CN104923049B - A kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method - Google Patents
A kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method Download PDFInfo
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Abstract
The present invention relates to a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method, described method be using ultraviolet light joint ozone/hydrogen peroxide solution produce strong oxidizing property hydroxyl radical free radical clash into bed in oxidation removal SO2﹑ NOxAnd Hg0.Partial fume from boiler is sprayed into by ram after mixing with part ozone/hydrogen peroxide solution and clashes into bed, another part flue gas mix with another part ozone/hydrogen peroxide solution after from coaxially to arrangement ram spray into clash into bed, two strands of air-flows clash into bed in there is impingement mix.Ultraviolet radiation ozone decomposition/hydrogen peroxide produces the hydroxyl radical free radical oxidation SO of strong oxidizing property2﹑ NOxAnd Hg0Er Jia Gong ﹑ sulfuric acid and nitric acid that generation resourcebility is utilized.The system can realize the integration removing of Liu ﹑ Dan ﹑ mercury, and without secondary pollution, with wide market application foreground.
Description
Technical field
The present invention relates to the Pollutant Control Technology field of air environmental protection, and in particular to a kind of light radiation ozone/hydrogen peroxide solution
The method of simultaneous SO_2 and NO removal demercuration.
Background technology
The SO produced in combustion process2﹑ NOxAnd Hg can cause Suan Yu ﹑ photochemical fogs and the serious air of carcinogenic grade
Pollution problem, endangers human health and the ecological balance.In the past few decades, taken off although being developed substantial amounts of flue gas desulfurization
Nitre demercuration technology, but existing various desulfurization denitration demercuration technologies are originally removing target only for Single Pollution thing in research and development,
Cannot realize being removed while multi-pollutant.
For example, being mainly wet desulfurization of flue gas by limestone-gypsum method technology using more flue gas desulfurization and denitrification technology at present
With ammine selectivity catalytic reduction method.Though both approaches can independent desulphurization denitration, cannot be realized in a reactor same
When remove.Although two kinds of technique superpositions are used and can realize simultaneous SO_2 and NO removal, cause whole system complicated, floor space
Greatly, investment and operating cost are high waits not enough.In addition, the continuous improvement with the mankind to environmental requirement, for mercury in flue gas discharge
The laws and regulations of control are also gradually put into effect, but obtain large-scale commercial applications there is presently no a kind of cost-effective flue gas demercuration technology
Using.If increasing single flue gas mercury removal system again in existing desulfurization and denitrating system afterbody, certainly will will cause whole
The initial cost and operating cost of individual system further increase, final to be difficult to obtain large-scale commercial applications application with developing country.
In sum, if it is possible to by SO in a reactor2﹑ NOx﹑ Hg are removed simultaneously, then be expected to substantially reduce system
Complexity and floor space, and then reduce system investment and operating cost.Therefore, the effective sulphur/nitrogen/mercury of exploiting economy is same
When removing sulfuldioxide be the current hot issue in the field.
The content 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 to use
The hydroxyl radical free radical of ultraviolet light joint ozone/hydrogen peroxide solution generation strong oxidizing property oxidation removal SO in bed is clashed into2﹑ NOxAnd Hg0。
Principle and course of reaction that method provided by the present invention is based on：
1st, as shown in Figure 1, can be measured in reaction system using electron spin resonance (ESR) kaleidophon and generate hydroxyl certainly
By
Base.Therefore, the system is to release the hydroxyl radical free radical with strong oxidizing property first, and detailed process can use following
Change
Reaction (1)-(5) are learned to represent：
H2O2+UV→2·OH (1)
O3+UV→·O+O2 (2)
H2O2→HO- 2+H+ (3)
O3+HO- 2→·OH+O- 2+O2 (4)
·O+H2O2→·OH+HO2· (5)
2nd, the hydroxyl radical free radical of the strong oxidizing property for producing can be by the SO in flue gas2﹑ NOxAnd Hg0Oxidation generation Er Jia Gong ﹑ sulphur
Acid
With nitric acid mixed solution.Available following reaction (6)-(8) of detailed process represent：
a·OH+bSO2→cH2SO4+other products (6)
a·OH+bNO→cHNO3+other products (7)
a·OH+bHg0→cHgO+other products (8)
3rd, the Er Jia Gong ﹑ sulfuric acid and nitric acid that oxidation is produced are separated and recovered in the product postprocessing system of afterbody.For example,
Bivalent mercury can first pass through addition sulfidion reaction and produce mercuric sulphide sediment separation and recovery, and remaining sulfuric acid and nitric acid are mixed
Closing solution can generate ammonium sulfate and ammonium nitrate agricultural fertilizer by adding ammonium.The system can realize that the integration of Liu ﹑ Dan ﹑ mercury is de-
Remove, and product resourcebility is utilized, with wide market application foreground.
To realize object above, the embodiment that the present invention is used 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 is by after deduster dedusting
Into cooler.The hydroxyl radical free radical of ultraviolet light joint ozone/hydrogen peroxide solution generation strong oxidizing property oxidation removal in bed is clashed into
SO2﹑ NOxAnd Hg0, Er Jia Gong ﹑ sulfuric acid and nitric acid.
Ozone and hydrogen peroxide can be caused to occur to shift to an earlier date selfdecomposition waste costliness because the smoke inlet temperature for clashing into bed is too high
Oxidant, but if temperature is too low and the chemical reaction rate will be caused to reduce, and then influence removal efficiency.The research of inventor
It was found that, flue gas to the optimal inlet temperature for clashing into bed is 30-75 DEG C.Liquid-gas ratio is too low, and the removal efficiency of pollutant is too low, it is impossible to
Meet environmental requirement, but liquid-gas ratio set it is too high, the power of circulating pump crosses conference causes the energy consumption of system to greatly increase.Invention
People has found that optimal liquid-gas ratio is 0.2-3.5L/m by the experiment and theoretical research of system3。
Gas-liquid mixture is formed after the flue gas lowered the temperature mixes with ozone, hydrogen peroxide.The too low nothing of ozone, hydrogen peroxide concentration
The sufficient free-radical oxidation removing pollutant of method release, but once deliver the too ozone of high concentration, hydrogen peroxide can cause it is extra
Selfdecomposition and side reaction, selfdecomposition can cause ozone, hydrogen peroxide oxidant consumption serious, increase operating cost, and side reaction can be led
Cause to produce various harmful components in product, influence recycling for final product.By the experiment and detection point of inventor
Found after analysis, the optimal entrance concentration of ozone is 20ppm-500ppm, and the optimal input concentration of hydrogen peroxide is 0.2mol/L-
Between 2.5mol/L.
Gas-liquid mixture is respectively from coaxially to spraying into shock bed to the ram of arrangement, two strands of air-flows are clashing into generation in bed
Impingement mix.The research of inventor finds, when the equalization point that clashes into of the described two strands gas-liquid mixtures of atomization is located at shock bed
When on vertical center line, gas-liquid mixture can reach optimal impact strength (now mass transfer rate highest) and optimal in reactor
Mixed effect, the removal efficiency highest of pollutant.Conversely, when two strands of described gas-liquid mixtures clash into and glance off (i.e.
When not on vertical center line), gas-liquid mixture cannot realize uniform mixing in reactor, and mass transfer rate is substantially reduced, dirty
Dye thing removal efficiency is decreased obviously, it is impossible to meet environmental protection index.Therefore, the shock equalization point of the gas-liquid mixture should be located at
Clash on the center line of bed.
Inventor is using discovery after electronic self-rotary resonant technology detection, and it is too low by nothing that ultraviolet light Net long wave radiation intensity is set
Method generates sufficient concentrations of free-radical oxidation removing pollutant, but the ultraviolet radiation intensity energy consumption that will cause system too high is big
Amplitude is improved, and reduces the economy of system.Therefore, it is 20 μ W/cm to clash into the effective ultraviolet radiation intensity in bed2-500μW/
cm2.If the selection of ultraviolet EWL is too short, propagation distance of the ultraviolet light in reactor is too short, under unit power
Pollutant process amount is substantially reduced, it is impossible to meet basic processing requirement, if but ultraviolet wavelength selection oversize, ultraviolet light
The energy of son will be reduced substantially, and the ultraviolet photon of low energy cannot destroy the molecular link of peroxide, so as to cannot produce enough
The free-radical oxidation removing pollutant of concentration.By being found after comprehensive detection and analysis, ultraviolet EWL is 160nm-
365nm。
The pH of peroxide solutions is too high to cause peroxide to accelerate selfdecomposition and consume, and increase application cost, but pH
Chemical absorbing balance can be suppressed when too low, cause pollutant removing efficiency to be maintained at low-level, it is impossible to meet environmental protection index.Invention
People has found that the Optimal pH of solution is located between 1.0-7.5 after the Shi of system tests Yan Jiu ﹑ theoretical researches and detection and analysis.It is molten
Liquid temperature spends height can cause peroxide to occur to shift to an earlier date selfdecomposition, but if temperature is too low, can reduce chemical reaction rate, from
And reduce pollutant removing efficiency.20-65 DEG C is optimal solution temperature of the inventor according to acquisition after orthogonal experiment and comprehensive analysis
Degree, solution temperature more than 65 DEG C after the decomposition rate of ozone and hydrogen peroxide increase considerably, but less than 20 DEG C after chemically react speed
Rate reduction, causes the removal efficiency of pollutant significantly to decline.Therefore, optimal solution temperature is 20-65 DEG C.
Inventor is by discovery, middle SO in flue gas after the experiment and detection and analysis of system2﹑ NOx﹑ Hg0Content too high will lead
Removal efficiency is caused significantly to decline, the unabsorbed middle SO of afterbody2﹑ NOx﹑ Hg0Escape amount is increased considerably, and is easily caused serious
Secondary pollution, therefore by after research find, SO in flue gas2﹑ NOx﹑ Hg0Content be respectively no higher than 8000ppm ﹑
The μ g/m of 2000ppm ﹑ 3003。
Described ram is made up of solution conduit and flue gas accelerating tube, and described solution conduit one end is water-soluble with dioxygen
Liquid entrance, the other end is provided with atomizer；Enter ram after flue gas removing dust device dedusting and cooler cooling from boiler
Flue gas accelerating tube；Flue gas accelerating tube of the ozone gas from ozone generator also into ram；Streams of ozone and flue gas
It is pre-mixed in the flue gas accelerating tube of ram；Hydrogen peroxide after the atomizer atomization at the top of solution conduit by producing atomization
Drop；Ozone carries hydrogen peroxide atomized drop after accelerating through flue gas accelerating tube after mixing with flue gas enters high speed nozzle.
Preferred technical parameter, the SO in flue gas2﹑ NOxWith Hg0Concentration is respectively 2000ppm, 400ppm and 50 μ g/
m3, the smoke inlet temperature for clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m3, hydrogen peroxide concentration is 0.5mol/L, and pH value of solution is
3.1, solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm2, ultraviolet EWL is 254nm.
Preferred technical parameter, the SO in flue gas2﹑ NOxWith Hg0Concentration is respectively 2000ppm, 400ppm and 50 μ g/
m3, the smoke inlet temperature for clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is
3.1, solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm2, ultraviolet EWL is 254nm.
Preferred technical parameter, the SO in flue gas2﹑ NOxWith Hg0Concentration is respectively 2000ppm, 400ppm and 50 μ g/
m3, the smoke inlet temperature for clashing into bed is 60 DEG C, and liquid-gas ratio is 1.5L/m3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is
3.1, solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm2, ultraviolet EWL is 254nm.
Preferred technical parameter, the SO in flue gas2﹑ NOxWith Hg0Concentration is respectively 2000ppm, 400ppm and 50 μ g/
m3, the smoke inlet temperature for clashing into bed is 60 DEG C, and liquid-gas ratio is 2.5L/m3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is
3.1, solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm2, ultraviolet EWL is 254nm.
Preferred technical parameter, the SO in flue gas2﹑ NOxWith Hg0Concentration is respectively 2000ppm, 400ppm and 50 μ g/
m3, the smoke inlet temperature for clashing into bed is 50 DEG C, and liquid-gas ratio is 2.5L/m3, hydrogen peroxide concentration is 2.5mol/L, and pH value of solution is
3.1, solution temperature is 50 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm2, ultraviolet EWL is 254nm.
The atomization droplets diameter that the solution sprays from nozzle is not more than 15 microns；The flue gas that flue gas flows out from conduit outlet
Flow velocity is located between 5m/s-30m/s.It is smelly that the system that the removal methods are based on is provided with Guo Lu ﹑ Chu Chen Qi ﹑ Jiang Wen Qi ﹑ shock Qi ﹑
Yang Fa Sheng Qi ﹑ clash into Chuan ﹑ uviol lamps and quartz sleeve Guan ﹑ Chu Wu Qi ﹑ Xun Huan Beng ﹑ Chu Ye Guan ﹑ chimneys and product postprocessing system etc..
The ram and ultraviolet lamp tube clashed into bed are arranged using multi-stage cross.Ram and the alternate arrangement of ultraviolet lamp tube,
And adjacent ram and ultraviolet lamp tube are arranged using cocurrent and parallel.Vertical interval A between ultraviolet lamp tube adjacent two layers is located at
Between 5cm-60cm, to reach optimal light radiation effect.Two ram tops positioned opposite are (between two atomizers
Distance) the distance between B be located at 20cm-350cm between, to reach optimal atomizing effect.Ram is arranged in adjacent two
Central spot between layer ultraviolet lamp tube.Adjacent two-stage ram using 90 degree of arranged crosswises for staggering, and adjacent two-stage purple
Outer fluorescent tube equally uses 90 degree of arranged crosswises for staggering, to reach optimal impingement mix effect.
Ram is made up of solution conduit and flue gas accelerating tube.Solution conduit one end carries hydrogen peroxide solution entrance, another
End is provided with atomizer.Flue gas accelerating tube carries ozone inlet and smoke inlet, and ozone inlet and smoke inlet using coaxial
It is positioned opposite.The optimum length C of solution conduit is located between 60cm-150cm, and the optimum length D of flue gas accelerating tube is located at 50cm-
Between 130cm.The diameter of solution conduit is relevant with liquid inventory, but to ensure atomization droplets diameter that solution sprayed from nozzle not
More than 15 microns.The diameter of flue gas accelerating tube is relevant with flue gas flow, but to ensure the flue gas stream that flue gas flows out from conduit outlet
Speed is located between 5m/s-30m/s.
It is significant to note that：Various Optimal Parameters selected above, are that inventor closes Shi Yan ﹑ by substantial amounts of Zong
Just obtained after theoretical calculation and detection and analysis.Because each operating parameter generally also suffers from other one or more parameters
Combined influence or interference, therefore acquisition cannot be contrasted by simple scene experiment of single factor or document.The present invention is provided in addition
Optimal Parameters be to determine after Comprehensive Correlation in equipment in mini-plant and after amplifying, considered equipment amplification process
Issuable " enlarge-effect ", therefore field technician can not speculate that acquisition safety can after to existing equipment simple analysis
The Optimal Parameters for leaning on.
Advantages of the present invention and remarkable result (with prior art or Patent Reference)：
(1) according to internationally famous chemical industry expert Danckwerts[1]Found with the research that Zhang Chengfang teaches[2], for quick
Chemical reaction system, the rate-determining steps of whole pollutant removing are concentrated mainly on mass transfer link, i.e., if it is desired to increasing substantially dirt
Contaminate thing removal efficiency must preferential consolidation system mass transfer rate.Due to traditional bubble tower and spray column mass transfer rate compared with
It is low, it is impossible to meet the high-speed chemical reaction system of free radical initiation.In addition, the research table of the famous scholar Wu Yuan professors of China
It is bright[2], under the same terms, the mass transfer rate of bed is clashed into than bubbling bed and is sprayed more than height of bed an order of magnitude, with high
Mass transfer rate, is very suitable for the fast chemical reaction system of free radical initiation.The system realizes 100% pollutant removing
Efficiency is that provable shock bed is a kind of superior gas-liquid reactor, is suitable for the fast reaction system of free yl induction.Therefore,
Inventor proposes the hydrogen sulfide that will clash into bed in free radical fast reaction system is combined for removing flue gas first, has substantially
Novelty and practical value, it may have good development potentiality and market prospects.
(bibliography [1] Danckwerts, P.V.Gas-Liquid Reactions.New York:McGraw-Hill,
1970. [2] Zhang Chengfang gas liquid reactions and reactor [M] Beijing:Chemical Industry Press, 1985. [3] Wu Yuan percussion flows-original
Rationality matter application [M] Beijing:Chemical Industry Press, 2005.)
(2) Chinese patent of Patent No. 201310683135.8 proposes a kind of photoactivation persulfuric acid based on spray column
Salt simultaneous SO_2 and NO removal demercuration system, but because the mass transfer rate of spray column is low, it is impossible to meet the fast reaction of free radical initiation,
Cause pollutant removing inefficient, and photochemistry proposed by the present invention is clashed into bed accessory and has extremely strong mass transfer rate, can be obvious
Mass transfer rate is improved, so as to increase substantially the removal efficiency of pollutant.System of the present invention can realize SO2﹑ NOxTri- kinds of dirts of ﹑ Hg
100% removal efficiency for contaminating thing is to demonstrate the outstanding removing performance of the system.
(3) Chinese patent of Patent No. 201010296492.5 is proposed one kind and is produced from using light radiation hydrogen peroxide
System for desulfuration and denitration while by base, but the system can only simultaneous SO_2 and NO removal, it is impossible to demercuration is realized, and the present invention can be one
SO is realized in individual reactor2﹑ NOxRemoved while tri- kinds of pollutants of ﹑ Hg, it is thus possible to reduce the initial cost and running cost of system
With.Continuous improvement with the mankind to environmental requirement, this advantage of the invention will be highlighted gradually.In addition, the patent institute
The removal methods and technique stated use the mass transfer rate very low and small bubbling column reactor of market application potential, and of the invention
The photochemistry of proposition clashes into bed accessory extremely strong mass transfer rate, mass transfer rate can be significantly improved, so as to increase substantially pollution
The removal efficiency of thing.
Brief description of the drawings
The hydroxyl radical free radical ESR light captured in a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration systems of Fig. 1 is general
Figure.
Fig. 2 is technological process and the structure chart of present system.
Fig. 3 is the product postprocessing device and flow chart of present system.
Fig. 4 is the structural representation that the present invention clashes into bed inner impact device and ultraviolet lamp tube two adjacent groups arrangement.
Fig. 5 is the structural representation of ram.
Fig. 6 is the critical size mark schematic diagram of ram.
Specific embodiment
Below in conjunction with the accompanying drawings, specific embodiment of the invention is further described.
As shown in Fig. 2 the system that a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method is based on, is provided with pot
The ﹑ of 11 ﹑ ozone generators of stove 1 ﹑ dedusters, 2 ﹑ coolers, 3 ﹑ rams 4 clashes into the ﹑ uviol lamps 13 of bed 5 and the ﹑ demisters of quartz socket tube 14
The ﹑ circulating pumps 28 of 9 ﹑ circulating pumps 1, the ﹑ chimneys 10 of fluid reservoir 6 and product postprocessing system.
Hydrogen peroxide enters fluid reservoir 6 from the entrance c of fluid reservoir 6, is then sent by circulating pump 1 or the suction of circulating pump 28
Enter the solution conduit 11-1 of ram 11；The dedusting of flue gas removing dust device 2 and cooler 3 from boiler 1 enter after lowering the temperature clashes into
The flue gas accelerating tube 11-2 of device 11.Flue gas accelerating tube 11-2 of the ozone gas from ozone generator 4 also into ram 11；
Streams of ozone is pre-mixed with flue gas in the flue gas accelerating tube 11-2 of ram 11.
As shown in Figure 5 and Figure 6, ram 11 is by solution conduit 11-1, flue gas accelerating tube 11-2 and 12 groups of atomizer
Into solution conduit 11-1 one end carries hydrogen peroxide solution entrance m, and the other end is provided with atomizer 12.Flue gas accelerating tube is with smelly
Oxygen entrance n and smoke inlet p, and ozone inlet n and smoke inlet p is using coaxial 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 has with liquid inventory
Close, but to ensure that the atomization droplets diameter that solution sprays from nozzle is not more than 15 microns.The diameter of flue gas accelerating tube and flue gas stream
Amount is relevant, but to ensure that the flue gas flow rate that flue gas flows out from conduit outlet is located between 5m/s-30m/s.
Hydrogen peroxide produces atomized drop after the atomizer 12 at the top of solution conduit 11-1 is atomized.Ozone is mixed with flue gas
The atomized drop air-flow same with opposite is carried after accelerating through flue gas accelerating tube after conjunction mutually to clash into.Ultraviolet radiation ozone/bis-
The hydroxyl radical free radical of oxygen water generation strong oxidizing property SO in oxidation removal flue gas in clashing into bed2﹑ NOxAnd Hg0Generation resourcebility profit
Er Jia Gong ﹑ sulfuric acid and nitric acid.The Er Jia Gong ﹑ sulfuric acid and nitric acid mixed solution of generation are by exporting product processing system after a sends into
System 15, and the flue gas of cleaning is by the outlet of shock bed, and d is into chimney and enters air.
As shown in figure 3, product postprocessing system is made up of mercury knockout tower 16, neutralizing tower 17 and evaporating and crystallizing tower 18, steam
Hair crystallizing tower 18 utilizes the heat of smoke waste heat utilization system 19.In mercury knockout tower 16 bivalent mercury first pass through addition divalent sulfur from
Son reaction produces mercuric sulphide sediment separation and recovery, and remaining sulfuric acid and nitric acid mixed solution can be by adding in neutralizing tower 17
Plus ammonium is neutralized, subsequently into evaporating and crystallizing tower 18 heating generation ammonium sulfate and ammonium nitrate agricultural fertilizer.
As shown in figure 4, the ram 11 and ultraviolet lamp tube 13 that clash into bed 5 are arranged using multi-stage cross.Ultraviolet lamp tube 13
Quartz socket tube 14 is provided with, quartz socket tube 14 plays a protective role to ultraviolet lamp tube 13.Ram 11 and the alternate cloth of ultraviolet lamp tube 13
Put, and adjacent ram 11 and ultraviolet lamp tube 13 are arranged using cocurrent and parallel.It is vertical between the adjacent two layers of ultraviolet lamp tube 13
Spacing A is located between 5cm-60cm.Two tops of ram 11 positioned opposite the distance between (two atomizer 12) it
Between apart from B be located at 20cm-350cm between.
Ram 11 is arranged in the central spot between adjacent two layers ultraviolet lamp tube.Adjacent two-stage ram 11 uses 90 degree
The arranged crosswise for staggering, and the ultraviolet lamp tube of adjacent two-stage equally uses 90 degree of arranged crosswises for staggering.
Course of reaction is as follows：The flue gas of the discharge of boiler 1 is by entering cooler 3, SO in flue gas after the dedusting of deduster 22﹑
NOx﹑ Hg0Content be respectively no higher than the μ g/m of 8000ppm ﹑ 2000ppm ﹑ 3003.Flue gas extremely clashes into the inlet temperature of bed 5 after cooling
It is 30-75 DEG C；Gas-liquid mixture is formed after the flue gas lowered the temperature mixes with ozone, hydrogen peroxide, the entrance concentration of ozone is
20ppm-500ppm, the concentration of hydrogen peroxide is between 0.2mol/L-2.5mol/L, effective liquid-gas ratio is 0.2-3.5L/m3；Gas-liquid
Respectively from coaxially spraying into shock bed 5 to the ram 11 to arrangement, there is impingement mix in two strands of air-flows to mixture in shock bed,
The equalization point that clashes into of the gas-liquid mixture is located on the center line for clashing into bed；The uviol lamp clashed into bed launches ultraviolet light,
Ultraviolet light Net long wave radiation intensity is 20-500, and ultraviolet EWL is 160nm-365nm；Ultraviolet light combines ozone/hydrogen peroxide solution
The hydroxyl radical free radical of generation strong oxidizing property oxidation removal SO2 ﹑ NOx and Hg0, Er Jia Gong ﹑ sulfuric acid and nitric acid in bed is clashed into.
The length of the solution conduit of embodiment 1. is located at 60cm, and flue gas accelerates length of tube 50cm.Two shocks positioned opposite
The distance between device top the distance between (two atomizer) B is 25cm.SO in flue gas2﹑ NOxWith Hg0Concentration is respectively
2000ppm, 400ppm and 50 μ g/m3, the smoke inlet temperature for clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m3, hydrogen peroxide is dense
It is 0.5mol/L to spend, 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/cm2, ultraviolet has
Length is 254nm.Pilot run is：SO in flue gas2﹑ NOxWith Hg0While removal efficiency can respectively reach 89.2%,
65.7% and 73.5%.
The length of the solution conduit of embodiment 2. is located at 60cm, and flue gas accelerates length of tube 50cm.Two shocks positioned opposite
The distance between device top the distance between (two atomizer) B is 25cm.SO in flue gas2﹑ NOxWith Hg0Concentration is respectively
2000ppm, 400ppm and 50 μ g/m3, the smoke inlet temperature for clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m3, hydrogen peroxide is dense
It is 1.0mol/L to spend, 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/cm2, ultraviolet has
Length is 254nm.Pilot run is：SO in flue gas2﹑ NOxWith Hg0While removal efficiency can respectively reach 96.8%,
75.1% and 83.7%.
The length of the solution conduit of embodiment 3. is located at 60cm, and flue gas accelerates length of tube 50cm.Two shocks positioned opposite
The distance between device top the distance between (two atomizer) B is 25cm.SO in flue gas2﹑ NOxWith Hg0Concentration is respectively
2000ppm, 400ppm and 50 μ g/m3, the smoke inlet temperature for clashing into bed is 60 DEG C, and liquid-gas ratio is 1.5L/m3, hydrogen peroxide is dense
It is 1.5mol/L to spend, 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/cm2, ultraviolet has
Length is 254nm.Pilot run is：SO in flue gas2﹑ NOxWith Hg0While removal efficiency can respectively reach 100%,
85.9% and 93.8%.
The length of the solution conduit of embodiment 4. is located at 60cm, and flue gas accelerates length of tube 50cm.Two shocks positioned opposite
The distance between device top the distance between (two atomizer) B is 25cm.SO in flue gas2﹑ NOxWith Hg0Concentration is respectively
2000ppm, 400ppm and 50 μ g/m3, the smoke inlet temperature for clashing into bed is 60 DEG C, and liquid-gas ratio is 2.5L/m3, hydrogen peroxide is dense
It is 1.5mol/L to spend, 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/cm2, ultraviolet has
Length is 254nm.Pilot run is：SO in flue gas2﹑ NOxWith Hg0While removal efficiency can respectively reach 100%,
94.1% and 100%.
The length of the solution conduit of embodiment 5. is located at 60cm, and flue gas accelerates length of tube 50cm.Two shocks positioned opposite
The distance between device top the distance between (two atomizer) B is 25cm.SO in flue gas2﹑ NOxWith Hg0Concentration is respectively
2000ppm, 400ppm and 50 μ g/m3, the smoke inlet temperature for clashing into bed is 50 DEG C, and liquid-gas ratio is 2.5L/m3, hydrogen peroxide is dense
It is 2.5mol/L to spend, 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/cm2, ultraviolet has
Length is 254nm.Pilot run is：SO in flue gas2﹑ NOxWith Hg0While removal efficiency can respectively reach 100%, 100%
With 100%.
Understand that embodiment 5 has optimal removal effect, SO by the Comprehensive Correlation of above example2﹑ NOxWith Hg0Removing
Efficiency reaches 100%, can be consulted and used as most preferred embodiment.
Claims (8)
1. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method, it is characterised in that：The flue gas of discharge is by dedusting
Enter cooler after device dedusting, flue gas to the inlet temperature for clashing into bed is 30-75 DEG C after cooling；Through cooling flue gas with it is smelly
Gas-liquid mixture is formed after oxygen, hydrogen peroxide mixing, the entrance concentration of ozone is 20ppm-500ppm, and the concentration of hydrogen peroxide is
Between 0.2mol/L-2.5mol/L, effective liquid-gas ratio is 0.2-3.5L/m3；Gas-liquid mixture is respectively from coaxially to arrangement
Ram is sprayed into and clashes into bed, and two strands of air-flows occur impingement mix, the shock equalization point position of the gas-liquid mixture in shock bed
In on the center line for clashing into bed；Clash into the ultraviolet lamp tube in bed and launch ultraviolet light, ultraviolet light Net long wave radiation intensity is 20 μ W/
cm2-500μW/cm2, ultraviolet EWL is 160nm-365nm；Ultraviolet light joint ozone/hydrogen peroxide solution produces strong oxidizing property
Hydroxyl radical free radical oxidation removal SO in bed is clashed into2﹑ NOxAnd Hg0, generate Er Jia Gong ﹑ sulfuric acid and nitric acid；Described ram by
Solution conduit and flue gas accelerating tube are constituted, and described solution conduit one end carries hydrogen peroxide solution entrance, and the other end is provided with atomization
Nozzle；Enter the flue gas accelerating tube of ram after flue gas removing dust device dedusting and cooler cooling from boiler；From ozone
Flue gas accelerating tube of the ozone gas of generator also into ram；Streams of ozone is with flue gas in the flue gas accelerating tube of ram
It is pre-mixed；Hydrogen peroxide after the atomizer atomization at the top of solution conduit by producing atomized drop；After ozone mixes with flue gas
The atomized drop that hydrogen peroxide is carried after accelerating through flue gas accelerating tube enters high speed nozzle；Clash into the ram and ultraviolet lamp tube in bed
Arranged using multi-stage cross；Ram and the alternate arrangement of ultraviolet lamp tube, and adjacent ram and ultraviolet lamp tube use same-directional flat
Row arrangement；Vertical interval A between ultraviolet lamp tube adjacent two layers is located between 5cm-60cm, is imitated with reaching optimal light radiation
Really；Two ram tops positioned opposite, the distance between B be located between 20cm-350cm, imitated with reaching optimal atomization
Really；Ram is arranged in the central spot between adjacent two layers ultraviolet lamp tube；Adjacent two-stage ram is using 90 degree of friendships staggered
Fork arrangement, and the ultraviolet lamp tube of adjacent two-stage equally uses 90 degree of arranged crosswise rams for staggering to be added by solution conduit and flue gas
Fast pipe is constituted；Solution conduit one end carries hydrogen peroxide solution entrance, and the other end is provided with atomizer, and flue gas accelerating tube carries ozone
Entrance and smoke inlet, and ozone inlet and smoke inlet use coaxial positioned opposite, the optimum length C of solution conduit is located at
Between 60cm-150cm, the optimum length D of flue gas accelerating tube is located between 50cm-130cm；The diameter of solution conduit and solution stream
Amount is relevant, but to ensure that the atomization droplets diameter that solution sprays from nozzle is not more than 15 microns；The diameter and cigarette of flue gas accelerating tube
Throughput is relevant, but to ensure that the flue gas flow rate that flue gas flows out from conduit outlet is located between 5m/s-30m/s.
2. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1, its feature exists
In：The pH of hydrogen peroxide solution is located between 1.0-7.5, and hydrogen peroxide solution temperature is 20-65 DEG C；SO in flue gas2﹑ NOx﹑ Hg0Contain
Amount is respectively no higher than the μ g/m of 8000ppm ﹑ 2000ppm ﹑ 3003。
3. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1 and 2, its feature
It is：SO in flue gas2﹑ NOxWith Hg0Concentration is respectively 2000ppm, 400ppm and 50 μ g/m3, clash into the smoke inlet of bed
Temperature is 60 DEG C, and liquid-gas ratio is 1.0L/m3, hydrogen peroxide concentration is 0.5mol/L, and hydrogen peroxide solution pH is 3.1, and solution temperature is
60 DEG C, ultraviolet light Net long wave radiation intensity is 30 μ W/cm2, ultraviolet EWL is 254nm.
4. a kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method according to claim 1 and 2, its feature
It is：SO in flue gas2﹑ NOxWith Hg0Concentration is respectively 2000ppm, 400ppm and 50 μ g/m3, clash into the smoke inlet of bed
Temperature is 60 DEG C, and liquid-gas ratio is 1.0L/m3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, purple
Outer smooth Net long wave radiation intensity is 30 μ W/cm2, 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, its feature
It is：SO in flue gas2﹑ NOxWith Hg0Concentration is respectively 2000ppm, 400ppm and 50 μ g/m3, clash into the smoke inlet of bed
Temperature is 60 DEG C, and liquid-gas ratio is 1.5L/m3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, purple
Outer smooth Net long wave radiation intensity is 30 μ W/cm2, 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, its feature
It is：SO in flue gas2﹑ NOxWith Hg0Concentration is respectively 2000ppm, 400ppm and 50 μ g/m3, clash into the smoke inlet of bed
Temperature is 60 DEG C, and liquid-gas ratio is 2.5L/m3, hydrogen peroxide concentration is 1.5mol/L, and pH value of solution is 3.1, and solution temperature is 60 DEG C, purple
Outer smooth Net long wave radiation intensity is 30 μ W/cm2, 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, its feature
It is：SO in flue gas2﹑ NOxWith Hg0Concentration is respectively 2000ppm, 400ppm and 50 μ g/m3, clash into the smoke inlet of bed
Temperature is 50 DEG C, and liquid-gas ratio is 2.5L/m3, hydrogen peroxide concentration is 2.5mol/L, and pH value of solution is 3.1, and solution temperature is 50 DEG C, purple
Outer smooth Net long wave radiation intensity is 30 μ W/cm2, 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, its feature exists
In：The atomization droplets diameter that the solution sprays from nozzle is not more than 15 microns；The flue gas flow rate that flue gas flows out from conduit outlet
Between 5m/s-30m/s.
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| CN105536466B (en) * | 2016-01-25 | 2017-11-03 | 华北电力大学（保定） | The device and method of multi-pollutant in a kind of photocatalytic oxidation removing flue gas |
| CN105561751A (en) * | 2016-03-17 | 2016-05-11 | 南京格洛特环境工程股份有限公司 | Low temperature denitrification process for multi-phase catalytic oxidation and equipment thereof |
| CN105771630A (en) * | 2016-03-17 | 2016-07-20 | 南京格洛特环境工程股份有限公司 | VOCs treatment process and equipment using heterogeneous catalytic oxidation |
| CN106139841B (en) * | 2016-04-18 | 2019-01-08 | 江苏大学 | A kind of method and device of light radiation electrolysis coupling demercuration |
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| CN105727724B (en) * | 2016-04-18 | 2018-02-27 | 江苏大学 | A kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization |
| CN106823722A (en) * | 2017-03-10 | 2017-06-13 | 东南大学 | A kind of apparatus and method of thermal activation oxidant combined steam synergistic purification flue gas |
| CN109603523A (en) * | 2018-12-25 | 2019-04-12 | 清华大学 | A method of utilizing NOx in UV catalytic oxidative desulfurization flue gas |
| CN112067498B (en) * | 2020-07-25 | 2024-02-13 | 东北电力大学 | In-water discharge H 2 O 2 Particle space-time density distribution measuring device and measuring method thereof |
| CN111829099B (en) * | 2020-08-10 | 2024-02-27 | 中物院成都科学技术发展中心 | Device and method for sterilizing aerosol and degrading organic gas |
| CN112147248A (en) * | 2020-09-23 | 2020-12-29 | 浙江求实环境监测有限公司 | Method for rapidly determining content of benzene series components in waste gas of fixed pollution source |
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| CN200948420Y (en) * | 2006-03-27 | 2007-09-19 | 伍沅 | Air-liquid reactor of large quantity of striking flow |
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| CN103638796B (en) * | 2013-12-13 | 2016-06-15 | 江苏大学 | A kind of system of the desulfurization denitration demercuration based on photoactivation ammonium persulfate |
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