CN204637986U - Free radical pre-oxidation is in conjunction with the simultaneous SO_2 and NO removal demercuration system of wet absorption - Google Patents
Free radical pre-oxidation is in conjunction with the simultaneous SO_2 and NO removal demercuration system of wet absorption Download PDFInfo
- Publication number
- CN204637986U CN204637986U CN201520244728.9U CN201520244728U CN204637986U CN 204637986 U CN204637986 U CN 204637986U CN 201520244728 U CN201520244728 U CN 201520244728U CN 204637986 U CN204637986 U CN 204637986U
- Authority
- CN
- China
- Prior art keywords
- high speed
- bed
- oxidation
- sprayer
- adjacent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- 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 utility model relates to a kind of based on the simultaneous SO_2 and NO removal demercuration system of free radical pre-oxidation in conjunction with wet absorption, and described system is the hydroxyl or the potentiometric titrations oxidation removal SO in shock bed that adopt ultraviolet light united catalyst decompose hydroperoxide to produce strong oxidizing property
2﹑ NO
xand Hg
0.Spray into shock bed by high speed nozzle after mixing with partially catalyzed agent particle from the partial fume of emission source, the high speed nozzle arranged by coaxial subtend after another part flue gas mixes with another part catalyst granules sprays into shock bed.Ultraviolet light united catalyst decompose hydroperoxide produces hydroxyl or the potentiometric titrations oxidation SO of strong oxidizing property
2﹑ NO
xand Hg
0generate gaseous state Er Jia Gong ﹑ bis-Yangization Dan ﹑ tri-Yangization Liu ﹑ sulfuric acid and nitric acid, then in the wet desulfurization system of afterbody by absorbing and removing.This system can be used in transforming existing coal-burning boiler and realizes the integration of Liu ﹑ Dan ﹑ mercury and remove, and has wide market application foreground.
Description
Technical field
The utility model relates to combustion product gases pollutant catabolic gene field, is specifically related to a kind of based on the simultaneous SO_2 and NO removal demercuration system of free radical pre-oxidation in conjunction with wet absorption.
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 utility model relates to a kind of based on the simultaneous SO_2 and NO removal demercuration system of free radical pre-oxidation in conjunction with wet absorption, and described system is the hydroxyl or the potentiometric titrations oxidation removal SO in shock bed that adopt ultraviolet light united catalyst decompose hydroperoxide to produce strong oxidizing property
2﹑ NO
xand Hg
0.
Principle and the course of reaction removing system of the present utility model:
1, as shown in Figure 1, adopt electron spin resonance (ESR) kaleidophon can be measured in reaction system and create hydroxyl and potentiometric titrations.Therefore, first this system is release the hydroxyl and potentiometric titrations with strong oxidizing property, and detailed process can represent with following chemical reaction (1)-(3):
H
2o
2+ UV+ catalyst 2 × OH
(1)
(2)
(3)
SO2 ﹑ NOx in flue gas and Hg0 pre-oxidation can be generated gaseous state Er Jia Gong ﹑ bis-Yangization Dan ﹑ tri-Yangization Liu ﹑ sulfuric acid and nitric acid by the sulfate radical of the strong oxidizing property 2, produced and hydroxyl radical free radical.Detailed process can represent with following reaction (4)-(13):
a×OH+bSO
2cH
2SO
4+other products
(4)
a×OH+bSO
2cSO
3++other products
(5)
a×OH+bNO cNO
2++other products
(6)
a×OH+bNO cHNO
3+other products
(7)
a×OH+bHg
0cHgO+other products
(8)
cH
2SO
4+other products
(9)
cSO
3+other products
(10)
cNO
2+other products
(11)
cHNO
3+other products
(12)
cHgO+other products
(13)
3, pre-oxidation produce gaseous state Er Jia Gong ﹑ bis-Yangization Dan ﹑ tri-Yangization Liu ﹑ sulfuric acid and nitric acid in the Wet Limestone Desulfurization system of afterbody by absorbing and removing.This system can be used in transforming existing coal-burning boiler and realizes the integration of Liu ﹑ Dan ﹑ mercury and remove, and has wide market application foreground.
For realizing above object, the embodiment that the utility model adopts is as follows:
Based on the simultaneous SO_2 and NO removal demercuration system of free radical pre-oxidation in conjunction with wet absorption, described system is provided with Pai Fang Yuan ﹑ Feng Ji ﹑ Jiang Wen Qi ﹑ Hun He Qi ﹑ Fa Men ﹑ catalyst and stores Ta ﹑ shock Chuan ﹑ Pen Wu Beng ﹑ Chu Ye Xiang ﹑ Xun Huan Beng ﹑ Wet Limestone Desulfurization system and chimney; Emission source connects cooler entrance by flue, cooler outlet connects the smoke inlet of blender, the outlet of catalyst storage tower connects the catalyst inlet of blender, and the outlet of blender is provided with two, and the high speed nozzle arranged with the coaxial subtend of clashing on bed is respectively connected; Described shock bed is provided with exhanst gas outlet, demister, deduster, at a high speed spray mouth ﹑ spray mist device ﹑ uviol lamp and quartzy sleeve pipe ﹑ catalyst outlet from top to bottom successively; Described high speed Pen Zui ﹑ Pen Wu Qi ﹑ uviol lamp and quartz socket tube multistage staggered alternate setting in shock bed; Described liquid reserve tank is connected with the sprayer clashing into bed by pipeline; The exhanst gas outlet of described shock bed is connected with the entrance of Wet Limestone Desulfurization tower, and the outlet of Wet Limestone Desulfurization tower connects chimney.
The flue of described emission source and cooler is provided with the blower fan flue gas of emission source being introduced cooler; Described liquid reserve tank with clash into the pipeline that is connected of bed and be provided with as peroxide solutions provides the atomizing pump of power.
Clash into the high speed Pen Zui ﹑ sprayer in bed and ultraviolet lamp tube employing multi-stage cross layout; High speed Pen Zui ﹑ sprayer layout alternate with ultraviolet lamp tube, and adjacent high speed Pen Zui ﹑ sprayer and ultraviolet lamp tube adopt and arrange in the same way.
Vertical interval H between high speed nozzle adjacent two layers is between 20cm-120cm, and adjacent two-stage high speed nozzle adopts 90 degree of arranged crosswise staggered; Ultraviolet lamp tube is arranged in the central spot between adjacent two-stage high speed nozzle, and the ultraviolet lamp tube of adjacent two-stage adopts 90 degree of arranged crosswise staggered; Sprayer is arranged in the central spot between adjacent two-stage high speed nozzle and ultraviolet lamp tube, and the sprayer of adjacent two-stage adopts 90 degree of arranged crosswise staggered.
Spray into shock bed by high speed nozzle after mixing with partially catalyzed agent particle from the partial fume of emission source, the high speed nozzle arranged by coaxial subtend after another part flue gas mixes with another part catalyst granules sprays into shock bed.Meanwhile, peroxide solutions is sprayed into by sprayer and clashes in bed, and three strands of air-flows, in shock bed, impingement mix occur.Ultraviolet light united catalyst decompose hydroperoxide produces hydroxyl or the potentiometric titrations oxidation SO of strong oxidizing property
2﹑ NO
xand Hg
0generate gaseous state Er Jia Gong ﹑ bis-Yangization Dan ﹑ tri-Yangization Liu ﹑ sulfuric acid and nitric acid, then in the wet desulfurization system of afterbody by absorbing and removing.
Catalyst granules enters blender from the outlet a of catalyst storage tower, and flue gas also enters blender from the outlet b of emission source after cooler cooling, and flue gas and catalyst granules are divided into two strands of impartial air-flows after mixing in blender.Half air-flow sprays into shock bed by being arranged on high speed nozzle on one side through entrance c, and the high speed nozzle that second half air-flow is then arranged by the coaxial subtend being arranged on another side sprays into shock bed through entrance d.Meanwhile, the peroxide solutions from liquid reserve tank provides power by atomizing pump, is sprayed in shock bed from entrance e by sprayer.Impingement mix is there is in three strands of air-flows in shock bed.Ultraviolet light united catalyst decompose hydroperoxide produces hydroxyl or the potentiometric titrations oxidation SO of strong oxidizing property
2﹑ NO
xand Hg
0generate gaseous state Er Jia Gong ﹑ bis-Yangization Dan ﹑ tri-Yangization Liu ﹑ sulfuric acid and nitric acid, these gaseous products of generation enter absorbing and removing in tower from shock bed outlet g through the entrance h of Wet Limestone Desulfurization system, and the clean flue gas through washing enters air from chimney.
The best smoke inlet temperature of clashing into bed is 60-160 DEG C, and effective liquid-gas ratio is 0.2-3.0L/m
3, the optium concentration of peroxide is between 0.2mol/L-2.0mol/L, and the pH of solution is between 1.0-6.5, and best solution temperature is 70-95 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm
2-400 μ W/cm
2, ultraviolet EWL is 180nm-365nm.The atomization droplets diameter of the peroxide solutions of sprayer ejection is not more than 10 microns.The exit velocity of high speed nozzle the best is 5-25m/s.The optimum dosage of catalyst can add 0.1-4kg by every cubic metre of clashing into bed bioreactor volume.SO in flue gas
2﹑ NO
x﹑ Hg
0content respectively not higher than 8000ppm ﹑ 2000ppm ﹑ 300 μ g/m
3.
Described catalyst is one or more mixtures in Er Yangization Tai ﹑ Yangization Tie ﹑ bis-Yangization Meng ﹑ cupric oxide, also can be the support type of described catalyst, used carrier can be one or more the complex in Huo Tan ﹑ tri-Yangization Er Lv ﹑ Fen Shai ﹑ silica gel and biomass char.
Described emission source can be any one in Ran coal Guo Lu ﹑ La rubbish Fen Shao Lu ﹑ petrochemical equipment and linked medical waste incinerator.Described peroxide is one or more the mixing in Shuan Yang Shui ﹑ Guo Liu Suan An ﹑ sodium peroxydisulfate and potassium peroxydisulfate.
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 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 utility model proposes has extremely strong mass transfer rate, can mass transfer rate be significantly improved, thus increase substantially the removal efficiency of pollutant.System described in the utility model can realize SO
2﹑ NO
x100% removal efficiency of ﹑ Hg tri-kinds of pollutants namely demonstrate this system outstanding remove performance.
(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 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 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 photochemistry shock bed accessory that the utility model proposes has extremely strong mass transfer rate, mass transfer rate can be significantly improved, thus increase substantially the removal efficiency of pollutant.
(3) in the past twenty years, in state-owned a large amount of coal-burning boiler only wet desulfurization system is housed, but along with improving constantly of environmental requirement, country has put into effect multinomial measure requirement recently and has removed nitrogen oxide and mercury, and the utility model can utilize existing lime stone to wet desulphurization system in conjunction with pre-oxidation simultaneous SO_2 and NO removal demercuration.This technology is likely used to transform existing old boiler, possesses huge market potential and economic worth.
Accompanying drawing explanation
Fig. 1 based on free radical pre-oxidation in conjunction with the general figure of ESR light caught in wet absorption simultaneous SO_2 and NO removal demercuration
Fig. 2 is technological process and the structure chart of the utility model system
Fig. 3 is the structural representation that the utility model clashes into that in bed, high speed Pen Zui ﹑ sprayer and ultraviolet lamp tube two adjacent groups are arranged.
Fig. 4 is the structural representation of blender.
Fig. 5 is the structural representation of sprayer.
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 shown in Figure 2, based on the simultaneous SO_2 and NO removal demercuration method of free radical pre-oxidation in conjunction with wet absorption, described method based on system be provided with emission source 1 ﹑ blower fan 2 ﹑ cooler 3 ﹑ blender 4 ﹑ valve one 9-1 ﹑ valve two 9-2, catalyst storage tower 6 ﹑ and clash into bed 5 ﹑ high speed nozzle 11 ﹑ sprayer 12 ﹑ uviol lamp 13 and quartzy sleeve pipe ﹑ demister 17 ﹑ soot blower 16 ﹑ atomizing pump 8 ﹑ liquid reserve tank 7 ﹑ circulating pump 10 ﹑ Wet Limestone Desulfurization system 14 and chimney 15.
Emission source 1 connects cooler 3 entrance by flue, cooler 3 exports the smoke inlet m connecting blender 4, the outlet of catalyst storage tower 6 connects the catalyst inlet n of blender 4, and the outlet p of blender is provided with two, and the high speed nozzle 11 arranged with the coaxial subtend of clashing on bed 5 is respectively connected; Described shock bed 5 is provided with exhanst gas outlet g, demister 17, soot blower 16, high speed nozzle 11 ﹑ sprayer 12 ﹑ uviol lamp 13 and quartzy sleeve pipe ﹑ catalyst outlet f from top to bottom successively; Described high speed nozzle 11 ﹑ sprayer 12 ﹑ uviol lamp 13 and quartz socket tube multistage staggered alternate setting in shock bed 5; Described liquid reserve tank 7 is connected with the sprayer 12 clashing into bed 5 by pipeline; The exhanst gas outlet g of described shock bed 5 is connected with the entrance of Wet Limestone Desulfurization tower, and the outlet of Wet Limestone Desulfurization tower connects chimney.
As shown in Figure 3, the high speed nozzle 11 ﹑ sprayer 12 in shock bed 5 and ultraviolet lamp tube 13 all adopt multi-stage cross to arrange.
High speed nozzle 11 ﹑ sprayer 12 layout alternate with ultraviolet lamp tube 13, and adjacent high speed nozzle 11 ﹑ sprayer 12 and ultraviolet lamp tube 13 adopt and arrange in the same way.Vertical interval H between high speed nozzle 11 adjacent two layers is between 20cm-120cm, and adjacent two-stage high speed nozzle 11 adopts 90 degree of arranged crosswise staggered.Ultraviolet lamp tube 13 is arranged in the central spot between adjacent two-stage high speed nozzle 11, and the ultraviolet lamp tube 13 of adjacent two-stage adopts 90 degree of arranged crosswise staggered equally.Sprayer 12 is arranged in the central spot between adjacent two-stage high speed nozzle 11 and ultraviolet lamp tube 13, and the sprayer 11 of adjacent two-stage also adopts 90 degree of arranged crosswise staggered.
As shown in Figure 4, blender 4 is provided with smoke inlet m, outlet p after catalyst inlet n and flue gas and catalyst mix, electric stirring oar 4-1 is provided with in blender 4, flue gas enters blender by the smoke inlet m of blender after cooler 3 is lowered the temperature, catalyst granules has catalyst storage tower 6 to enter blender by the catalyst inlet n of blender, and electric stirring oar 4-1 mixes with flue gas for stirring catalyst, and gas-solid mixture is entered in shock bed by pipeline by exporting p.
As shown in Figure 5, sprayer 12 is provided with the micron order aperture 12-1 of atomized soln, and peroxide solutions enters sprayer by the entrance 12-3 of sprayer, and peroxide solutions is atomized by the micron order aperture 12-1 on sprayer.
Course of reaction is as follows: catalyst granules enters blender 4 from the outlet a of catalyst storage tower 6, flue gas introduces cooler 3 from the outlet b of emission source 1 by air-introduced machine 2, after cooler 3 is lowered the temperature, also enter blender 4, flue gas and catalyst granules are divided into two strands of impartial air-flows after mixing in blender 4.Half air-flow sprays into shock bed by being arranged on high speed nozzle 11 on one side through entrance c, and the high speed nozzle 11 that second half air-flow is then arranged by the coaxial subtend being arranged on another side sprays into shock bed through entrance d.Meanwhile, the peroxide solutions from liquid reserve tank 7 provides power by atomizing pump 8, is sprayed in shock bed 5 from entrance e by sprayer 12.Impingement mix is there is in three strands of air-flows in shock bed 5.
Ultraviolet light united catalyst decompose hydroperoxide produces hydroxyl or the potentiometric titrations oxidation SO of strong oxidizing property
2﹑ NO
xand Hg
0generate gaseous state Er Jia Gong ﹑ bis-Yangization Dan ﹑ tri-Yangization Liu ﹑ sulfuric acid and nitric acid, these gaseous products generated enter absorbing and removing in tower from shock bed outlet g through the entrance h of Wet Limestone Desulfurization system 14, and the clean flue gas through washing enters air from chimney 15.
SO in embodiment 1. 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 100 DEG C, and liquid-gas ratio is 0.5L/m
3, iron oxide dosage is 0.1kg/m
3, hydrogen peroxide concentration is 0.5mol/L, and pH value of solution is 3.4, and solution temperature is 70 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 88.2%, 62.5% and 71.2% respectively.
SO in embodiment 2. 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 100 DEG C, and liquid-gas ratio is 0.5L/m
3, iron oxide dosage is 0.1kg/m
3, ammonium persulfate concentrations is 0.5mol/L, and pH value of solution is 3.4, and solution temperature is 70 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 86.2%, 60.1% and 68.5% respectively.
SO in embodiment 3. 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 100 DEG C, and liquid-gas ratio is 0.5L/m
3, iron oxide dosage is 0.1kg/m
3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 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 95.8%, 73.6% and 83.7% respectively.
SO in embodiment 4. 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 100 DEG C, and liquid-gas ratio is 0.5L/m
3, iron oxide dosage is 0.1kg/m
3, ammonium persulfate concentrations is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 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 94.1%, 70.1% and 79.9% respectively.
SO in embodiment 5. 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 100 DEG C, and liquid-gas ratio is 1.5L/m
3, iron oxide dosage is 0.1kg/m
3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 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%, 91.6% and 93.5% respectively.
SO in embodiment 6. 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 100 DEG C, and liquid-gas ratio is 1.5L/m
3, iron oxide dosage is 0.1kg/m
3, ammonium persulfate concentrations is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 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%, 88.5% and 89.6% respectively.
SO in embodiment 7. 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 100 DEG C, and liquid-gas ratio is 1.5L/m
3, iron oxide dosage is 0.2kg/m
3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and ultraviolet light Net long wave radiation intensity is 65 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.
SO in embodiment 8. 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 100 DEG C, and liquid-gas ratio is 1.5L/m
3, iron oxide dosage is 0.2kg/m
3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and ultraviolet light Net long wave radiation intensity is 65 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 7 and 8 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 (4)
1. based on the simultaneous SO_2 and NO removal demercuration system of free radical pre-oxidation in conjunction with wet absorption, it is characterized in that: described system is provided with row and puts source ﹑ wind machine ﹑ and fall the mixed device ﹑ valve door ﹑ catalyst that closes of warm device ﹑ and store tower ﹑ and clash into bed ﹑ and spray mist pump ﹑ and store up liquid case ﹑ and follow ring pump ﹑ Wet Limestone Desulfurization system and chimney; Emission source connects cooler entrance by flue, cooler outlet connects the smoke inlet of blender, the outlet of catalyst storage tower connects the catalyst inlet of blender, and the outlet of blender is provided with two, and the high speed nozzle arranged with the coaxial subtend of clashing on bed is respectively connected; Described shock bed is provided with exhanst gas outlet, demister, deduster, at a high speed spray mouth ﹑ spray mist device ﹑ uviol lamp and quartzy sleeve pipe ﹑ catalyst outlet from top to bottom successively; Described high speed Pen Zui ﹑ Pen Wu Qi ﹑ uviol lamp and quartz socket tube multistage staggered alternate setting in shock bed; Described liquid reserve tank is connected with the sprayer clashing into bed by pipeline; The exhanst gas outlet of described shock bed is connected with the entrance of Wet Limestone Desulfurization tower, and the outlet of Wet Limestone Desulfurization tower connects chimney.
2. according to claim 1 a kind of based on the simultaneous SO_2 and NO removal demercuration system of free radical pre-oxidation in conjunction with wet absorption, it is characterized in that: the flue of described emission source and cooler is provided with the blower fan flue gas of emission source being introduced cooler; Described liquid reserve tank with clash into the pipeline that is connected of bed and be provided with as peroxide solutions provides the atomizing pump of power.
3. according to claim 1 a kind of based on the simultaneous SO_2 and NO removal demercuration system of free radical pre-oxidation in conjunction with wet absorption, it is characterized in that: clash into the high speed Pen Zui ﹑ sprayer in bed and ultraviolet lamp tube employing multi-stage cross layout; High speed Pen Zui ﹑ sprayer layout alternate with ultraviolet lamp tube, and adjacent high speed Pen Zui ﹑ sprayer and ultraviolet lamp tube adopt and arrange in the same way.
4. according to claim 1 a kind of based on the simultaneous SO_2 and NO removal demercuration system of free radical pre-oxidation in conjunction with wet absorption, it is characterized in that: the vertical interval H between high speed nozzle adjacent two layers is between 20cm-120cm, and adjacent two-stage high speed nozzle adopts 90 degree of arranged crosswise staggered; Ultraviolet lamp tube is arranged in the central spot between adjacent two-stage high speed nozzle, and the ultraviolet lamp tube of adjacent two-stage adopts 90 degree of arranged crosswise staggered; Sprayer is arranged in the central spot between adjacent two-stage high speed nozzle and ultraviolet lamp tube, and the sprayer of adjacent two-stage adopts 90 degree of arranged crosswise staggered.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520244728.9U CN204637986U (en) | 2015-04-21 | 2015-04-21 | Free radical pre-oxidation is in conjunction with the simultaneous SO_2 and NO removal demercuration system of wet absorption |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520244728.9U CN204637986U (en) | 2015-04-21 | 2015-04-21 | Free radical pre-oxidation is in conjunction with the simultaneous SO_2 and NO removal demercuration system of wet absorption |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204637986U true CN204637986U (en) | 2015-09-16 |
Family
ID=54090762
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520244728.9U Expired - Fee Related CN204637986U (en) | 2015-04-21 | 2015-04-21 | Free radical pre-oxidation is in conjunction with the simultaneous SO_2 and NO removal demercuration system of wet absorption |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204637986U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105727713A (en) * | 2016-03-21 | 2016-07-06 | 孙若浩 | Method of using desulfurizing and denitrifying agent to purify flue gas |
| CN105771583A (en) * | 2016-03-21 | 2016-07-20 | 孙若浩 | Denitrifying agent and method using same to purify flue gas |
| CN115739088A (en) * | 2022-11-16 | 2023-03-07 | 江苏大学 | Method and device for integrally removing gaseous multi-pollutants based on multi-element synergistic modified catalyst |
-
2015
- 2015-04-21 CN CN201520244728.9U patent/CN204637986U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105727713A (en) * | 2016-03-21 | 2016-07-06 | 孙若浩 | Method of using desulfurizing and denitrifying agent to purify flue gas |
| CN105771583A (en) * | 2016-03-21 | 2016-07-20 | 孙若浩 | Denitrifying agent and method using same to purify flue gas |
| CN115739088A (en) * | 2022-11-16 | 2023-03-07 | 江苏大学 | Method and device for integrally removing gaseous multi-pollutants based on multi-element synergistic modified catalyst |
| CN115739088B (en) * | 2022-11-16 | 2024-03-22 | 江苏大学 | Method and device for integrally removing gaseous multi-pollutants based on multielement synergistic modified catalyst |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104801178B (en) | Method for simultaneously desulfurizing, denitrifying and removing mercury by combining radical pre-oxidation with wet absorption | |
| CN102343212B (en) | Denitration process combining co-oxidation of ozone and hydrogen peroxide with wet absorption | |
| CN104923049B (en) | A kind of light radiation ozone/hydrogen peroxide solution simultaneous SO_2 and NO removal demercuration method | |
| CN103752151B (en) | A kind of magnesium sulfite flue-gas denitration process | |
| CN204973545U (en) | SOx/NOx control demercuration system simultaneously based on hydroxyl and sulfate radical oxidation | |
| CN104785076B (en) | Desulfurization denitration demercuration method while aoxidizing based on hydroxyl and potentiometric titrations | |
| CN104923072A (en) | Hydrogen sulfide removal method based on photocatalytic spraying | |
| CN103638796A (en) | System and method for desulfurizing, denitrifying and removing mercury based on photoactivation ammonium persulfate | |
| CN102772986B (en) | Flue gas desulfurization and denitration integrated process | |
| CN105771600A (en) | Method and device for integrally removing multiple pollutants in tail gas through plant ash seriflux | |
| CN104474859B (en) | A kind of method of flue gas desulfurization and denitrification, device and application thereof | |
| CN204637986U (en) | Free radical pre-oxidation is in conjunction with the simultaneous SO_2 and NO removal demercuration system of wet absorption | |
| CN104524935A (en) | Single-tower type double-circulation sprinkling composite absorption device and method | |
| CN203899431U (en) | Desulfurization, denitrification and demercuration system based on photoactivated ammonium persulfate | |
| CN102160959A (en) | Fume purification system based on advanced oxygenation combining wet scrubbing | |
| CN107715666B (en) | Method and system for removing hydrogen sulfide by microwave activation persulfate spray induction of free radicals | |
| CN103611400B (en) | A kind of vertical pneumatic revolution self-excitation waste gas purification apparatus | |
| Ma et al. | Jet absorption and desulfurization technology of sulfur waste gas in the acrylonitrile apparatus | |
| CN105311947A (en) | Boiler fume denitration and desulfuration dedusting device and process | |
| CN103357260A (en) | Flue gas desulfurization-denitration integrated process for strengthening urea by applying ferrous complexing agent | |
| CN104857852B (en) | VOCs removing method based on photocatalytic free radical advanced oxidation | |
| CN201807286U (en) | Photochemical advanced oxidation-based synchronous desulfuration and denitration system | |
| CN105536466A (en) | Device and method for removing various pollutants in flue gas through photoassisted catalytic oxidization | |
| CN112121616A (en) | Flue gas multi-pollutant purification device for coupling microwave ultraviolet light with hydrogen peroxide | |
| CN106853329B (en) | Method and device for generating hydroxyl free radical by ozone for low-temperature flue gas denitration |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150916 Termination date: 20160421 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |