CN204973597U - Agent of ray radiation concerted catalysis arouses ozone peroxide's flue gas demercuration system - Google Patents
Agent of ray radiation concerted catalysis arouses ozone peroxide's flue gas demercuration system Download PDFInfo
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- CN204973597U CN204973597U CN201520245758.1U CN201520245758U CN204973597U CN 204973597 U CN204973597 U CN 204973597U CN 201520245758 U CN201520245758 U CN 201520245758U CN 204973597 U CN204973597 U CN 204973597U
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Abstract
The utility model relates to an agent of ray radiation concerted catalysis arouses ozone peroxide's flue gas demercuration system, the system adopt the ultraviolet ray to unite the catalyst to arouse hydroxyl that ozone peroxide produced the strong oxidizing property and the sulfate radical hg0 in the oxidation desorption flue gas in striking bed. The partial flue gas that comes from the boiler mixes the back with partial ozone peroxide catalyst and is spouted into the striking bed by the impinger, and another part flue gas mixes the back with another part ozone peroxide catalyst and is spouted into the striking bed to the impinger of arranging by the coaxial pair, and two strands of air currents take place the striking in the striking bed mixes. The agent of ultraviolet ray radiation concerted catalysis is decomposed ozone peroxide and is produced the hydroxyl of strong oxidizing property and the bivalent mercury that sulfate radical oxidation hg0 generated the resourcebility utilization. Hg0 in can the high -efficient desorption coal -fired flue gas of this system, but and desorption result recycle, no secondary pollution has wide municipality's development prospect.
Description
Technical field
The utility model relates to Air Pollution Control field, is specifically related to the flue gas mercury removal system that a kind of light radiation synergistic catalyst excites ozone/peroxide.
Background technology
Mercury is a kind of hypertoxicity and the traces of heavy metals element being easy to deposition in vivo, has great harm to health and ecological environment.United Nations Environment Programme points out in a survey report delivered, and coal-burning boiler is the maximum man-made pollution source of mercury emissions.China is the large consumption of coal state of the first in the world, and in energy resource structure, the ratio of coal is up to 75%, and this general layout does not still have large change within the quite a long time from now on.Along with the increasingly stringent of pollution that caused by coal burning thing air environmental protection standard, estimate in the near future, the appearance of coal-fired flue-gas mercury pollution control criterion will be inexorable trend.Therefore, researching and developing effective coal-fired flue-gas mercury pollution control method is one of vital task of facing of Environmental Protection in China scientific and technical personnel.
In recent years, Chinese scholars has done a large amount of fruitful work at research demercuration new theory and new technical field.At present, in numerous demercuration method, adsorbent and wet scrubbing are considered to the main flow demercuration technology that two of coal-fired flue gas mercury removal field have development potentiality most.In wet scrubbing demercuration technology, most study is that the existing wet method fume desulfurizing system of application combines washing demercuration.This technology can realize higher Hg
2+(g) removal efficiency, but the Hg to indissoluble
0g () does not have obvious removal effect, partial oxidation state mercury also may be reduced to Elemental Mercury.Many scholars attempt with some oxidation technologies before desulfurizing tower by the Hg in flue gas
0g () initial oxidation is Hg
2+(g), and then remove Hg with wet method fume desulfurizing system washing
2+(g).More SCR (SCR) the catalytic oxidation demercuration of current research can realize part Hg
0g () is converted into Hg
2+(g), but demercuration effect is subject to the obvious impact of coal-fired component, catalyst type, combustion system and burner structure, and associated catalytic oxidation mechanism is still not fully aware of.Other oxidation technology, such as ﹑ photochemical catalytic oxidation such as Yangization such as gas ions such as Deng and ozone oxidation etc. are still in the laboratory exploratory stage.Utilize conventional oxidation agent oxidative absorption Hg in absorption tower such as Gao mangaic acid Jia ﹑ potassium peroxydisulfate and sodium chlorite
0g () also achieves good result, but also there is the deficiencies such as absorbent costliness or the process of product component complicated difficult, and correlation technique needs perfect further.Absorption method is mainly by the Hg in active carbon or other adsorbent flue gas
2+(g) and Hg
0g (), is first translated into particulate Hg, then utilize existing cleaner caught and reach demercuration object.Current research is more and technology is the most ripe active carbon adsorption has higher demercuration efficiency, but application cost is high, and enterprise is difficult to bear.Other adsorbent, although such as your Jin Shu ﹑ Jin belongs to Yangization Wu ﹑ Fei Hui ﹑ Huo Jiao ﹑ calcium Ji Cai Liao ﹑ molecular sieve and natural minerals etc. have potential development prospect, but due in application cost, demercuration efficiency, the shortcoming of the aspects such as adsorbent stability and adsorption mechanism research, with not enough, also cannot obtain large-scale industrial application at present.In sum, a kind of coal-fired flue gas mercury removal technology being suitable for large-scale commercial is not also had at present.
Utility model content
The utility model relates to the flue gas mercury removal system that a kind of light radiation synergistic catalyst excites ozone/peroxide, and described system adopts ultraviolet light united catalyst to excite ozone/peroxide to produce hydroxyl and the Hg of potentiometric titrations in shock bed in oxidation removal flue gas of strong oxidizing property
0.
Mercury removal system of the present utility model based on principle and course of reaction as follows:
1, as shown in Figure 1, adopt electron spin resonance (ESR) kaleidophon can be measured in reaction system and create sulfate radical and hydroxyl radical free radical.Therefore, first this system is release the sulfate radical and hydroxyl radical free radical with strong oxidizing property, and detailed process can represent with following chemical reaction (1)-(6):
H
2O
2+UV→2·OH(1)
O
3+UV→·O+O
2(3)
·O+H
2O
2→·OH+HO
2·(6)
Sulfate radical and the hydroxyl radical free radical of the strong oxidizing property 2, produced can by the Hg in flue gas
0oxidation generates bivalent mercury.Detailed process can represent with following reaction (7) and (8):
a·OH+bHg
0→cHgO+otherproducts(7)
3, bivalent mercury separated recovery in the product postprocessing system of afterbody of oxidation generation.Such as, bivalent mercury first can produce mercuric sulphide sediment separation and recovery by adding sulfidion reaction.This system can realize the efficient removal of coal-fired flue-gas mercury, and product resourcebility utilizes, and non-secondary pollution, has wide market development prospect.
For realizing above object, the embodiment that the utility model adopts is as follows:
Light radiation synergistic catalyst excites a flue gas mercury removal system for ozone/peroxide, and described system is provided with pot stove ﹑ and clashes into device ﹑ smelly oxygen and send out device ﹑ raw clash into bed ﹑ uviol lamp except warm device ﹑ falls in dirt device ﹑ and quartzy sleeve pipe ﹑ stores up liquid tank ﹑ chimney except mist device ﹑ follows ring pump ﹑; Described shock bed is provided with exhanst gas outlet, demister, uviol lamp and quartz socket tube and peroxide outlet from top to bottom successively; Described boiler is connected with deduster entrance by flue, and the outlet of deduster connects the entrance of cooler, and cooler is provided with two outlets, and two flue gas accelerating tubes exporting the ram arranged with coaxial subtend respectively of described cooler are connected; Described ozone generator connects the ram flue gas accelerating tube that coaxial subtend is arranged respectively, and described ram is made up of solution conduit and gas accelerating tube; Described solution conduit one end is with peroxide solutions entrance, and the other end is provided with atomizer; The entrance of the fluid reservoir of peroxide is connected with the outlet of the peroxide clashed into bottom bed, and the solution conduit of the ram that the outlet of fluid reservoir is arranged with coaxial subtend is connected.
Clash into the ram in bed and ultraviolet lamp tube employing multi-stage cross layout.Ram layout alternate with ultraviolet lamp tube, and adjacent ram and ultraviolet lamp tube adopt cocurrent and parallel to arrange.Vertical interval A between ultraviolet lamp tube adjacent two layers is between 5cm-50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is between 20cm-350cm.Ram is arranged in the central spot between adjacent two layers ultraviolet lamp tube.Adjacent two-stage ram adopts 90 degree of arranged crosswise staggered, and the ultraviolet lamp tube of adjacent two-stage adopts 90 degree of arranged crosswise staggered equally.
Ram is made up of solution conduit and gas accelerating tube.Solution conduit one end is with peroxide solutions and catalyst inlet, and the other end is provided with atomizer.Gas accelerating tube is with ozone entrance and smoke inlet, and ozone entrance and smoke inlet adopt coaxially positioned opposite.The optimum length C of solution conduit is between 60cm-120cm, and the optimum length D of flue gas accelerating tube is between 50cm-100cm.The diameter of solution conduit is relevant with liquid inventory, but will ensure that solution is not more than 10 microns from the atomization droplets diameter that nozzle sprays.The diameter of flue gas accelerating tube is relevant with flue gas flow, but will ensure that flue gas flow rate that flue gas flows out from conduit outlet is between 5m/s-25m/s.
The length C of described solution conduit is between 60cm-150cm, and the optimum length D of flue gas accelerating tube is between 50cm-130cm.
The process of reaction of the present utility model is as follows: peroxide and catalyst fines enter fluid reservoir from the entrance c of fluid reservoir, is then aspirated the solution conduit sending into ram by circulating pump.Flue gas from boiler enters the flue gas accelerating tube of ram after deduster dedusting and cooler cooling.Ozone gas from ozone generator also enters the flue gas accelerating tube of ram.Streams of ozone and flue gas are pre-mixed in the flue gas accelerating tube of ram.The atomized drop containing catalyst granules is produced after the atomizer atomization through solution conduit top of peroxide and catalyst fines.After flue gas accelerating tube accelerates, carry the same air-flow of atomized drop and opposite after ozone mixes with flue gas mutually clash into.Ultraviolet radiation synergistic catalyst excites ozone/peroxide to produce the sulfate radical of strong oxidizing property and hydroxyl radical free radical Hg in oxidation removal flue gas in shock bed
0and generate the bivalent mercury of resourcebility utilization.What produce sends into afterproduct treatment system containing bivalent mercury solution by exporting a, and the flue gas of cleaning enters chimney by clashing into bed outlet d and enters air.
The best smoke inlet temperature of clashing into bed is 30-70 DEG C, and effective liquid-gas ratio is 0.2-3.5L/m
3, the optium concentration of peroxide is between 0.2mol/L-2.5mol/L, and the best entrance concentration of ozone is 20ppm-500ppm, and the pH of solution is between 1.0-7.5, and best solution temperature is 20-65 DEG C.Ultraviolet light Net long wave radiation intensity is 20 μ W/cm
2-500 μ W/cm
2, ultraviolet EWL is 160nm-365nm.Hg in flue gas
0content not higher than 300 μ g/m
3.Described peroxide comprises one or both the mixing in hydrogen peroxide and ammonium persulfate.Described catalyst comprises one or more the mixing in Ling Jia Tie ﹑ Yangization Tie ﹑ bis-Yangization Meng ﹑ cupric oxide, and the powder diameter of catalyst is not more than 10 microns, and the optimum dosage of catalyst is often liter of solution 10g-50g (10-50g/L).
Advantage of the present utility model and remarkable result:
The hydroxyl that ultraviolet radiation synergistic catalyst ozone decomposition/peroxide produces and potentiometric titrations have extremely strong oxidisability, can by the Hg in coal-fired flue-gas
0be oxidized to the bivalent mercury that resourcebility utilizes, the highest removal efficiency can reach 100%, and removes product recoverable, non-secondary pollution, has wide city's development prospect.
Accompanying drawing explanation
A kind of light radiation of Fig. 1 synergistic catalyst excites the general figure of ESR light of the flue gas demercuration of ozone/peroxide.
Fig. 2 is technological process and the structure chart of the utility model system.
Fig. 3 is product postprocessing device and the flow chart of the utility model system.
Fig. 4 is the structural representation that the utility model clashes into bed inner impact device and ultraviolet lamp tube two adjacent groups layout.
Fig. 5 is the structural representation of ram.
Fig. 6 is the critical size mark schematic diagram of ram.
Detailed description of the invention
Below in conjunction with accompanying drawing, detailed description of the invention of the present utility model is further described.
As shown in Figure 2, a kind of light radiation synergistic catalyst excites the flue gas mercury removal system of ozone/peroxide to be provided with boiler 1 ﹑ deduster 2 ﹑ cooler 3 ﹑ ram 11 ﹑ ozone generator 4 ﹑ shock bed 5 ﹑ uviol lamp 13 and quartz socket tube 14 ﹑ demister 9 ﹑ circulating pump 1 ﹑ circulating pump 28, fluid reservoir 6 ﹑ chimney 10 and product postprocessing system 15.Clash into bed 5 and be provided with exhanst gas outlet d, demister 9, uviol lamp 13 and quartz socket tube and peroxide outlet b and product exit a from top to bottom successively; Described boiler 1 is connected with deduster 2 entrance by flue, and the outlet of deduster 2 connects the entrance of cooler 3, and cooler 3 is provided with two outlets, and two flue gas accelerating tube 11-2 exporting the ram 11 arranged with coaxial subtend respectively of described cooler 3 are connected; Described ozone generator 4 connects the ram flue gas accelerating tube 11-2 that coaxial subtend is arranged respectively, and described ram 11 is made up of solution conduit 11-1 and gas accelerating tube 11-2; Described solution conduit 11-1 one end is with the entrance m of peroxide and catalyst granules, and the other end is provided with atomizer 12; The entrance of the fluid reservoir 6 of peroxide is connected with the outlet b of the peroxide clashed into bottom bed 5, and the solution conduit 11-1 of the ram 11 that outlet and the coaxial subtend of fluid reservoir are arranged is connected.
Peroxide and catalyst fines enter fluid reservoir 6 from the entrance c of fluid reservoir 6, are then aspirated the solution conduit 11-1 sending into ram 11 by circulating pump 1.Flue gas from boiler 1 enters the flue gas accelerating tube 11-2 of ram 11 after deduster 2 dedusting and cooler 3 are lowered the temperature.
As shown in Figure 5 and Figure 6, ram 11 is made up of solution conduit 11-1, flue gas accelerating tube 11-2 and atomizer 12, and solution conduit 11-1 one end is with the entrance m of peroxide and catalyst granules, and the other end is provided with atomizer 12.Flue gas accelerating tube 11-2 is with ozone entrance n and smoke inlet p, and ozone entrance n and smoke inlet p adopts coaxially positioned opposite.Ozone gas from ozone generator 4 enters the flue gas accelerating tube 11-2 of ram 11, and streams of ozone and flue gas are pre-mixed in the flue gas accelerating tube 11-2 of ram 11.The atomized drop containing catalyst granules is produced after peroxide and the catalyst fines atomizer 12 through solution conduit 11-1 top is atomized.
After flue gas accelerating tube accelerates, carry the same air-flow of atomized drop and opposite after ozone mixes with flue gas mutually clash into.The hydroxyl radical free radical that ultraviolet radiation ozone/hydrogen peroxide solution produces strong oxidizing property Hg in oxidation removal flue gas in shock bed
0generate the bivalent mercury that resourcebility utilizes.What produce sends into afterproduct treatment system 15 containing bivalent mercury solution by exporting a, and the flue gas of cleaning exports d and enters chimney 10 by clashing into bed 5 and enter air.
The optimum length C of solution conduit between 60cm-150cm, between the length 50cm-130cm of flue gas accelerating tube D.The diameter of solution conduit is relevant with liquid inventory, but will ensure that solution is not more than 15 microns from the atomization droplets diameter that nozzle sprays.The diameter of flue gas accelerating tube is relevant with flue gas flow, but will ensure that flue gas flow rate that flue gas flows out from conduit outlet is between 5m/s-30m/s.
As shown in Figure 3, product postprocessing system 15 is connected with the outlet a clashing into bed, and product postprocessing system 15 is provided with mercury knockout tower 16, and in mercury knockout tower 16, bivalent mercury first produces mercuric sulphide sediment separation and recovery by adding sulfidion reaction.
As shown in Figure 4, the ram 11 in shock bed 5 and ultraviolet lamp tube 13 adopt multi-stage cross to arrange.Ultraviolet lamp tube 13 is provided with quartz socket tube 14, and quartz socket tube 14 pairs of ultraviolet lamp tubes 13 play a protective role.Ram 11 layout alternate with ultraviolet lamp tube 13, and adjacent ram 11 and ultraviolet lamp tube 13 adopt cocurrent and parallel to arrange.Vertical interval A between ultraviolet lamp tube 13 adjacent two layers is between 5cm-60cm.Distance B between two ram 11 tops (distances between two atomizers 12) positioned opposite is between 20cm-350cm.
Ram 11 is arranged in the central spot between adjacent two layers ultraviolet lamp tube.Adjacent two-stage ram 11 adopts 90 degree of arranged crosswise staggered, and the ultraviolet lamp tube of adjacent two-stage adopts 90 degree of arranged crosswise staggered equally.
The optimum length of solution conduit, between 60cm-120cm, (is specifically shown in Fig. 5 and 6) between the length 50cm-100cm of flue gas accelerating tube.The diameter of solution conduit is relevant with liquid inventory, but will ensure that solution is not more than 10 microns from the atomization droplets diameter that nozzle sprays.The diameter of flue gas accelerating tube is relevant with flue gas flow, but will ensure that flue gas flow rate that flue gas flows out from conduit outlet is between 5m/s-25m/s.
Course of reaction is as follows: from the flue gas of boiler 1 after deduster 2 dedusting, enter cooler 3 to lower the temperature, flue gas through cooling enters by two outlets of cooler 3 ram 11 that coaxial subtend is arranged in shock bed 5 respectively, described ozone enters ram 11 by ozone generator 4, and the entrance concentration of ozone is 20ppm-500ppm; Described peroxide solutions enters ram 11 by fluid reservoir 6 through circulating pump, and the concentration of peroxide is between 0.2mol/L-2.5mol/L, and the pH of solution is between 1.0-7.5, and solution temperature is 20-65 DEG C, and effective liquid-gas ratio is 0.2-3.5L/m3; Described flue gas, ozone, peroxide are mixed to form gas-liquid mixture in ram, and two strands of gas-liquid mixtures, in shock bed 5, impingement mix occur; The uviol lamp clashed in bed 5 launches ultraviolet light, and ultraviolet light Net long wave radiation intensity is 20-500, and ultraviolet EWL is 160nm-365nm; Ultraviolet light united catalyst excites ozone/peroxide to produce hydroxyl and the Hg of potentiometric titrations in shock bed in oxidation removal flue gas of strong oxidizing property
0.
Described peroxide comprises one or both the mixing in hydrogen peroxide and ammonium persulfate.Described catalyst comprises one or more the mixing in Ling Jia Tie ﹑ Yangization Tie ﹑ bis-Yangization Meng ﹑ cupric oxide, and the powder diameter of catalyst is not more than 10 microns, and the best of catalyst adds concentration for often liter of solution 10g-50g (10-50g/L).
The length of embodiment 1. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.Hg in flue gas
0concentration is respectively 50 μ g/m
3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m
3, hydrogen peroxide concentration is 0.5mol/L, and iron oxide concentration is 10g/L, and liquid pH is 3.2, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: Hg in flue gas
0removal efficiency reach 69.1%.
The length of embodiment 2. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.Hg in flue gas
0concentration is respectively 50 μ g/m
3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m
3, ammonium persulfate concentrations is 0.5mol/L, and iron oxide concentration is 10g/L, and liquid pH is 3.4, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: Hg in flue gas
0removal efficiency reach 62.7%.
The length of embodiment 3. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.Hg in flue gas
0concentration is respectively 50 μ g/m
3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m
3, hydrogen peroxide concentration is 1.0mol/L, and iron oxide concentration is 10g/L, and liquid pH is 3.2, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: Hg in flue gas
0removal efficiency reach 85.4%.
The length of embodiment 4. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.Hg in flue gas
0concentration is respectively 50 μ g/m
3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.0L/m
3, ammonium persulfate concentrations is 1.0mol/L, and iron oxide concentration is 10g/L, and liquid pH is 3.4, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: Hg in flue gas
0removal efficiency reach 81.9%.
The length of embodiment 5. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.Hg in flue gas
0concentration is respectively 50 μ g/m
3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.5L/m
3, hydrogen peroxide concentration is 1.0mol/L, and iron oxide concentration is 10g/L, and liquid pH is 3.2, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: Hg in flue gas
0removal efficiency reach 95.1%.
The length of embodiment 6. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.Hg in flue gas
0concentration is respectively 50 μ g/m
3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.5L/m
3, ammonium persulfate concentrations is 1.0mol/L, and iron oxide concentration is 10g/L, and liquid pH is 3.4, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: Hg in flue gas
0removal efficiency reach 91.8%.
The length of embodiment 7. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.Hg in flue gas
0concentration is respectively 50 μ g/m
3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.5L/m
3, hydrogen peroxide concentration is 1.5mol/L, and manganese dioxide concentration is 10g/L, and liquid pH is 3.0, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: Hg in flue gas
0removal efficiency reach 100%.
The length of embodiment 8. solution conduit is positioned at 60cm, flue gas accelerating tube length 50cm.Distance B between two ram tops (distances between two atomizers) positioned opposite is 25cm.Hg in flue gas
0concentration is respectively 50 μ g/m
3, the smoke inlet temperature of clashing into bed is 60 DEG C, and liquid-gas ratio is 1.5L/m
3, ammonium persulfate concentrations is 1.5mol/L, and manganese dioxide concentration is 10g/L, and liquid pH is 3.2, and solution temperature is 60 DEG C, and ultraviolet light Net long wave radiation intensity is 30 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: Hg in flue gas
0removal efficiency reach 100%.
Comprehensive Correlation through above embodiment is known, and embodiment 7 and 8 has best removal effect, Hg under two kinds of operational modes
0removal efficiency all reach 100%, can be used as most preferred embodiment and consult and use.
Claims (4)
1. light radiation synergistic catalyst excites the flue gas mercury removal system of ozone/peroxide, it is characterized in that: described system is provided with pot stove ﹑ and clashes into device ﹑ smelly oxygen and send out device ﹑ raw clash into bed ﹑ uviol lamp except warm device ﹑ falls in dirt device ﹑ and quartzy sleeve pipe ﹑ stores up liquid tank ﹑ chimney except mist device ﹑ follows ring pump ﹑; Described shock bed is provided with exhanst gas outlet, demister, uviol lamp and quartz socket tube and peroxide outlet from top to bottom successively; Described boiler is connected with deduster entrance by flue, and the outlet of deduster connects the entrance of cooler, and cooler is provided with two outlets, and two flue gas accelerating tubes exporting the ram arranged with coaxial subtend respectively of described cooler are connected; Described ozone generator connects the ram flue gas accelerating tube that coaxial subtend is arranged respectively, and described ram is made up of solution conduit and gas accelerating tube; Described solution conduit one end is with peroxide solutions entrance, and the other end is provided with atomizer; The entrance of the fluid reservoir of peroxide is connected with the outlet of the peroxide clashed into bottom bed, and the solution conduit of the ram that the outlet of fluid reservoir is arranged with coaxial subtend is connected.
2. light radiation synergistic catalyst according to claim 1 excites the flue gas mercury removal system of ozone/peroxide, it is characterized in that: clash into the ram in bed and ultraviolet lamp tube employing multi-stage cross layout; Ram layout alternate with ultraviolet lamp tube, and adjacent ram and ultraviolet lamp tube adopt cocurrent and parallel to arrange; Vertical interval A between ultraviolet lamp tube adjacent two layers is between 5cm-60cm.
3. light radiation synergistic catalyst according to claim 2 excites the flue gas mercury removal system of ozone/peroxide, it is characterized in that: the distance B between two ram tops positioned opposite is between 20cm-350cm; Ram is arranged in the central spot between adjacent two layers ultraviolet lamp tube; Adjacent two-stage ram adopts 90 degree of arranged crosswise staggered, and the ultraviolet lamp tube of adjacent two-stage adopts 90 degree of arranged crosswise staggered.
4. light radiation synergistic catalyst according to claim 1 excites the flue gas mercury removal system of ozone/peroxide, it is characterized in that: the length C of described solution conduit is between 60cm-150cm, and the optimum length D of flue gas accelerating tube is between 50cm-130cm.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107497264A (en) * | 2017-09-30 | 2017-12-22 | 江苏大学 | Ozone United microwave excite can Magnetic Isolation catalyst simultaneous SO_2 and NO removal demercuration method and system |
| CN108310967A (en) * | 2018-02-01 | 2018-07-24 | 国家能源投资集团有限责任公司 | Flue gas mercury removal device and method |
-
2015
- 2015-04-21 CN CN201520245758.1U patent/CN204973597U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107497264A (en) * | 2017-09-30 | 2017-12-22 | 江苏大学 | Ozone United microwave excite can Magnetic Isolation catalyst simultaneous SO_2 and NO removal demercuration method and system |
| CN107497264B (en) * | 2017-09-30 | 2020-01-24 | 江苏大学 | Method and system for simultaneously desulfurizing, denitrifying and removing mercury by using ozone and microwave to excite magnetically separable catalyst |
| CN108310967A (en) * | 2018-02-01 | 2018-07-24 | 国家能源投资集团有限责任公司 | Flue gas mercury removal device and method |
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