CN215924643U - Integrated advanced oxidation reaction device - Google Patents
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- CN215924643U CN215924643U CN202121618503.7U CN202121618503U CN215924643U CN 215924643 U CN215924643 U CN 215924643U CN 202121618503 U CN202121618503 U CN 202121618503U CN 215924643 U CN215924643 U CN 215924643U
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Abstract
An integrated advanced oxidation reaction device comprises a first electrolytic chamber, a second electrolytic chamber, a mixing chamber, a first catalytic bed layer, a gas-water separation chamber, a sedimentation tank, an acidification chamber and a second catalytic bed layer; the first anode chamber of the first electrolysis chamber is communicated with the first cathode chamber, and the first cathode chamber is communicated with the mixing chamber; the mixing chamber is provided with a water inlet, the upper end of the mixing chamber is communicated with the first catalytic bed layer, and the upper end of the first catalytic bed layer is communicated with the gas-water separation chamber; the effluent of the gas-water separation chamber is communicated with a sedimentation tank; a sludge discharge port of the sedimentation tank is communicated with the acidification chamber, the lower end of the acidification chamber is communicated with the second catalytic bed layer, and the acidification chamber is also communicated with the mixing chamber; the second anode chamber and the second cathode chamber of the second electrolysis chamber receive effluent of the sedimentation tank, and the effluent also enters the first anode chamber; a gas outlet of the second anode chamber is communicated with the first cathode chamber; and a gas outlet of the second cathode chamber is communicated with the second catalytic bed layer. The method takes the water in the wastewater as a treatment medium, and has the advantages of high efficiency, environmental friendliness, no secondary pollution and the like when the polluted water body is repaired.
Description
Technical Field
The utility model relates to the technical field of water pollution control, in particular to an integrated advanced oxidation reaction device.
Background
In the last four decades, with the rapid development of the industry in China, a large amount of industrial organic wastewater and waste are discharged into water in disorder, the self-purification capacity of the water body is exceeded, and the water environment is seriously polluted. Because organic pollution components in industrial wastewater are complex and have certain biological toxicity, the organic pollution components cannot be effectively removed by a conventional water treatment process. If people and livestock drink polluted water, pollutants can be taken into the body through drinking water, can significantly affect the endocrine system, are accumulated in the body, are difficult to metabolize rapidly, and can cause canceration, distortion and gene mutation of organisms for a long time. With the increasing importance of people on their health, a water treatment process capable of efficiently removing organic pollution is urgently needed to ensure the safety of water body environment.
A physicochemical treatment mode represented by advanced Oxidation AOPs (advanced Oxidation processes) technology is a new water treatment technology which has emerged for nearly 20 years, and the essence of the technology is to generate active species (such as hydroxyl radical. OH and singlet oxygen) through artificial enhancement1O2Sulfate radical SO4 -·Reactive Oxygen Species (ROS) represented by a percarbonate radical, or atomic hydrogen) and the degradation thereof to remove organic substances in water, so that the active Oxygen Species are rapidly mineralized and degraded into CO2And water, or is efficiently reduced to biodegradable matter.
The physicochemical treatment mode has the characteristic of fast process reaction and is theoretically suitable for treating all organic wastewater, but no matter which active species is taken as the main species, the physicochemical treatment mode can only singly oxidize or reduce specific pollutants and cannot treat the pollutants at the same time; meanwhile, in order to produce active species to degrade pollutants, a large amount of chemical agents are usually added, only part of components in the chemical agents usually play a role, the rest components do not play a role, and finally the chemical agents enter a water body and can further react with other substances in the water to generate potential/actual new pollutants so as to cause secondary pollution. For example, a large amount of ferrous salt and hydrogen peroxide are required to be added in the Fenton reaction (Fenton reaction) to maintain the generation of OH, and a large amount of iron mud is generated when the pH is adjusted to 6-9 after the reaction is finished to meet the discharge requirement; with SO4 -·In the advanced oxidation reaction which is mainly carried out, persulfate needs to be continuously added to meet the requirement of SO4 -·Is continuously generated, after the reaction is finished, SO in the effluent is generated4 2-The content is extremely high. The reason for this is that the above treatment methods all regard water and pollutants as two independent individuals, and water can only be purified passively by removing pollutants, and cannot participate in the purification treatment itself.
Therefore, how to solve the above-mentioned deficiencies of the prior art is a problem to be solved by the present invention.
Disclosure of Invention
The utility model aims to provide an integrated advanced oxidation reaction device.
In order to achieve the purpose, the utility model adopts the technical scheme that:
an integrated advanced oxidation reaction device comprises a first electrolytic chamber, a second electrolytic chamber, a mixing chamber, a first catalytic bed layer, a gas-water separation chamber, a sedimentation tank, an acidification chamber and a second catalytic bed layer;
wherein the first electrolysis chamber, the mixing chamber, the first catalytic bed layer and the gas-water separation chamber are sequentially combined from bottom to top;
the first electrolysis chamber comprises a first power supply, a first anode chamber and a first cathode chamber; the anode of the first power supply corresponds to the first anode chamber, and the cathode of the first power supply corresponds to the first cathode chamber; the first anode chamber is provided with a water inlet and is communicated with the first cathode chamber; the first cathode chamber is communicated with the mixing chamber; the mixing chamber is also provided with a water inlet; the upper end of the mixing chamber is communicated with the first catalytic bed layer, and the upper end of the first catalytic bed layer is communicated with the gas-water separation chamber; the gas-water separation chamber is communicated with the mixing chamber through a gas return pipe, and meanwhile, the water outlet of the gas-water separation chamber is communicated with the sedimentation tank;
the sedimentation tank, the acidification chamber and the second catalytic bed layer are sequentially combined from top to bottom; the sludge discharge port at the lower end of the sedimentation tank is communicated with the acidification chamber, the lower end of the acidification chamber is communicated with the second catalytic bed layer, and the acidification chamber is also communicated with the mixing chamber;
the second electrolysis chamber comprises a second power supply, a second anode chamber and a second cathode chamber; the anode of the second power supply corresponds to the second anode chamber, and the cathode of the second power supply corresponds to the second cathode chamber; the second anode chamber and the second cathode chamber are respectively provided with a water inlet, the water inlet receives the effluent of the sedimentation tank, and the effluent of the sedimentation tank is also communicated with the water inlet of the first anode chamber;
the gas outlet of the second anode chamber is communicated with the first cathode chamber of the first electrolysis chamber;
and a gas outlet of the second cathode chamber is communicated with the second catalytic bed layer.
The relevant content in the above technical solution is explained as follows:
1. in the above scheme, the device further comprises a first gas and water distribution plate, and the first gas and water distribution plate is arranged between the first cathode chamber and the mixing chamber.
2. In the above scheme, still include the mixing plate, this mixing plate sets up in the top of mixing chamber.
3. In the above scheme, the catalyst bed further comprises a stirrer, and the stirrer is arranged in a space between the mixing chamber and the first catalyst bed layer.
4. In the above scheme, the catalyst bed further comprises a second gas and water distribution plate, and the second gas and water distribution plate is arranged at the bottom of the second catalytic bed layer.
5. In the above scheme, the device further comprises a first water outlet return pipe, a second water outlet return pipe, a third water outlet return pipe and a fourth water outlet return pipe, wherein each water outlet return pipe is communicated with the water outlet of the sedimentation tank, the first water outlet return pipe is communicated with the first anode chamber, the second water outlet return pipe is communicated with the mixing chamber, and the third water outlet return pipe is communicated with the second anode chamber and the second cathode chamber; and the fourth water outlet return pipe is communicated with the acidification chamber.
The working principle and the advantages of the utility model are as follows:
the utility model regards pollutants and water in the waste water as a unified whole, takes the water in the waste water as a medium, and spontaneously generates active substances for purifying the pollutants in the waste water through manual regulation, thereby achieving the purpose of reducing secondary pollution; after the purification is finished, redundant active substances can be artificially regulated to generate water again.
The utility model removes floating materials and particles in water through pretreatment, adjusts pH, and then leads water and dissolved oxygen in the wastewater to be spontaneously decomposed to generate oxidative ROS (hydrogen peroxide, ozone, OH and singlet oxygen) through external input light, electricity, sound, heat or radiation or specific catalysts1O2) And alsoThe original atomic hydrogen and hydrogen gas directly react with the pollutants in the water to degrade and remove the pollutants.
The utility model solves the problems of physicochemical treatment, particularly large-scale storage and addition of reaction reagents in advanced oxidation reaction, all the reaction reagents are prepared on site in real time, and the problem of generating a large amount of iron mud in the application of a Fenton method is also solved. The method is used for repairing the organic substance polluted water body and has the advantages of high efficiency, environmental friendliness, no secondary pollution and the like.
The advantages of the utility model include:
1. the reaction can be carried out at normal temperature and normal pressure, complex operation is not needed, the process is compact and easy to operate, the design of a water treatment unit module is simple, and reaction modules can be flexibly increased and decreased according to needs;
2. only acid and alkali agents are added to adjust the pH value, so that the periodic self-supplement of Fe (II) can be realized, the mineralization and degradation of organic matters are fast and thorough, the application range is wide, and the catalyst can be repeatedly used for a long time;
3. the method is environment-friendly and does not cause secondary pollution;
4. the utilization rate of the iron mud is improved, and the disposal cost of the iron mud is reduced.
Drawings
Fig. 1 is a block diagram of the structure of an embodiment of the present invention.
In the above drawings: 1. a first electrolysis chamber; 2. a second electrolysis chamber; 3. a mixing chamber; 4. a first catalytic bed layer; 5. a gas-water separation chamber; 6. a sedimentation tank; 7. an acidification chamber; 8. a second catalytic bed layer; 9. a first power supply; 10. a first anode chamber; 11. a first cathode compartment; 12. a first gas and water distribution plate; 13. a water inlet; 14. a mixing plate; 15. a stirrer; 16. a gas return pipe; 17. a second gas and water distribution plate; 18. a partition plate; 19. a first hydrogen return pipe; 20. a second hydrogen reflux pipe; 21. a second power supply; 22. a second anode chamber; 23. a second cathode compartment; 24. an oxygen pipeline; 25. a first water outlet return pipe; 26. a second water outlet return pipe; 27. a third water outlet return pipe; 28. and a fourth water outlet return pipe.
Detailed Description
The utility model is further described with reference to the following figures and examples:
example (b): the present disclosure will be described more fully hereinafter with reference to the accompanying drawings, in which embodiments of the disclosure may be shown and described, and which, when modified and varied by the techniques taught herein, can be made by those skilled in the art without departing from the spirit and scope of the disclosure.
The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the disclosure. The singular forms "a", "an", "the" and "the", as used herein, also include the plural forms.
The terms "first," "second," and the like, as used herein, do not denote any order or importance, nor do they denote any order or importance, but rather are used to distinguish one element from another element or operation described in such technical terms.
As used herein, the terms "comprising," "including," "having," and the like are open-ended terms that mean including, but not limited to.
As used herein, the term (terms), unless otherwise indicated, shall generally have the ordinary meaning as commonly understood by one of ordinary skill in the art, in this written description and in the claims. Certain words used to describe the disclosure are discussed below or elsewhere in this specification to provide additional guidance to those skilled in the art in describing the disclosure.
Referring to the attached figure 1, the integrated advanced oxidation reaction device comprises a first electrolytic chamber 1, a second electrolytic chamber 2, a mixing chamber 3, a first catalytic bed layer 4, a gas-water separation chamber 5, a sedimentation tank 6, an acidification chamber 7 and a second catalytic bed layer 8.
The first electrolysis chamber 1, the mixing chamber 3, the first catalytic bed layer 4 and the gas-water separation chamber 5 are sequentially combined from bottom to top.
The first electrolysis chamber 1 comprises a first power supply 9, a first anode chamber 10 and a first cathode chamber 11; the anode of the first power supply 9 corresponds to the first anode chamber 10, and the cathode corresponds to the first cathode chamber 11. The first anode chamber 10 is provided with a water inlet, the first anode chamber 10 is communicated with the first cathode chamber 11, oxygen generated by the first anode chamber 10 enters the first cathode chamber 11 along with effluent to participate in electrochemical reaction to generate hydrogen peroxide, and the first cathode chamber 11 is communicated with the mixing chamber 3.
The device also comprises a first gas and water distribution plate 12, wherein the first gas and water distribution plate 12 is arranged between the first cathode chamber 11 and the mixing chamber 3.
The mixing chamber 3 also has a water inlet 13 for receiving pretreated wastewater. The upper end of the mixing chamber 3 is communicated with the first catalytic bed layer 4, and the upper end of the first catalytic bed layer 4 is communicated with the gas-water separation chamber 5.
A mixing plate 14 is also included, which mixing plate 14 is arranged above the mixing chamber 3. Hydrogen peroxide and hydrogen enter the mixing chamber 3 after being rectified by the first gas distribution and water distribution plate 12, are fully mixed with wastewater after suspended particles and large floaters in the water are removed by pretreatment and Fe (II) obtained by activation and regeneration of the acidification chamber, are uniformly distributed by the mixing plate 14, and are mineralized by ROS (reactive oxygen species) generated by reaction of hydrogen peroxide and Fe (II).
And the device also comprises an agitator 15, and the agitator 15 is arranged in a space between the mixing chamber 3 and the first catalytic bed layer 4. The gas is rotated at high speed by the stirrer 15 and broken into micro-nano bubbles, part of odor, chromaticity, germs and organic matters in the water can be removed, the organic matters in the wastewater are mineralized and degraded by the catalysis of the catalyst in the first catalytic bed layer 4, and part of Fe (III) can be reduced into Fe (II) in an accelerated way.
The catalyst in the first catalyst bed 4 can be a mixture of palladium-plated iron shavings and copper shavings, or a mixture of palladium-plated iron shavings and activated carbon. The mixture is compressed and framed to be fixed to form the first catalytic bed layer 4. The catalytic mechanism is as follows: through the primary cell reaction (iron-carbon primary cell, iron-copper primary cell, palladium-iron primary cell), ferrous iron is dissolved out to participate in Fenton reaction, and meanwhile, hydrogen escaping from the cathode chamber is subjected to Pd0Active hydrogen is generated by adsorption and activation, and is used for accelerating the reduction of Fe (III) to Fe (II) after the Fenton reaction, and further participating in the Fenton reaction to generate ROS to degrade organic matters.
The gas-water separation chamber 5 is communicated with the mixing chamber 3 through a gas return pipe 16, and meanwhile, the water outlet of the gas-water separation chamber 5 is communicated with the sedimentation tank 6; after the gas-water mixture is separated by the gas-water separation chamber 5, the gas flows back to the mixing chamber 3 through the gas return pipe 16 to continue to participate in the reaction, and the effluent enters the sedimentation tank 6 to be subjected to mud-water separation after the pH value of the effluent is adjusted to 6-9, and then the effluent is discharged after reaching the standard.
The sedimentation tank 6, the acidification chamber 7 and the second catalytic bed layer 8 are sequentially combined from top to bottom; and a sludge discharge port at the lower end of the sedimentation tank 6 is communicated with the acidification chamber 7, the lower end of the acidification chamber 7 is communicated with the second catalytic bed layer 8, and the acidification chamber 7 is also communicated with the mixing chamber 3. The catalyst also comprises a second gas and water distribution plate 17, and the second gas and water distribution plate 17 is arranged at the bottom of the second catalytic bed layer 8.
The sludge is concentrated under the action of gravity, enters the acidification chamber 7 through a sludge discharge port, is catalyzed by a catalyst in the second catalytic bed layer 8, Fe (III) in the sludge can be reduced into Fe (II) by hydrogen rectified by the second gas distribution and water distribution plate 17 in an accelerating way, enters the mixing chamber 3 through a channel formed by the partition plate 18 and continues to react, and redundant hydrogen is connected into the first hydrogen return pipe 19 through the second hydrogen return pipe 20 and returns to the acidification chamber 7 to continue to react.
The catalyst in the second catalytic bed layer 8 can be made of palladium-loaded MOFs materials or COFs materials, and the materials are compressed and then framed to be fixed to form the second catalytic bed layer 8. The catalytic mechanism is as follows: active hydrogen is generated through the adsorption activation of the active hydrogen, and is used for accelerating the reduction of Fe (III) into Fe (II) after the Fenton reaction.
The second electrolysis chamber 2 comprises a second power supply 21, a second anode chamber 22 and a second cathode chamber 23; the anode of the second power supply 21 corresponds to the second anode chamber 22, and the cathode corresponds to the second cathode chamber 23; the second anode chamber 22 and the second cathode chamber 23 each have a water inlet that receives the effluent of the sedimentation tank 6, and the effluent of the sedimentation tank 6 is also communicated with the water inlet of the first anode chamber 10.
The second anode chamber 22 is used for generating oxygen, and is communicated with the first cathode chamber 11 of the first electrolysis chamber 1 through an oxygen pipeline 24 for electrolyzing to generate hydrogen peroxide.
The second cathode chamber 23 is used for generating hydrogen, is communicated with the second catalyst bed 8 through a first hydrogen return pipe 19 and enters the acidification chamber 7, accelerates the reduction of Fe (III) and the regeneration of Fe (II) under the catalysis of the catalyst in the second catalyst bed 8, and enters the mixing chamber 3 after passing through the partition plate 18.
The device also comprises a first water outlet return pipe 25, a second water outlet return pipe 26, a third water outlet return pipe 27 and a fourth water outlet return pipe 28, wherein each water outlet return pipe is communicated with the water outlet of the sedimentation tank 6, and the first water outlet return pipe 25 is communicated with the first anode chamber 10 and is used for electrolyzing water to generate oxygen; the second water outlet return pipe 26 is communicated with the mixing chamber 3, and the outlet water is returned to the mixing chamber 3, so that the hydraulic mixing effect can be enhanced, and the pollutant concentration can be reduced; the third outlet return pipe 27 is connected to the second anode chamber 22 and the second cathode chamber 23 for generating oxygen and hydrogen by electrolysis. The fourth water return pipe 28 is communicated with the acidification chamber 7, and meanwhile, an acid substance is put into the acidification chamber 7 through the fourth water return pipe 28, so that the pH value in the acidification chamber 7 is adjusted, and the iron mud is conveniently acidified and dissolved.
The working principle of the present invention is now explained as follows:
after suspended particulate matters and large floaters in the wastewater are removed through pretreatment, the wastewater, hydrogen peroxide generated by the first cathode chamber 11, hydrogen which is not completely reacted and Fe (II) obtained by activation and regeneration of the acidification chamber 7 are fully mixed in the mixing chamber 3 and are uniformly distributed through a mixing plate 14, and gas is rotated at a high speed by a stirrer 15 and is smashed into micro-nano bubbles, so that part of odor, chroma, germs and organic matters in the water can be removed; through the catalytic action of the first catalytic bed layer 4, organic matters in the wastewater are mineralized and degraded, and part of Fe (III) can be reduced into Fe (II) in an accelerated way; after the gas-water mixture is separated by the gas-water separation chamber 5, the gas flows back to the mixing chamber 3 through the gas return pipe 16 to continue to participate in the reaction, and the effluent is subjected to sludge-water separation after the pH value is adjusted to 6-9 and then is discharged after reaching the standard; the sludge is concentrated under the action of gravity and then enters an acidification chamber 7, Fe (III) can be accelerated and reduced into Fe (II) by hydrogen under the action of a catalyst, and the Fe (III) can continue to react after entering a mixing chamber 3. After the effluent reaches the standard, part of the effluent flows back into the mixing chamber 3 to enhance the hydraulic mixing effect and reduce the concentration of pollutants; the other part of the hydrogen and oxygen are used as raw materials for generating hydrogen and oxygen and enter the second electrolysis chamber 2, the generated hydrogen is used for reducing Fe (III) in the acidification chamber 7, and the generated oxygen enters the first cathode chamber 11 of the first electrolysis chamber 1 and is used as a raw material for generating hydrogen peroxide.
The utility model solves the problems of physicochemical treatment, particularly large-scale storage and addition of reaction reagents in advanced oxidation reaction, all the reaction reagents are prepared on site in real time, and the problem of generating a large amount of iron mud in the application of a Fenton method is also solved. The method is used for repairing the organic substance polluted water body and has the advantages of high efficiency, no selectivity, environmental friendliness, no secondary pollution and the like.
The above embodiments are merely illustrative of the technical ideas and features of the present invention, and the purpose thereof is to enable those skilled in the art to understand the contents of the present invention and implement the present invention, and not to limit the protection scope of the present invention. All equivalent changes and modifications made according to the spirit of the present invention should be covered within the protection scope of the present invention.
Claims (6)
1. The utility model provides an advanced oxidation reaction unit of integral type which characterized in that: comprises a first electrolytic chamber, a second electrolytic chamber, a mixing chamber, a first catalytic bed layer, a gas-water separation chamber, a sedimentation tank, an acidification chamber and a second catalytic bed layer;
wherein the first electrolysis chamber, the mixing chamber, the first catalytic bed layer and the gas-water separation chamber are sequentially combined from bottom to top;
the first electrolysis chamber comprises a first power supply, a first anode chamber and a first cathode chamber; the anode of the first power supply corresponds to the first anode chamber, and the cathode of the first power supply corresponds to the first cathode chamber; the first anode chamber is provided with a water inlet and is communicated with the first cathode chamber; the first cathode chamber is communicated with the mixing chamber; the mixing chamber is also provided with a water inlet; the upper end of the mixing chamber is communicated with the first catalytic bed layer, and the upper end of the first catalytic bed layer is communicated with the gas-water separation chamber; the gas-water separation chamber is communicated with the mixing chamber through a gas return pipe, and meanwhile, the water outlet of the gas-water separation chamber is communicated with the sedimentation tank;
the sedimentation tank, the acidification chamber and the second catalytic bed layer are sequentially combined from top to bottom; the sludge discharge port at the lower end of the sedimentation tank is communicated with the acidification chamber, the lower end of the acidification chamber is communicated with the second catalytic bed layer, and the acidification chamber is also communicated with the mixing chamber;
the second electrolysis chamber comprises a second power supply, a second anode chamber and a second cathode chamber; the anode of the second power supply corresponds to the second anode chamber, and the cathode of the second power supply corresponds to the second cathode chamber; the second anode chamber and the second cathode chamber are respectively provided with a water inlet, the water inlet receives the effluent of the sedimentation tank, and the effluent of the sedimentation tank is also communicated with the water inlet of the first anode chamber;
the gas outlet of the second anode chamber is communicated with the first cathode chamber of the first electrolysis chamber;
and a gas outlet of the second cathode chamber is communicated with the second catalytic bed layer.
2. The integrated advanced oxidation reaction apparatus according to claim 1, wherein: the mixing chamber is characterized by also comprising a first gas and water distribution plate which is arranged between the first cathode chamber and the mixing chamber.
3. The integrated advanced oxidation reaction apparatus according to claim 1, wherein: also included is a mixing plate disposed above the mixing chamber.
4. The integrated advanced oxidation reaction apparatus according to claim 1, wherein: the catalyst also comprises a stirrer which is arranged in a space between the mixing chamber and the first catalytic bed layer.
5. The integrated advanced oxidation reaction apparatus according to claim 1, wherein: the catalyst also comprises a second gas and water distribution plate which is arranged at the bottom of the second catalytic bed layer.
6. The integrated advanced oxidation reaction apparatus according to claim 1, wherein: the device also comprises a first water outlet return pipe, a second water outlet return pipe, a third water outlet return pipe and a fourth water outlet return pipe, wherein each water outlet return pipe is communicated with the water outlet of the sedimentation tank, the first water outlet return pipe is communicated with the first anode chamber, the second water outlet return pipe is communicated with the mixing chamber, and the third water outlet return pipe is communicated with the second anode chamber and the second cathode chamber; and the fourth water outlet return pipe is communicated with the acidification chamber.
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| CN202121618503.7U CN215924643U (en) | 2021-07-15 | 2021-07-15 | Integrated advanced oxidation reaction device |
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| CN202121618503.7U CN215924643U (en) | 2021-07-15 | 2021-07-15 | Integrated advanced oxidation reaction device |
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