CN105727724B - A kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization - Google Patents

A kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization Download PDF

Info

Publication number
CN105727724B
CN105727724B CN201610239826.2A CN201610239826A CN105727724B CN 105727724 B CN105727724 B CN 105727724B CN 201610239826 A CN201610239826 A CN 201610239826A CN 105727724 B CN105727724 B CN 105727724B
Authority
CN
China
Prior art keywords
reactor
light radiation
hypochlorous acid
solution
flue gas
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.)
Active
Application number
CN201610239826.2A
Other languages
Chinese (zh)
Other versions
CN105727724A (en
Inventor
刘杨先
张军
潘剑锋
张永春
谢芳
郝建刚
刘勇
阮小娇
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Jiangsu University
Original Assignee
Jiangsu University
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Jiangsu University filed Critical Jiangsu University
Priority to CN201610239826.2A priority Critical patent/CN105727724B/en
Publication of CN105727724A publication Critical patent/CN105727724A/en
Application granted granted Critical
Publication of CN105727724B publication Critical patent/CN105727724B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/79—Injecting reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/007—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by irradiation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/64—Heavy metals or compounds thereof, e.g. mercury
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/10—Oxidants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/10—Oxidants
    • B01D2251/108—Halogens or halogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/60—Heavy metals or heavy metal compounds
    • B01D2257/602—Mercury or mercury compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/12—Methods and means for introducing reactants
    • B01D2259/124—Liquid reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/80—Employing electric, magnetic, electromagnetic or wave energy, or particle radiation
    • B01D2259/804—UV light
    • 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

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Biomedical Technology (AREA)
  • Toxicology (AREA)
  • Treating Waste Gases (AREA)

Abstract

The invention provides a kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization, described method is in light radiation injection reactor, first fixes CO as absorbent using sodium hypochlorite2, hypochlorous acid caused by reaction produces the SO that chlorine atom and hydroxyl can further in oxidation removal flue gas under ultraviolet radiation2﹑ NOx﹑ Hg0.The system has extremely strong oxidisability, can realize multi-pollutant zero-emission, and subtractive process non-secondary pollution, has wide market application foreground.

Description

A kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization
Technical field
The present invention relates to flue gas pollutant control field, and in particular to a kind of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal The method and device of demercuration decarburization.
Background technology
CO caused by burning2﹑ SO2﹑ NOxAnd Hg0Wen rooms Xiao Ying ﹑ Suan Yu ﹑ photochemical fogs and carcinogenic grade can be caused tight Endanger again.Therefore, it is one of vital task of various countries' environmental protection personnel to research and develop effective flue gas desulfurization and denitrification demercuration decarbonization method.To the greatest extent Pipe is developed substantial amounts of flue gas desulfurization and denitrification demercuration decarburization technique, but limitation and science skill due to human cognitive process Art develops gradual, and existing various desulfurization denitration demercuration decarburization techniques are originally removing only for Single Pollution thing in research and development Target, it can not typically realize and be removed while flue gas multiple pollutant.For example, more flue gas desulfurization and denitrification technology master is applied at present To be wet method limestone-gypsum method flue gas desulfurization technology and ammine selectivity catalytic reduction method.Although both approaches can be distinguished Independent desulphurization denitration, but can not realize in a reactor and remove simultaneously.Can although the joint superposition of two kinds of techniques uses To realize simultaneous SO_2 and NO removal, but whole system complexity is also resulted in simultaneously, floor space is big, and investment and operating cost height wait not Foot.In addition, with continuous improvement of the mankind to environmental requirement, for Hg in flue gas0And CO2The laws and regulations of emission control also by Gradually put into effect, but there is presently no a kind of cost-effective flue gas Hg0And CO2Removing sulfuldioxide obtains large-scale commercial applications application.If Existing desulfurization and denitrating system afterbody increase single flue gas Hg again0And CO2Removing system, then will certainly will cause be entirely The initial outlay of system and operating cost further sharply increase, and final is difficult to obtain large-scale commercial applications application in developing country.
In summary, if it is possible to by CO in a reactor2﹑ SO2﹑ NOxAnd Hg0Realization removes simultaneously, then is expected to big The big complexity and floor space for reducing system, and then reduce investment and the operating cost of system.Wet type flue gas desulphurization technology is A kind of traditional fume treatment technology, have initial cost little ﹑ technological processes simply and be easily achieved multi-pollutant while removing etc. Feature, be a kind of flue gases purification with good development and application prospect, but traditional wet type flue gas desulphurization technology is ground It is but relatively slow always to study carefully progress, its main cause is that in flue gas nitrogen oxide and mercury element difficult containing more than 90% respectively The Hg of molten NO and 40-80% indissolubles0.From double-film theory, gas molecule in space through mass transfer and must be diffused through by gaseous state first Journey dissolves in liquid phase, and chemical reaction then could occur and be fixed in absorbing liquid, and NO and Hg0The characteristic of indissoluble causes it in liquid phase Absorption resistance to mass tranfer greatly increase, only be difficult to significantly improve NO and Hg by regulating and controlling the method for absorption liquid pH and temperature0In liquid The solubility of phase, this characteristic cause traditional wet desulphurization denitration demercuration technology generally existing desulfuration efficiency height, but denitration The deficiency such as low with demercuration efficiency, it can not actually realize real simultaneous SO_2 and NO removal demercuration.Therefore, searching can by NO with Hg0The effective ways for being rapidly converted into readily soluble form are the keys for solving the problem, and realize that multi-pollutant is simultaneously in flue gas The important thinking of removing.In addition, although it have now been developed many kinds of CO2Capture technique, such as absorption Tuo Chu ﹑ burning chemistry chains skills Shu ﹑ oxygen-enriched combusting Ji Shu ﹑ ammonia absorption techniqueses, but both for single CO2Captured, do not consider to take off while multiple pollutant Remove.Therefore, the application, which takes the lead in proposing one kind, can be directed to CO2﹑ SO2﹑ NOxAnd Hg0Four kinds of pollutants carry out the new of removing simultaneously Method and new equipment, there is vast potential for future development.
The content of the invention
For Shortcomings in the prior art, the invention provides a kind of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal to take off The method and device of mercury decarburization.
The present invention is to realize above-mentioned technical purpose by following technological means.
A kind of device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization, it is characterised in that：Provided with a light Injection reactor is radiated, is provided with the uviol lamp on central axis inside light radiation injection reactor, outside the uviol lamp Provided with quartz plate, there is gap as air-cooling apparatus, the bottom of the air-cooling apparatus between quartz plate and uviol lamp Air outlet slit is provided with provided with air intake, top；The sidewall of reactor is provided with multiple vortex atomizing nozzles, and multiple flue gases enter Mouthful connected respectively with multiple vortex atomizing nozzles, exhanst gas outlet is set on the top surface of the reactor, the bottom for sending out reactor described Solution inlet port, taphole and product exit are additionally provided with face, the taphole connects with multiple vortex atomizing nozzles；It is molten Liquid exports is provided with circulating pump between multiple vortex atomizing nozzles.
Preferably, the smoke outlet is additionally provided with chlorine recovery device, and the chlorine recovery device also enters with flue gas Mouth is connected.
Preferably, the optimal lateral of vortex atomizing nozzle and longitudinal pitch A are respectively positioned between 10cm-45cm, uviol lamp with Horizontal spacing B between quartz plate between 1cm-4cm, the height C of light radiation injection reactor between 0.5m-8m, The width D of the reative cell of reactor is located at 0.1m-1.5m, and the horizontal spacing E of uviol lamp is between 0.1m-0.8m, light radiation For the length F of injection reactor between 0.1m-6m, the solution droplets diameter that vortex atomizing nozzle projects is not more than 80 microns, The exit velocity for the solution that vortex atomizing nozzle projects is not less than 1.5m/s.
Preferably, gas cooler is additionally provided with smoke inlet.
Preferably, the quantity of the reactor is multiple in parallel between multiple reactors and/or series connection.
A kind of method of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization, it is characterised in that including following step Suddenly：
(1) hypochlorous acid acid sodium solution is injected into light radiation injection reactor by solution inlet, makes the bottom of reactor Liquor natrii hypochloritis is filled, starts circulating pump, liquor natrii hypochloritis is ejected into described anti-by taphole, vortex atomizing nozzle Conversion zone more than liquid level in device is answered, and forms sodium hypochlorite atomized drop；
(2) sodium hypochlorite that flue gas enters in light radiation injection reactor from smoke inlet and come out with vortex atomizing nozzle The quartz plate on directive opposite after droplets mixing；During drop directive quartz plate, sodium hypochlorite and the CO in flue gas2Occur fast Speed is reacted and produces hypochlorous acid；After drop is struck on quartz plate, hypochlorous acid is attached in quartzy plate surface and in uviol lamp Lower decompose of radiation produces high activity chlorine atom and hydroxyl；SO in flue gas2﹑ NOx﹑ Hg0Oxygen can occur in quartzy plate surface and hydroxyl Change reaction, oxidation product caused by reaction can impact washing by subsequent shot and come off, so as to ensure that quartz plate has good purple Outer light peneration；
(3)SO2﹑ NOx﹑ Hg0Oxidation product be mainly Liu Suan ﹑ nitric acid and mercury oxide precipitation, into bottom after pass through product Go out to collect, be recycled；Flue gas is discharged by the exhanst gas outlet positioned at the reactor top surface.
Preferably, the method for described light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization, in the step (3) Also include, using the process of chlorine in chlorine recovery device recovered flue gas, the chlorine being recovered is again introduced into institute through smoke inlet Reactor is stated, and reacts to form hypochlorous acid with drop, participates in light decomposable process.
Preferably, for smoke inlet temperature not higher than 150 DEG C, the liquid-gas ratio of solution and flue gas is 1L/m3-30L/m3, in solution The concentration of sodium hypochlorite is 0.1mol/L-5mol/L, and the pH of solution is less demanding in 6.5, and solution temperature is ultraviolet not higher than 65 DEG C Light Net long wave radiation intensity is 30 μ W/cm2-250μW/cm2, ultraviolet EWL is 180nm-280nm.
Light radiation injection reactor bottom of the present invention is equipped with liquor natrii hypochloritis, and top is reacted as dispersed jet Region, reactor are arranged symmetrically centered on uviol lamp, and both sides are reative cells, and centre is uviol lamp arrangement and cooling chamber.It is described Method be in light radiation injection reactor, first using sodium hypochlorite as absorbent fix CO2, hypochlorous acid caused by reaction The SO that chlorine atom and hydroxyl can further in oxidation removal flue gas is produced under ultraviolet radiation2﹑ NOx﹑ Hg0.Contain from boiler CO2﹑ SO2﹑ NOx﹑ Hg0Flue gas time entering from smoke inlet in light radiation injection reactor and come out with vortex atomizing nozzle The quartz plate on directive opposite after sodium chlorate droplets mixing.During solution directive quartz plate, sodium hypochlorite and CO2Occur quick React and produce hypochlorous acid.After solution is struck on quartz plate, the hypochlorous acid in quartzy plate surface is attached in uviol lamp spoke Penetrate lower decompose and produce high activity chlorine atom and hydroxyl.SO in flue gas2﹑ NOx﹑ Hg0It can be aoxidized in quartzy plate surface with hydroxyl Reaction.Oxidation product caused by reaction can impact washing by subsequent shot and come off, so as to ensure that quartz plate has well ultraviolet Light peneration.SO2﹑ NOx﹑ Hg0Oxidation product be mainly Liu Suan ﹑ nitric acid and mercury oxide precipitation, into bottom after can be recovered profit With.The chlorine remained in flue gas can be recycled by the chlorine recovery device absorption and separation Posterior circle of afterbody, the flue gas warp after washing Exhanst gas outlet is discharged into air.Air-cooling apparatus provides air and uviol lamp is cooled down, to ensure that uviol lamp is high at low temperature Effect operation removing product be mainly Liu Suan Na ﹑ sodium nitrate and mercury oxide precipitation, mercury oxide enter bottom product separating tank after meeting Because self gravitation reason sinks to separating, sodium sulphate and sodium nitrate are the raw materials of industry, can be recycled.Remained in flue gas Chlorine can be by the chlorine knockout tower absorption and separation of afterbody and cycling and reutilization.The system has extremely strong oxidisability, can realize The zero-emission of four pollutants, and subtractive process non-secondary pollution, there is wide market application foreground.
A kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization of the present invention, has Equipment is simple, initial cost is small, can realize the zero-emission of a variety of flue gas pollutants and whole subtractive process non-secondary pollution etc. is all More advantages, there is wide exploitation and industrial prospect.
Brief description of the drawings
Fig. 1 is the front view and structural representation of light radiation injection reactor in the present invention.
Fig. 2 is the vortex atomizing nozzle arrangement schematic diagram of light radiation injection reactor in the present invention.
Fig. 3 is the ultraviolet lamp tube arrangement schematic diagram of light radiation injection reactor in the present invention.
Fig. 4 is the ESR spectrum figure of light radiation liquor natrii hypochloritis.
In figure：
1- reactors, 2- quartz plates, 3- uviol lamps, 4- chlorine recovery devices, 5- vortex atomizing nozzles, 6- circulating pumps.
Embodiment
Below in conjunction with the accompanying drawings and specific embodiment the present invention is further illustrated, but protection scope of the present invention is simultaneously Not limited to this.
As shown in figure 1, the device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization of the present invention, is provided with One light radiation injection reactor 1, the inner hub location of light radiation injection reactor 1 set multiple uviol lamps 3, the uviol lamp 3 outsides are provided with quartz plate 2, have gap between quartz plate 2 and uviol lamp 3 as air-cooling apparatus, the air cooling dress The bottom put is provided with air intake, top is provided with air outlet slit；The side wall of reactor 1 is provided with multiple vortex atomizing nozzles 5, Multiple smoke inlets are connected with multiple vortex atomizing nozzles 5 respectively, and exhanst gas outlet is set on the top surface of the reactor 1, send out institute State and solution inlet port, taphole and product exit are additionally provided with the bottom surface of reactor 1, the taphole and multiple eddy flow mists Change nozzle 5 to connect；Circulating pump 6 is provided between taphole and multiple vortex atomizing nozzles 5.The bottom of light radiation injection reactor 1 Portion is equipped with liquor natrii hypochloritis, and top is arranged symmetrically as dispersed jet conversion zone, reactor 1 centered on uviol lamp 3, and two Side is reative cell, and centre is that uviol lamp 3 is arranged and cooling chamber.The smoke outlet is additionally provided with chlorine recovery device 4, described Chlorine recovery device 4 is also connected with smoke inlet.Air-cooling apparatus provides air and uviol lamp 3 is cooled down, to ensure purple Outer lamp 3 Effec-tive Function at low temperature.
The method of described light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization, is in light radiation injection reactor In 1, CO is first fixed as absorbent using sodium hypochlorite2, hypochlorous acid produces chlorine atom under ultraviolet radiation caused by reaction With hydroxyl can further in oxidation removal flue gas SO2﹑ NOx﹑ Hg0.Specifically：
First, hypochlorous acid acid sodium solution is injected into light radiation injection reactor 1 by solution inlet, makes reactor 1 Underfill liquor natrii hypochloritis, starts circulating pump 6, and liquor natrii hypochloritis is ejected into by taphole, vortex atomizing nozzle 5 Conversion zone in the reactor 1 more than liquid level, and form sodium hypochlorite atomized drop.
Then, CO is contained from boiler2﹑ SO2﹑ NOx﹑ Hg0Flue gas enter from smoke inlet in light radiation injection reactor 1 And with vortex atomizing nozzle 5 come out sodium hypochlorite drop mix after directive opposite quartz plate 2；In drop directive quartz plate 2 During, sodium hypochlorite and the CO in flue gas2Generation fast reaction simultaneously produces hypochlorous acid；After drop is struck on quartz plate 2, Hypochlorous acid, which is attached on the surface of quartz plate 2 and decomposed under the radiation of uviol lamp 3, produces high activity chlorine atom and hydroxyl；Such as Fig. 4 institutes Show, can be measured to ultraviolet radiation hypochlorite solution using electronic self-rotary resonant technology generates chlorine atom and hydroxyl.
Detailed process can use following chemical reaction (1)-(6) to represent.
NaClO+H2O+CO2→NaHCO3+HCO (1)
Cl·+H2O→OH-+·OH (5)
·O-++H2O→OH-+·OH (6)
SO in flue gas2﹑ NOx﹑ Hg0Oxidation reaction can occur on the surface of quartz plate 2 and hydroxyl, react caused oxidation production Thing can impact washing by subsequent shot and come off, so as to ensure that quartz plate 2 has good ultraviolet light peneration.With active character Hydroxyl it is oxidable removing flue gas in SO2﹑ NOx﹑ Hg0, detailed process can use following chemical reaction (7)-(10) represent：
Hg0+·OH→HgO↓+·H (7)
NO+2·OH→HNO3+·H (8)
NO2+·OH→HNO3 (9)
SO2+·2OH→H2SO4 (10)
SO2﹑ NOx﹑ Hg0Oxidation product be mainly Liu Suan ﹑ nitric acid and mercury oxide precipitation, mercury oxide enter bottom product It can sink to separating because of self gravitation reason after separating tank, sodium sulphate and sodium nitrate are the raw materials of industry, can be recycled.Enter Go out to collect by product after entering bottom, be recycled；Flue gas is discharged by the exhanst gas outlet positioned at the top surface of reactor 1.
The chlorine remained in flue gas can be recycled by the absorption and separation Posterior circle of chlorine recovery device 4 of afterbody, be recovered Chlorine is again introduced into the reactor 1 through smoke inlet, and reacts to form hypochlorous acid with drop, participates in light decomposable process.Washing Flue gas afterwards is discharged into air through exhanst gas outlet.The system has extremely strong oxidisability, can realize the zero-emission of four pollutants, And subtractive process non-secondary pollution, there is wide market application foreground.
In light radiation injection reactor 1, the horizontal and vertical spacing of vortex atomizing nozzle 5 will be unable to greatly very much to be formed well Drop atomization covering, it is too small that droplet collision will be caused to merge aggravation, be equally unfavorable for the atomization covering of drop, therefore eddy flow mist The optimal lateral and longitudinal pitch A for changing nozzle 5 are respectively positioned between 10cm-45cm, as shown in Fig. 2 and for ease of installation, between transverse direction Away from equal with longitudinal pitch holding.The too small air flow that is unfavorable for of horizontal spacing between uviol lamp 3 and quartz plate 2 cools down, too It is big then cause the increase of ultraviolet propagation distance, increase energy consumption, therefore the optimal lateral spacing B between uviol lamp 3 and quartz plate 2 is located at Between 1cm-4cm.The height of light radiation injection reactor 1 is relevant with the residence time of flue gas/reaction time, and height increases, cigarette The gas residence time increases, and removal efficiency can increase, but height is too high, and reactor 1 is bulky, initial outlay increase, therefore light The optimum height C of injection reactor 1 is radiated between 0.5m-8m.The width of the reative cell of light radiation injection reactor 1 is too small Vortex atomizing nozzle 5 can be caused can not to deploy to cover, and width too conference causes the power of circulating pump 6 to increase, therefore reative cell Optimum width D is located at 0.1m-1.5m.The too conference of the horizontal spacing of uviol lamp 3 causes ultraviolet radiation underpower, and it is too small will Energy expenditure is caused to increase, therefore the optimal lateral spacing E of uviol lamp 3 is between 0.1m-0.8m, as shown in Figure 3.Light radiation is sprayed It is relevant with the flow and floor space for handling flue gas to penetrate the length of reactor 1, flue gas flow it is bigger, it is necessary to reactor 1 grow Degree is longer, but floor space also accordingly increases, and the optimum length F positions of light radiation injection reactor 1 are found after both comprehensive factors Between 0.1m-6m.The solution droplets diameter that vortex atomizing nozzle 5 projects can not provide greatly very much enough contacts area, therefore revolve Flow the solution droplets diameter that atomizer 5 projects and be not more than 80 microns.The solution droplets exit velocity that vortex atomizing nozzle 5 projects It is too small to form enough air-flow rigidity, it is impossible to quartz plate 2 is formed it is enough wash away, therefore vortex atomizing nozzle 5 project The exit velocity of solution is not less than 1.5m/s.
Smoke inlet temperature is too high will to be caused to be electrolysed caused hypochlorous acid acceleration selfdecomposition, be unfavorable for entering for subtractive process OK.In addition, flue-gas temperature is too high also to cool down burden by increase uviol lamp 3, therefore smoke inlet temperature is not higher than 150 DEG C, can lead to Cross after increasing preposition gas cooler cooling and enter back into reactor 1.The liquid-gas ratio of flue gas and solution is too high to cause removal effect Decline, and it is too low, cause reactor 1 not make full use of, therefore the optimal liquid-gas ratio of solution and flue gas is 1L/m3-30L/m3.It is molten Sodium hypochlorite is the main medium and raw material of electrolytic preparation chlorine in liquid, and its concentration is too high will to cause atomized soln viscosity to increase Add, the increase flow resistance of vortex atomizing nozzle 5 and atomization difficulty, while can also reduce gas solubility, and concentration too it is low then without Legal system takes sufficient concentrations of chlorine, therefore the optium concentration of sodium hypochlorite is 0.1mol/L-5mol/L in solution.The pH of solution is too Height is unfavorable for hypochlorous stabilization, is also unfavorable for the removing of pollutant, therefore the pH of solution is less demanding in 6.5.Solution temperature It is too high that hypochlorous acid decomposition and chlorine leach degree will be caused to decline, therefore solution temperature is not higher than 65 DEG C.Pollutant in flue gas Concentration is too high to cause discharge to be unable to reach environmental requirement, therefore, SO in flue gas2Concentration be not higher than 10000ppm, NOxIt is dense Degree is not higher than 5000ppm, Hg0Mercury concentration is not higher than 500 μ g/m3.Ultraviolet radiation intensity is higher, and removal efficiency is better, but energy consumption Also will greatly improve, therefore ultraviolet light Net long wave radiation intensity is 30 μ W/cm2-250μW/cm2.Ultraviolet wavelength is shorter, the light of release Sub- energy is bigger, and it is stronger to decompose hypochlorous ability, but propagation distance is decreased obviously, i.e. disposal ability deficiency, therefore ultraviolet EWL is 180nm-280nm.
According to overall targets such as the available floor spaces of fume treatment Liang ﹑ and pollutant removing efficiency, light radiation injection is anti- It can be that an alone or two or more serial or parallel connections use to answer device 1, and series connection can increase removing effect Rate, parallel connection can increase the exhaust gas volumn of processing.It may be provided with flue gas after washing with the presence of a small amount of chlorine, afterbody containing secondary The chlorine recovery device 4 of chlorination carbon, recovery chlorine can be further washed, the recyclable utilization of chlorine after recovery.Uviol lamp 3 It can produce substantial amounts of heat in running, the too high operational efficiency and service life that will substantially reduce uviol lamp 3 of temperature, because Need to set a set of cooling device using air circulation during this system operation, cooling air volume can be according to exit flow temperature It is general to keep the running temperature of uviol lamp 3 below 55 DEG C to determine.
Embodiment 1：
The horizontal and vertical spacing A of vortex atomizing nozzle 5 is 30cm.Horizontal spacing between uviol lamp 3 and quartz plate 2 B is 1cm.The height C of light radiation injection reactor 1 is between 2.0m.The width D of reative cell is 1.5m.Between the transverse direction of uviol lamp 3 It is 0.1m away from E.The length F of light radiation injection reactor 1 is 2.0m.The solution droplets a diameter of 60 that vortex atomizing nozzle 5 projects Micron, exit velocity 3.5m/s.Smoke inlet temperature is 80 DEG C, liquid-gas ratio 5L/m3, sodium hypochlorite concentration is 0.5mol/ L, pH value of solution 4.0, solution temperature are 50 DEG C, SO in flue gas2Concentration 4000ppm, NOxConcentration 500ppm, mercury concentration are 100 μ g/m3, CO2Concentration is 12%, and ultraviolet radiation intensity is 80 μ W/cm2, ultraviolet wavelength 254nm.In small test system Result be：The efficiency of desulfurization denitration demercuration decarburization respectively reaches 93.6%, 54.1%, 81.6%, 54.8%.
Embodiment 2：
The horizontal and vertical spacing A of vortex atomizing nozzle 5 is 30cm.Horizontal spacing between uviol lamp 3 and quartz plate 2 B is 1cm.The height C of light radiation injection reactor 1 is between 2.0m.The width D of reative cell is 1.5m.Between the transverse direction of uviol lamp 3 It is 0.1m away from E.The length F of light radiation injection reactor 1 is 2.0m.The solution droplets a diameter of 60 that vortex atomizing nozzle 5 projects Micron, exit velocity 3.5m/s.Smoke inlet temperature is 80 DEG C, liquid-gas ratio 4L/m3, sodium hypochlorite concentration is 0.5mol/ L, pH value of solution 4.0, solution temperature are 50 DEG C, SO in flue gas2Concentration 4000ppm, NOxConcentration 500ppm, mercury concentration are 100 μ g/m3, CO2Concentration is 12%, and ultraviolet radiation intensity is 120 μ W/cm2, ultraviolet wavelength 254nm.In small test system On result be：The efficiency of desulfurization denitration demercuration decarburization respectively reaches 100%, 75.2%, 90.7%, 74.3%.
Embodiment 3：
The horizontal and vertical spacing A of vortex atomizing nozzle 5 is 30cm.Horizontal spacing between uviol lamp 3 and quartz plate 2 B is 1cm.The height C of light radiation injection reactor 1 is between 2.0m.The width D of reative cell is 1.5m.Between the transverse direction of uviol lamp 3 It is 0.1m away from E.The length F of light radiation injection reactor 1 is 2.0m.The solution droplets a diameter of 60 that vortex atomizing nozzle 5 projects Micron, exit velocity 3.5m/s.Smoke inlet temperature is 80 DEG C, liquid-gas ratio 4L/m3, sodium hypochlorite concentration is 1.0mol/ L, pH value of solution 4.0, solution temperature are 50 DEG C, SO in flue gas2Concentration 4000ppm, NOxConcentration 500ppm, mercury concentration are 100 μ g/m3, CO2Concentration is 12%, and ultraviolet radiation intensity is 120 μ W/cm2, ultraviolet wavelength 254nm.In small test system On result be：The efficiency of desulfurization denitration demercuration decarburization respectively reaches 100%, 89.3%, 97.2%, 89.9%.
Embodiment 4：
The horizontal and vertical spacing A of vortex atomizing nozzle 5 is 30cm.Horizontal spacing between uviol lamp 3 and quartz plate 2 B is 1cm.The height C of light radiation injection reactor 1 is between 2.0m.The width D of reative cell is 1.5m.Between the transverse direction of uviol lamp 3 It is 0.1m away from E.The length F of light radiation injection reactor 1 is 2.0m.The solution droplets a diameter of 60 that vortex atomizing nozzle 5 projects Micron, exit velocity 3.5m/s.Smoke inlet temperature is 80 DEG C, liquid-gas ratio 3L/m3, sodium hypochlorite concentration is 1.0mol/ L, pH value of solution 4.0, solution temperature are 50 DEG C, SO in flue gas2Concentration 4000ppm, NOxConcentration 500ppm, mercury concentration are 100 μ g/m3, CO2Concentration is 12%, and ultraviolet radiation intensity is 120 μ W/cm2, ultraviolet wavelength 254nm.In small test system On result be：The efficiency of desulfurization denitration demercuration decarburization respectively reaches 100%, 94.3%, 100%, 94.1%.
Embodiment 5：
The horizontal and vertical spacing A of vortex atomizing nozzle 5 is 30cm.Horizontal spacing between uviol lamp 3 and quartz plate 2 B is 1cm.The height C of light radiation injection reactor 1 is between 2.0m.The width D of reative cell is 1.5m.Between the transverse direction of uviol lamp 3 It is 0.1m away from E.The length F of light radiation injection reactor 1 is 2.0m.The solution droplets a diameter of 60 that vortex atomizing nozzle 5 projects Micron, exit velocity 3.5m/s.Smoke inlet temperature is 80 DEG C, liquid-gas ratio 3L/m3, sodium hypochlorite concentration is 1.0mol/ L, pH value of solution 4.0, solution temperature are 50 DEG C, SO in flue gas2Concentration 4000ppm, NOxConcentration 300ppm, mercury concentration are 100 μ g/m3, CO2Concentration is 8%, and ultraviolet radiation intensity is 120 μ W/cm2, ultraviolet wavelength 254nm.In small test system Result be：The efficiency of desulfurization denitration demercuration decarburization respectively reaches 100%, 100%, 100%, 100%.
Embodiment 6：
The horizontal and vertical spacing A of vortex atomizing nozzle 5 is 30cm.Horizontal spacing between uviol lamp 3 and quartz plate 2 B is 1cm.The height C of light radiation injection reactor 1 is between 2.0m.The width D of reative cell is 1.5m.Between the transverse direction of uviol lamp 3 It is 0.1m away from E.The length F of light radiation injection reactor 1 is 2.0m.The solution droplets a diameter of 60 that vortex atomizing nozzle 5 projects Micron, exit velocity 3.5m/s.Smoke inlet temperature is 80 DEG C, liquid-gas ratio 3L/m3, sodium hypochlorite concentration is 1.0mol/ L, pH value of solution 4.0, solution temperature are 50 DEG C, SO in flue gas2Concentration 4000ppm, NOxConcentration 300ppm, mercury concentration are 100 μ g/m3, CO2Concentration is 8%, and ultraviolet radiation intensity is 120 μ W/cm2, ultraviolet wavelength 185nm.In small test system Result be：The efficiency of desulfurization denitration demercuration decarburization respectively reaches 100%, 100%, 100%, 100%.
Comprehensive Correlation by above example understands that removal effect while embodiment 5 and 6 has optimal, desulfurization takes off The efficiency of nitre demercuration decarburization reaches 100%, 100%, 100%, 100%, realizes the zero-emission of multi-pollutant, can be used as most Good embodiment is consulted and used.
The embodiment is preferred embodiment of the invention, but the present invention is not limited to above-mentioned embodiment, not Away from the present invention substantive content in the case of, those skilled in the art can make it is any it is conspicuously improved, replace Or modification belongs to protection scope of the present invention.

Claims (6)

  1. A kind of 1. device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization, it is characterised in that：Provided with a light spoke Injection reactor (1) is penetrated, light radiation injection reactor (1) inner hub location sets multiple uviol lamps (3), the uviol lamp (3) it is outside to be provided with quartz plate (2), there is gap as cooling air channel, the sky between quartz plate (2) and uviol lamp (3) The bottom of air cooling passage is provided with air intake, top is provided with air outlet slit；Reactor (1) side wall is provided with multiple eddy flows Atomizer (5), multiple smoke inlets connect with multiple vortex atomizing nozzles (5) respectively, are set on the top surface of the reactor (1) Exhanst gas outlet is put, solution inlet port, taphole and product exit, the solution are additionally provided with the bottom surface of the reactor (1) Outlet connects with multiple vortex atomizing nozzles (5)；Circulating pump is provided between taphole and multiple vortex atomizing nozzles (5) (6)；The smoke outlet is additionally provided with chlorine recovery device (4), the chlorine recovery device (4) also with smoke inlet phase Even.
  2. 2. the device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization according to claim 1, its feature exist In：The optimal lateral and longitudinal pitch A of vortex atomizing nozzle (5) are respectively positioned between 10cm-45cm, uviol lamp (3) and quartz plate (2) the horizontal spacing B between 1cm-4cm, the height C of light radiation injection reactor (1) between 0.5m-8m, The width D of the reative cell of reactor (1) is located at 0.1m-1.5m, the horizontal spacing E of uviol lamp (3) between 0.1m-0.8m, The length F of light radiation injection reactor (1) is between 0.1m-6m, and the solution droplets diameter that vortex atomizing nozzle (5) projects is not More than 80 microns, the exit velocity for the solution that vortex atomizing nozzle (5) projects is not less than 1.5m/s.
  3. 3. the device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization according to claim 1, its feature exist In：Gas cooler is additionally provided with smoke inlet.
  4. 4. the device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization according to claim 1, its feature exist In：The quantity of the reactor (1) is multiple, in parallel between multiple reactors (1) and/or series connection.
  5. A kind of 5. method of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization, it is characterised in that comprise the following steps：
    (1) hypochlorous acid acid sodium solution is injected into light radiation injection reactor (1) by solution inlet, makes the bottom of reactor (1) Liquor natrii hypochloritis is filled in portion, starts circulating pump (6), and liquor natrii hypochloritis sprays by taphole, vortex atomizing nozzle (5) Conversion zone to more than the reactor (1) interior liquid level, and form sodium hypochlorite atomized drop；
    (2) hypochlorous acid that flue gas enters in light radiation injection reactor (1) from smoke inlet and come out with vortex atomizing nozzle (5) The quartz plate (2) on directive opposite after sodium droplets mixing；During drop directive quartz plate (2), in sodium hypochlorite and flue gas CO2Generation fast reaction simultaneously produces hypochlorous acid；After drop is struck on quartz plate (2), hypochlorous acid is attached to quartz plate (2) table Decompose on face and under uviol lamp (3) radiation and produce high activity chlorine atom and hydroxyl；SO in flue gas2﹑ NOx﹑ Hg0Can be in quartz With hydroxyl oxidation reaction occurs for plate (2) surface, and oxidation product caused by reaction can impact washing by subsequent shot and come off, so as to protect Demonstrate,proving quartz plate (2) has good ultraviolet light peneration；
    (3)SO2﹑ NOx﹑ Hg0Oxidation product be mainly Liu Suan ﹑ nitric acid and mercury oxide precipitation, into bottom after by product go out receive Collection, is recycled；Flue gas is discharged by the exhanst gas outlet positioned at the reactor (1) top surface；Using chlorine recovery device (4) The process of chlorine in recovered flue gas, the chlorine being recovered is again introduced into the reactor (1) through smoke inlet, and is reacted with drop Hypochlorous acid is formed, participates in light decomposable process.
  6. 6. the method for light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization according to claim 5, its feature exist In：For smoke inlet temperature not higher than 150 DEG C, the liquid-gas ratio of solution and flue gas is 1L/m3-30L/m3, sodium hypochlorite is dense in solution Spend for 0.1mol/L-5mol/L, the pH of solution is less demanding in 6.5, and solution temperature is not higher than 65 DEG C, and ultraviolet light Net long wave radiation is strong Spend for 30 μ W/cm2-250μW/cm2, ultraviolet EWL is 180nm-280nm.
CN201610239826.2A 2016-04-18 2016-04-18 A kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization Active CN105727724B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610239826.2A CN105727724B (en) 2016-04-18 2016-04-18 A kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610239826.2A CN105727724B (en) 2016-04-18 2016-04-18 A kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization

Publications (2)

Publication Number Publication Date
CN105727724A CN105727724A (en) 2016-07-06
CN105727724B true CN105727724B (en) 2018-02-27

Family

ID=56255452

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610239826.2A Active CN105727724B (en) 2016-04-18 2016-04-18 A kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization

Country Status (1)

Country Link
CN (1) CN105727724B (en)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106000029B (en) * 2016-04-18 2019-02-05 江苏大学 A kind of method and device of light excitation electrolysis simultaneous SO_2 and NO removal demercuration
CN108057344A (en) * 2018-01-15 2018-05-22 大连海事大学 A kind of wet type desulfurizing denitrating system and its process suitable for ship
CN109289491A (en) * 2018-11-13 2019-02-01 上海氯碱化工股份有限公司 A kind of processing method of carbonated tail gas
CN112121616A (en) * 2020-09-09 2020-12-25 华中科技大学 Flue gas multi-pollutant purification device for coupling microwave ultraviolet light with hydrogen peroxide
CN115475478A (en) * 2022-09-05 2022-12-16 南京理工大学 Symmetrical double-section mercury removal and carbon fixation waste heat recovery integrated device

Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN200948420Y (en) * 2006-03-27 2007-09-19 伍沅 Air-liquid reactor of large quantity of striking flow
CN101352646A (en) * 2008-08-29 2009-01-28 浙江大学 Flue gas denitration method using ultraviolet light double action
CN101940871A (en) * 2010-09-29 2011-01-12 东南大学 Photochemical advanced oxygenation-based simultaneous desulfuration and denitration system
CN102160959A (en) * 2011-02-25 2011-08-24 东南大学 Fume purification system based on advanced oxygenation combining wet scrubbing
CN102430328A (en) * 2011-09-26 2012-05-02 上海电力学院 Device for removing gas mercury by photo-catalysis and application thereof
CN102908883A (en) * 2012-09-27 2013-02-06 北京大学 Method for simultaneously desulfurizing and denitrating flue gas
CN103638796A (en) * 2013-12-13 2014-03-19 江苏大学 System and method for desulfurizing, denitrifying and removing mercury based on photoactivation ammonium persulfate
CN203899431U (en) * 2013-12-13 2014-10-29 江苏大学 Desulfurization, denitrification and demercuration system based on photoactivated ammonium persulfate
CN104258711A (en) * 2014-09-30 2015-01-07 上海援梦电力能源科技咨询中心 Comprehensive treatment method for carrying out desulfurization, denitration, mercury removal and recycling on flue gas of boiler
CN104785076A (en) * 2015-04-21 2015-07-22 南京朗洁环保科技有限公司 Method for simultaneous desulfurization denitrification and mercury removal based on hydroxyl and sulphate radical oxidation
CN204637945U (en) * 2015-04-21 2015-09-16 南京朗洁环保科技有限公司 A kind of ozone is in conjunction with the desulfurization denitration demercuration system of light radiation peroxide
CN104923049A (en) * 2015-04-21 2015-09-23 江苏大学 Simultaneous desulfurization, denitrification and demercuration optical radiation method for ozone and hydrogen peroxide

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN200948420Y (en) * 2006-03-27 2007-09-19 伍沅 Air-liquid reactor of large quantity of striking flow
CN101352646A (en) * 2008-08-29 2009-01-28 浙江大学 Flue gas denitration method using ultraviolet light double action
CN101940871A (en) * 2010-09-29 2011-01-12 东南大学 Photochemical advanced oxygenation-based simultaneous desulfuration and denitration system
CN102160959A (en) * 2011-02-25 2011-08-24 东南大学 Fume purification system based on advanced oxygenation combining wet scrubbing
CN102430328A (en) * 2011-09-26 2012-05-02 上海电力学院 Device for removing gas mercury by photo-catalysis and application thereof
CN102908883A (en) * 2012-09-27 2013-02-06 北京大学 Method for simultaneously desulfurizing and denitrating flue gas
CN103638796A (en) * 2013-12-13 2014-03-19 江苏大学 System and method for desulfurizing, denitrifying and removing mercury based on photoactivation ammonium persulfate
CN203899431U (en) * 2013-12-13 2014-10-29 江苏大学 Desulfurization, denitrification and demercuration system based on photoactivated ammonium persulfate
CN104258711A (en) * 2014-09-30 2015-01-07 上海援梦电力能源科技咨询中心 Comprehensive treatment method for carrying out desulfurization, denitration, mercury removal and recycling on flue gas of boiler
CN104785076A (en) * 2015-04-21 2015-07-22 南京朗洁环保科技有限公司 Method for simultaneous desulfurization denitrification and mercury removal based on hydroxyl and sulphate radical oxidation
CN204637945U (en) * 2015-04-21 2015-09-16 南京朗洁环保科技有限公司 A kind of ozone is in conjunction with the desulfurization denitration demercuration system of light radiation peroxide
CN104923049A (en) * 2015-04-21 2015-09-23 江苏大学 Simultaneous desulfurization, denitrification and demercuration optical radiation method for ozone and hydrogen peroxide

Also Published As

Publication number Publication date
CN105727724A (en) 2016-07-06

Similar Documents

Publication Publication Date Title
CN105727724B (en) A kind of method and device of light radiation hypochlorous acid acid sodium simultaneous SO_2 and NO removal demercuration decarburization
CN104043325B (en) The flue gas purifying method of a kind of ozone activation persulfate and device
US7052662B2 (en) NOx, Hg, and SO2 removal using alkali hydroxide
CN104923072B (en) Hydrogen sulfide removal method based on photocatalytic spraying
CN101940871B (en) Photochemical advanced oxygenation-based simultaneous desulfuration and denitration system
CN202096874U (en) Flue gas purification device based on advanced oxidization combined with wet washing
CN103990365B (en) The flue gas purifying method of a kind of ozone/hydrogen peroxide induced radical and system
CN104785081B (en) Desulfurization, denitrification and demercuration method by combining ozone with light radiation peroxide
CN104785076B (en) Desulfurization denitration demercuration method while aoxidizing based on hydroxyl and potentiometric titrations
Wang et al. Removal of gaseous hydrogen sulfide using ultraviolet/Oxone-induced oxidation scrubbing system
CN101337153A (en) Ultrasonic integration desulfurization denitration demercuration method and device thereof
CN101947409B (en) Flue gas mercury removal system based on photochemical advanced oxidation
CN204365118U (en) A kind of simultaneous SO_2 and NO removal system based on optical excitation ozone associating wet scrubbing
CN106000029B (en) A kind of method and device of light excitation electrolysis simultaneous SO_2 and NO removal demercuration
CN102160959A (en) Fume purification system based on advanced oxygenation combining wet scrubbing
CN107497265B (en) Integrated flue gas purification system and method for inducing free radicals by exciting fly ash through cooperation of ozone and microwaves
CN105727725B (en) A kind of photoelectrolysis induced radical takes off the method and device of VOCs
CN107684826B (en) Multi-pollutant combined removal method and system for activating free radicals through microwave spraying
CN201807286U (en) Photochemical advanced oxidation-based synchronous desulfuration and denitration system
CN104857852B (en) VOCs removing method based on photocatalytic free radical advanced oxidation
CN205965447U (en) Optical excitation electrolysis is device of SOx/NOx control demercuration simultaneously
CN206660930U (en) The new novel oxidized method dust-removal and desulfurizing denitrification apparatus of high temperature oil shaft furnace wet method low temperature
CN105498480A (en) Ultraviolet radiation enhancement based method and device for simultaneous desulfurization, denitrification and particulate removal of pypocholoride
CN104923061B (en) Hydrogen sulfide removal method based on photochemical free radicals
CN104857825B (en) A kind of photochemistry is atomized the hydrogen sulfide removal system of bed

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant