CN204637987U - A kind of hydrogen sulfide removal system based on photocatalysis spray - Google Patents
A kind of hydrogen sulfide removal system based on photocatalysis spray Download PDFInfo
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Abstract
The utility model relates to a kind of hydrogen sulfide removal system based on photocatalysis spray, described system based on method be adopt ultraviolet cooperating catalyst decomposes peroxide to produce the hydroxyl of strong oxidizing property or potentiometric titrations as oxidant, clashing into the hydrogen sulfide in bed in oxidation removal flue gas.The high speed nozzle arranged by coaxial subtend respectively after mixing with catalyst granules from the flue gas of emission source sprays into shock bed.Meanwhile, peroxide solutions is sprayed into by atomizer and clashes in bed, and three strands of gas-liquid-solid mixtures, in shock bed, fully mixing occur, and mass transfer rate improves greatly.Ultraviolet cooperating catalyst decomposes peroxide produces hydroxyl or the potentiometric titrations oxidation removal hydrogen sulfide of strong oxidizing property, and the sulfuric acid solution that reaction produces enters after-treatment system and generates ammonium sulfate fertilizer; This system can realize the hydrogen sulfide stripping rate of 100%, and product recoverable, there is wide DEVELOPMENT PROSPECT.
Description
Technical field
The utility model relates to combustion product gases Environmental capacity field, is specifically related to a kind of hydrogen sulfide stripping method and system based on photocatalysis spray.
Background technology
Hydrogen sulfide is a kind of high irritating hypertoxic gas, is one of atmosphere pollution.Under aerobic and wet heat condition, hydrogen sulfide not only can cause equipment corrosion and catalyst poisoning, also can serious threat personal safety.Along with the fast development of economy and the raising of people's environmental consciousness, in industrial waste gas, hydrogen sulfide stripping problem more and more receives the concern of people.Country has also formulated the discharge of corresponding laws and regulations to hydrogen sulfide and has done strict restriction simultaneously.The efficient removal technology of research and development hydrogen sulfide has become the hot issue paid close attention to countries in the world.In the past few decades, domestic and international researcher has made large quantifier elimination to hydrogen sulfide stripping problem in waste gas and has developed many hydrogen sulfide stripping methods.According to the dry wet form of subtractive process, waste gas hydrogen sulfide stripping method can be divided into dry method and the large class of wet method two substantially.Dry method is the reproducibility and the combustibility that utilize hydrogen sulfide, carrys out desulfurization or directly burn with fixed oxygen agent or absorbent.The method comprises Claus method, non-renewable ADSORPTION IN A FIXED BED method, membrane separation process, sieve method, pressure-variable adsorption (PSA) method, low temperature processing etc.Desulfurizer therefor, catalyst mainly contain active carbon, iron oxide, zinc oxide, manganese dioxide and bauxite etc., the resources such as general recyclable sulphur, sulfur dioxide, sulfuric acid and sulfate.Dry removal process efficiency, compared with high but have that equipment investment is large, desulfurizing agent needs super regeneration and the deficiency such as sulfur capacity is low, is generally suitable for the meticulous desulfurization of gas.Although Claus method may be used for removing of high-concentration hydrogen sulfide, there is the deficiencies such as removal efficiency difference.
Wet method removing sulfuldioxide can be divided into chemical absorption method, Physical Absorption method, physical chemistry absorption process and wet oxidation process according to removal mechanism.Chemical absorption method utilizes the reversible reaction occurred between hydrogen sulfide and chemical solvent to remove hydrogen sulfide.Common method comprises amine method, hot carbonate method and ammonia process etc.Physical Absorption method utilizes different component dissolubility difference and remove hydrogen sulfide in specific solvent, then separates out hydrogen sulfide and absorbent regeneration by measures such as step-down flash distillations.Conventional physical solvent process comprises low-temp methanol method, polyglycol dimethyl ether process, N methylpyrrolidone process etc.Physical chemistry absorption process is that make it have the characteristic of two kinds of solvents concurrently, its Typical Representative is sulfone amine method by physical solvent and chemical solvent mixing.Wet oxidation process refers to and adopts oxidant to be that elemental sulfur or sulfuric acid solution reclaim by Oxidation of Hydrogen Sulfide.According to the difference of oxidation mechanism, wet oxidation process mainly can be divided into iron-based, vanadium base etc. for the catalytic oxidation of representative and the direct oxidation method that is representative with hydrogen peroxide, potassium permanganate etc.At present, also there is a lot of problem in hydrogen sulfide wet method removing process, and the various organic absorbent of such as new synthesis or oxidant Jia Ge Gao ﹑ performance Bu Wen are Dinged ﹑ and even also had toxicity.The oxidant reaction processes such as potassium permanganate can produce complicated accessory substance, cause product utilization difficulty.Although the clean environmental protection of the oxidants such as hydrogen peroxide, oxidation efficiency is very low, causes subtractive process cannot meet the environmental requirement of increasingly stringent.In sum, also do not have a kind of Wen to determine Ke Kao ﹑ economical and effective at present, and be suitable for the technique of middle low concentration gas hydrogen sulfide stripping.Therefore, while improving existing removing sulfuldioxide, the new waste gas hydrogen sulfide stripping technology of active development economical and efficient has most important theories and realistic meaning.
Summary of the invention
The utility model relates to a kind of hydrogen sulfide removal system based on photocatalysis spray, described deviate from system based on method be adopt ultraviolet cooperating catalyst decomposes peroxide to produce the hydroxyl of strong oxidizing property or potentiometric titrations as Oxidation of Hydrogen Sulfide agent, clashing into the hydrogen sulfide in bed in oxidation removal flue gas.
The utility model remove the course of reaction of system and principle as follows:
1, as shown in Figure 1, adopt electron spin resonance kaleidophon can be measured in ultraviolet cooperating metal oxide catalyst catalytic decomposition peroxide process and create hydroxyl and potentiometric titrations.Therefore, first ultraviolet cooperating metal oxide catalyst catalytic decomposition peroxide is release the hydroxyl and potentiometric titrations with strong oxidizing property, and detailed process can represent with following chemical reaction (1)-(3):
H
2o
2+ UV+ catalyst 2 × OH (1)
Oxidation of Hydrogen Sulfide in flue gas can remove by sulfate radical and the hydroxyl radical free radical of the strong oxidizing property 2, produced, and detailed process can represent with following chemical reaction (4)-(5):
2×OH+H
2S H
2SO
4+H
2O (4)
3, the sulfuric acid solution that reaction produces can be used as the raw material of industry and recycles.Such as, producing ammonium sulfate by adding ammonia neutralisation of sulphuric acid, obtaining the solid-state ammonium sulfate that can be used for agricultural fertilizer after utilizing residual heat from boiler fume evaporative crystallization, whole demercuration process non-secondary pollution.
For realizing above object, based on above-mentioned principle, the technical solution adopted in the utility model is as follows:
Based on a hydrogen sulfide removal system for photocatalysis spray, described system is provided with Pai Fang Yuan ﹑ Feng Ji ﹑ Tiao Wen Qi ﹑ Hun He Qi ﹑ and clashes into bed, Fa Men ﹑ Wuization Qi ﹑ atomizing pump one and atomizing pump Er ﹑ Chu Ye Xiang ﹑ Zai Sheng Ta ﹑ catalyst storage tower and circulating pump; Emission source is connected with the air inlet of thermosistor by flue, the outlet of thermosistor connects an entrance of blender, catalyst storage tower connects another entrance of blender, and blender is provided with two groups of outlets, and the high speed nozzle clashed on bed with left and right is respectively connected; Described shock bed is provided with Chu Wu Qi ﹑ ash disposal Qi ﹑ high speed Pen Zui ﹑ uviol lamp and quartz socket tube and atomizer from top to bottom successively; Described high speed nozzle and uviol lamp and quartz socket tube be located at clash into bed inwall on, be provided with outlet g bottom described shock bed, outlet g connects regenerator; The liquid reserve tank of described storage peroxide solutions is connected with the entrance e clashing into bed by connecting pipe, the connecting pipe that bed is clashed in described liquid reserve tank and left and right is respectively equipped with for peroxide solutions provides atomizing pump one, the atomizing pump two of power source; Described atomizer is located at and is clashed between ultraviolet lamp tube in bed and high speed nozzle, and peroxide solutions sprays into and enters shock bed after atomizer atomization.
The often group outlet of described blender is clashed into bed with left and right respectively and is connected, the outlet of described often group is connected with two flues, one of them flue connects the high speed nozzle entrance c clashing into bed, and another flue connects the high speed nozzle entrance d being arranged on the coaxial subtend layout of clashing into bed another side.
The top of described shock bed is provided with outlet i, and outlet i is connected with after-treatment system, and the gaseous by-products that oxidation produces enters after-treatment system by the i outlet of clashing into bed and generates ammonium sulfate fertilizer, and the flue gas through purification enters air.The bottom of described shock bed is provided with outlet f, and outlet f is connected with catalyst storage tower, and catalyst granules comes back to catalyst storage tower by clashing into bed outlet f, and then enters blender and clash into bed, and so circulation is carried out.
The bottom of described shock bed is provided with outlet g, and outlet g is connected with regenerator, and regenerator is connected with catalyst storage tower entrance; After catalyst runs a period of time inactivation, the catalyst of inactivation then exports g by shock bed and enters regenerator regeneration activating, and the catalyst after regeneration is sent into catalyst storage tower further and recycled.
Catalyst granules enters blender from the outlet a of catalyst storage tower, and flue gas also enters blender from the outlet b of emission source after thermosistor temperature adjustment, and flue gas and catalyst granules are divided into two strands of impartial air-flows after mixing in blender.Half air-flow sprays into shock bed by being arranged on high speed nozzle on one side through entrance c, and the high speed nozzle that second half air-flow is then arranged by the coaxial subtend being arranged on another side sprays into shock bed through entrance d.Meanwhile, the peroxide solutions from liquid reserve tank provides power by atomizing pump one, is sprayed in shock bed from entrance e by atomizer.There is fully mixing in three strands of gas-liquid-solid mixtures, mass transfer rate improves greatly in shock bed.Ultraviolet cooperating catalyst decomposes peroxide produces hydroxyl or the potentiometric titrations oxidation removal hydrogen sulfide of strong oxidizing property.The gaseous by-products that oxidation produces is exported by the i clashing into bed and enters after-treatment system generation ammonium sulfate fertilizer, and the flue gas through purification enters air.Catalyst granules comes back to catalyst storage tower by clashing into bed outlet f, and then enters blender and clash into bed, and so circulation is carried out.After catalyst runs a period of time inactivation, the catalyst of inactivation then exports g by shock bed and enters regenerator regeneration activating, and the catalyst after regeneration is sent into catalyst storage tower further and recycled.When one clashes into (such as left shock bed) when bed regenerates, for removing hydrogen sulfide, both are used alternatingly the shock bed (such as right shock bed) that another one is identical.
In described system, left and right shock bed is arranged symmetrically with, left and right is clashed into bed and is used alternatingly, two switchings of clashing between beds are controlled by valve one to six, and described valve one is located on the flue that blender is connected with left shock bed, and described valve two is located on the flue that blender is connected with right shock bed; Described catalyst storage tower exports with left shock bed catalyst the pipeline be connected and is provided with valve three, and described catalyst storage tower exports with right shock bed catalyst the pipeline be connected and is provided with valve five; The pipeline that described regenerator is connected with the catalyst outlet of the inactivation of left shock bed is provided with valve four, and the pipeline that described regenerator is connected with the catalyst outlet of the inactivation of right shock bed is provided with valve six.
When left shock bed is used for removing hydrogen sulfide, valve Yi ﹑ tri-﹑ tetra-opens, and Fa Men bis-﹑ Wu ﹑ six closes; When left shock bed is used for activating catalyst, valve Yi ﹑ tri-﹑ tetra-closes, and Fa Men bis-﹑ Wu ﹑ six then opens, and now right shock bed is used for removing hydrogen sulfide.
High speed Pen Zui ﹑ atomizer in shock bed and ultraviolet lamp tube all adopt multi-stage cross to arrange.High speed Pen Zui ﹑ atomizer layout alternate with ultraviolet lamp tube, and adjacent high speed Pen Zui ﹑ atomizer and ultraviolet lamp tube adopt and arrange in the same way.Vertical interval H between high speed nozzle adjacent two layers is between 10cm-100cm, and adjacent two-stage high speed nozzle adopts 90 degree of arranged crosswise staggered.Ultraviolet lamp tube is arranged in the central spot between adjacent two-stage high speed nozzle, and the ultraviolet lamp tube of adjacent two-stage adopts 90 degree of arranged crosswise staggered equally.Atomizer is arranged in the central spot between adjacent two-stage high speed nozzle and ultraviolet lamp tube, and the atomizer of adjacent two-stage also adopts 90 degree of arranged crosswise staggered.
The best smoke inlet temperature of clashing into bed is 70-160 DEG C, and effective liquid-gas ratio is 0.1-5.0L/m
3, the optium concentration of peroxide is between 0.2mol/L-2.0mol/L, and the pH of solution is between 1.0-7.0, and best solution temperature is 70-95 DEG C, and the content of sulfureous in flue gas hydrogen is not higher than 5000ppm, and ultraviolet light Net long wave radiation intensity is 20 μ W/cm
2-500 μ W/cm
2, ultraviolet EWL is 180nm-365nm.The atomization droplets diameter of the peroxide solutions of atomizer ejection is not more than 10 microns.The exit velocity of high speed nozzle the best is 5-25m/s.The optimum dosage of catalyst can add 0.1-5kg by every cubic metre of clashing into bed bioreactor volume.
Described emission source can be any one in Ran coal Guo Lu ﹑ La rubbish Fen Shao Lu ﹑ oil work She Bei ﹑ biomass combustion boiler and linked medical waste incinerator.Described peroxide is one or more the mixing in Shuan Yang Shui ﹑ Guo Liu Suan An ﹑ sodium peroxydisulfate and potassium peroxydisulfate.Described catalyst is one or more mixtures in Er Yangization Tai ﹑ Yangization Tie ﹑ bis-Yangization Meng ﹑ cupric oxide, also can be the support type of described catalyst, used carrier can be one or more the complex in Huo Tan ﹑ tri-Yangization Er Lv ﹑ Fen Shai ﹑ silica gel and biomass char.
Described after-treatment system is formed with tower ﹑ evaporating and crystallizing tower and smoke waste heat utilization system primarily of in ammonia.The gaseous products produced in shock bed, such as gaseous sulfuric acid and sulfur trioxide etc. export i by shock bed and first enter ammonia neutralizing tower reaction generation ammonium sulfate, the ammonium sulfate produced enters the evaporating and crystallizing tower of afterbody again, utilizes smoke waste heat utilization system evaporative crystallization to produce solid-state ammonium sulfate fertilizer and recycles.Described regenerator is a kind of regenerative system utilizing washing and fume afterheat activation, namely the catalyst of inactivation first rinses out all residues on catalyst through clear water, and then providing residual heat high-temperature activating catalyst by flue gas, the catalyst after regeneration is again sent into catalyst storage tower and is recycled.
Described blender is made up of electrically driven (operated) mechanical stirring kettle, drives paddle to stir, and then be sent to high speed nozzle and spray into shock bed after flue gas and catalyst enter blender by motor.
Advantage of the present utility model and remarkable result (with the contrast of existing patent):
1. Chinese patent (ZL201210075896.0) proposes the hydrogen sulfide stripping Method and process of hydrogen peroxide oxidation absorption and afterbody UF membrane, but the method hydrogen peroxide absorbent oxidability Cha ﹑ removal efficiency used is low, low concentration hydrogen sulphide can only be removed, and the film of afterbody is easily corroded by hydrogen peroxide, cause system cloud gray model expense height ﹑ system reliability poor.The oxidisability of the hydroxyl that the utility model utilizes ultraviolet cooperating catalyst decomposes peroxide to produce or potentiometric titrations is more much better than than hydrogen peroxide, and similar light decomposing system is in the existing successful operation case widely of water treatment field, therefore the operational reliability of native system is higher, technology is mature and reliable more.
2. Chinese patent (ZL 201310490922.0) proposes one and utilizes sodium carbonate absorbing hydrogen sulphide, and by the removal methods of oxygen recovery and technique, but the method complex process, and the sodium acid carbonate accessory substance containing impurity that reaction produces cannot recycling, and the technique that the utility model proposes is relatively simple, especially the product ammonium sulfate produced is a kind of good agricultural fertilizer, therefore whole subtractive process does not have secondary pollution.
3. Chinese patent (ZL201210410079.6) propose a kind of utilize iron system to remove agent catalytic decomposition hydrogen sulfide method and technique, but the method propose to remove agent preparation method very complicated, absorbent stability is not high, and process operation reliability described in the utility model is higher, the continuous operation of feasible system, has better prospects for commercial application.
Chinese patent (ZL201310648205.6) proposes a kind of method utilizing ionic liquid to catch hydrogen sulfide, but the method for synthesizing ionic liquid that the method uses is very complicated, and application cost is high, and absorbent properties is unstable, and product separation is difficult.The method that the utility model adopts is relatively simple, and subtractive process is reliable and stable, and application cost is lower.
Accompanying drawing explanation
Fig. 1 is the general figure of electron spin resonance light caught in the hydrogen sulfide stripping process based on photocatalysis spray.
Fig. 2 is technological process and the structure chart of the utility model system.
Fig. 3 is the structural representation that the utility model clashes into that in bed, high speed Pen Zui ﹑ atomizer and ultraviolet lamp tube two adjacent groups are arranged.
Fig. 4 is the schematic diagram of after-treatment system.
Fig. 5 is the structural representation of regenerator.
Fig. 6 is the structural representation of blender.
Fig. 7 is the structural representation of atomizer.
Detailed description of the invention
Below in conjunction with accompanying drawing, detailed description of the invention of the present utility model is further described.
As shown in Figure 2, based on the system of the hydrogen sulfide stripping method of photocatalysis spray, be provided with emission source 1 ﹑ blower fan 2 ﹑ thermosistor 3 ﹑ blender 4 ﹑ valve 9 ﹑ and clash into bed 8 ﹑ high speed nozzle 16 ﹑ atomizer 12 ﹑ uviol lamp 17 and quartzy sleeve pipe ﹑ demister 14 ﹑ soot blower 13 ﹑ atomizing pump 1 and atomizing pump 2 11 ﹑ liquid reserve tank 15 ﹑ regenerator 7 ﹑ catalyst storage tower 6 and circulating pump 5, after-treatment system 16.
As shown in Figure 3, the high speed nozzle 16 ﹑ atomizer 12 in shock bed and ultraviolet lamp tube 17 all adopt multi-stage cross to arrange.High speed nozzle 16 ﹑ atomizer 12 layout alternate with ultraviolet lamp tube 17, and adjacent high speed nozzle 16 ﹑ atomizer 12 and ultraviolet lamp tube 17 adopt and arrange in the same way.
Vertical interval H between high speed nozzle 16 adjacent two layers is between 10cm-100cm, and adjacent two-stage high speed nozzle adopts 90 degree of arranged crosswise staggered.Ultraviolet lamp tube 17 is arranged in the central spot between adjacent two-stage high speed nozzle 16, and the ultraviolet lamp tube 17 of adjacent two-stage adopts 90 degree of arranged crosswise staggered equally.
Atomizer 12 is arranged in the central spot between adjacent two-stage high speed nozzle 16 and ultraviolet lamp tube 17, and the atomizer of adjacent two-stage also adopts 90 degree of arranged crosswise staggered.
As shown in Figure 4, after-treatment system 18 is formed primarily of ammonia neutralizing tower 19 ﹑ evaporating and crystallizing tower 20 and smoke waste heat utilization system 21.The gaseous products produced in shock bed 8, first gaseous sulfuric acid and sulfur trioxide etc. enter the entrance m of after-treatment system 18 by the outlet i clashing into bed 8, ammonia neutralizing tower 19 is entered through solution circulation pump, what neutralizing tower 19 was provided with ammonia passes into a mouthful n, neutralization reaction produces ammonium sulfate, and the ammonium sulfate of generation enters the evaporating and crystallizing tower 20 of afterbody again, utilizes smoke waste heat utilization system 21 evaporative crystallization to produce solid-state ammonium sulfate, solid-state ammonium sulfate is recycled by exporting p, and solid-state ammonium sulfate can as fertilizer.
As shown in Figure 5, regenerator 7 is a kind of regenerative systems utilizing washing and fume afterheat activation, it is provided with storage tank 22, spray pump 23, washer jet 24, clear water in storage tank 22 introduces the washer jet 24 in regenerator 7 through spray pump 23, the catalyst of inactivation enters regenerator by entrance q1, the catalyst of inactivation first rinses out all residues on catalyst through clear water, and then provide residual heat high-temperature activating catalyst by flue gas, catalyst after regeneration is again sent into catalyst storage tower recycle by being exported q2, and the water that spray produces is discharged by discharge outlet q3.
As shown in Figure 6, blender 4 is made up of electrically driven (operated) mechanical stirring kettle, drive paddle 4-1 to stir by motor after flue gas enters blender 4 by the smoke inlet u1 of blender and catalyst u2, be then sent to high speed nozzle 16 again by mixer outlet u3 and spray into and clash into bed 8.
As shown in Figure 7, atomizer 12 is cylindric atomizer, and the hole on atomizer is micron order aperture 12-1, and micron order aperture is used for atomized soln, and atomizer is provided with peroxide solutions entrance 12-3.
Course of reaction is as follows:
Catalyst granules enters blender 4 from the outlet a of catalyst storage tower 6, flue gas introduces thermosistor 3 from the outlet b of emission source 1 by blower fan 2, flue gas also enters blender 4 after thermosistor 3 temperature adjustment, flue gas and catalyst granules are divided into two strands of impartial air-flows after mixing in blender 4: half air-flow by arrange clash into bed 8 high speed nozzle 16 to spray into through entrance c and clash into bed 8, second half air-flow then sprays into shock bed 8 by being arranged on the high speed nozzle 16 that the coaxial subtend of clashing into bed 8 another side arranges through entrance d.Meanwhile, the peroxide solutions from liquid reserve tank 15 provides power by atomizing pump 1, is sprayed in shock bed 8 from the entrance e clashing into bed 8 by atomizer 12.
There is fully mixing in three strands of gas-liquid-solid mixtures, mass transfer rate improves greatly in shock bed 8.Ultraviolet cooperating catalyst decomposes peroxide produces hydroxyl or the potentiometric titrations oxidation removal hydrogen sulfide of strong oxidizing property.
The gaseous by-products that oxidation produces enters after-treatment system 16 by the i outlet of clashing into bed 8 and generates ammonium sulfate fertilizer, and the flue gas through purification enters air.
Catalyst granules exports f come back to catalyst storage tower 6 by clashing into bed 8, and then enters blender 4 and clash into bed 8, and so circulation is carried out.
After catalyst runs a period of time inactivation, the catalyst of inactivation then exports g by shock bed 8 and enters regenerator 7 regeneration activating, and the catalyst after regeneration is sent into catalyst storage tower 6 further and recycled.
When one clashes into (such as left shock bed 8-1) when bed 8 regenerates, for removing hydrogen sulfide, both are used alternatingly the identical shock bed 8 (such as right shock bed 8-2) of another one.
This removes system and is located at two and clashes into bed 8 i.e. left shock bed 8-1 and right shock bed 8-2, and when a shock bed 8 regenerates, the identical shock bed 8 of another one is for removing hydrogen sulfide, and both are used alternatingly.
Two switchings of clashing between bed 8 are controlled by valve one to six (9-1 to 9-6), and described valve one 9-1 is located at blender 4 with on the exhaust gases passes of left shock bed 8-1, and described valve two 9-2 is located at blender 4 with on the exhaust gases passes of right shock bed 8-2; Described valve three 9-3 is located on the recovery inlet duct of catalyst outlet f bottom left shock bed 8-1 and catalyst storage tower 6; Described valve five 9-5 is located on the recovery inlet duct of catalyst outlet bottom right shock bed 8-2 and catalyst storage tower 6; Described valve four 9-4 is located on the pipeline of the recovery entrance of catalyst outlet g and regenerator 7 bottom left shock bed 8-1; Described valve six 9-6 is located on the pipeline of the recovery entrance of catalyst outlet and regenerator 7 bottom right shock bed 8-2.
The best smoke inlet temperature of clashing into bed is 70-160 DEG C, and effective liquid-gas ratio is 0.1-5.0L/m
3, the optium concentration of peroxide is between 0.2mol/L-2.0mol/L, and the pH of solution is between 1.0-7.0, and best solution temperature is 70-95 DEG C, and the content of sulfureous in flue gas hydrogen is not higher than 5000ppm, and ultraviolet light Net long wave radiation intensity is 20 μ W/cm
2-500 μ W/cm
2, ultraviolet EWL is 180nm-365nm.The atomization droplets diameter of the peroxide solutions of atomizer ejection is not more than 10 microns.The exit velocity of high speed nozzle the best is 5-25m/s.
The optimum dosage of catalyst can add 0.1-5kg by every cubic metre of clashing into bed bioreactor volume.Described emission source can be any one in Ran coal Guo Lu ﹑ La rubbish Fen Shao Lu ﹑ oil work She Bei ﹑ biomass combustion boiler and linked medical waste incinerator.
Described peroxide is one or more the mixing in Shuan Yang Shui ﹑ Guo Liu Suan An ﹑ sodium peroxydisulfate and potassium peroxydisulfate.Described catalyst is one or more mixtures in Er Yangization Tai ﹑ Yangization Tie ﹑ bis-Yangization Meng ﹑ cupric oxide, also can be the support type of described catalyst, used carrier can be one or more the complex in Huo Tan ﹑ tri-Yangization Er Lv ﹑ Fen Shai ﹑ silica gel and biomass char.
The smoke inlet temperature that embodiment 1. clashes into bed is 100 DEG C, and liquid-gas ratio is 0.5L/m
3, titanium dioxide dosage is 0.1kg/m
3, hydrogen peroxide concentration is 0.5mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and sulfureous in flue gas hydrogen content is 300ppm, and ultraviolet light Net long wave radiation intensity is 25 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: hydrogen sulfide stripping efficiency reaches 58.2%.
The smoke inlet temperature that embodiment 2. clashes into bed is 100 DEG C, and liquid-gas ratio is 0.5L/m
3, titanium dioxide dosage is 0.1kg/m
3, ammonium persulfate concentrations is 0.5mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and sulfureous in flue gas hydrogen content is 300ppm, and ultraviolet light Net long wave radiation intensity is 25 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: hydrogen sulfide stripping efficiency reaches 50.8%.
The smoke inlet temperature that embodiment 3. clashes into bed is 100 DEG C, and liquid-gas ratio is 0.5L/m
3, titanium dioxide dosage is 0.3kg/m
3, hydrogen peroxide concentration is 0.5mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and sulfureous in flue gas hydrogen content is 300ppm, and ultraviolet light Net long wave radiation intensity is 25 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: hydrogen sulfide stripping efficiency reaches 67.2%.
The smoke inlet temperature that embodiment 4. clashes into bed is 100 DEG C, and liquid-gas ratio is 0.5L/m
3, titanium dioxide dosage is 0.3kg/m
3, ammonium persulfate concentrations is 0.5mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and sulfureous in flue gas hydrogen content is 300ppm, and ultraviolet light Net long wave radiation intensity is 25 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: hydrogen sulfide stripping efficiency reaches 65.1%.
The smoke inlet temperature that embodiment 5. clashes into bed is 100 DEG C, and liquid-gas ratio is 0.5L/m
3, titanium dioxide dosage is 0.5kg/m
3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and sulfureous in flue gas hydrogen content is 300ppm, and ultraviolet light Net long wave radiation intensity is 78 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: hydrogen sulfide stripping efficiency reaches 92.2%.
The smoke inlet temperature that embodiment 6. clashes into bed is 100 DEG C, and liquid-gas ratio is 0.5L/m
3, titanium dioxide dosage is 0.5kg/m
3, ammonium persulfate concentrations is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and sulfureous in flue gas hydrogen content is 300ppm, and ultraviolet light Net long wave radiation intensity is 78 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: hydrogen sulfide stripping efficiency reaches 87.3%.
The smoke inlet temperature that embodiment 7. clashes into bed is 100 DEG C, and liquid-gas ratio is 1.0L/m
3, titanium dioxide dosage is 1.0kg/m
3, hydrogen peroxide concentration is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and sulfureous in flue gas hydrogen content is 300ppm, and ultraviolet light Net long wave radiation intensity is 108 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: hydrogen sulfide stripping efficiency reaches 100%.
The smoke inlet temperature that embodiment 8. clashes into bed is 100 DEG C, and liquid-gas ratio is 1.0L/m
3, titanium dioxide dosage is 1.0kg/m
3, ammonium persulfate concentrations concentration is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and sulfureous in flue gas hydrogen content is 300ppm, and ultraviolet light Net long wave radiation intensity is 108 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: hydrogen sulfide stripping efficiency reaches 100%.
The smoke inlet temperature that embodiment 9. clashes into bed is 100 DEG C, and liquid-gas ratio is 1.0L/m
3, iron oxide dosage is 1.0kg/m
3, ammonium persulfate concentrations concentration is 1.0mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and sulfureous in flue gas hydrogen content is 300ppm, and ultraviolet light Net long wave radiation intensity is 108 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: hydrogen sulfide stripping efficiency reaches 100%.
The smoke inlet temperature that embodiment 10. clashes into bed is 100 DEG C, and liquid-gas ratio is 0.5L/m
3, iron oxide dosage is 0.3kg/m
3, hydrogen peroxide concentration is 0.5mol/L, and pH value of solution is 3.4, and solution temperature is 70 DEG C, and sulfureous in flue gas hydrogen content is 300ppm, and ultraviolet light Net long wave radiation intensity is 25 μ W/cm
2, ultraviolet EWL is 254nm.Pilot run is: hydrogen sulfide stripping efficiency reaches 100%.
Comprehensive Correlation through above embodiment is known, and embodiment 8-10 has removal effect relatively preferably, and hydrogen sulfide stripping efficiency all reaches 100%, can be used as embodiment and consults and uses.
Claims (7)
1. based on a hydrogen sulfide removal system for photocatalysis spray, it is characterized in that: described system is provided with row and puts source ﹑ wind machine ﹑ and adjust the mixed device ﹑ that closes of warm device ﹑ to clash into bed, valve door ﹑ mist device ﹑ atomizing pump one and atomizing pump two ﹑ and store up liquid case ﹑ raw tower ﹑ catalyst storage tower and circulating pump again; Emission source is connected with the air inlet of thermosistor by flue, the outlet of thermosistor connects an entrance of blender, catalyst storage tower connects another entrance of blender, and blender is provided with two groups of outlets, and the high speed nozzle clashed on bed with left and right is respectively connected; Described shock bed is provided with Chu Wu Qi ﹑ ash disposal Qi ﹑ high speed Pen Zui ﹑ uviol lamp and quartz socket tube and atomizer from top to bottom successively; Described high speed nozzle and uviol lamp and quartz socket tube be located at clash into bed inwall on, be provided with outlet g bottom described shock bed, outlet g connects regenerator; The liquid reserve tank of described storage peroxide solutions is connected with the entrance e clashing into bed by connecting pipe, the connecting pipe that bed is clashed in described liquid reserve tank and left and right is respectively equipped with for peroxide solutions provides atomizing pump one, the atomizing pump two of power source; Described atomizer is located at and is clashed between ultraviolet lamp tube in bed and high speed nozzle, and peroxide solutions sprays into and enters shock bed after atomizer atomization.
2. a kind of hydrogen sulfide removal system based on photocatalysis spray according to claim 1, it is characterized in that: the often group outlet of described blender is clashed into bed with left and right respectively and is connected, the outlet of described often group is connected with two flues, one of them flue connects the high speed nozzle entrance c clashing into bed, and another flue connects the high speed nozzle entrance d being arranged on the coaxial subtend layout of clashing into bed another side.
3. a kind of hydrogen sulfide removal system based on photocatalysis spray according to claim 1, it is characterized in that: the top of described shock bed is provided with outlet i, outlet i is connected with after-treatment system, the gaseous by-products that oxidation produces is exported by the i clashing into bed and enters after-treatment system generation ammonium sulfate fertilizer, and the flue gas through purification enters air.
4. a kind of hydrogen sulfide removal system based on photocatalysis spray according to claim 1, it is characterized in that: the bottom of described shock bed is provided with outlet f, outlet f is connected with catalyst storage tower, catalyst granules comes back to catalyst storage tower by clashing into bed outlet f, and then enter blender and clash into bed, so circulation is carried out.
5. a kind of hydrogen sulfide removal system based on photocatalysis spray according to claim 1, is characterized in that: the bottom of described shock bed is provided with outlet g, and outlet g is connected with regenerator, and regenerator is connected with catalyst storage tower entrance; After catalyst runs a period of time inactivation, the catalyst of inactivation then exports g by shock bed and enters regenerator regeneration activating, and the catalyst after regeneration is sent into catalyst storage tower further and recycled.
6. a kind of hydrogen sulfide removal system based on photocatalysis spray according to claim 1, it is characterized in that: in described system, left and right shock bed is arranged symmetrically with, left and right is clashed into bed and is used alternatingly, two switchings of clashing between bed are controlled by valve one to six, described valve one is located on the flue that blender is connected with left shock bed, and described valve two is located on the flue that blender is connected with right shock bed; Described catalyst storage tower exports with left shock bed catalyst the pipeline be connected and is provided with valve three, and described catalyst storage tower exports with right shock bed catalyst the pipeline be connected and is provided with valve five; The pipeline that described regenerator is connected with the catalyst outlet of the inactivation of left shock bed is provided with valve four, and the pipeline that described regenerator is connected with the catalyst outlet of the inactivation of right shock bed is provided with valve six.
7. a kind of hydrogen sulfide removal system based on photocatalysis spray according to claim 6, it is characterized in that: when left shock bed is used for removing hydrogen sulfide, valve Yi ﹑ tri-﹑ tetra-opens, and Fa Men bis-﹑ Wu ﹑ six closes; When left shock bed is used for activating catalyst, valve Yi ﹑ tri-﹑ tetra-closes, and Fa Men bis-﹑ Wu ﹑ six then opens, and now right shock bed is used for removing hydrogen sulfide.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110721567A (en) * | 2019-10-10 | 2020-01-24 | 上海鸿来环保设备有限公司 | Be applicable to lavatory developments dry process deodorization equipment |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110721567A (en) * | 2019-10-10 | 2020-01-24 | 上海鸿来环保设备有限公司 | Be applicable to lavatory developments dry process deodorization equipment |
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