CN102229445A - Homogeneous phase photo-oxidation device capable of degrading aromatic compound waste water continuously and processing method thereof - Google Patents
Homogeneous phase photo-oxidation device capable of degrading aromatic compound waste water continuously and processing method thereof Download PDFInfo
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- CN102229445A CN102229445A CN2011101341601A CN201110134160A CN102229445A CN 102229445 A CN102229445 A CN 102229445A CN 2011101341601 A CN2011101341601 A CN 2011101341601A CN 201110134160 A CN201110134160 A CN 201110134160A CN 102229445 A CN102229445 A CN 102229445A
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Abstract
The invention provides a homogeneous phase photo-oxidation device capable of degrading aromatic compound waste water continuously and a processing method thereof. The method comprises the following steps: delivering waste water to be processed into a regulator, mixing the waster water to be processed with a photocatalyst which is added from the upper part of the regulator, and regulating the pH value to 3-4; delivering the mixture into a stirring mixer, and mixing the mixture with H2O2 which is added from the upper part of the stirring mixer; and entering a photoreactor through a constant flow pump after mixing, and carrying out continuous photo Fenton oxidation and degradation to finally obtain qualified clarified water. By the adoption of the processing method provided by the invention, problems of pollution and regeneration of the catalyst cannot be caused, the catalyst and an oxidizer have no secondary pollution, the reaction is carried out at normal temperature and pressure, the occupied area is small, the operation is simple and convenient, the waste water processing capability and processing effect are adjustable and controllable, and the aromatic compound waste water which is difficult to degrade can be processed continuously; and the aromatic compound waste water which is difficult to degrade is processed continuously by adopting the processing method, and the removal rate of a parent aromatic compound is more than 98%.
Description
Technical field
The present invention relates to the devices and methods therefor of homogeneous phase photo-oxidative degradation waste water, but specifically be meant the homogeneous phase photooxidation reaction device and the treatment process thereof of continuous degradation aromatic compound waste water.
Background technology
Developing rapidly of modern industry brought the trade effluent that contains the high density toxic organic pollutant in a large number, comprising aromatic compound waste water such as the wastewater from chemical industry that contains aromatic compounds such as benzene, phenol, chlorophenol, aniline, benzoquinones, oil of mirbane, anthraquinone in a large number, medical factory effluent, pesticide wastewater, dyeing waste waters, this class wastewater biological degradation property is poor, adopts traditional biologic treating technique efficient low; Adopt physical chemistry methods such as gas is carried, absorption, coagulation, extraction then to exist waste material to pile up and secondary pollution problems.How economical and to handle this class waste water effectively be the important topic of research both at home and abroad always, high-level oxidation technology (the Advanced Oxidation Processes that grow up nearly decades, be called for short AOPs), utilize the strong oxidation that produces high mars free radical (OH), oxidation operation can be degraded to CO
2Reach other small-molecule substance nontoxic or low toxicity, be particularly suitable for the processing of difficult for biological degradation poisonous organic wastewater.Esplugas and Huang etc. have compared the relative merits of various high-level oxidation technologies, propose light Fenton technology and be one of the most promising treatment technology.Light Fenton oxidation technology is owing to reaction conditions gentleness (normal temperature, normal pressure), simple, the Fenton reagent (Fe of equipment
2+-H
2O
2Combination) non-secondary pollution, oxidation capacity is strong, compares problems such as the pollution of the recovery that there is not catalyzer in light Fenton oxidation and fixing, catalyzer and activation with the conductor photocatalysis oxidation technology, thereby have very big application potential, be subjected to home and abroad environment worker's attention day by day.
At present, existing photoreactor is by using catalyst form can be divided into two big classes:
One class is to be the heterogeneous photoreactor of catalyzer with nano semiconductor materials such as titanium dioxide, this class reactor uses Nano semiconductor dispersion system or working load type Nano semiconductor multiphase photocatalysis system, the Preparation of catalysts complexity, have problems such as Separation and Recovery and regeneration, and the photo-quantum efficiency of catalyzer is low, the photocatalysis treatment limited efficiency.For this reason, the disclosed a kind of continuous degradation of Chinese patent publication number CN1431155 contains in the photocatalytic reaction device of organic pollutant waste water and the treatment process thereof by adding pro-oxidant H
2O
2Improve processing efficiency, adopt H in the light catalytic treatment method of the disclosed a kind of organic waste water of Chinese patent publication number CN1301668 and the device thereof
2O
2, O
3Come enhancement process efficient with divalent iron salt as secondary oxidizer.
Another kind of is with iron ion (Fe
2+Or Fe
3+) be the homogeneous phase photooxidation reaction device of catalyzer, purify the method and apparatus that contains organic pollutant waste water as the disclosed homogeneous phase photoxidation continuously of CN1289728, the degradation efficiency height of this class photoreactor does not exist the recovery and the regeneration problem of catalyzer, operation is simple, non-secondary pollution.
The modes of emplacement of light source mainly contains two kinds in the present existing photoreactor.The first is inserted light source in the glass bushing that is immersed in the pending waste water foregoing CN1431155, CN1301668 and CN1289728.This light source modes of emplacement is single lamp list sleeve pipe, and light path is short, and the distance between light source and the pending waste water is bigger, and the light source utilising efficiency and the processing efficiency of single photoreactor are not high, needs the series multistage reactor can reach better effects.It two is, light source is placed flat-plate reactor on the pending waste water reaction pond, as CN 2399374 disclosed waste water photocatalysis treatment devices, the plate photocatalytic water treatment device of the continuously adjustable fixedly film in CN 2354931 disclosed inclination angles.This light source modes of emplacement exists that the distance between light source and the pending waste water is big, optical energy utilization efficiency is not high, treatment capacity is less, be not suitable for problem such as processing continuously.
Summary of the invention
The objective of the invention is deficiency, but a kind of homogeneous phase photooxidation reaction device and treatment process thereof of continuous degradation aromatic compound waste water are provided at the problems referred to above.
But the method for continuous degradation aromatic compound waste water provided by the present invention may further comprise the steps:
A. pending waste water is delivered to the photocatalyst that adds with setter top in the setter and mixes, regulating the pH value with acid or alkali is 3～4;
B. coming the pending waste water of self tuning regulator to enter stirring mixer mixes with the hydrogen peroxide that adds from stirring mixer top;
C. the mixed pending waste water that contains photocatalyst and hydrogen peroxide enters photoreactor with 50mL/min～1000mL/min flow velocity from the opening for feed of photoreactor one side bottom by constant flow pump, top feeding pressurized air from photoreactor makes the bubbling pipe bubbling that is positioned at the reaction tank bottom simultaneously in reaction process, and under irradiation from the light source of the inside groove of photoreactor, carry out continuous light Fenton oxidative degradation, treating water after reaction finishes flows out from the discharge port of photoreactor, this outflow water obtains qualified purifying waste water after conventional method such as alkaline chemical precipitation are isolated catalyzer.
Can be among the present invention according to the requirement of treatment capacity, can only use a photoreactor, also can be after discharge port flows out at the water after first step photoreactor is handled, in parallel again or 1～2 photoreactor of connecting, the upper level water outlet is transported to the opening for feed of next stage photoreactor, flows out to the discharge port of last step photoreactor.
Used photocatalyst ferrous iron or ferric soluble inorganic salt among the present invention is specially ferrous sulfate, iron protochloride, Iron nitrate, ferric sulfate, iron(ic) chloride or iron nitrate.The amount of substance that catalyzer adds is 1/15～1/30 of the amount of substance that adds of hydrogen peroxide.
Used hydrogen peroxide dosage is 30%～90% of the theoretical dosage of the pairing hydrogen peroxide of chemical oxygen demand (COD) among the present invention.
Hydrogen peroxide (H
2O
2) theoretical dosage be meant the pairing theoretical amount of hydrogen peroxide of chemical oxygen demand (COD) (COD).Because every 2mol hydrogen peroxide produces the 1mol oxygen molecule, therefore, the theoretical dosage of the hydrogen peroxide of 1mg/L COD correspondence is 2.125mg/L.
The present invention can increase or reduce the dosage of hydrogen peroxide according to the requirement of degree of treatment.Carry out advanced treatment by the hydrogen peroxide that adds higher dosage, can reach the purpose of efficient purification.Sometimes for reducing cost, can only carry out pre-treatment by the hydrogen peroxide that adds low dosage, the aromatic compound that toxicity is bigger destroys, make it to change into the less intermediate product of toxicity, to significantly improve the biological degradability of difficult degradation aromatic compound waste water, again with biological process coupling (biological process is most economical treatment process), thereby reach the purpose of economical and efficient.
But the homogeneous phase photooxidation reaction device of continuous degradation aromatic compound waste water provided by the present invention, it comprise setter, in establish the stirring mixer of stepless speed-regulating motor and mechanical stirring device, with the mass transport in the stirring mixer to the constant flow pump and the photoreactor of photoreactor, described photoreactor is the open container that is provided with opening for feed and discharge port, be provided with transparent inside groove in the described photoreactor, be provided with 2～5 artificial light fluorescent tubes in the described inside groove, described is 0.5～1.0 centimetre near the artificial light fluorescent tube of inside groove and the distance of inside groove inwall; The shell of described photoreactor and inside groove constitute reaction tank, and the bottom of described reaction tank is provided with bubbling pipe.
Preferably, the rear of the inherent opening for feed of described reaction tank is provided with an inlet damper, makes current be evenly distributed in the wide transverse section of overall optical reaction tank, thereby makes reaction solution fully accept illumination, improves optical energy utilization efficiency and photoresponse efficient; When flow velocity was big, its effect was more obvious, owing to the shock absorption that stops of baffle plate, can avoid forming plume.
Preferably, described inside groove adopting quartz glass plate or silicate ultra-clear glasses plate, with silica glass the best, the thickness of sheet glass is 3～4 millimeters.
Particularly, the one-sided length of described reaction tank is 50～100 centimetres, and the width of described reaction tank is 2.5～3.0 centimetres, highly is 40～50 centimetres.
Particularly, the one end sealing of the bubbling pipe that the present invention is used, the other end is connected with the compressed-air actuated flexible pipe that photoreactor top feeds, described bubbling pipe is a hollow elongated tubular, each bubbling pipe evenly is furnished with 15～20 production wells, the length of described bubbling pipe is less than the length of reaction tank, and the internal diameter of described bubbling pipe is 1.0～2.0 centimetres.Bubbling pipe places bottom, photooxidation reaction pond, and evenly air-blowing makes the reaction solution in the reaction tank evenly accept illumination in vertical direction.
Particularly, the used artificial light fluorescent tube of the present invention is ultraviolet germicidal lamp or the low pressure mercury lamp of power 24W～55W, preferred ultraviolet germicidal lamp.The length of described artificial light fluorescent tube and the length of inside groove or highly be complementary.
Beneficial effect of the present invention: can place a plurality of artificial light fluorescent tubes in the single photoreactor, the artificial light fluorescent tube is short apart from the distance of reaction solution, and waste water flows with plug flow mode in reaction tank, the optical length of accepting, the optical energy utilization efficiency height, photoresponse efficient height, continuously-running.The present invention can reach the purpose that improves processing efficiency and increase the wastewater treatment ability by fluorescent tube number of placing in the middle of the inside groove that changes photoreactor and the progression of connecting photoreactor.There is not the pollution and the regeneration problem of catalyzer in treatment process of the present invention, catalyzer and oxygenant non-secondary pollution, and reaction is carried out at normal temperatures and pressures, floor space is little, operational management is easy, and it is controlled that wastewater treatment ability and treatment effect are adjustable, can handle difficult degradation aromatic compound waste water continuously.Shortcomings such as traditional photoreactor residence time that the present invention effectively overcome single lamp list sleeve pipe, mix streaming is short, the efficiency of light energy utilization is not high and the photo-quantum efficiency conductor photocatalysis oxidation is lower, the recovery of catalyzer and regeneration difficulty.Adopt this treatment process to handle difficult degradation aromatic compound waste water continuously, the clearance of parent aromatic compound reaches more than 98%.Treatment process of the present invention is not only applicable to difficult degradation aromatic compound waste water, as contain the wastewater from chemical industry of aromatic compounds such as benzene, phenol, chlorophenol, aniline, benzoquinones, anthraquinone, medical factory effluent, pesticide wastewater, dyeing waste water etc., also can be used for the continuous processing of other organic waste waters.
Description of drawings
Fig. 1 is the process flow sheet of continuous degradation aromatic compound waste water of the present invention.
Fig. 2 is the front view of photoreactor of the present invention.
Fig. 3 is the left view of photoreactor of the present invention.
Fig. 4 is the vertical view of photoreactor of the present invention.
Embodiment
Below further specify the present invention by specific embodiment:
With chemical oxygen demand (COD) (COD) starting point concentration is that 1378.4mg/L, volatile phenol starting point concentration are that the coal gas phenolic wastewater of 221.6mg/L is as pending waste water.The process flow sheet of continuous degradation aromatic compound waste water of the present invention as shown in Figure 1.Pending waste water mixes in setter 1 with the catalyst sulfuric acid ferrous iron solution, the consumption of ferrous ion is 40mg/L, with the sulphur acid for adjusting pH value is 3.5, come the pending waste water of self tuning regulator 1 to enter stirring mixer 2 and mix with hydrogen peroxide from stirring mixer 2 tops, the hydrogen peroxide dosage is 90% (2600mg/L) of theoretical dosage.The mixed pending waste water that contains photocatalyst and hydrogen peroxide enters photoreactor 4 with the 120mL/min flow velocity from the opening for feed 4.1 of photoreactor 4 left bottom by constant flow pump 3, top feeding pressurized air from photoreactor 4 makes bubbling pipe 4.7 bubblings that are positioned at reaction tank 4.8 bottoms simultaneously in reaction process, and under irradiation from the light source of the inside groove 4.4 of photoreactor 4, carry out continuous light Fenton oxidative degradation, treating water after reaction finishes flows out from the discharge port 4.2 of photoreactor 4, this outflow water obtains qualified purifying waste water after alkaline chemical precipitation is isolated catalyzer.The COD of discharge port 4.2 water outlets of photoreactor 4 is 129.3mg/L, and the clearance of COD is 90.6%; The volatile phenol concentration of water outlet is 0.19mg/L, and the clearance of volatile phenol is 99.94%; Water outlet COD and volatile phenol concentration all reach discharging standards.
Embodiment 2
Except the hydrogen peroxide dosage is reduced to 35% (1000mg/L) of theoretical dosage, other experiment conditions are with embodiment 1.The COD of water outlet is 702.1mg/L behind the photo-oxidative degradation, and the clearance of COD is 49.1%; The volatile phenol concentration of water outlet is 0.92mg/L, and the clearance of volatile phenol is 99.69%; Water outlet BOD
5The ratio of/COD is increased to 0.52 by 0.28 of raw wastewater, and the biological degradability of handling the back water outlet significantly strengthens.
Embodiment 3
Except the input speed of pending waste water increases to 180mL/min, other experiment conditions are with embodiment 1.The COD of water outlet is 139.5mg/L behind the photo-oxidative degradation, and the clearance of COD is 90.1%; The volatile phenol concentration of water outlet is 0.26mg/L, and the clearance of volatile phenol is 99.91%.
With chemical oxygen demand (COD) (COD) starting point concentration is that 1378.4mg/L, volatile phenol starting point concentration are that the coal gas phenolic wastewater of 221.6mg/L is as pending waste water.Pending waste water mixes in setter 1 with the catalyst sulfuric acid ferrous solution, the consumption of iron ion is 40mg/L, with the sulphur acid for adjusting pH value is 3.5, come the pending waste water of self tuning regulator 1 to enter stirring mixer 2 and mix with hydrogen peroxide from stirring mixer 2 tops, the hydrogen peroxide dosage is 90% (2600mg/L) of theoretical dosage.The mixed pending waste water that contains photocatalyst and hydrogen peroxide enters photoreactor 4 with the 120mL/min flow velocity from the opening for feed 4.1 of photoreactor 4 left bottom by constant flow pump 3, top feeding pressurized air from photoreactor 4 makes bubbling pipe 4.7 bubblings that are positioned at reaction tank 4.8 bottoms simultaneously in reaction process, and under irradiation from the light source of the inside groove 4.4 of photoreactor 4, carry out continuous light Fenton oxidative degradation, treating water after reaction finishes flows out from the discharge port 4.2 of photoreactor 4, this outflow water obtains qualified purifying waste water after alkaline chemical precipitation is isolated catalyzer.The COD of discharge port 4.2 water outlets of photoreactor 4 is 154.3mg/L, and the clearance of COD is 88.8%; The volatile phenol concentration of water outlet is 0.30mg/L, and the clearance of volatile phenol is 99.9%.
Embodiment 5
With initial phenol concentration is that 300mg/L, COD starting point concentration are that the phenolic waste water of 699.7mg/L is as pending waste water.Pending waste water mixes in setter 1 with the catalyzer solution of ferrous chloride, the consumption of ferrous ion is 30mg/L, with the sulphur acid for adjusting pH value is 3.0, come the pending waste water of self tuning regulator 1 to enter stirring mixer 2 and mix with hydrogen peroxide from stirring mixer 2 tops, the hydrogen peroxide dosage is 54% (800mg/L) of theoretical dosage.The mixed pending waste water that contains photocatalyst and hydrogen peroxide enters photoreactor 4 with the 120mL/min flow velocity from the opening for feed 4.1 of photoreactor 4 left bottom by constant flow pump 3, top feeding pressurized air from photoreactor 4 makes bubbling pipe 4.7 bubblings that are positioned at reaction tank 4.8 bottoms simultaneously in reaction process, and under irradiation from the light source of the inside groove 4.4 of photoreactor 4, carry out continuous light Fenton oxidative degradation, treating water after reaction finishes flows out from the discharge port 4.2 of photoreactor 4, this outflow water obtains qualified purifying waste water after alkaline chemical precipitation is isolated catalyzer.The COD of discharge port 4.2 water outlets of photoreactor 4 is 171.5mg/L, and the clearance of COD is 75.5%; The phenol concentration of water outlet is 0.17mg/L, and the clearance of phenol is 99.94%.
Embodiment 6
Except the hydrogen peroxide dosage is 88% (1300mg/L) of theoretical dosage, other experiment conditions are with embodiment 5.The COD of water outlet is 46.3mg/L behind the photo-oxidative degradation, and the clearance of COD is 93.4%; The phenol concentration of water outlet is lower than detectability, and the clearance of phenol is 100%.
Embodiment 7
Except pending waste water is that 300mg/L, COD starting point concentration are the orthomonochlorphenol waste water of 528.5mg/L for the ortho chloro phenol starting point concentration, the hydrogen peroxide dosage is that 55% (600mg/L) other experiment conditions of theoretical dosage are with embodiment 5.The COD of water outlet is 146.3mg/L behind the photo-oxidative degradation, and the clearance of COD is 72.3%; The orthomonochlorphenol concentration of water outlet is 0.49mg/L, and the clearance of ortho chloro phenol is 99.83%.
Embodiment 8
Except pending waste water is that 300mg/L, COD starting point concentration are the 2,4 dichloro phenol waste water of 445.7mg/L for the 2,4 dichloro phenol starting point concentration, the hydrogen peroxide dosage is that 60% (550mg/L) other experiment conditions of theoretical dosage are with embodiment 5.The COD of water outlet is 150.3mg/L behind the photo-oxidative degradation, and the clearance of COD is 66.3%; The 2,4 dichloro phenol concentration of water outlet is 2.86mg/L, and the clearance of 2,4 dichloro phenol is 99.05%.
Embodiment 9
Except pending waste water is that 300mg/L, COD starting point concentration are the aniline waste water of 717.9mg/L for the aniline starting point concentration, the hydrogen peroxide dosage is that 53% (800mg/L) other experiment conditions of theoretical dosage are with embodiment 5.The COD of water outlet is 162.7mg/L behind the photo-oxidative degradation, and the clearance of COD is 77.4%; The aniline concentration of water outlet is 0.47mg/L, and the clearance of aniline is 99.84%.
Embodiment 10
Except pending waste water is that 150mg/L, colourity are 1200 times reactive brilliant red x-3b waste water from dyestuff for the reactive brilliant red x-3b starting point concentration, the hydrogen peroxide dosage is 70% (200mg/L) of theoretical dosage, and other experiment conditions are with embodiment 5.The concentration of water outlet reactive brilliant red x-3b is 2.04mg/L behind the photo-oxidative degradation, and the clearance of reactive brilliant red x-3b is 98.98%; The colourity of water outlet is 100 times, and the clearance of colourity is 91.67%.
Embodiment 11
With the COD starting point concentration is that 1257.1mg/L, oil of mirbane starting point concentration are that the pharmacy waste water of 114.9mg/L is as pending waste water.Pending waste water mixes in setter 1 with the catalyzer ferrous nitrate solution, the consumption of ferrous ion is 50mg/L, with the nitre acid for adjusting pH value is 3.0, come the pending waste water of self tuning regulator 1 to enter stirring mixer 2 and mix with hydrogen peroxide from stirring mixer 2 tops, the hydrogen peroxide dosage is 60% (1600mg/L) of theoretical dosage.The mixed pending waste water that contains photocatalyst and hydrogen peroxide enters photoreactor 4 with the 120mL/min flow velocity from the opening for feed 4.1 of photoreactor 4 left bottom by constant flow pump 3, top feeding pressurized air from photoreactor 4 makes bubbling pipe 4.7 bubblings that are positioned at reaction tank 4.8 bottoms simultaneously in reaction process, and under irradiation from the light source of the inside groove 4.4 of photoreactor 4, carry out continuous light Fenton oxidative degradation, treating water after reaction finishes flows out from the discharge port 4.2 of photoreactor 4, this outflow water obtains qualified purifying waste water after alkaline chemical precipitation is isolated catalyzer.The COD of discharge port 4.2 water outlets of photoreactor 4 is 367.5mg/L, and the clearance of COD is 70.8%; The nitro phenenyl concentration of water outlet is 11.24mg/L, and the clearance of oil of mirbane is 90.43%.
Embodiment 12
Except the treating water with the discharge port 4.2 of photoreactor 4 inserts the opening for feed 4.1 of next stage photoreactor 4 by pipeline, other experiment conditions are with embodiment 11.The COD of discharge port 4.2 water outlets of second stage photoreactor 4 is 221.5mg/L, and the clearance of COD is 82.4%; The nitro phenenyl concentration of water outlet is 5.84mg/L, and the clearance of oil of mirbane is 94.96%.
Embodiment 13
Except the hydrogen peroxide dosage increases to 86% (2300mg/L) of theoretical dosage, other experiment conditions are with embodiment 11.The COD of discharge port 4.2 water outlets of photoreactor 4 is 160.8mg/L, and the clearance of COD is 87.3%; The nitro phenenyl concentration of water outlet is 0.63mg/L, and the clearance of oil of mirbane is 99.45%.
All can find out by above embodiment, adopt this treatment process to handle difficult degradation aromatic compound waste water continuously, when the hydrogen peroxide dosage be the theoretical dosage of the pairing hydrogen peroxide of chemical oxygen demand (COD) 30%～90% the time, the clearance of parent aromatic compound just can reach more than 98%; Only can reach higher removal with the one-level photoreactor.
Claims (9)
1. but the method for a continuous degradation aromatic compound waste water may further comprise the steps:
A. pending waste water is delivered to the photocatalyst that adds with setter (2) top in the setter (1) and mixes, regulating the pH value is 3～4;
B. coming the pending waste water of self tuning regulator (1) to enter stirring mixer (2) mixes with the hydrogen peroxide that adds from stirring mixer (2) top;
C. the mixed pending waste water that contains photocatalyst and hydrogen peroxide enters photoreactor (4) with 50mL/min～1000mL/min flow velocity from the opening for feed (4.1) of photoreactor (4) by constant flow pump (3), in reaction process, feed pressurized air in the while phototropic reaction device (4) and make bubbling pipe (4.7) bubbling that is positioned at reaction tank (4.8) bottom, and under irradiation from the light source of the inside groove (4.4) of photoreactor (4), carry out continuous light Fenton oxidative degradation, treating water after reaction finishes flows out from the discharge port (4.2) of photoreactor (4), this outflow water obtains qualified purifying waste water after alkaline chemical precipitation is isolated catalyzer.
2. but according to the method for the described continuous degradation aromatic compound of claim 1 waste water, it is characterized in that: described photoreactor (4) also can in parallel or 1～2 photoreactor (4) of connecting.
3. but according to the method for claim 1 or 2 described continuous degradation aromatic compound waste water, it is characterized in that: described photocatalyst is ferrous sulfate, iron protochloride, Iron nitrate, ferric sulfate, iron(ic) chloride or iron nitrate; Described hydrogen peroxide dosage is 30%～90% of the theoretical dosage of the pairing hydrogen peroxide of chemical oxygen demand (COD), and the amount of substance that described catalyzer adds is 1/15～1/30 of the amount of substance that adds of hydrogen peroxide.
4. but the homogeneous phase photooxidation reaction device of a continuous degradation aromatic compound waste water, it is characterized in that: it comprises setter (1), in establish the stirring mixer (2) of stepless speed-regulating motor and mechanical stirring device, with constant flow pump (3) and the photoreactor (4) of the mass transport in the stirring mixer (2) to photoreactor (4), described photoreactor (4) is for being provided with the open container of opening for feed (4.1) and discharge port (4.2), be provided with transparent inside groove (4.4) in the described photoreactor (4), be provided with 2～5 artificial light fluorescent tubes (4.6) in the described inside groove (4.4), described is 0.5～1.0 centimetre near the artificial light fluorescent tube (4.6) of inside groove (4.4) and the distance of inside groove (4.4) inwall; The shell (4.3) of described photoreactor (4) and inside groove (4.4) constitute reaction tank (4.8), and the bottom of described reaction tank (4.8) is provided with bubbling pipe (4.7).
5. but according to the homogeneous phase photooxidation reaction device of the described continuous degradation aromatic compound of claim 4 waste water, it is characterized in that: the rear of the inherent opening for feed of described reaction tank (4.8) (4.1) is provided with an inlet damper (4.5).
6. but according to the homogeneous phase photooxidation reaction device of the described continuous degradation aromatic compound of claim 4 waste water, it is characterized in that: the one-sided length of described reaction tank (4.8) is 50～100 centimetres, the width of described reaction tank (4.8) is 2.5～3.0 centimetres, highly is 40～50 centimetres.
7. but according to the homogeneous phase photooxidation reaction device of the described continuous degradation aromatic compound of claim 4 waste water, it is characterized in that: the end sealing of described bubbling pipe (4.7), the other end is connected with the compressed-air actuated flexible pipe that photoreactor (4) top feeds, described bubbling pipe (4.7) is a hollow elongated tubular, each bubbling pipe (4.7) evenly is furnished with 15～20 production wells, the length of described bubbling pipe (4.7) is less than the length of reaction tank (4.8), and the internal diameter of described bubbling pipe (4.7) is 1.0～2.0 centimetres.
8. but according to the homogeneous phase photooxidation reaction device of the described continuous degradation aromatic compound of claim 4 waste water, it is characterized in that: described artificial light fluorescent tube (4.6) is ultraviolet germicidal lamp or the low pressure mercury lamp of power 24W～55W, the length of the length of described artificial light fluorescent tube (4.6) and inside groove (4.4) or highly be complementary.
9. but according to the homogeneous phase photooxidation reaction device of the described continuous degradation aromatic compound of claim 4 waste water, it is characterized in that: described inside groove (4.4) adopting quartz glass plate or silicate ultra-clear glasses plate, the thickness of sheet glass is 3～4 millimeters.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104709962A (en) * | 2015-02-13 | 2015-06-17 | 浙江三龙催化剂有限公司 | Photodegradation catalysis treatment device for printing and dyeing wastewater |
| CN104860470A (en) * | 2015-04-28 | 2015-08-26 | 山东先达农化股份有限公司 | Acrolein wastewater treatment method and device |
| CN114516673A (en) * | 2022-01-12 | 2022-05-20 | 浙江万里学院 | Plane tube type continuous flow-photocatalytic oxidation degradation water treatment device, system and method |
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| JP2007136372A (en) * | 2005-11-18 | 2007-06-07 | Nomura Micro Sci Co Ltd | Ultrapure water production device |
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| CN104709962A (en) * | 2015-02-13 | 2015-06-17 | 浙江三龙催化剂有限公司 | Photodegradation catalysis treatment device for printing and dyeing wastewater |
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Application publication date: 20111102 |