CN221051697U - Advanced oxidation combined process reactor - Google Patents
Advanced oxidation combined process reactor Download PDFInfo
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- CN221051697U CN221051697U CN202322568383.XU CN202322568383U CN221051697U CN 221051697 U CN221051697 U CN 221051697U CN 202322568383 U CN202322568383 U CN 202322568383U CN 221051697 U CN221051697 U CN 221051697U
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- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 78
- 230000003647 oxidation Effects 0.000 title claims abstract description 72
- 238000000034 method Methods 0.000 title abstract description 16
- 230000008569 process Effects 0.000 title abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 68
- 238000006243 chemical reaction Methods 0.000 claims abstract description 63
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000003054 catalyst Substances 0.000 claims abstract description 25
- 238000005273 aeration Methods 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 16
- 238000000926 separation method Methods 0.000 claims abstract description 15
- 229920000742 Cotton Polymers 0.000 claims abstract description 8
- 239000000945 filler Substances 0.000 claims description 32
- 238000012856 packing Methods 0.000 claims description 12
- 239000010453 quartz Substances 0.000 claims description 11
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 11
- 238000004148 unit process Methods 0.000 claims description 9
- 238000007789 sealing Methods 0.000 claims description 3
- 239000003814 drug Substances 0.000 claims description 2
- 230000015556 catabolic process Effects 0.000 abstract description 9
- 238000006731 degradation reaction Methods 0.000 abstract description 9
- 239000010865 sewage Substances 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 description 19
- 238000001816 cooling Methods 0.000 description 9
- 238000012360 testing method Methods 0.000 description 9
- JRKICGRDRMAZLK-UHFFFAOYSA-L peroxydisulfate Chemical class [O-]S(=O)(=O)OOS([O-])(=O)=O JRKICGRDRMAZLK-UHFFFAOYSA-L 0.000 description 7
- 239000011941 photocatalyst Substances 0.000 description 7
- 238000009303 advanced oxidation process reaction Methods 0.000 description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 230000001699 photocatalysis Effects 0.000 description 6
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical group O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 4
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 4
- 239000010432 diamond Substances 0.000 description 4
- 229910003460 diamond Inorganic materials 0.000 description 4
- 229910052719 titanium Inorganic materials 0.000 description 4
- 239000010936 titanium Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- WUPHOULIZUERAE-UHFFFAOYSA-N 3-(oxolan-2-yl)propanoic acid Chemical compound OC(=O)CCC1CCCO1 WUPHOULIZUERAE-UHFFFAOYSA-N 0.000 description 2
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 229910052796 boron Inorganic materials 0.000 description 2
- 229910052980 cadmium sulfide Inorganic materials 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 2
- 238000007146 photocatalysis Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000004408 titanium dioxide Substances 0.000 description 2
- LCPVQAHEFVXVKT-UHFFFAOYSA-N 2-(2,4-difluorophenoxy)pyridin-3-amine Chemical compound NC1=CC=CN=C1OC1=CC=C(F)C=C1F LCPVQAHEFVXVKT-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- CSDREXVUYHZDNP-UHFFFAOYSA-N alumanylidynesilicon Chemical compound [Al].[Si] CSDREXVUYHZDNP-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
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- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000010525 oxidative degradation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- SOQBVABWOPYFQZ-UHFFFAOYSA-N oxygen(2-);titanium(4+) Chemical compound [O-2].[O-2].[Ti+4] SOQBVABWOPYFQZ-UHFFFAOYSA-N 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- CHQMHPLRPQMAMX-UHFFFAOYSA-L sodium persulfate Substances [Na+].[Na+].[O-]S(=O)(=O)OOS([O-])(=O)=O CHQMHPLRPQMAMX-UHFFFAOYSA-L 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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- Treatment Of Water By Oxidation Or Reduction (AREA)
- Physical Water Treatments (AREA)
Abstract
The application relates to the technical field of sewage treatment, and provides a high-grade oxidation combined process reactor, which comprises the following steps: the electrocatalytic oxidation device comprises electrocatalytic oxidation equipment and a reaction tank body, wherein a gas-liquid separation area, a reaction area, a filling area and an aeration area are sequentially arranged in the reaction tank body from top to bottom, a water inlet pipe is arranged at the upper part of the reaction tank body, a water outlet pipe is arranged at the lower part of the reaction tank body, a reactor cover is arranged at the top of the reaction tank body, an exhaust pipe and a dosing device are arranged on the reactor cover, a filter screen is arranged in the gas-liquid separation area, filter cotton is arranged on the filter screen, an ultraviolet lamp tube is arranged in the reaction area, a catalyst filling is arranged in the filling area, an aeration disc is arranged in the aeration area, the aeration disc is connected with an ozone generator arranged outside the reaction tank body, the electrocatalytic oxidation equipment is communicated with the gas-liquid separation area through a water inlet circulation pipe, and the electrocatalytic oxidation equipment is communicated with the aeration area through a water outlet circulation pipe. The advanced oxidation combined process reactor has the characteristics of flexible operation, high treatment efficiency, thorough degradation, small occupied space and the like.
Description
Technical Field
The application belongs to the technical field of sewage treatment, and particularly relates to a high-grade oxidation combined process reactor.
Background
With the rapid development of the industry in China, the types and the quantity of organic species in industrial production are increased, a large amount of refractory organic wastewater is generated, the organic matters in the refractory organic wastewater are difficult to biodegrade, and the main method for treating the refractory organic wastewater at present is advanced oxidation technology, including electrocatalytic oxidation, ozone oxidation, fenton oxidation, photocatalysis, ultraviolet activated persulfate oxidation and the like.
Although the existing advanced oxidation technology has remarkable effect of treating the organic wastewater difficult to degrade, the problems of low treatment capacity, low treatment efficiency and the like still have more limitations in engineering application due to high investment cost and operation cost. The electrocatalytic oxidation technology has strong oxidative degradation capability, but has low current efficiency and higher electric energy consumption; the ozone oxidation technology has small occupied area of equipment, but has large energy consumption and high investment cost; the Fenton oxidation technology needs to add a large amount of medicaments, and needs to treat a large amount of sludge, so that the operation cost is high; the photocatalytic oxidation technology has the problems that the catalyst is difficult to separate from the wastewater and the like; the ultraviolet activated persulfate oxidation has the problems of low treatment efficiency and the like. And the single advanced oxidation process has various defects of single OH conversion path, limited organic matter degradation efficiency and the like.
Therefore, it is an urgent problem to widen the conversion route of OH, and further improve the yield of OH and the organic degradation efficiency.
Disclosure of utility model
Aiming at the problems existing in the single advanced oxidation process in the prior art, the embodiment of the application aims to provide an advanced oxidation combined process reactor which has the characteristics of flexible operation, high treatment efficiency, thorough degradation, small occupied space and the like.
In order to achieve the above purpose, the application adopts the following technical scheme: an advanced oxidation combined process reactor is provided comprising: the electro-catalytic oxidation device comprises electro-catalytic oxidation equipment and a reaction tank body, wherein a gas-liquid separation area, a reaction area, a filler area and an aeration area are sequentially arranged in the reaction tank body from top to bottom, a water inlet pipe is arranged on the upper portion of the reaction tank body, a water outlet pipe is arranged on the lower portion of the reaction tank body, a reactor cover is arranged on the top of the reaction tank body, an exhaust pipe and a dosing device are arranged on the reactor cover, a filter screen is arranged in the gas-liquid separation area, filter cotton is arranged on the filter screen, an ultraviolet lamp tube is arranged in the reaction area, a catalyst filler is arranged in the filler area, an aeration disc is arranged in the aeration area, the aeration disc is connected with an ozone generator arranged outside the reaction tank body, the electro-catalytic oxidation equipment is communicated with the gas-liquid separation area through a water inlet circulation pipe, and the electro-catalytic oxidation equipment is communicated with the aeration area through a water outlet circulation pipe.
In one embodiment, valves are arranged on the water inlet pipe, the water outlet pipe, the exhaust pipe, the water inlet circulating pipe and the water outlet circulating pipe.
In one embodiment, the height ratio of the reaction zone to the packing zone is 3-4:1.
In one embodiment, the reactor cover is a tamper evident closure.
In one embodiment, the catalyst filler comprises an ozone catalyst filler and a photocatalyst.
In one embodiment, the ozone catalyst filler is an activated carbon filler, a silica-alumina composite filler or an alumina filler, and the particle size of the ozone catalyst filler is 3-6mm.
In one embodiment, the photocatalyst is titanium dioxide, cadmium sulfide, or carbon nitride.
In one embodiment, the photocatalyst is located above the ozone catalyst filler.
In one embodiment, the bottom of the filling area is provided with a filling bearing plate, and the aperture of the water passing holes on the filling bearing plate is smaller than 2mm.
In one embodiment, a quartz tube is arranged in the reaction zone, the ultraviolet lamp tube is arranged in the quartz tube, and a condensation water tube is arranged around the quartz tube in the reaction zone.
The advanced oxidation combined process reactor provided by the application has the beneficial effects that:
1. The advanced oxidation combined process reactor combines electrocatalytic oxidation, ozone oxidation, photocatalytic oxidation and ultraviolet activated persulfate oxidation together for coupling reaction, so that three phases of gas, liquid and solid are fully contacted, the advantages of various advanced oxidation processes are synergistically enhanced, the yield and the production rate of OH can be improved, and the degradation rate and the degradation effect of organic matters are improved.
2. The advanced oxidation combined process reactor can realize flexible combination of 4 advanced oxidation processes, carries out multistage treatment according to the requirement, carries out multistage oxidation on organic pollutants difficult to degrade, and solves the problems of low single-stage oxidation efficiency and incomplete oxidation.
3. The advanced oxidation combined process reactor can share 4 advanced oxidation processes in the same reaction space and simultaneously run, improves the space utilization rate of the reaction tank body, and is beneficial to reducing the volume of the reaction tank body and the construction cost thereof.
4. The advanced oxidation combined process reactor is simple to operate, easy to control, safe and reliable.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are needed in the embodiments or the description of the prior art will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a combined advanced oxidation reactor according to an embodiment of the present application;
FIG. 2 is a schematic top view of a packing support plate in an advanced oxidation unit process reactor according to an embodiment of the present application;
FIG. 3 is a graph showing the degradation of organic wastewater by the advanced oxidation unit process reactor according to the embodiment of the application.
Wherein, each reference sign in the figure:
1. An electrocatalytic oxidation device; 2. a reaction tank body; 21. a gas-liquid separation zone; 211. a filter screen; 212. filtering cotton; 22. a reaction zone; 221. an ultraviolet lamp tube; 222. a quartz tube; 223. a condenser water pipe; 23. a filler zone; 231. a catalyst filler; 232. a filler bearing plate; 233. a water passing hole; 24. an aeration zone; 241. an aeration disc; 25. a reactor cover; 3. a water inlet pipe; 31. a water inlet valve; 4. a water outlet pipe; 41. a water outlet valve; 5. an exhaust pipe; 51. an exhaust valve; 6. a dosing device; 7. an ozone generator; 71. an air inlet pipe; 72. an intake valve; 8. a water inlet circulation pipe; 81. a circulating water inlet valve; 9. a water outlet circulation pipe; 91. and (5) circulating a water outlet valve.
Detailed Description
In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the application is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the application.
It will be understood that when an element is referred to as being "mounted" or "disposed" on another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element.
It is to be understood that the terms "length," "width," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are merely for convenience in describing and simplifying the description based on the orientation or positional relationship shown in the drawings, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus are not to be construed as limiting the application.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present application, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
Referring to fig. 1 and 2, an advanced oxidation unit process reactor according to an embodiment of the application will now be described. The advanced oxidation combined process reactor comprises: an electrocatalytic oxidation device 1 and a reaction tank 2, wherein the electrocatalytic oxidation device 1 is described in the patent with publication number CN214693433U filed by the applicant.
In this embodiment, a gas-liquid separation zone 21, a reaction zone 22, a packing zone 23 and an aeration zone 24 are provided in the reaction tank 2 in this order from top to bottom. The upper portion of the reaction tank body 2 is provided with a water inlet pipe 3 communicated with the gas-liquid separation zone 21, the water inlet pipe 3 is provided with a water inlet valve 31, the lower portion of the reaction tank body 2 is provided with a water outlet pipe 4 communicated with the aeration zone 24, and the water outlet pipe 4 is provided with a water outlet valve 41.
The top of the reaction tank body 2 is provided with a reactor cover 25, the whole reaction tank body 2 is of a sealing structure, the reactor cover 25 is an opening and closing type sealing cover, namely, the reactor cover 25 can be opened and closed, and the filter cotton 212, the ultraviolet lamp tube 221 and the catalyst filler 231 are convenient to replace. The reactor cover 25 is provided with an exhaust pipe 5 and a dosing device 6, and the exhaust pipe 5 is provided with an exhaust valve 51; the dosing device 6 is used for adding sulfate into the reaction tank body 2, and generating oxidation reaction to degrade pollutants after ultraviolet light activation. A filter screen 211 is arranged in the gas-liquid separation zone 21, filter cotton 212 is arranged on the filter screen 211, and the filter cotton 212 is used for filtering catalyst powder. An ultraviolet lamp tube 221 is arranged in the reaction zone 22 and is used for realizing ultraviolet activated persulfate oxidation reaction; a catalyst packing 231 is arranged in the packing area 23 and is used for photocatalytic oxidation; an aeration disc 241 is arranged in the aeration zone 24, the aeration disc 241 is connected with an ozone generator 7 arranged outside the reaction tank body 2 through an air inlet pipe 71 and is used for realizing ozone oxidation, and an air inlet valve 72 is arranged on the air inlet pipe 71; the electrocatalytic oxidation device 1 is communicated with the gas-liquid separation zone 21 through the water inlet circulating pipe 8, the electrocatalytic oxidation device 1 is communicated with the aeration zone 24 through the water outlet circulating pipe 9, the water inlet circulating pipe 8 is provided with a circulating water inlet valve 81, the water outlet circulating pipe 9 is provided with a circulating water outlet valve 91, sewage in the gas-liquid separation zone 21 enters the electrocatalytic oxidation device 1 through the water inlet circulating pipe 8, and thus after the filtering effect of the filter cotton 212, the catalyst powder can be effectively prevented from entering the electrocatalytic oxidation device 1 to cause the current mass transfer efficiency.
In this embodiment, the ozone generator 7 is an oxygen source generator, and the ozone concentration is 95% or more.
In the embodiment, a circulating pump and an electrode group are arranged in the electrocatalytic oxidation equipment 1, wherein the cathode is a titanium electrode, the anode is a boron-doped diamond electrode, and the distance between the cathode and the anode is 1.5-2mm; in this embodiment, the height ratio of the reaction zone 22 to the packing zone 23 is 3-4:1, so that the reaction can be more sufficient.
In the present embodiment, the catalyst filler 231 includes an ozone catalyst filler 231 and a photocatalyst. Wherein, the ozone catalyst filler 231 is activated carbon filler, silicon-aluminum composite material filler or alumina filler, and the particle size of the ozone catalyst filler 231 is 3-6mm. The photocatalyst is titanium dioxide, cadmium sulfide or carbon nitride, and can produce oxidation to degrade pollutant under ultraviolet irradiation, and its grain size is nano-scale. Wherein the photocatalyst is located above the ozone catalyst pad 231.
In the present embodiment, the bottom of the packing region 23 is provided with a packing support plate 232, and the diameter of the water passing holes 233 in the packing support plate 232 is smaller than 2mm, preferably 1mm, so that the size of the water passing holes 233 is smaller than the size of the catalyst packing 231, and thus the catalyst packing 231 can be prevented from falling down while passing air through the water.
In this embodiment, a quartz tube 222 is disposed in the reaction area 22, an ultraviolet tube 221 is disposed in the quartz tube 222, the quartz tube 222 is used for protecting the ultraviolet tube 221, a condensation water tube 223 is disposed around the quartz tube 222 in the reaction area 22, water is introduced into the lower end of the condensation water tube 223, water is introduced into the upper end of the condensation water tube 223, and the condensation water tube 223 is communicated with a cooling device outside the reaction tank 2 for cooling the reaction area 22. The cooling device is an existing cooling water circulation device, such as a cooling water circulation machine.
The working procedure of this embodiment is: the high-concentration organic wastewater enters the reaction tank body 2 from the water inlet pipe 3, the circulating water inlet valve 81 and the circulating water outlet valve 91 are opened, the electrocatalytic oxidation equipment 1 is started, the wastewater starts to circulate while undergoing electrocatalytic oxidation reaction, persulfate is added from the dosing device 6, the ultraviolet lamp tube 221 is started, ultraviolet activated persulfate and photocatalytic oxidation reaction are simultaneously carried out, the air inlet valve 72 and the air outlet valve are opened, the ozone generator 7 is started, ozone catalytic oxidation is carried out, the cold water equipment is started, the wastewater enters from the lower part of the condensate pipe 223 and is discharged from the upper part, heat dissipation and cooling are carried out in the reaction process, the water outlet valve is opened after the reaction is completed, and the treated wastewater is discharged from the water outlet pipe 4.
In this example, 4 sets of comparative tests are provided, as follows:
Test 1:
1L of chemical wastewater is added into a reaction tank body 2, the COD of raw water is about 15000mg/L, a circulating water inlet valve 81 and a circulating water outlet valve 91 are closed, an air inlet valve 72 and an air outlet valve are opened, an ozone generator 7 is opened, the ozone yield is 10g/L, the concentration of generated ozone is 95%, a cooling device is opened for cooling, the used catalyst filler 231 is alumina filler with the particle size of 3-6mm, and the COD removal rate of the wastewater is 65.81% after ozone catalytic oxidation reaction for 4 hours.
Test 2:
1L of wastewater which is the same as that of the test 1 is added into a reaction tank body 2, a circulating water inlet valve 81, a circulating water outlet valve 91 and an exhaust valve are opened, an electrocatalytic oxidation device 1 is started, a cathode is a titanium electrode, an anode is a boron doped diamond electrode, the distance between a cathode plate and an anode plate is 2mm, the area of the anode is 420cm 2, the current density is 70mA/cm 2, a cooling device is started in the reaction process to cool, and after electrocatalytic oxidation reaction is carried out for 4 hours, the COD removal rate of the wastewater is measured to be 78.45%.
Test 3:
adding 1L of wastewater which is the same as that of the test 1 into a reaction tank body 2, opening a circulating water inlet and outlet valve, an exhaust valve and an air inlet valve 72, starting an electrocatalytic oxidation device 1, wherein a cathode is a titanium electrode, an anode is a boron-doped diamond electrode, the distance between the cathode and the anode is 2mm, the area of the anode is 420cm < 2 >, and the current density is 70mA/cm 2; simultaneously, the ozone generator 7 is started, the ozone yield is 10g/L, the concentration of the generated ozone is 95%, and the used catalyst filler 231 is alumina filler with the particle size of 3-6 mm; in the reaction process, a cooling device is started to cool, and after 4 hours of electrocatalytic and ozone oxidation coupling reaction, the COD removal rate of the wastewater is measured to be 89.69 percent.
Test 4:
1L of wastewater which is the same as that in test 1 is added into a reaction tank body 2, 5g of sodium persulfate is added into the wastewater through a dosing device 6, the photocatalyst in a catalyst filler 231 is 2g of nano titanium dioxide, and an ultraviolet lamp with 254nm wavelength is started; the exhaust valve and the air inlet valve 72 are opened, the ozone generator 7 is opened, the ozone yield is 10g/L, the concentration of the generated ozone is 95%, and the used catalyst filler 231 is alumina filler with the particle size of 3-6 mm; opening a circulating water inlet valve 81 and a circulating water outlet valve 91, simultaneously opening the electrocatalytic oxidation equipment 1, wherein a cathode is a titanium electrode, an anode is a boron doped diamond electrode, the distance between a cathode plate and an anode plate is 2mm, the area of the anode is 420cm < 2 >, and the current density is 70mA/cm 2; in the reaction process, a cooling device is started to cool, and after 4 hours of electro-catalysis, ozone oxidation, photocatalysis and ultraviolet activation persulfate coupling reaction, the COD removal rate of the wastewater is measured to be 97.91 percent.
As shown in FIG. 3, the comparative effects of tests 1-4 show that the degradation efficiency of a single oxidation process can be improved and the degradation can be more thorough by the combination of advanced oxidation processes.
The foregoing description of the preferred embodiments of the application is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the application.
Claims (6)
1. An advanced oxidation unit process reactor comprising: the electro-catalytic oxidation device comprises electro-catalytic oxidation equipment (1) and a reaction tank body (2), a gas-liquid separation zone (21), a reaction zone (22), a filler zone (23) and an aeration zone (24) are sequentially arranged in the reaction tank body (2), a water inlet pipe (3) is arranged on the upper portion of the reaction tank body (2), a water outlet pipe (4) is arranged on the lower portion of the reaction tank body, a reactor cover (25) is arranged at the top of the reaction tank body (2), an exhaust pipe (5) and a medicine adding device (6) are arranged on the reactor cover (25), a filter screen (211) is arranged in the gas-liquid separation zone (21), filter cotton (212) is arranged on the filter screen (211), an ultraviolet lamp tube (221) is arranged in the reaction zone (22), a catalyst filler (231) is arranged in the filler zone (23), an aeration disc (241) is arranged in the aeration zone (24), the aeration disc (241) is connected with an ozone generator (7) arranged outside the reaction tank body (2), and the electro-catalytic oxidation equipment (1) is communicated with the electro-catalytic oxidation equipment (9) through water inlet (8) and the gas-liquid separation zone (21).
2. The advanced oxidation unit process reactor according to claim 1 wherein: valves are arranged on the water inlet pipe (3), the water outlet pipe (4), the exhaust pipe (5), the water inlet circulating pipe (8) and the water outlet circulating pipe (9).
3. The advanced oxidation unit process reactor according to claim 1 wherein: the height ratio of the reaction zone (22) to the packing zone (23) is 3-4:1.
4. The advanced oxidation unit process reactor according to claim 1 wherein: the reactor cover (25) is an open-close type sealing cover.
5. The advanced oxidation unit process reactor according to claim 4 wherein: the bottom of the filling area (23) is provided with a filling bearing plate (232), and the aperture of a water passing hole (233) on the filling bearing plate (232) is smaller than 2mm.
6. The advanced oxidation unit process reactor according to any one of claims 1 to 5, characterized in that: a quartz tube (222) is arranged in the reaction zone (22), the ultraviolet lamp tube (221) is arranged in the quartz tube (222), and a condensate pipe (223) is arranged in the reaction zone (22) around the quartz tube (222).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322568383.XU CN221051697U (en) | 2023-09-20 | 2023-09-20 | Advanced oxidation combined process reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322568383.XU CN221051697U (en) | 2023-09-20 | 2023-09-20 | Advanced oxidation combined process reactor |
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| Publication Number | Publication Date |
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| CN221051697U true CN221051697U (en) | 2024-05-31 |
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| CN202322568383.XU Active CN221051697U (en) | 2023-09-20 | 2023-09-20 | Advanced oxidation combined process reactor |
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