CN111099715A - Plug flow type reactor based on multi-point feeding - Google Patents
Plug flow type reactor based on multi-point feeding Download PDFInfo
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- CN111099715A CN111099715A CN202010023458.4A CN202010023458A CN111099715A CN 111099715 A CN111099715 A CN 111099715A CN 202010023458 A CN202010023458 A CN 202010023458A CN 111099715 A CN111099715 A CN 111099715A
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 230000007704 transition Effects 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 33
- 238000000926 separation method Methods 0.000 claims abstract description 30
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 14
- 238000007254 oxidation reaction Methods 0.000 claims description 29
- 230000003647 oxidation Effects 0.000 claims description 20
- 239000002351 wastewater Substances 0.000 claims description 11
- 239000010865 sewage Substances 0.000 claims description 6
- 238000000034 method Methods 0.000 abstract description 12
- 230000010354 integration Effects 0.000 abstract description 4
- 239000002957 persistent organic pollutant Substances 0.000 abstract description 4
- 230000015556 catabolic process Effects 0.000 abstract description 2
- 238000006731 degradation reaction Methods 0.000 abstract description 2
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 230000036632 reaction speed Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 230000008569 process Effects 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 4
- 239000010842 industrial wastewater Substances 0.000 description 4
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- SXDBWCPKPHAZSM-UHFFFAOYSA-M bromate Inorganic materials [O-]Br(=O)=O SXDBWCPKPHAZSM-UHFFFAOYSA-M 0.000 description 1
- SXDBWCPKPHAZSM-UHFFFAOYSA-N bromic acid Chemical compound OBr(=O)=O SXDBWCPKPHAZSM-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000006056 electrooxidation reaction Methods 0.000 description 1
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000008239 natural water Substances 0.000 description 1
- 231100000956 nontoxicity Toxicity 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000009279 wet oxidation reaction Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The application provides a plug flow reactor based on multi-point feeding. The plug-flow reactor has a water inlet, a water outlet, and a reactor wall2O2An adding and mixing integrated module connected with the water inlet, the H2O2At least one group of O is connected in sequence under the feeding and mixing integrated module3/H2O2Dosing integration module and O3/H2O2A reaction transition module, a gas-liquid separation module connected with the water outlet and arranged at the upstream side of the water outlet, wherein the pipe diameter of the gas-liquid separation module is larger than the O connected with the gas-liquid separation module3/H2O2The pipe diameter of the reaction transition module. The invention has the advantages of high reaction speed, short time, full reaction, low energy consumption, high reaction efficiency and difficult degradation of organic pollutants, and the utilization rate of O3 reaches more than 90 percentThe removal rate reaches more than 60 percent, and the method has the advantages of no secondary pollution, simple and convenient operation, small occupied area and high automation level.
Description
Technical Field
The application relates to the field of sewage treatment, in particular to a multipoint feeding plug flow type reactor based on a high-efficiency ozone oxidation water treatment technology.
Background
The whole wastewater discharge amount of China increases year by year, and the natural water body deteriorates continuously. The pH value, the Chemical Oxygen Demand (COD) and the ammonia nitrogen are three main pollutants, and the Chemical Oxygen Demand (COD) is at the top. In terms of pollution sources, industrial wastewater is the most serious pollution.
The treated water source of the industrial wastewater upgrading and advanced treatment project is effluent subjected to biological aerobic treatment, the ratio of BOD/COD (biochemical oxygen demand/chemical oxygen demand) (B/C ratio for short) is quite low and even lower than 0.1, and the industrial wastewater is called refractory wastewater. Therefore, in order to further reduce the COD (chemical oxygen demand) value, a more efficient oxidation treatment technique must be employed. The advanced oxidation technology is a key technology meeting the requirement, and removes or degrades pollutants in water, solid and gas by generating hydroxyl radicals with strong oxidation capacity to perform oxidation reaction, so that organic pollutants with difficult degradation of macromolecules are degraded into low-toxicity or non-toxicity micromolecules or water. Advanced oxidation techniques can be classified into photochemical oxidation techniques, electrochemical oxidation techniques, and O, depending on the mechanism of hydroxyl radical generation and reaction conditions3/H2O2Oxidation technology, Fenton (Fenton) oxidation technology, catalytic wet oxidation technology, and the like. Wherein, compared with other advanced oxidation technologies, O3/H2O2The advanced oxidation technology has the remarkable advantages of no secondary pollution, mild reaction conditions and clean and easily-obtained oxidant, and becomes a great hotspot in the technical field of industrial wastewater upgrading and advanced treatment in recent years.
However, O3/H2O2In practical application of advanced oxidation technology, the phenomenon that the oxygen is caused by O often appears3Large equipment scale, high operation energy consumption, unsatisfactory treatment effect and the like caused by low utilization rateThe method has multiple problems and reflects the project investment cost and the operation cost, namely the technical economy is poor.
Therefore, the existing O needs to be treated3/H2O2Advanced oxidation technology is upgraded.
Disclosure of Invention
In view of the above, the present application provides a multi-point feeding plug flow reactor based on the high efficiency ozone oxidation water treatment technology. The reactor is added with O through a plurality of feeding points3And/or H2O2To degrade organic pollutants in sewage (wastewater) and to suppress the formation of bromate therein. The reactor O3The utilization rate of the water-based anti-impact agent reaches more than 90 percent, the reaction is rapid, the volume load is high, the occupied area is small, the process conditions can be flexibly adjusted according to the water quality, and the anti-impact capability is strong.
In order to achieve the above-mentioned purpose, the present application adopts the following scheme,
a plug-flow reactor based on multi-point feeding is characterized by comprising a water inlet, a water outlet and a reactor body, wherein the reactor body is provided with a water inlet, a water outlet and a reactor body2O2The upstream side of the feeding and mixing integrated module is connected with the water inlet, and the downstream side of the feeding and mixing integrated module is sequentially connected with at least one group of O3/H2O2Dosing integration module and O3/H2O2A reaction transition module;
a gas-liquid separation module connected to the water outlet and disposed upstream of the water outlet, the gas-liquid separation module having a pipe diameter larger than the O connected thereto3/H2O2The pipe diameter of the reaction transition module. The reactor O3 has a utilization rate of more than 90%, and has the advantages of rapid reaction, high volume load, small occupied area, flexible adjustment of process conditions according to water quality, and strong impact resistance.
Preferably, the pipe diameter of the gas-liquid separation module is equal to the diameter of the O3/H2O2The ratio of the pipe diameters of the reaction transition modules is 1.2-5.
Preferably, the pipe diameter of the gas-liquid separation module is equal to the diameter of the O3/H2O2The tube diameter ratio of the reaction transition modules is 1.5, 2, 3, 4 and 5.
Preferably, the O is3/H2O2The feeding and mixing integrated module comprises a pressing device and a turbulent mixer,
wherein the forcer is located upstream of the turbulator.
Preferably, the pressing device adopts a right-angle retraction tube or a step perforation tube, O3/H2O2Is added and then converges at O3/H2O2And adding the radial center of the mixing integrated module.
Preferably, the turbulator is a rotating mixer or a plate mixer.
Preferably, the gas-liquid separation module is located at the last group of O3/H2O2The pipe diameter of the gas-liquid separation module is larger than that of the reaction transition module at the downstream side3/H2O2The pipe diameter of the reaction transition module.
Preferably, the plug-flow reactor comprises a transverse S-shaped structure or a vertical S-shaped structure,
wherein, when the plug flow type reactor is in a transverse S-shaped structure, the gas-liquid separation module is positioned in the last group of O3/H2O2After the reaction transition module;
when the plug-flow reactor is of a vertical S-shaped structure, the gas-liquid separation modules are distributed at the highest point of the reactor.
Preferably, the plug-flow reactor operates on O3Oxidation module or O3/H2O2In the oxidation mode, the oxidation reaction solution is prepared,
wherein, O3In the oxidation mode, H is not provided2O2Feeding and mixing integrated module, O3O is arranged after the feeding and mixing integrated module3A reaction transition module; o is3-H2O2In the oxidation mode, set H2O2Feeding and mixing integrated module, O3O is arranged after the feeding and mixing integrated module3-H2O2And a reaction transition module.
Preferably, the plug-flow reactor based on multi-point feeding is characterized in that H is fed2O2The concentration is between 0 and 50mg/L, further comprises O3Adding O into a mixing and integrating module3Gas/liquid ratio (Nm) to influent wastewater3/m3) 0.01 to 0.50, the retention time of the sewage in the plug flow reactor is 10s to 10min, and the flow velocity is 0.3 to 3.0 m/s.
Advantageous effects
Compared with the prior art, the implementation mode of the reactor has the advantages that the utilization rate of the O3 of the reactor is over 90 percent, the reaction is rapid, the volume load is high, the occupied area is small, the process conditions can be flexibly adjusted according to the water quality, and the impact resistance is strong.
Drawings
Other features and aspects of the present application will become apparent from the following detailed description of exemplary embodiments, which proceeds with reference to the accompanying drawings.
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate exemplary embodiments, features, and aspects of the application and, together with the description, serve to explain the principles of the application.
FIG. 1a, FIG. 1b, and FIG. 1c are schematic structural diagrams of a lateral plug-flow reactor according to an embodiment of the present invention;
FIGS. 2a and 2b are schematic structural diagrams of a vertical plug-flow reactor according to an embodiment of the present disclosure;
FIG. 3a and FIG. 3b are O in the embodiment of the present application3/H2O2And the structural schematic diagram of the feeding and mixing integrated module.
Detailed Description
Various exemplary embodiments, features and aspects of the present application will be described in detail below with reference to the accompanying drawings. In the drawings, like reference numbers can indicate functionally identical or similar elements. While the various aspects of the embodiments are presented in drawings, the drawings are not necessarily drawn to scale unless specifically indicated.
The embodiment of the application provides a plug flow type reactor with an S-shaped structure, wherein O is added to the plug flow type reactor through a plurality of adding points3(ozone) and/or H2O2(Hydrogen peroxide) to degrade organic pollutants in wastewater having H2O2Dosing and mixing integrated module, the connection of whichThe water inlet is arranged at the downstream side of the water inlet side H2O2The downstream of the feeding and mixing integrated module is sequentially connected with at least one O3/H2O2Dosing integration Module, O3/H2O2A reaction transition module, a gas-liquid separation module connected with the water outlet and arranged at the upstream side of the water outlet, wherein the pipe diameter of the gas-liquid separation module is larger than O3/H2O2The pipe diameter of the reaction transition module. Thus the reactor O3The utilization rate is more than 90%, the reaction is rapid, the volume load is high, the occupied area is small, the process conditions can be flexibly adjusted according to the water quality, and the impact resistance is strong.
The embodiments presented in this application are described below with reference to examples.
FIG. 1a, FIG. 1b, and FIG. 1c are schematic structural diagrams of a lateral plug-flow reactor according to an embodiment of the present invention; a plug-flow reactor with a water inlet 101, a water outlet 102 and an O3/H2O2The reaction transition module 103 is provided with an H at the foremost end2O2And a dosing and mixing integrated module (101 a). H2O26 groups of O are arranged behind the feeding and mixing integrated module (101a)3/H2O2A dosing and mixing integrated module (105). Each group of O3O is arranged after the feeding and mixing integrated module3/H2O2A reaction transition module (103). And then a gas-liquid separation module (104) is arranged. In other embodiments, the oxygen content may be 2, 3, 4, 5, etc3/H2O2Dosing mixing integrated module and O3/H2O2The reaction transition module is not limited herein. In this embodiment, 1O is used3/H2O2Adding and mixing integrated module and 1O connected with same3/H2O2The reaction transition module is referred to as group 1. The plug flow type reactor is in a spiral pushing and rising structure, a water inlet 101 is arranged on one side of the bottom of the plug flow type reactor, a water outlet 102 is arranged on the top of the plug flow type reactor, and a gas-liquid separation module 104 is arranged on the upstream side of the water outlet 102. Preferably, the pipe diameter of the gas-liquid separation module 104 is larger than O3/H2O2The tube diameter of the reaction transition module (or the tube diameter of the reaction transition module connected thereto), in one embodiment, each group O3/H2O2Dosing mixing integrated module and O3/H2O2The pipe diameters of the reaction transition modules are the same. Through such design pipe diameter increase through reducing in order to reduce the water velocity in it, realize release and separation of excess gas. In one embodiment, the ratio of the pipe diameter of the gas-liquid separation module to the pipe diameter of the upstream side thereof is 1.2 to 5. For example, the ratio of the tube diameter of the gas-liquid separation module to the tube diameter of the upstream side thereof is 1.5, 2, 3, 4, 5. In the present embodiment, the upstream/downstream is in terms of the flow direction of the wastewater in the plug flow reactor. In the plug flow reactor, the components are connected with each other through flanges. For example, a seal is provided between two flanges, which reduces the possibility of leakage. And in terms of the water flow direction, the front end faces of all the feeding and mixing integrated modules are consistent and can be replaced mutually. The rear end faces of all the feeding and mixing integrated modules are kept consistent. So that they can be interchanged.
In one embodiment, O3/H2O2The feeding and mixing integrated module consists of a pressing device and a turbulent mixer, wherein the pressing device is arranged in front of the turbulent mixer. The pressing device adopts a right-angle retraction tube O3/H2O2And the press-in is converged at the radial center of the integrated module. Preferably, the turbulators are rotating mixers (2002 in FIG. 3 a) that are oriented perpendicular to each other to ensure uniform mixing, sufficient reaction, and relatively low tube resistance.
The plug-flow reactor can work at O3Oxidation mode, O3-H2O2Oxidation mode.
At O3In the oxidation mode, H is not provided2O2Adding and mixing integrated module (or setting H)2O2Dosed and mixed integrated module without dosing), O3O is arranged after the feeding and mixing integrated module3And a reaction transition module.
At O3-H2O2In the oxidation mode, set H2O2Feeding and mixing integrated dieBlock, O3O is arranged after the feeding and mixing integrated module3-H2O2And a reaction transition module.
In one embodiment, taking typical comprehensive wastewater in the coal chemical industry as an example, after pre-treatment and biochemical treatment, the conductivity is 1500-. After the treatment by the equipment and the process of the embodiment, the COD is reduced to below 50mg/L, and the removal efficiency of the COD is up to more than 80%. O in the Process of this example3Adding and mixing O in integrated module3Gas/liquid ratio (Nm) to wastewater3/m3) The suitable range is 0.10-0.30, H2O2The concentration is 20-40mg/L, the residence time is 5min, and the flow rate is 1.0 m/s.
Fig. 2a and 2b are schematic structural diagrams of a vertical plug-flow reactor according to another embodiment of the present application;
the plug flow reactor contains a gas-liquid separation module 205 distributed at the highest point (horizontal position) of the reactor. O, O3/H2O2The reaction transition module 203 is provided with an H at the most front end2O2And a dosing and mixing integrated module (201 a). H2O26 groups of O are arranged behind the feeding and mixing integrated module (201a)3/H2O2Adding and mixing integrated module (204) and O matched with same respectively3/H2O2The reaction transition module 203. In other embodiments, the oxygen content may be 2, 3, 4, 5, etc3/H2O2Dosing mixing integrated module and O3/H2O2The reaction transition module is not limited herein. In the plug-flow reactor of this example, O3/H2O2The feeding and mixing integrated module (204) consists of a pressing device and a turbulent mixer, wherein the pressing device is positioned on the upstream side of the turbulent mixer. Preferably, the pressing device adopts a stepped perforated pipe O3/H2O2After being pressed (added), the mixture converges at the radial center of the hybrid integrated module (refer to FIG. 3a or FIG. 3b, O)3/H2O2The pressing-in pass 2001/3001 presses in the radial center of the hybrid integrated module, which flows to the medium in fig. 3a or fig. 3bRight hand schematic). The turbulent mixer adopts a flashboard mixer (refer to 3002 in figure 3 b), the directions are vertical to each other, thereby ensuring uniform mixing, full reaction and relatively small pipe resistance.
In one embodiment, the plug flow reactor is operated as O3Oxidation mode in which O is3Adding and mixing O in integrated module3Gas/liquid ratio (Nm) to wastewater3/m3) The proper range is 0.01-0.10, the proper range of the residence time is 10min, and the proper range of the flow velocity is 1.5 m/s. Taking typical clean wastewater in petrochemical industry as an example, after preoperative pretreatment and biochemical treatment, the conductivity is 10000-. After the treatment of the embodiment, the COD is reduced to below 50mg/L, and the removal efficiency of the COD is as high as more than 60%.
The multi-point feeding in the above embodiment means that a plurality of contact points feed O into the reactor through the multi-point feeding3Or H2O2。
In the above-mentioned embodiment, H2O2The upstream side of the feeding and mixing integrated module is called the downstream side in the flow direction of the medium (sewage) and the flow direction of the medium (sewage), and O3/H2O2Dosing integration Module, O3/H2O2The reaction transition module and the gas-liquid separation module are defined as H2O2And adding and mixing the integrated module, which is not described repeatedly.
The above embodiments are merely illustrative of the technical concepts and features of the present application, and the purpose of the embodiments is to enable those skilled in the art to understand the content of the present application and implement the present application, and not to limit the protection scope of the present application. All modifications made according to the spirit of the main technical scheme of the present application shall be covered by the protection scope of the present application.
Claims (10)
1. A plug-flow reactor based on multi-point feeding is characterized by comprising a water inlet, a water outlet and a reactor body, wherein the reactor body is provided with a water inlet, a water outlet and a reactor body2O2An adding and mixing integrated module, wherein the upstream side of the adding and mixing integrated module is connected with the water inlet, and the downstream side of the adding and mixing integrated module is sequentially connected with at least one group of O3/H2O2Dosing integrationModule and matched O3/H2O2A reaction transition module;
a gas-liquid separation module connected to the water outlet and disposed upstream of the water outlet,
the pipe diameter of the gas-liquid separation module is larger than the pipe diameter of the O connected with the gas-liquid separation module3/H2O2The pipe diameter of the reaction transition module.
2. The multi-feed based push-flow reactor of claim 1,
the pipe diameter of the gas-liquid separation module and the O3/H2O2The ratio of the pipe diameters of the reaction transition modules is 1.2-5.
3. The multi-feed based push-flow reactor of claim 2,
the pipe diameter of the gas-liquid separation module and the O3/H2O2The tube diameter ratio of the reaction transition modules is 1.5, 2, 3, 4 and 5.
4. The multi-feed based plug flow reactor of claim 1 wherein said O3/H2O2The feeding and mixing integrated module comprises a pressing device and a turbulent mixer, wherein the pressing device is positioned on the upstream side of the turbulent mixer.
5. The multi-feed based push-flow reactor of claim 4,
the pressing device adopts a right-angle retraction tube or a step perforation tube, O3/H2O2Is added and then converges at O3/H2O2And adding the radial center of the mixing integrated module.
6. The multi-feed based plug flow reactor of claim 4 wherein the turbulator is a rotating mixer or a bayonet mixer.
7. The multi-feed based plug flow reactor of claim 1 wherein the gas-liquid separation module is located in the last group of O' s3/H2O2The pipe diameter of the gas-liquid separation module is larger than that of the reaction transition module at the downstream side3/H2O2The pipe diameter of the reaction transition module.
8. The multi-feed based plug flow reactor of claim 1, wherein the plug flow reactor comprises a transverse S-shaped structure or a vertical S-shaped structure,
wherein, when the plug flow type reactor is in a transverse S-shaped structure, the gas-liquid separation module is positioned in the last group of O3/H2O2After the reaction transition module;
when the plug-flow reactor is of a vertical S-shaped structure, the gas-liquid separation modules are distributed at the highest point of the reactor.
9. The multi-feed based plug flow reactor of claim 1, wherein the plug flow reactor operates at O3Oxidation module or O3/H2O2In the oxidation mode, the oxidation reaction solution is prepared,
wherein,
O3in the oxidation mode, H is not provided2O2Feeding and mixing integrated module, O3O is arranged after the feeding and mixing integrated module3A reaction transition module;
O3-H2O2in the oxidation mode, set H2O2Feeding and mixing integrated module, O3O is arranged after the feeding and mixing integrated module3-H2O2And a reaction transition module.
10. The multi-feed based push-flow reactor of claim 1,
added H2O2The concentration is 0-50 mg/L, and further comprises O3Throw and mix integrated moduleIn (1),
o added thereto3Gas/liquid ratio (Nm) to influent wastewater3/m3) Between 0.01 and 0.50,
the residence time of the sewage in the plug flow type reactor is between 10s and 10min, and the flow velocity is between 0.3 and 3.0 m/s.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101327985A (en) * | 2008-07-31 | 2008-12-24 | 哈尔滨工业大学 | Method for removing organic pollutant in water by catalysis ozonation |
| CN202880985U (en) * | 2012-11-15 | 2013-04-17 | 广东卓信水处理设备有限公司 | Advanced oxidation process test device |
| CN204958648U (en) * | 2015-06-25 | 2016-01-13 | 麦王环境技术股份有限公司 | Ozone and biological nest processing technique combination treatment refractory wastewater equipment |
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2020
- 2020-01-09 CN CN202010023458.4A patent/CN111099715A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101327985A (en) * | 2008-07-31 | 2008-12-24 | 哈尔滨工业大学 | Method for removing organic pollutant in water by catalysis ozonation |
| CN202880985U (en) * | 2012-11-15 | 2013-04-17 | 广东卓信水处理设备有限公司 | Advanced oxidation process test device |
| CN204958648U (en) * | 2015-06-25 | 2016-01-13 | 麦王环境技术股份有限公司 | Ozone and biological nest processing technique combination treatment refractory wastewater equipment |
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