160nm-365nm; Ultraviolet light associating ozone/hydrogen peroxide solution produces hydroxyl radical free radical oxidation removal SO in shock bed of strong oxidizing property 2﹑ NO xand Hg 0, Er Jia Gong ﹑ sulfuric acid and nitric acid.
2. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1, is characterized in that: the pH of solution is between 1.0-7.5, and solution temperature is 20-65 DEG C; SO in flue gas 2﹑ NO x﹑ Hg 0content respectively not higher than 8000ppm ﹑ 2000ppm ﹑ 300 μ g/m 3.
3. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1, it is characterized in that: described ram is made up of solution conduit and gas accelerating tube, described solution conduit one end is with hydrogen peroxide solution entrance, and the other end is provided with atomizer; Flue gas from boiler enters the flue gas accelerating tube of ram after deduster dedusting and cooler cooling; Ozone gas from ozone generator also enters the flue gas accelerating tube of ram; Streams of ozone and flue gas are pre-mixed in the flue gas accelerating tube of ram; Atomized drop is produced after the atomizer atomization of hydrogen peroxide through solution conduit top; The atomized drop carrying hydrogen peroxide after ozone mixes with flue gas after flue gas accelerating tube accelerates enters high speed nozzle.
4. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1 and 2, is characterized in that: the SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m 3, hydrogen peroxide concentration is 0.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.
5. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1 and 2, is characterized in that: the SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m 3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.
6. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1 and 2, is characterized in that: the SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.5L/m 3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.
7. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1 and 2, is characterized in that: the SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 2.5L/m 3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.
8. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1 and 2, is characterized in that: the SO in flue gas 2﹑ NO xwith Hg 0concentration is respectively 2000ppm, 400ppm and 50 μ g/m 3, the smoke inlet temperature of clashing into bed is 50 DEG C, and liquid-gas ratio is 2.5L/m 3, hydrogen peroxide concentration is 2.5mol/L, and pH value of solution is 3.1, and solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm 2, ultraviolet EWL is 254nm.
9. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1, is characterized in that: described solution is not more than 15 microns from the atomization droplets diameter that nozzle sprays; The flue gas flow rate that flue gas flows out from conduit outlet is between 5m/s-30m/s.
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