CN105833676A - Method and device for removing VOCs (Volatile Organic Compounds) in waste gas by light radiation on chlorine atoms and hydroxyl - Google Patents
Method and device for removing VOCs (Volatile Organic Compounds) in waste gas by light radiation on chlorine atoms and hydroxyl Download PDFInfo
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- CN105833676A CN105833676A CN201610239751.8A CN201610239751A CN105833676A CN 105833676 A CN105833676 A CN 105833676A CN 201610239751 A CN201610239751 A CN 201610239751A CN 105833676 A CN105833676 A CN 105833676A
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- 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
- B01D53/38—Removing components of undefined structure
- B01D53/44—Organic components
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- 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
- B01D53/78—Liquid phase processes with gas-liquid contact
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- 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
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
The invention provides a method and device for removing VOCs (Volatile Organic Compounds) in waste gas by light radiation on chlorine atoms and hydroxyl. According to the method, hypochlorous acid is decomposed by ultraviolet light radiation to generate chlorine atoms and hydroxyl, which then are used as an oxidant of the VOCs and are used for oxidizing and removing the VOCs in flue gas in a photolysis desorption bed. The system has an extremely high oxidization property, and can obtain a 100% removing rate of VOCs; and in a removing process, no secondary pollution is caused, and the system has a wide market application prospect.
Description
Technical field
The present invention relates to combustion product gases pollutant catabolic gene field, be specifically related in a kind of light radiation chlorine atom and hydroxyl removing waste gas
The method and device of VOCs.
Background technology
VOCs is the english abbreviation of VOC (Volatile Organic Compounds).Numerous studies show,
After VOCs enters human body by respiratory tract and skin, cause temporary and permanent can to the organs such as the breathing of people, blood, liver
Venereal disease becomes (such as can cause various blood disease and cancer).Industrial production can produce various organic compounds, mainly include various
Hydro carbons, alcohols, aldehydes, acids, ketone and amine etc., these organic exhaust gas can cause atmosphere pollution, is detrimental to health.
Along with economic fast development and the raising of people's environmental consciousness, in tail gas, VOCs removing problem is increasingly paid close attention to by people.
Simultaneously country has also formulated corresponding laws and regulations the discharge capacity of VOCs has been made strict restriction.Research and development VOCs's is efficient
Removing sulfuldioxide has become the hot issue that countries in the world are paid close attention to.
In the past few decades, VOCs removing problem in waste gas has been made substantial amounts of research and has developed by domestic and international researcher
Multiple VOCs removal methods.According to the general principle of removing, waste gas VOCs removal methods mainly includes that condensing absorption method inhales
Receipts method direct combustion method Production by Catalytic Combustion Process and absorption method etc..Condensation absorption method is applicable to that organic exhaust gas concentration is high, temperature is low,
The operating mode that air quantity is little, needs attached freezing equipment, is mainly used in pharmacy, chemical industry, and the less employing of printing enterprise, should
Limited to by scope.What absorption process was conventional is Physical Absorption, i.e. introduces exhaust gas into absorbing liquid and purifies, warp after liquid to be absorbed is saturated
Heat, resolve, condense recovery.This method is applicable to the waste gas of atm number, low temperature, low concentration, but need to be equipped with and add pyrolysis
Analysis retracting device, equipment volume is big, investment is higher.Directly combustion method is to utilize the aid fuel combustion such as combustion gas or fuel oil, will be mixed
Conjunction gas heats, and makes harmful substance be decomposed into innocuous substance under high temperature action.The method technique is simple, it is little to invest, it is adaptable to
High concentration, the waste gas of little air quantity, but safe practice, operation are required higher.Production by Catalytic Combustion Process is through catalysis combustion waste gas heating
Burn and change into carbon dioxide and the water of harmless odorless, this method initiation temperature is low, energy-conservation, purifying rate is high, easy to operate, account for
Ground area is few, be applicable to high temperature or the organic exhaust gas of high concentration, but the easy poisoning and deactivation of catalyst, poor stability.Activated carbon is inhaled
Attached method removal efficiency is up to 95%, and equipment is simple, it is little to invest, but activated carbon is changed frequently, adds handling, transports, changes
Etc. working procedure, operating cost is caused to increase.Therefore, up to the present, be developed despite multiple VOCs removing sulfuldioxide and
Utilize, but each technology nearly all has the restriction of range of application and has shortcomings.Therefore, continual exploitation is the most effective
VOCs removing sulfuldioxide have important practical significance.
Summary of the invention
For Shortcomings in prior art, the invention provides VOCs in a kind of light radiation chlorine atom and hydroxyl removing waste gas
Method and device.
The present invention realizes above-mentioned technical purpose by techniques below means.
The device of VOCs in a kind of light radiation chlorine atom and hydroxyl removing waste gas, it is characterised in that: it is provided with a photodissociation adsorbent bed,
Described photodissociation adsorbent bed is an airtight reactor, has the product separating tank for containing water in described reactor, described point
Be provided with product recovery port from groove bottom, described reactor wall is provided with smoke inlet exhanst gas outlet chlorine inlet fluid infusion mouth,
In described chlorine inlet extends to reactor and connect with the aeration tube that can be positioned at below liquid level, also set up in described reactor
There is the uviol lamp being loaded on adsorbing separation post on sidewall, being loaded on reactor top board, outside uviol lamp, be cased with quartz socket tube, described suction
The surface of attached splitter is provided with activated carbon fiber, and adsorbing separation post is connected with power transmission shaft and is connected with sidewall of reactor revolute pair,
The latter half of described adsorbing separation post can be immersed in below liquid level.
Further, also include that ultrasonic cleaning equipment, described ultrasonic cleaning equipment are in below liquid level and are positioned at adsorbing separation
The ultrasonic transmitter of post bottom.
Further, it is characterised in that: described exhanst gas outlet is connected with chlorine knockout tower, described chlorine knockout tower and chimney breast
Connect with chlorine inlet.
Further, described adsorbing separation element of a cylinder and reactor top plate contact, both ends of the surface contact with sidewall of reactor.
Further, the quantity of described adsorbing separation post is 1-6, and the quantity of uviol lamp is also multiple, and adsorbing separation post (10)
And uviol lamp interval is arranged.
Further, longitudinal pitch A between adsorbing separation post and uviol lamp is between 15cm-25cm；Uviol lamp and ultraviolet
Optimal lateral space D between lamp is between 10cm-30cm；Smoke inlet spacing C is between 15cm-40cm；Chlorine
The bubble mean diameter that aeration tube bloats is not more than 100 microns；Adsorbing separation element cylinder enters the depth B of solution and is positioned at
5cm-10cm；Uviol lamp and quartz socket tube insert below liquid level more than 10cm；Ultrasonic transmitter and adsorbing separation post bottom position
End face keeps vertical range 2cm-5cm centimetre；The diameter of adsorbing separation post is 30cm-90cm.
A kind of method of VOCs in light radiation chlorine atom and hydroxyl removing waste gas, it is characterised in that comprise the following steps:
(1) chlorine is sprayed into by chlorine aeration tube by chlorine inlet and forms hypochlorite solution in water, the activated carbon on adsorbing separation post
Fiber is by having hypochlorous acid from the teeth outwards after rotating immersion hypochlorite solution；Under ultraviolet radiation, the work of adsorbing separation post
Property carbon fiber surface hypochlorous acid decompose and produce high activity chlorine atom and hydroxyl；
(2) containing VOCs flue gas from smoke inlet enter light radiation absorption washing bed and with the activated carbon fiber on adsorbing separation post
Contact, the activated carbon fiber surface on adsorbing separation post of the mercury VOCs in flue gas and hydroxyl generation oxidation reaction, generate organic
Carbon slag and CO2,
Organic carbon slag is fixed on activated carbon fiber surface, CO2Air is entered with flue gas；
(3) after adsorbing separation post continues to rotate and be again dipped into solution, the absorption organic carbon slag on activated carbon fiber surface comes off
Rear entrance solution, thus complete continual removing VOCs and washing process, the product separating tank bottom the entrance of organic carbon slag
After, can sink to separating because of self gravitation reason, be recycled.
Further, in described step (3), mercury oxidation product comes off is to use supersonic oscillations mode, in described step (1)
Also including the process using chlorine knockout tower to reclaim chlorine, the chlorine of recovery enters aeration tube again by chlorine inlet.
Further, in described step, adsorbing separation post is in counterclockwise rotating, and the rolling tangential speed of adsorbing separation post
Direction is in opposite direction with flow of flue gas.
Further, the rotating speed r of adsorbing separation post is between 5 revs/min-30 revs/min；Smoke inlet temperature is not higher than
200 DEG C, solution is 1L/m with the liquid-gas ratio of flue gas3-25m3L/m3；The dosage of chlorine is 0.3L (chlorine volume)/m3(molten
Liquid amasss)-5.0L (chlorine volume)/m3Between (liquor capacity), the pH of solution is not higher than 5.5；Solution temperature is general not
Higher than 65 DEG C；Ultraviolet light Net long wave radiation intensity is 30 μ W/cm2-200μW/cm2；The EWL of ultraviolet light should be maintained at
180nm-366nm。
In light radiation chlorine atom of the present invention and hydroxyl removing waste gas, the method for VOCs, is to use ultraviolet radiation decomposition time
Chloric acid produces chlorine atom and the hydroxyl oxidant as VOCs, the VOCs in oxidation removal flue gas in photodissociation adsorbent bed.Come
Enter photodissociation adsorbent bed containing VOCs flue gas from smoke inlet from commercial plant and connect with the activated carbon fiber on adsorbing separation post
Touch.Chlorine is sprayed into by chlorine aeration tube by chlorine inlet and forms hypochlorite solution in water.Activated carbon fiber on adsorbing separation post
By having hypochlorous acid after rotating immersion solution from the teeth outwards.Activated carbon fiber under ultraviolet radiation, on adsorbing separation post
Surface can produce high activity chlorine atom and hydroxyl because hypochlorous acid decomposes.VOCs in flue gas can activity on adsorbing separation post
Carbon fiber surface and hydroxyl generation oxidation reaction, and it is fixed on activated carbon fiber surface.When adsorbing separation post continues to rotate also
After being again dipped into solution, adsorbing superincumbent VOCs oxidation product can enter solution after coming off because of supersonic oscillations, thus complete
Become continual removing VOCs process.The oxidation product of VOCs is mainly CO2Precipitating with organic carbon residue, organic carbon is residual
Can sink to separating because of self gravitation reason after product separating tank bottom slag precipitation entrance, thus be recycled, CO2The most adjoint
Flue gas enters air.In flue gas, the chlorine of residual can be by the chlorine knockout tower absorption and separation of afterbody cycling and reutilization.
This system has extremely strong oxidisability, it is possible to realize the VOCs removal efficiency of 100%, and subtractive process non-secondary pollution, tool
There are the plurality of advantages such as equipment is simple, initial cost is little, de-VOCs efficiency subtractive process non-secondary pollution high, whole, have wide
Development and application prospect.
Accompanying drawing explanation
Fig. 1 is the ESR spectrum figure of light radiation chlorine atom and hydroxyl.
Fig. 2 is front view and the structural representation of photodissociation adsorbent bed in the present invention.
Fig. 3 is left view and the structural representation of photodissociation adsorbent bed in the present invention.
Fig. 4 is the fluorescent tube arrangement schematic diagram of photodissociation adsorbent bed in the present invention.
In figure:
1-smoke inlet, 2-chlorine inlet, 3-exhanst gas outlet, 4-aeration tube, 5-uviol lamp, 6-product recovery port, 7-fluid infusion mouth,
8-product separating tank, 9-chlorine knockout tower, 10-adsorbing separation post, 11-reactor, 12-ultrasonic cleaning equipment, 13-ultrasound emission
Device, 14-reactor top board, 15-sidewall of reactor, 16-power transmission shaft.
Detailed description of the invention
Below in conjunction with the accompanying drawings and specific embodiment the present invention is further illustrated, but protection scope of the present invention is not limited to
This.
As in figure 2 it is shown, light radiation chlorine atom of the present invention and hydroxyl remove the device of VOCs in waste gas, it is provided with a light
Desorption bed, described photodissociation adsorbent bed is an airtight reactor 11, has the product for containing water in described reactor 11
Thing separating tank 8, described separating tank bottom is provided with product recovery port 6, and described reactor 11 wall is provided with smoke inlet 1 flue gas
Export 3 chlorine inlet 2 fluid infusion mouths 7, in described chlorine inlet 2 extends to reactor 11 and with can be positioned at liquid level with
Under aeration tube 4 connect, described exhanst gas outlet 3 is connected with chlorine knockout tower 9, described chlorine knockout tower 9 and chimney breast and
Chlorine inlet 2 connects.It is additionally provided with in described reactor 11 and is loaded on adsorbing separation post 10 on sidewall, be loaded on reactor top board 14
On uviol lamp 5, uviol lamp 5 is outside is cased with quartz socket tube, and the surface of described adsorbing separation post 10 is provided with activated carbon fiber, inhales
Attached splitter 10 is connected with power transmission shaft 16 and is connected with sidewall of reactor 15 revolute pair, the lower half of described adsorbing separation post 10
Part can be immersed in below liquid level.
As shown in Figure 3 and Figure 4, the bus of described adsorbing separation post 10 and reactor top board 14 keep being fully contacted, both ends of the surface
Keep being fully contacted, to prevent flue gas from escaping from gap rather than through activated carbon fiber adsorption layer with sidewall of reactor 15.Root
According to flue gas flow and VOCs entrance concentration, the quantity of described adsorbing separation post 10 can be 1-6, and usual flue gas flow is the biggest,
VOCs entrance concentration is the highest, and adsorbing separation post quantity is the most, and the emission request with specific reference to on-the-spot test and VOCs determines
The quantity of adsorbing separation post, cannot meet removal efficiency requirement very little, can strengthen reactor volume too much, and increase system is run into
This.The quantity of uviol lamp 5 is also multiple, and adsorbing separation post 10 and uviol lamp 5 interval are arranged.
Being additionally provided with ultrasonic cleaning equipment 12 in reactor, described ultrasonic cleaning equipment 12 is in below liquid level and is positioned at absorption
The ultrasonic transmitter 13 of splitter 10 bottom.Absorption organic carbon residue on adsorbing separation post 10, is come off by ultrasonic cleaning
To solution.
In photodissociation adsorbent bed, the concrete grammar of the VOCs in oxidation removal flue gas is: chlorine is passed through aeration tube by chlorine inlet 2
4 spray into formation hypochlorite solution in water.Activated carbon fiber on adsorbing separation post 10 is by meeting after rotating immersion solution from the teeth outwards
With hypochlorous acid.Under ultraviolet radiation, the activated carbon fiber surface on adsorbing separation post 10 can produce height because hypochlorous acid decomposes
Active chlorine atom and hydroxyl.Fig. 1 show employing electron spin resonance spectrometer and can be measured in the ultraviolet radiation chlorine aqueous solution
Create chlorine atom and hydroxyl.Detailed process can represent with following chemical reaction (1)-(6):
Cl·+H2O→OH-+·OH (5)
·O-++H2O→OH-+·OH (6)
Enter photodissociation adsorbent bed from smoke inlet 1 from commercial plant containing VOCs flue gas and with the activity on adsorbing separation post 10
Carbon fiber contacts.VOCs in flue gas can activated carbon fiber surface on adsorbing separation post 10 and hydroxyl generation oxidation reaction.
Having the simple substance VOCs in the hydroxyl oxidable removing flue gas of active character, detailed process can represent with following chemical reaction (7):
VOCs+n OH → organic carbon residue ↓+CO2 (7)
The oxidation product of VOCs is mainly CO2With organic carbon residue, organic carbon slag is fixed on activated carbon fiber surface, CO2
Air is entered with flue gas.After adsorbing separation post 10 continues to rotate and be again dipped into solution, adsorb superincumbent organic carbon slag meeting
Because supersonic oscillations enter solution after coming off, thus complete continual removing VOCs process.Organic carbon residue precipitate into
Can sink to separating because of self gravitation reason after entering the product separating tank 8 of bottom, thus be recycled, CO2Then arrange with flue gas
Enter air.In flue gas, the chlorine of residual can be by chlorine knockout tower 9 absorption and separation of afterbody cycling and reutilization.This system has pole
Strong oxidisability, it is possible to realize the VOCs removal efficiency of 100%, and subtractive process non-secondary pollution, has wide market application
Prospect.
In photodissociation adsorbent bed, longitudinal pitch A between adsorbing separation post 10 and uviol lamp 5 then cannot ensure light radiation too greatly
Uniformity and radiation intensity, the least then energy consumption is too high, and uviol lamp 5 input cost is greatly increased, therefore adsorbing separation post 10 and ultraviolet
Optimal longitudinal pitch A between lamp 5 is between 15cm-25cm.In like manner, the optimal horizontal stroke between uviol lamp 5 and uviol lamp 5
To space D between 10cm-30cm.Smoke inlet 1 spacing C too conference causes smoke distribution uneven, and the least meeting is made
Becoming flow of flue gas disorderly, flow resistance increases, therefore smoke inlet 1 optimal spacing C is between 15cm-40cm.Chlorine aeration
The bubble diameter that pipe 4 bloats cannot meet the most greatly enough gas liquid interfacial area, therefore the bubble that chlorine aeration tube 4 bloats is the most straight
Footpath is not more than 100 microns.Adsorbing separation post 10 bus enters the vertical range of solution or depth B is the least cannot provide enough
NACF wetting areas, oversize, rotation and VOCs capturing efficiency can be reduced, therefore adsorbing separation post 10 bus enters molten
The optimal vertical range of liquid or depth B should be positioned at 5cm-10cm.Uviol lamp 5 and quartz socket tube should insert below liquid level 10cm
Above, to ensure that uviol lamp 5 washes away lower acquisition efficient liquid phase cooling effect at high-temperature flue gas, liquid cooling effectiveness is the highest
In flue gas cooling effect.Ultrasonic transmitter 13 keeps vertical range 2cm-5cm centimetre with the end face of adsorbing separation post 10 bottom position,
Because Cavitation effect the most closely can be caused, destroy ultrasonic probe, too far then reduce cleaning oscillation effect.Adsorbing separation post 10 is necessary
In counterclockwise rotating, and the rolling tangential velocity attitude of adsorbing separation post 10 is in opposite direction with flow of flue gas, the most permissible
Ensure that with flue gas stream be countercurrent direction, thus heat and mass transfer enhancement, improve capturing efficiency.The diameter of adsorbing separation post 10 is the least
Activated carbon pricker dimension can be caused to lay area the least, catch area and efficiency declines, diameter then adds reactor volume too greatly,
Therefore the optimum diameter of adsorbing separation post 10 is 30cm-90cm.Adsorbing separation post 10 rotating speed is the lowest, and single rotates and catches and reaction
Time is the longest, and single removal effect improves, but the lowest meeting of rotating speed causes system entirety removal efficiency to decline, therefore adsorbing separation post
The optimum speed r of 10, between 5 revs/min-30 revs/min, specifically also needs to come according to on-the-spot emission request and removal efficiency
Determine optimized rotating speed.
The highest meeting of smoke inlet 1 temperature causes uviol lamp 5 operating efficiency to be greatly reduced, and increases the cooling difficulty of solution, reduces chlorine
The solubility of gas and utilization rate, and aggravate hypochlorous selfdecomposition, therefore smoke inlet 1 temperature is not above 200 DEG C.Solution with
The highest meeting of liquid-gas ratio of flue gas causes the treatment quantity of unit reactor to increase considerably, and then causes removal efficiency to decline, and
Solution is the lowest with the liquid-gas ratio of flue gas, and reactor can be caused to make full use of, and utilization rate reduces, therefore solution and flue gas is optimal
Liquid-gas ratio is 1L/m3-25L/m3.Chlorine addition amount improves can improve hypochlorous concentration in solution, promotes that chlorine atom and hydroxyl produce
Rate improves, thus improves the removal efficiency of VOCs, but the escape amount that the highest meeting of dosage causes chlorine in tail gas is greatly improved,
Thus increase separating difficulty and the cost of afterbody chlorine knockout tower, thus the optimum dosage of chlorine is 0.3L (chlorine volume)/m3
(liquor capacity)-5.0L (chlorine volume)/m3Between (liquor capacity).The pH of solution is the highest can accelerate hypochlorous acid selfdecomposition,
Therefore it is generally not more than 5.5.The highest meeting of solution temperature causes hypochlorous acid to accelerate selfdecomposition, and reduces the solubility of VOCs, thus
Reduce removal efficiency, therefore solution temperature is generally not more than 65 DEG C.In flue gas, the concentration of VOCs is more than 1000mg/m3Shi Huida is not
To removing requirement, therefore in flue gas, VOCs concentration should be less than 1000mg/m3.Ultraviolet radiation intensity is the lowest cannot meet radiation
Requirement, the highest meeting causes system energy consumption to be greatly improved, therefore ultraviolet light Net long wave radiation intensity is 50 μ W/cm2-500μW/cm2.Purple
Outside line wavelength is the shortest, and the photon energy given off is the highest, and the hypochlorous ability of photodissociation is the strongest, but the transmission capacity of now ultraviolet light
The lowest, i.e. disposal ability is limited, and contrary ultraviolet wavelength is the longest, photon decompose hypochlorous ability decline, but have effect spread away from
From increase, i.e. disposal ability rises, and therefore the EWL of ultraviolet light should be maintained at 160nm-280nm.
Embodiment 1:
Longitudinal pitch A between adsorbing separation post 10 and uviol lamp 5 is 20cm, horizontal between uviol lamp 5 and uviol lamp 5
Space D is 20cm, and smoke inlet 1 spacing C is 25cm, and the minute bubbles average diameter that chlorine aeration tube 4 bloats is 50 micro-
Rice, vertical range or the depth B of adsorbing separation post 10 bus entrance solution are 7cm, and uviol lamp 5 and quartz socket tube insert liquid level
Following 15cm, ultrasonic transmitter 13 keeps vertical range to be 3cm with the end face of adsorbing separation post 10 bottom position, adsorbing separation post
10 in counterclockwise rotating, and the diameter of adsorbing separation post 10 is 50cm, and rotating speed r is 15 revs/min.Smoke inlet 1 temperature
Degree is 120 DEG C, and liquid-gas ratio is 8L/m3, the dosage of chlorine is 2.0L (chlorine volume)/m3(liquor capacity), pH value of solution
Being 4.5, solution temperature is 45 DEG C, and in flue gas, VOCs concentration is 100mg/m3, ultraviolet radiation intensity is 100 μ W/cm2,
Ultraviolet wavelength is 254nm.Result in small test system is: de-VOCs efficiency reaches 58.6%.
Embodiment 2:
Longitudinal pitch A between adsorbing separation post 10 and uviol lamp 5 is 20cm, horizontal between uviol lamp 5 and uviol lamp 5
Space D is 20cm, and smoke inlet 1 spacing C is 25cm, and the minute bubbles average diameter that chlorine aeration tube 4 bloats is 50 micro-
Rice, vertical range or the depth B of adsorbing separation post 10 bus entrance solution are 7cm, and uviol lamp 5 and quartz socket tube insert liquid level
Following 15cm, ultrasonic transmitter 13 keeps vertical range to be 3cm with the end face of adsorbing separation post 10 bottom position, adsorbing separation post
10 in counterclockwise rotating, and the diameter of adsorbing separation post 10 is 50cm, and rotating speed r is 15 revs/min.Smoke inlet 1 temperature
Degree is 120 DEG C, and liquid-gas ratio is 5L/m3, the dosage of chlorine is 3.0L (chlorine volume)/m3(liquor capacity), pH value of solution
Being 4.5, solution temperature is 45 DEG C, and in flue gas, VOCs concentration is 100mg/m3, ultraviolet radiation intensity is 150 μ W/cm2,
Ultraviolet wavelength is 254nm.Result in small test system is: de-VOCs efficiency reaches 69.8%.
Embodiment 3:
Longitudinal pitch A between adsorbing separation post 10 and uviol lamp 5 is 20cm, horizontal between uviol lamp 5 and uviol lamp 5
Space D is 20cm, and smoke inlet 1 spacing C is 25cm, and the minute bubbles average diameter that chlorine aeration tube 4 bloats is 50 micro-
Rice, vertical range or the depth B of adsorbing separation post 10 bus entrance solution are 7cm, and uviol lamp 5 and quartz socket tube insert liquid level
Following 15cm, ultrasonic transmitter 13 keeps vertical range to be 3cm with the end face of adsorbing separation post 10 bottom position, adsorbing separation post
10 in counterclockwise rotating, and the diameter of adsorbing separation post 10 is 50cm, and rotating speed r is 15 revs/min.Smoke inlet 1 temperature
Degree is 120 DEG C, and liquid-gas ratio is 5L/m3, the dosage of chlorine is 1.0L (chlorine volume)/m3(liquor capacity), pH value of solution
Being 4.5, solution temperature is 45 DEG C, and in flue gas, VOCs concentration is 100mg/m3, ultraviolet radiation intensity is 200 μ W/cm2,
Ultraviolet wavelength is 254nm.Result in small test system is: de-VOCs efficiency reaches 88.8%.
Embodiment 4:
Longitudinal pitch A between adsorbing separation post 10 and uviol lamp 5 is 20cm, horizontal between uviol lamp 5 and uviol lamp 5
Space D is 20cm, and smoke inlet 1 spacing C is 25cm, and the minute bubbles average diameter that chlorine aeration tube 4 bloats is 50 micro-
Rice, vertical range or the depth B of adsorbing separation post 10 bus entrance solution are 7cm, and uviol lamp 5 and quartz socket tube insert liquid level
Following 15cm, ultrasonic transmitter 13 keeps vertical range to be 3cm with the end face of adsorbing separation post 10 bottom position, adsorbing separation post
10 in counterclockwise rotating, and the diameter of adsorbing separation post 10 is 50cm, and rotating speed r is 15 revs/min.Smoke inlet 1 temperature
Degree is 120 DEG C, and liquid-gas ratio is 5L/m3, the dosage of chlorine is 3.0L (chlorine volume)/m3(liquor capacity), pH value of solution
Being 4.5, solution temperature is 45 DEG C, and in flue gas, VOCs concentration is 100mg/m3, ultraviolet radiation intensity is 200 μ W/cm2,
Ultraviolet wavelength is 185nm.Result in small test system is: de-VOCs efficiency reaches 96.6%.
Embodiment 5:
Longitudinal pitch A between adsorbing separation post 10 and uviol lamp 5 is 20cm, horizontal between uviol lamp 5 and uviol lamp 5
Space D is 20cm, and smoke inlet 1 spacing C is 25cm, and the minute bubbles average diameter that chlorine aeration tube 4 bloats is 50 micro-
Rice, vertical range or the depth B of adsorbing separation post 10 bus entrance solution are 7cm, and uviol lamp 5 and quartz socket tube insert liquid level
Following 15cm, ultrasonic transmitter 13 keeps vertical range to be 3cm with the end face of adsorbing separation post 10 bottom position, adsorbing separation post
10 in counterclockwise rotating, and the diameter of adsorbing separation post 10 is 50cm, and rotating speed r is 15 revs/min.Smoke inlet 1 temperature
Degree is 120 DEG C, and liquid-gas ratio is 5L/m3, the dosage of chlorine is 3.0L (chlorine volume)/m3(liquor capacity), pH value of solution
Being 4.5, solution temperature is 45 DEG C, and in flue gas, VOCs concentration is 100mg/m3, ultraviolet radiation intensity is 300 μ W/cm2,
Ultraviolet wavelength is 185nm.Result in small test system is: de-VOCs efficiency reaches 100%.
Embodiment 6:
Longitudinal pitch A between adsorbing separation post 10 and uviol lamp 5 is 20cm, horizontal between uviol lamp 5 and uviol lamp 5
Space D is 20cm, and smoke inlet 1 spacing C is 25cm, and the minute bubbles average diameter that chlorine aeration tube 4 bloats is 50 micro-
Rice, vertical range or the depth B of adsorbing separation post 10 bus entrance solution are 7cm, and uviol lamp 5 and quartz socket tube insert liquid level
Following 15cm, ultrasonic transmitter 13 keeps vertical range to be 3cm with the end face of adsorbing separation post 10 bottom position, adsorbing separation post
10 in counterclockwise rotating, and the diameter of adsorbing separation post 10 is 50cm, and rotating speed r is 15 revs/min.Smoke inlet 1 temperature
Degree is 120 DEG C, and liquid-gas ratio is 5L/m3, the dosage of chlorine is 3.0L (chlorine volume)/m3(liquor capacity), pH value of solution
Being 4.5, solution temperature is 45 DEG C, and in flue gas, VOCs concentration is 100mg/m3, ultraviolet radiation intensity is 200 μ W/cm2,
Ultraviolet wavelength is 185nm.Result in small test system is: de-VOCs efficiency reaches 91.6%
Embodiment 7:
Longitudinal pitch A between adsorbing separation post 10 and uviol lamp 5 is 20cm, horizontal between uviol lamp 5 and uviol lamp 5
Space D is 20cm, and smoke inlet 1 spacing C is 25cm, and the minute bubbles average diameter that chlorine aeration tube 4 bloats is 50 micro-
Rice, vertical range or the depth B of adsorbing separation post 10 bus entrance solution are 7cm, and uviol lamp 5 and quartz socket tube insert liquid level
Following 15cm, ultrasonic transmitter 13 keeps vertical range to be 3cm with the end face of adsorbing separation post 10 bottom position, adsorbing separation post
10 in counterclockwise rotating, and the diameter of adsorbing separation post 10 is 50cm, and rotating speed r is 15 revs/min.Smoke inlet 1 temperature
Degree is 120 DEG C, and liquid-gas ratio is 5L/m3, the dosage of chlorine is 1.0L (chlorine volume)/m3(liquor capacity), pH value of solution
Being 4.5, solution temperature is 45 DEG C, and in flue gas, VOCs concentration is 200mg/m3, ultraviolet radiation intensity is 200 μ W/cm2,
Ultraviolet wavelength is 185nm.Result in small test system is: de-VOCs efficiency reaches 90.9%
Embodiment 8:
Longitudinal pitch A between adsorbing separation post 10 and uviol lamp 5 is 20cm, horizontal between uviol lamp 5 and uviol lamp 5
Space D is 20cm, and smoke inlet 1 spacing C is 25cm, and the minute bubbles average diameter that chlorine aeration tube 4 bloats is 50 micro-
Rice, vertical range or the depth B of adsorbing separation post 10 bus entrance solution are 7cm, and uviol lamp 5 and quartz socket tube insert liquid level
Following 15cm, ultrasonic transmitter 13 keeps vertical range to be 3cm with the end face of adsorbing separation post 10 bottom position, adsorbing separation post
10 in counterclockwise rotating, and the diameter of adsorbing separation post 10 is 50cm, and rotating speed r is 15 revs/min.Smoke inlet 1 temperature
Degree is 120 DEG C, and liquid-gas ratio is 10L/m3, the dosage of chlorine is 1.0L (chlorine volume)/m3(liquor capacity), pH value of solution
Being 4.5, solution temperature is 45 DEG C, and in flue gas, VOCs concentration is 300mg/m3, ultraviolet radiation intensity is 200 μ W/cm2,
Ultraviolet wavelength is 185nm.Result in small test system is: de-VOCs efficiency reaches 80.5%
Comprehensive Correlation through above example understands, and embodiment 5 has optimal removal effect, and the removal efficiency of VOCs reaches
To 100%, can consult and use as most preferred embodiment.
Described embodiment be the present invention preferred embodiment, but the present invention is not limited to above-mentioned embodiment, without departing substantially from this
In the case of the flesh and blood of invention, any conspicuously improved, replacement or modification that those skilled in the art can make are equal
Belong to protection scope of the present invention.
Claims (10)
1. a light radiation chlorine atom and hydroxyl remove the device of VOCs in waste gas, it is characterised in that: it is provided with a photodissociation absorption
Bed, described photodissociation adsorbent bed is an airtight reactor (11), has the product for containing water in described reactor (11)
Separating tank (8), described separating tank bottom is provided with product recovery port (6), and described reactor (11) wall is provided with smoke inlet (1)
Exhanst gas outlet (3) chlorine inlet (2) fluid infusion mouth (7), in described chlorine inlet (2) extends to reactor (11),
And connect with the aeration tube (4) that can be positioned at below liquid level, described reactor is additionally provided with, in (11), the absorption being loaded on sidewall
Splitter (10), the uviol lamp (5) being loaded on reactor top board (14), uviol lamp (5) is outside is cased with quartz socket tube, institute
The surface stating adsorbing separation post (10) is provided with activated carbon fiber, adsorbing separation post (10) be connected with power transmission shaft (16) and with
Sidewall of reactor (15) revolute pair connects, and the latter half of described adsorbing separation post (10) is immersed in below liquid level.
The device of VOCs in light radiation chlorine atom the most according to claim 1 and hydroxyl removing waste gas, it is characterised in that:
Also include that ultrasonic cleaning equipment (12), described ultrasonic cleaning equipment (12) are in below liquid level and are positioned at adsorbing separation post (10)
The ultrasonic transmitter (13) of bottom.
The device of VOCs in light radiation chlorine atom the most according to claim 1 and hydroxyl removing waste gas, it is characterised in that:
Described exhanst gas outlet (3) is connected with chlorine knockout tower (9), described chlorine knockout tower (9) and chimney breast and chlorine inlet (2)
Connection.
The device of VOCs in light radiation chlorine atom the most according to claim 1 and hydroxyl removing waste gas, it is characterised in that:
The bus of described adsorbing separation post (10) contacts with reactor top board (14), and both ends of the surface contact with sidewall of reactor (15).
The device of VOCs in light radiation chlorine atom the most according to claim 1 and hydroxyl removing waste gas, it is characterised in that:
The quantity of described adsorbing separation post (10) is 1-6, and the quantity of uviol lamp (5) is also multiple, and adsorbing separation post (10)
And uviol lamp (5) interval is arranged.
The device of VOCs in light radiation chlorine atom the most according to claim 1 and hydroxyl removing waste gas, it is characterised in that:
Longitudinal pitch A between adsorbing separation post (10) and uviol lamp (5) is between 15cm-25cm；Uviol lamp (5) is with purple
Optimal lateral space D between outer lamp (5) is between 10cm-30cm；Smoke inlet (1) spacing C is at 15cm-40cm
Between；The bubble mean diameter that chlorine aeration tube (4) bloats is not more than 100 microns；Adsorbing separation post (10) bus enters molten
The depth B of liquid is positioned at 5cm-10cm；Uviol lamp (5) and quartz socket tube insert below liquid level more than 10cm；Ultrasonic transmitter
(13) end face with adsorbing separation post (10) bottom position keeps vertical range 2cm-5cm centimetre；Adsorbing separation post (10)
Diameter is 30cm-90cm.
7. a light radiation chlorine atom and hydroxyl remove the method for VOCs in waste gas, it is characterised in that comprise the following steps:
(1) chlorine is sprayed into by chlorine inlet (2) formed hypochlorite solution in water by chlorine aeration tube (4), adsorbing separation post
(10) activated carbon fiber on is by having hypochlorous acid from the teeth outwards after rotating immersion hypochlorite solution；Under ultraviolet radiation,
The hypochlorous acid on the activated carbon fiber surface of adsorbing separation post (10) decomposes generation high activity chlorine atom and hydroxyl；
(2) containing VOCs flue gas from smoke inlet (1) enter light radiation absorption washing bed and with on adsorbing separation post (10)
Activated carbon fiber contact, the activated carbon fiber surface on adsorbing separation post (10) of the VOCs in flue gas and hydroxyl generation oxygen
Change reaction, generate organic carbon slag and CO2, chemical reaction such as (7) represents:
Organic carbon slag is fixed on activated carbon fiber surface, CO2Air is entered with flue gas；
(3) after adsorbing separation post (10) continues to rotate and be again dipped into solution, the absorption organic carbon on activated carbon fiber surface
Slag enters solution after coming off, thus completes continual removing VOCs and washing process, the product bottom the entrance of organic carbon slag
After separating tank (8), can sink to separating because of self gravitation reason, be recycled.
The method of VOCs in light radiation chlorine atom the most according to claim 1 and hydroxyl removing waste gas, it is characterised in that:
In described step (3), VOCs oxidation product comes off is to use supersonic oscillations mode, also includes using in described step (1)
Chlorine knockout tower (9) reclaims the process of chlorine, and the chlorine of recovery enters aeration tube (4) again by chlorine inlet (2).
The method of VOCs in light radiation chlorine atom the most according to claim 1 and hydroxyl removing waste gas, it is characterised in that:
In described step (2), adsorbing separation post (10) is in counterclockwise rotating, and the rotary cutting linear speed of adsorbing separation post (10)
Degree direction is in opposite direction with flow of flue gas.
The method of VOCs in light radiation chlorine atom the most according to claim 1 and hydroxyl removing waste gas, it is characterised in that:
The rotating speed r of adsorbing separation post (10) is between 5 revs/min-30 revs/min；Smoke inlet (1) temperature is not higher than 200 DEG C,
Solution is 1L/m with the liquid-gas ratio of flue gas3-25L/m3；The dosage of chlorine is 0.3L (chlorine volume)/m3(liquor capacity)
-5.0L (chlorine volume)/m3Between (liquor capacity), the pH of solution is not higher than 5.5；Solution temperature is generally not more than 65 DEG C；
Ultraviolet light Net long wave radiation intensity is 30 μ W/cm2-200μW/cm2；The EWL of ultraviolet light should be maintained at 180nm-366nm.
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