CN202185259U - Integrated flue gas purification device based on heterogeneous Photo-Fenton - Google Patents
Integrated flue gas purification device based on heterogeneous Photo-Fenton Download PDFInfo
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- CN202185259U CN202185259U CN2011200480250U CN201120048025U CN202185259U CN 202185259 U CN202185259 U CN 202185259U CN 2011200480250 U CN2011200480250 U CN 2011200480250U CN 201120048025 U CN201120048025 U CN 201120048025U CN 202185259 U CN202185259 U CN 202185259U
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- 239000003546 flue gas Substances 0.000 title claims abstract description 47
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 238000000746 purification Methods 0.000 title description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000012028 Fenton's reagent Substances 0.000 claims abstract description 7
- 238000001816 cooling Methods 0.000 claims abstract description 3
- 239000007788 liquid Substances 0.000 claims description 19
- 230000005855 radiation Effects 0.000 claims description 12
- 239000003517 fume Substances 0.000 claims description 7
- 238000002485 combustion reaction Methods 0.000 claims description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 3
- 239000011800 void material Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- 230000008676 import Effects 0.000 claims description 2
- 239000011949 solid catalyst Substances 0.000 abstract description 19
- 239000000243 solution Substances 0.000 abstract description 16
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 abstract description 10
- 238000006243 chemical reaction Methods 0.000 abstract description 10
- 230000005587 bubbling Effects 0.000 abstract description 8
- 239000011259 mixed solution Substances 0.000 abstract description 8
- 239000007789 gas Substances 0.000 abstract description 6
- 238000007254 oxidation reaction Methods 0.000 abstract description 6
- 230000008929 regeneration Effects 0.000 abstract description 5
- 238000011069 regeneration method Methods 0.000 abstract description 5
- 230000010354 integration Effects 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 4
- 238000004064 recycling Methods 0.000 abstract description 4
- 238000000926 separation method Methods 0.000 abstract description 4
- 229910017604 nitric acid Inorganic materials 0.000 abstract description 3
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 abstract description 2
- 238000001556 precipitation Methods 0.000 abstract 2
- 238000004140 cleaning Methods 0.000 abstract 1
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- 238000005086 pumping Methods 0.000 abstract 1
- 229910052753 mercury Inorganic materials 0.000 description 16
- -1 hydroxyl radical free radical Chemical class 0.000 description 14
- 238000006477 desulfuration reaction Methods 0.000 description 13
- 239000002245 particle Substances 0.000 description 13
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 12
- 238000000034 method Methods 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 11
- 239000003344 environmental pollutant Substances 0.000 description 11
- 230000023556 desulfurization Effects 0.000 description 10
- 231100000719 pollutant Toxicity 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 239000002244 precipitate Substances 0.000 description 8
- 238000010521 absorption reaction Methods 0.000 description 7
- 230000007613 environmental effect Effects 0.000 description 7
- 239000007791 liquid phase Substances 0.000 description 7
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 7
- 230000003647 oxidation Effects 0.000 description 5
- 239000010453 quartz Substances 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 238000009303 advanced oxidation process reaction Methods 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 3
- 230000003213 activating effect Effects 0.000 description 2
- 239000000356 contaminant Substances 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000005284 excitation Effects 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000012805 post-processing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 208000031320 Teratogenesis Diseases 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 230000019771 cognition Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- WKPSFPXMYGFAQW-UHFFFAOYSA-N iron;hydrate Chemical compound O.[Fe] WKPSFPXMYGFAQW-UHFFFAOYSA-N 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000000877 morphologic effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000006862 quantum yield reaction Methods 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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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
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- Treating Waste Gases (AREA)
Abstract
The utility model provides an integration gas cleaning device based on heterogeneous Photo-Fenton, the flue gas that the combustor burning produced after the heat exchanger cooling, lets in the bubbling tower from bubbling tower bottom nozzle, also lets in the bubbling tower by the upper portion of bubbling tower after adding the liquid-adding tower with heterogeneous Fenton reagent of hydrogen peroxide solution and solid catalyst, is equipped with the ultraviolet fluorescent tube in the bubbling tower, and the ultraviolet light arouses decomposes heterogeneous Fenton reagent, with the SO in the flue gas2、NOxAnd Hg0Oxidation to H2SO4、HNO3And Hg2+And fixing the solid catalyst in the mixed solution after reaction in the solution, and realizing cyclic regeneration and utilization of the solid catalyst in the mixed solution after primary precipitation and separation, wherein Hg in the solution2+By adding S in an equimolar ratio2-And generating insoluble HgS, then recovering after secondary precipitation separation, recycling the residual sulfuric acid and nitric acid solution as industrial raw materials, and pumping the washed flue gas into a chimney through a draught fan from the top of the bubble column for discharge.
Description
Technical field
The utility model relates to the control of smoke emissioning pollution thing in the combustion process, relates in particular to a kind of integrated fume purifier based on heterogeneous Photo-Fenton.
Background technology
The oxysulfide that produces in the combustion process, nitrogen oxide and mercury can cause acid rain, photochemical fog and serious harms such as carcinogenic and teratogenesis.Therefore, researching and developing effective flue gas desulfurization and denitrification demercuration method is one of vital task of various countries' environmental protection scientific and technical personnel.In the last few years; Although people have developed a large amount of flue gas desulfurization and denitrification demercuration technology; But because human cognitive process's limitation and scientific technological advance is gradual; Existing various desulfurization denitration demercuration technology only was directed against single pollutant for removing target originally in research and development, removed when generally can't realize flue gas multiple pollutant.For example, use more flue gas desulfurization and denitrification technology at present and be mainly wet method limestone-gypsum method flue gas desulfurization technology (Ca-WFGD) and ammine selectivity catalytic reduction method (NH
3-SCR),, all can't in a reactor, realize removing simultaneously though these two kinds of technologies can be distinguished independent desulphurization denitration.Though the stack of uniting of two kinds of technologies is used and can be realized desulphurization denitration simultaneously, also causes whole system complicated simultaneously, floor space is big, investment and the high deficiency of operating cost.In addition, along with the mankind to the improving constantly of environmental requirement, also put into effect gradually to the laws and regulations of mercury emissions control in the flue gas, use but also there is a kind of cost-effective flue gas demercuration technology to obtain large-scale commercial applications at present.If at existing C a-WFGD and NH
3-SCR system for desulfuration and denitration afterbody increases independent flue gas demercuration system once more, then certainly will will cause the initial outlay of whole system and operating cost further sharply to increase, and finally is difficult in developing country's acquisition large-scale commercial applications and uses.
In sum, if can in a reactor, oxysulfide, nitrogen oxide and mercury realized removing simultaneously, then can reduce the complexity and the floor space of system greatly, and then reduce the initial cost and the operating cost of system.The wet type flue gas desulphurization technology is a kind of traditional flue gas treatment technology; Have that initial cost is little, technological process is simple and is easy to realize characteristics such as multi-pollutant removes simultaneously; It is the flue gases purification that a kind of extremely has the development and application prospect; But the progress of traditional wet flue gases purification is slow relatively always, and its main cause just is to contain respectively in nitrogen oxide and the mercury element NO of 90% above indissoluble and the Hg of 40-80% indissoluble
0Can know that by double-film theory gas molecule in space must at first dissolve in liquid phase by gaseous state through mass transfer and diffusion process, chemical reaction could take place then be fixed in the absorption liquid, and NO and Hg
0The characteristic of indissoluble makes its absorption resistance to mass tranfer in liquid phase increase greatly, only is difficult to significantly improve NO and Hg through regulation and control absorption liquid pH and method of temperature
0In the solubility of liquid phase, this characteristic has caused traditional wet desulfurization denitration demercuration technology ubiquity desulfuration efficiency high, but deficiency such as denitration and demercuration efficient is low, in fact can't realize desulfurization denitration demercuration real the time.Therefore, searching can be with NO and Hg
0Being converted into easy molten effective morphological fast is one of key that addresses this problem.
Summary of the invention
The utility model discloses a kind of integrated fume purifier based on heterogeneous Photo-Fenton; Promptly utilize heterogeneous Photo-Fenton (ultraviolet light, hydrogen peroxide solution, solid catalyst advanced oxidation processes) to produce hydroxyl radical free radical (OH), with the SO in the flue gas with strong oxidizing property
2, NO
xAnd Hg
0Be oxidized to H respectively
2SO
4, HNO
3And Hg
2+Be fixed in the solution, the solid catalyst in the solution of reaction back can be through realizing recycling after the simple precipitate and separate, the Hg in the solution
2+Can be through the sulfidion S of mol ratios such as interpolation
2-Generate the HgS of indissoluble; Recycle through realizing after the precipitate and separate then; Further recycle and remaining sulfuric acid and salpeter solution can be used as the raw material of industry, whole integration desulfurization denitration demercuration process non-secondary pollution is the flue gases purification that a kind of extremely has application prospect.
For realizing above purpose, the embodiment that the utility model adopts is: a kind of integrated fume purifier based on heterogeneous Photo-Fenton is characterized in that: the burning and the exhaust system that be provided with burner, heat exchanger, bubble tower, add the liquid tower, two-stage knockout tower, regenerator, air-introduced machine and chimney constitute; After the flue gas that burner combustion produces feeds the heat exchanger cooling through pipeline; The nozzle that is provided with from bubble tower bottom through pipeline feeds bubble tower, adds the liquid top of tower and is provided with heterogeneous Fenton reagent and adds inlet, adds liquid tower top outlet is set; Feed bubble tower through pipeline from the top of bubble tower by first circulating pump; Be provided with ultraviolet lamp tube in the bubble tower, the bubble tower bottom is provided with first outlet, adds the liquid tower through pipeline by the second circulating pump suction; The bubble tower bottom is provided with second outlet; By the 3rd circulating pump suction one-level knockout tower, one-level knockout tower top is provided with first outlet, sends into the regenerator bottom inlet through pipeline by the 4th circulating pump through pipeline; The regenerator top sets out mouth, is fed by the 5th circulating pump through pipeline and adds the liquid tower; One-level knockout tower bottom is provided with outlet, and by the 6th circulating pump suction secondary knockout tower, secondary knockout tower top is provided with sulfidion S through pipeline
2-Add import, the secondary knockout tower also is respectively equipped with mercuric sulphide and high-concentration sulfuric acid and salpeter solution discharging and reclaims mouth, and the bubble tower top is communicated with chimney through pipeline and air-introduced machine.
Ultraviolet lamp tube is vertical with the bubble tower bottom surface, and unit volume ultraviolet radiation power is 5W/m in the bubble tower
3-200W/m
3, the W/m of unit
3Be meant bubble tower before uviol lamp is not installed, the needed ultraviolet radiation power of unit volume when bubble tower is void tower, ultraviolet wavelength is 120nm-360nm.When many ultraviolet lamp tubes were set, many ultraviolet lamp tubes were the concentric circles setting, and distance is identical between the neighboring concentric circle; Many ultraviolet lamp tubes are distributed on the circumference of different-diameter; Along same diameter line setting, the central angle between each adjacent two diameter line is identical, and circle centre position is provided with ultraviolet lamp tube; Nozzle is arranged on the concentric circumference with ultraviolet lamp tube concentric circles alternate intervals and is uniformly distributed with, and places on the diameter line of two ultraviolet lamp tube central angle half-angles.
This device reaction process:
1, heterogeneous Photo-Fenton advanced oxidation processes discharges the hydroxyl radical free radical (OH) with strong oxidizing property:
Fe
2+-S+H
2O
2-S→Fe
3+-S+·OH-S+OH
--S (1)
Fe
3+-S+H
2O
2-S→Fe
3+(HO
2)
2+-S+H
+-S (2)
FeOH
2+-S+H
2O
2-S→Fe
3+(OH)(HO
2)
+-S+H
+-S (3)
Fe
3+(HO
2)
2+-S+hv-S→Fe
2+-S+·HO
2-S (4)
Fe
3+(OH)(HO
2)
+-S+hv-S→Fe
2+-S+·HO
2-S+OH
--S?(5)
2, the SO in the burner discharged flue gas
2, NO
xAnd Hg
0Generated H by hydroxyl radical free radical (OH) oxidation
2SO
4, HNO
3And Hg
2+Mixed solution:
NO-S+·OH-S→HNO
2-S (6)
NO
2-S+·OH-S→HNO
3-S (7)
SO
2-S+·OH-S→HSO
3-S (8)
HSO
3-S+·OH-S→H
2SO
4-S (9)
Hg
0-S+·OH-S→HgO-S+·H-S (10)
Hg
0-S+·OH-S→Hg(OH)
2-S (11)
3, solid catalyst can be sent into regenerator activating and regenerating, cycling and reutilization then after precipitate and separate in the one-level knockout tower;
4, the Hg of reaction generation
2+The S that can be added
2+Absorb and react the HgS sediment that generates indissoluble, recycle through after the precipitate and separate then:
Hg
2++S
2-→HgS?↓ (12)
5, after the heavy metal Hg element is hunted down recovery, the sulfuric acid and the nitric acid mixed solution that only are left high concentration in the solution can be used as raw material of industry recycling, whole integration desulfurization denitration demercuration process non-secondary pollution.
Advantage of the utility model and remarkable result: heterogeneous Photo-Fenton advanced oxidation processes can discharge the hydroxyl radical free radical (OH) with extremely strong oxidability, and the reaction rate constant of OH and most organic is up to 10
6-10
10Mol/Ls can attack all contaminations easily and it is degraded to harmless product, and the solid catalyst in the course of reaction is easy to separate and regeneration cycle is used, and is that a kind of oxidability is strong, the advanced oxidation removing process of clean environmental protection and non-selectivity.With the applicant (a kind of system for desulfuration and denitration based on the photochemistry advanced oxidation time: 201012096592.5) with (a kind of flue gas demercuration system: 201012096592.8) compare, the utlity model has following remarkable advantages based on the effect of photochemistry advanced oxidation:
(1) Along with people's improving constantly to environmental requirement; Laws and regulations to mercury emissions control in the flue gas are also put into effect gradually; The present invention can realize removing in three kinds of pollutants such as oxysulfide, nitrogen oxide and heavy metal element mercury in a reactor, thereby can further reduce the initial outlay and the operating cost of system.Along with the mankind to the improving constantly of environmental requirement, this advantage of the utility model will be highlighted gradually, and 201012096592.5 and 201012096592.8 all can't realize removing in three kinds of pollutants in same reactor.
(2) the utility model can be through adding the removal efficiency that callable high-performance solid catalyst further improves pollutant, and the same terms can also reduce the dosage of hydrogen peroxide solution down significantly, and then can reduce the use cost of hydrogen peroxide solution significantly.In addition, solid catalyst can be realized the regeneration cycle use in the utility model after the simple precipitate and separate of process, whole subtractive process non-secondary pollution, thereby be the novel flue gases purification that a kind of extremely has application prospect.
Description of drawings
Fig. 1 is the utility model device flow chart;
Fig. 2 is the fitting arrangement of the utility model bubbling bed inner nozzle and ultraviolet lamp tube.
The specific embodiment
Referring to Fig. 1,2, from containing finite concentration SO in the burner (boiler) 1
2, NO
xAnd Hg
0Flue gas at first be cooled to suitable temperature through heat exchanger, feed the liquid phase reactor districts from the nozzle 3 of bubbling bed 4 bottoms then and participate in the Gas-Liquid Absorption reaction; Heterogeneous Fenton reagent at first adds and adds liquid tower 12, is added from the top of bubble tower 4 by first circulating pump 7 then to the liquid phase reactor districts participate in the Gas-Liquid Absorption reaction in the bubbling bed 4; The uviol lamp 6 that is with quartz socket tube 5 excites and decomposes the hydroxyl radical free radical OH that heterogeneous Fenton reagent release has strong oxidizing property, and rapidly with the SO in the flue gas
2, NO
xAnd Hg
0Be oxidized to H respectively
2SO
4, HNO
3And Hg
2+Solution; For sulfuric acid and the salpeter solution of producing high concentration; Reduce the processing cost of liquid product; The partially mixed solution that reaction generates needs by 12 recycles of second circulating pump 8 suction the adding liquid tower; Remaining mixed solution is then by the 3rd circulating pump 9 suction one-level knockout towers 10; Solid catalyst is realized regeneration activatings through sending into regenerator 14 by the 4th circulating pump 11 after the simple precipitate and separate in one-level knockout tower 10, the solid catalyst after the regeneration is fed once more by the 5th circulating pump 13 and adds liquid tower 12 and recycle; Through the Hg that contains after the one-level separation
2+Solution passes through the sulfidion S of mol ratios such as interpolation then then by the 6th circulating pump 15 suction secondary knockout towers 16
2-Reaction generates the HgS of indissoluble, and through realizing the recycling of mercury element mercuric sulphide after the precipitate and separate, last remaining high-concentration sulfuric acid and salpeter solution then can be used as the raw material of industry and recycle; Enter atmosphere from bubble tower 4 tops after by air-introduced machine 17 suction chimneys 18 through the flue gas after the washing.
In the said apparatus:
Because flue-gas temperature is higher, if high-temperature flue gas directly feeds bubble tower liquid phase reactor district, then the solubility of vapor phase contaminants will descend, and causes the removal efficiency of target contaminant to descend.In addition, high temperature also can cause hydrogen peroxide solution directly to be decomposed into oxygen, and utilization rate descends.Therefore, before flue gas fed bubble tower, high-temperature flue gas need effectively cool off through heat exchanger, so the bubble tower entrance flue gas temperature generally should be controlled between 15-75 ℃.
Owing to contain fine particle in the flue gas, if uviol lamp is directly exposed in the flue gas, then uviol lamp is easy to wash away because of the high speed of particle and damages.Therefore, uviol lamp need put the quartz socket tube of being processed by the quartz material of high-penetration light rate at outer surface, the internal diameter of quartz socket tube need be than the external diameter of uviol lamp big 2-4mm, length keeps equating with uviol lamp or is close.In order to maximally utilise luminous energy, improve ultraviolet radiation intensity, the uviol lamp in the reactor must keep vertical with the bubble tower bottom surface when mounted.In addition, even in order to keep in the reactor ultraviolet radiation, increase the luminous energy effective rate of utilization, it is equal that the spacing b between the uviol lamp must keep, and central angle a also must keep equating.Simultaneously; If the layout density of uviol lamp in reactor is too big; Then the flow resistance of flue gas will increase in the reactor, causes the operating load of system and energy consumption to increase, if but the interior uviol lamp of reactor arranges that density is too little; Then be difficult to the light radiation intensity that reaches enough, thereby cause the pollutant removing index not reach environmental requirement.Therefore, the optimum range of uviol lamp spacing b and central angle a generally is respectively 2cm-30cm and 10-40 degree.The uv light irradiation strength relationship is to the size of quantum yield or the productive rate of hydroxyl radical free radical OH.Be difficult to fully excite ozone to decompose the hydroxyl radical free radical OH oxidation removal pollutant that produces sufficient amount if ultraviolet light irradiation intensity is too little, but if ultraviolet light irradiation intensity is too big, then the energy consumption of system will significantly increase.Therefore, ultraviolet ray intensity need remain on 5W/m
3-200W/m
3, the W/m of unit wherein
3Be meant reactor before uviol lamp is not installed, the needed ultraviolet radiation power of unit volume when reactor is void tower.When ultraviolet wavelength more in short-term, the photon excitation of ultraviolet light can increase relatively, but this moment ultraviolet light propagation distance shorter, the Pollutant Treatment ability that shows as the unit power ultraviolet light is lower.When ultraviolet wavelength is longer; Although the propagation distance of ultraviolet light can increase; But this moment, the excitation energy of ultraviolet light photons significantly reduced; Cause ultraviolet light photons to excite and decompose the energy shortage that heterogeneous Fenton reagent discharges hydroxyl radical free radical OH, finally cause the removal efficiency of pollutant to be difficult to satisfy environmental requirement.Therefore, the EWL of ultraviolet light should remain in the 160nm-360nm scope.
The effective mass concentration that solid catalyst adds should remain in the 0.5g/L-5.0g/L scope, and effective molar concentration that hydrogen peroxide solution adds should remain on 0.1mol/L-2.5mol/L.If dosage is too high, then will cause application cost to rise, otherwise then the removal efficiency of pollutant is difficult to reach requirement.In addition, the particle diameter of the solid catalyst that adds also has strict requirement, if the particle diameter that adds is too big, then the specific area of catalyst can descend, if bring very big difficulty can for the one-level precipitate and separate but the solid catalyst particle diameter is too little, increases the post processing cost.Therefore, the particle diameter of solid catalyst generally should remain between 80 orders-200 order.
The sulfidion S that adds in the Gas-Liquid Absorption tower
2-Amount need strict control criterion, if excessive interpolation S
2-Will cause secondary pollution and application cost to increase, but S
2-Addition is too little then can to cause the MODEL OF CHEMICAL ABSORPTION PROCESS in the secondary knockout tower abundant inadequately, Hg
2+Capture rate low.Therefore, in the practical application, add S
2-Mole should with Hg solution
2+Mole keep to equate, promptly need keep n (S
2-): n (Hg
2+)=1: 1.
Owing to need pass through after-treatment during liquid-phase mixing product Separation and Recovery.Therefore, if mixed solution concentration is too rare, then the after-treatment expense certainly will will be increased.Therefore, the whole system that removes need be provided with solution part recirculating system, and promptly the mixed solution that produces of reaction back generally needs 20-40% and added the recycle of liquid tower by suction again, so that increase solution concentration, and then reduces the post processing cost of product.
SO in embodiment 1. flue gases
2, NO and Hg
0Concentration is respectively 2000ppm, 500ppm and 100ug/m
3, solid catalyst is Fe
2O
3Particle (mass concentration is 1.0g/L, and particle diameter is 100 orders), flue-gas temperature is 25 ℃, and ultraviolet wavelength is 254nm, and the UV radiation intensity is 100W/m
3, the hydrogen peroxide solution molar concentration is 1.0mol/L, liquid-gas ratio is 20L/m
3, the effect time of staying is 10s, uviol lamp spacing b and central angle a are respectively 10cm and 25 when spending, SO in the flue gas
2, NO and Hg
0Integrated removal efficiency can reach 92.1%, 80.9% and 98.8% respectively.
SO in embodiment 2. flue gases
2, NO and Hg
0Concentration is respectively 2000ppm, 500ppm and 100ug/m
3, solid catalyst is Fe
2O
3Particle (mass concentration is 1.0g/L, and particle diameter is 100 orders), flue-gas temperature is 25 ℃, and ultraviolet wavelength is 254nm, and the UV radiation intensity is 150W/m
3, the hydrogen peroxide solution molar concentration is 1.0mol/L, liquid-gas ratio is 20L/m
3, the effect time of staying is 10s, uviol lamp spacing b and central angle a are respectively 10cm and 25 when spending, SO in the flue gas
2, NO and Hg
0Integrated removal efficiency can reach 100%, 92.2% and 100% respectively.
SO in embodiment 3. flue gases
2, NO and Hg
0Concentration is respectively 2000ppm, 500ppm and 100ug/m
3, solid catalyst is Fe
2O
3Particle (mass concentration is 1.0g/L, and particle diameter is 100 orders), flue-gas temperature is 25 ℃, and ultraviolet wavelength is 254nm, and the UV radiation intensity is 100W/m
3, the hydrogen peroxide solution molar concentration is 1.0mol/L, liquid-gas ratio is 20L/m
3, the effect time of staying is 10s, uviol lamp spacing b and central angle a are respectively 10cm and 25 when spending, SO in the flue gas
2, NO and Hg
0Integrated removal efficiency can reach 89.2%, 83.2% and 100% respectively.
SO in embodiment 4. flue gases
2, NO and Hg
0Concentration is respectively 2000ppm, 500ppm and 100ug/m
3, solid catalyst is Fe
2O
3Particle (mass concentration is 1.0g/L, and particle diameter is 100 orders), flue-gas temperature is 25 ℃, and ultraviolet wavelength is 254nm, and the UV radiation intensity is 50W/m
3, the hydrogen peroxide solution molar concentration is 1.0mol/L, liquid-gas ratio is 15L/m
3, the effect time of staying is 10s, uviol lamp spacing b and central angle a are respectively 10cm and 25 when spending, SO in the flue gas
2, NO and Hg
0Integrated removal efficiency can reach 85.8%, 70.8% and 93.7% respectively.
In sum, embodiment 2 has best integration desulfurization denitration demercuration effect, can be used as most preferred embodiment and consults and uses.
Claims (3)
1. integrated fume purifier based on heterogeneous Photo-Fenton is characterized in that: the burning and the exhaust system that be provided with burner, heat exchanger, bubble tower, add the liquid tower, two-stage knockout tower, regenerator, air-introduced machine and chimney constitute, after the flue gas that burner combustion produces feeds the heat exchanger cooling through pipeline; The nozzle that is provided with from bubble tower bottom through pipeline feeds bubble tower, adds the liquid top of tower and is provided with heterogeneous Fenton reagent and adds inlet, adds liquid tower top outlet is set; Feed bubble tower through pipeline from the top of bubble tower by first circulating pump; Be provided with ultraviolet lamp tube in the bubble tower, the bubble tower bottom is provided with first outlet, adds the liquid tower through pipeline by the second circulating pump suction; The bubble tower bottom is provided with second outlet; By the 3rd circulating pump suction one-level knockout tower, one-level knockout tower top is provided with first outlet, sends into the regenerator bottom inlet through pipeline by the 4th circulating pump through pipeline; The regenerator top sets out mouth, is fed by the 5th circulating pump through pipeline and adds the liquid tower; One-level knockout tower bottom is provided with outlet, and by the 6th circulating pump suction secondary knockout tower, secondary knockout tower top is provided with sulfidion S through pipeline
2-Add import, the secondary knockout tower also is respectively equipped with mercuric sulphide and high-concentration sulfuric acid and salpeter solution discharging and reclaims mouth, and the bubble tower top is communicated with chimney through pipeline and air-introduced machine.
2. the integrated fume purifier based on heterogeneous Photo-Fenton according to claim 1, it is characterized in that: ultraviolet lamp tube is vertical with the bubble tower bottom surface, and unit volume ultraviolet radiation power is 5W/m in the bubble tower
3-200W/m
3, the W/m of unit
3Be meant bubble tower before uviol lamp is not installed, the needed ultraviolet radiation power of unit volume when bubble tower is void tower, ultraviolet wavelength is 120nm-360nm.
3. the integrated fume purifier based on heterogeneous Photo-Fenton according to claim 2; It is characterized in that: when many ultraviolet lamp tubes were set, many ultraviolet lamp tubes were the concentric circles setting, and distance is identical between the neighboring concentric circle; Many ultraviolet lamp tubes are distributed on the circumference of different-diameter; Along same diameter line setting, the central angle between each adjacent two diameter line is identical, and circle centre position is provided with ultraviolet lamp tube; Nozzle is arranged on the concentric circumference with ultraviolet lamp tube concentric circles alternate intervals and is uniformly distributed with, and places on the diameter line of two ultraviolet lamp tube central angle half-angles.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011200480250U CN202185259U (en) | 2011-02-25 | 2011-02-25 | Integrated flue gas purification device based on heterogeneous Photo-Fenton |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011200480250U CN202185259U (en) | 2011-02-25 | 2011-02-25 | Integrated flue gas purification device based on heterogeneous Photo-Fenton |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103691280A (en) * | 2013-12-13 | 2014-04-02 | 江苏大学 | Method and system for removing flue gas mercury based on ultrasonic excitation of sodium persulfate |
| CN104740989A (en) * | 2015-04-13 | 2015-07-01 | 华东理工大学 | Method and device for vortex-Fenton demercuration of flue gas |
| WO2015161671A1 (en) * | 2014-04-23 | 2015-10-29 | 林小晓 | Polluted air purification system and working method therefor |
-
2011
- 2011-02-25 CN CN2011200480250U patent/CN202185259U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103691280A (en) * | 2013-12-13 | 2014-04-02 | 江苏大学 | Method and system for removing flue gas mercury based on ultrasonic excitation of sodium persulfate |
| CN103691280B (en) * | 2013-12-13 | 2016-03-02 | 江苏大学 | A kind of method and system removing gas mercury based on ultrasonic excitation sodium peroxydisulfate |
| WO2015161671A1 (en) * | 2014-04-23 | 2015-10-29 | 林小晓 | Polluted air purification system and working method therefor |
| CN104740989A (en) * | 2015-04-13 | 2015-07-01 | 华东理工大学 | Method and device for vortex-Fenton demercuration of flue gas |
| CN104740989B (en) * | 2015-04-13 | 2017-05-10 | 华东理工大学 | Method and device for vortex-Fenton demercuration of flue gas |
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