CN220432498U - Countercurrent contact type sewage ozone catalytic oxidation device - Google Patents
Countercurrent contact type sewage ozone catalytic oxidation device Download PDFInfo
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- CN220432498U CN220432498U CN202322016198.XU CN202322016198U CN220432498U CN 220432498 U CN220432498 U CN 220432498U CN 202322016198 U CN202322016198 U CN 202322016198U CN 220432498 U CN220432498 U CN 220432498U
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 139
- 239000010865 sewage Substances 0.000 title claims abstract description 47
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 27
- 230000003647 oxidation Effects 0.000 title claims abstract description 25
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 109
- 238000006243 chemical reaction Methods 0.000 claims abstract description 71
- 238000010517 secondary reaction Methods 0.000 claims abstract description 30
- 239000007788 liquid Substances 0.000 claims abstract description 15
- 230000001105 regulatory effect Effects 0.000 claims description 56
- 239000003054 catalyst Substances 0.000 claims description 19
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 4
- 238000012544 monitoring process Methods 0.000 claims description 4
- 229910052751 metal Inorganic materials 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- 239000007800 oxidant agent Substances 0.000 claims description 2
- 230000001590 oxidative effect Effects 0.000 claims description 2
- 230000000149 penetrating effect Effects 0.000 claims description 2
- 235000012239 silicon dioxide Nutrition 0.000 claims description 2
- 239000000377 silicon dioxide Substances 0.000 claims description 2
- 239000003344 environmental pollutant Substances 0.000 abstract description 5
- 231100000719 pollutant Toxicity 0.000 abstract description 5
- 238000013461 design Methods 0.000 abstract description 3
- 238000012546 transfer Methods 0.000 abstract description 3
- 238000000034 method Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 42
- 239000002351 wastewater Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 6
- 238000009826 distribution Methods 0.000 description 4
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 229910052938 sodium sulfate Inorganic materials 0.000 description 3
- 235000011152 sodium sulphate Nutrition 0.000 description 3
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052744 lithium Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The utility model discloses a countercurrent contact type sewage ozone catalytic oxidation device, and belongs to the technical field of sewage treatment equipment. The utility model comprises a primary reaction tank, a secondary reaction tank, a liquid conveying system and a gas conveying system which are communicated with the primary reaction tank and the secondary reaction tank. The sewage to be treated sequentially passes through the first-stage reaction tank and the second-stage reaction tank, and ozone is sequentially reversely flowed to the first-stage reaction tank from the bottom of the second-stage reaction tank, so that the high-concentration ozone and the low-concentration COD are opposite-flushed, and the low-concentration ozone and the high-concentration COD are fully reacted. The method adopts a double-tank countercurrent contact type design, ensures stable water outlet, enables the ozone with the highest concentration to react with COD of the part which is the least difficult to treat with low concentration, and provides the highest mass transfer driving force for the pollutant of the part which is difficult to treat so as to achieve the highest removal rate; the low-concentration ozone tail gas reacts with the high-concentration easily-treated part of COD, so that the power consumption of the ozone generator and the tail gas destructor is reduced to reduce the running cost.
Description
Technical Field
The utility model belongs to the technical field of sewage treatment equipment, and particularly relates to a countercurrent contact type sewage ozone catalytic oxidation device.
Background
Along with the increasing trend of domestic environmental protection policy, the sewage discharge standard is increasingly strict. The standard improvement of sewage treatment plants and the near zero and zero discharge of industrial wastewater become the development trend of sewage treatment industry. Ozone oxidation technology is now widely used in water treatment technology. As disclosed in chinese patent 2020115535419, the sewage treatment device comprises a reaction tank, a spraying device is positioned in the reaction tank, a filter disc is positioned at the bottom of the spraying device, a catalyst storage net is arranged at the bottom of the filter disc, and a gap between an inner net and an outer net of the catalyst storage net is filled with a granular catalyst; the vertical rotating shaft of the spoiler device is connected with the driving mechanism, and a plurality of spoilers are axially and uniformly arranged on the vertical rotating shaft along the vertical rotating shaft; the first ozone nozzle is arranged at the bottom of the reaction tank and positioned below the outer net, and is connected with an ozone generator. However, this device has the following disadvantages compared with the prior devices:
1. the existing countercurrent reaction device can not strictly control the flow direction and concentration gradient of gas and water, and most of the reflux part of the ozone device only considers the water quality to be as uniform as possible, does not consider the concentration gradient distribution of pollutants, and the highest ozone concentration position does not react with COD (chemical oxygen demand) of the part which is least difficult to treat with low concentration, so that the theoretical highest removal rate can not be achieved.
2. The existing countercurrent reaction device has no tail gas utilization device or has poor tail gas utilization effect. When the partial ozone device utilizes the tail gas, the tail gas is simply beaten into the reaction main body again, firstly, the tail gas is mixed with the inlet gas to reduce the concentration of the whole ozone, and secondly, the low-concentration tail gas occupies part of the space of the high-concentration inlet gas, so that the residence time of the high-concentration inlet gas is reduced.
3. When partial ozone device utilizes tail gas, concentration gradient distribution of pollutants is not considered, low-concentration ozone tail gas does not contact and react with high-concentration easily-treated partial COD, and the tail gas utilization effect is poor.
Therefore, a countercurrent contact type sewage ozone catalytic oxidation device is provided, and the problems are solved.
Disclosure of Invention
The utility model aims to provide a countercurrent contact type sewage ozone catalytic oxidation device, and aims to solve the problems that in the prior art, the existing countercurrent type sewage treatment device cannot strictly control the flow direction and concentration gradient of air and water, and has no tail gas utilization device or poor tail gas utilization effect. In order to achieve the purpose, the utility model adopts the following technical scheme: a countercurrent contact type sewage ozone catalytic oxidation device comprises a primary reaction tank, a secondary reaction tank, a liquid conveying system and a gas conveying system, wherein the liquid conveying system and the gas conveying system are communicated with the primary reaction tank and the secondary reaction tank in a penetrating manner. The sewage is connected with a primary tank water inlet and distribution device in the primary reaction tank through a pipeline, a primary tank catalyst area is arranged below the primary tank water inlet and distribution device, and the bottom of the primary reaction tank is connected with a primary tank circulating water regulating valve and a primary tank water outlet regulating valve. The sewage after the treatment of the primary tank is conveyed to a secondary tank water inlet distributor in the secondary reaction tank by the primary tank water outlet regulating valve through a secondary tank water inlet lifting pump, and the sewage passes through a secondary tank catalyst area in the middle of the secondary reaction tank and is connected with the secondary tank circulating water regulating valve and the secondary tank water outlet regulating valve from the bottom through pipelines. The gas conveying system comprises an ozone air inlet, a flowmeter and an ozone tail gas destructor, wherein the ozone air inlet is sequentially connected with the second-stage tank ozone air inlet flowmeter, the second-stage tank ozone air inlet regulating valve and the second-stage tank jet device, an inlet and an outlet of the second-stage tank jet device are respectively connected with the second-stage tank circulating water regulating valve and the second-stage reaction tank, ozone is mixed with the second-stage tank circulating water in the second-stage tank jet device and enters the second-stage reaction tank, after countercurrent reaction, the ozone passes through the first-stage tank ozone air inlet regulating valve, is fully mixed with the first-stage tank circulating water in the first-stage tank jet device, enters the first-stage reaction tank, and after countercurrent reaction, the ozone passes through the first-stage tank ozone air exhaust regulating valve and the ozone tail gas destructor and is discharged. According to the technical scheme, the flow direction and concentration gradient of each gas and water are strictly controlled, so that the highest ozone concentration position reacts with COD (chemical oxygen demand) of the part which is least difficult to treat with low concentration, and the highest removal rate is realized; and the tail gas is recycled, the low-concentration tail gas and the high-concentration and easy-to-treat part COD with high concentration are in contact reaction, so that the tail gas utilization effect is improved.
Further describing the scheme, the primary tank circulating water regulating valve is sequentially connected with a primary tank ozone adding pump, a primary tank circulating water flowmeter and a primary tank jet device; the secondary tank circulating water regulating valve is sequentially connected with a secondary tank ozone adding pump, a secondary tank circulating water flowmeter and a secondary tank jet device.
Further, a second-stage tank exhaust regulating valve is arranged between the first-stage tank ozone inlet regulating valve and the second-stage reaction tank, and an outlet of the second-stage tank exhaust regulating valve is connected with an ozone tail gas destructor. The ozone exhaust regulating valve of the secondary tank is in a closed state when working normally, and is automatically opened to exhaust when the secondary tank needs to exhaust or the pressure exceeds a warning value.
More preferably, the valve, the water pump, the sensor and the flowmeter are automatically controlled by a PLC (programmable logic controller), so that full-automatic operation is realized, and manual pressure is reduced.
Further, the pressure of the secondary reaction tank is higher than that of the primary reaction tank, so that the tail gas of the secondary reaction tank is reused.
Optionally, the ozone tail gas destructor adopts an ozone tail gas thermal destructor or an ozone tail gas catalytic destructor.
Further, the ozone oxidation catalyst in the first-stage tank catalyst zone and the second-stage tank catalyst zone adopts a metal oxidant taking silicon dioxide as a carrier.
Further, sewage sequentially passes through a primary tank water inlet pump and a primary tank water inlet flowmeter to be connected with a primary tank water inlet distributor, and a secondary tank water inlet flowmeter for displaying flow is arranged between the secondary tank water inlet lifting pump and the secondary tank water inlet distributor. The primary reaction tank and the secondary reaction tank are respectively provided with a primary tank liquid level transmitter and a secondary tank liquid level transmitter for monitoring the liquid level of the reaction tank in real time and automatically adjusting a water outlet regulating valve of the reaction tank so as to control the water outlet flow of the reaction tank. Further, the primary reaction tank and the secondary reaction tank are respectively provided with a primary tank pressure transmitter and a secondary tank pressure transmitter for monitoring the pressure of the reaction tank in real time and automatically adjusting an exhaust regulating valve of the reaction tank to control the pressure of the reaction tank.
Compared with the prior art, the utility model has the following beneficial effects:
1. the utility model adopts a double-tank countercurrent contact type design, ensures stable water outlet, and strictly controls gas-water countercurrent contact reaction, so that the highest concentration ozone reacts with the COD of the part which is the least difficult to treat with low concentration, and the highest mass transfer driving force is provided for the pollutant of the part which is difficult to treat, thereby achieving the highest removal rate;
2. the low-concentration ozone tail gas reacts with the high-concentration easily-treated part of COD to increase the ozone utilization rate, thereby reducing the power consumption of an ozone generator and a tail gas destructor to reduce the running cost;
3. the low-concentration ozone tail gas is independently fed into the front-end tank body, so that the reaction of the high-concentration ozone gas at the rear end is not influenced.
Drawings
FIG. 1 is a schematic diagram of the present utility model of China patent 2020115535419;
FIG. 2 is a schematic diagram of an embodiment of the present utility model;
FIG. 3 is a table showing the treatment effect of the countercurrent contact type ozone reactor according to the present utility model;
FIG. 4 is a table of the treatment effect of a secondary ozone advanced catalytic oxidation reactor;
wherein, each reference sign in the figure:
100. a first-stage reaction tank; 101. a first stage tank catalyst zone; 102. a primary tank water inlet distributor; 103. a primary tank pressure transmitter; 104. a primary tank level transmitter; 105. a primary tank water inlet pump; 106. a primary tank water inlet flowmeter; 107. a first-stage tank circulating water regulating valve; 108. a first-stage tank ozone adding pump; 109. a first-stage tank circulating water flowmeter; 110. a primary tank jet; 111. a first-stage tank water outlet regulating valve; 112. a secondary tank water inlet lift pump; 113. a secondary tank water inlet flowmeter;
200. a secondary reaction tank; 201. a secondary tank catalyst zone; 202. a secondary tank water inlet distributor; 203. a secondary tank pressure transmitter; 204. a secondary tank level transmitter; 205. a secondary tank circulating water regulating valve; 206. a secondary tank ozone adding pump; 207. a secondary tank circulating water flow meter; 208. a secondary tank ejector; 209. a secondary tank water outlet regulating valve;
210. a secondary tank ozone inlet flow meter; 211. an ozone inlet regulating valve of the secondary tank; 212. an ozone inlet regulating valve of the first-stage tank; 213. a secondary tank exhaust regulating valve; 214. a first-stage tank exhaust regulating valve; 215. ozone tail gas destructor.
Detailed Description
In order that the utility model may be readily understood, a more complete description of the utility model will be rendered by reference to the appended drawings. The drawings illustrate preferred embodiments of the utility model. This utility model may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete.
The technical scheme of the patent is further described in detail below with reference to the specific embodiments.
Referring to fig. 2, sewage water sequentially passes through a pump front valve, a filter, a primary tank water inlet pump 105, a one-way valve, a pump rear valve, a primary tank water inlet flowmeter 106, a primary tank water inlet distributor 102, and evenly distributes water at the upper part of the primary reaction tank 100. In the first-stage reaction tank 100, sewage flows from top to bottom, fully contacts and reacts with ozone microbubbles flowing upwards, and the catalyst in the first-stage tank catalyst zone 101 promotes the ozone advanced oxidation reaction. The sewage part after the reaction of the primary reaction tank 100 sequentially passes through a primary tank circulating water regulating valve 107, a primary tank ozone adding pump 108 and a primary tank circulating water flowmeter 109, is mixed with secondary tank ozone tail gas passing through a primary tank ozone inlet regulating valve 212 in a primary tank jet device 110 to form ozone water, and flows back to the lower part of the primary reaction tank 100 to form fine ozone microbubbles; part of the water is sequentially connected into the secondary reaction tank 200 through the primary tank water outlet regulating valve 111, the secondary tank water inlet lifting pump 112 and the secondary tank water inlet flowmeter 113.
Referring to fig. 2, in the secondary reaction tank 200, the sewage treated in the primary reaction tank 100 is uniformly distributed by the secondary tank water inlet distributor 202 and flows from top to bottom, and fully contacts with ozone microbubbles flowing up to the top for reaction, and the catalyst in the catalyst zone 201 of the secondary tank promotes the advanced oxidation reaction of ozone. The sewage part after the reaction of the secondary reaction tank 200 sequentially passes through a secondary tank circulating water regulating valve 205, a secondary tank ozone adding pump 206 and a secondary tank circulating water flowmeter 207, is mixed with ozone air entering through a secondary tank ozone air inlet regulating valve 211 in a secondary tank ejector 208 to form ozone water, and flows back to the lower part of the secondary reaction tank 200 to form fine ozone microbubbles; part of the water is discharged through the secondary tank water outlet regulating valve 209 in turn.
Referring to fig. 2, ozone gas sequentially passes through a secondary tank ozone inlet flow meter 210 and a secondary tank ozone inlet regulating valve 211, is fully mixed with secondary tank circulating water in a secondary tank jet device 208 to enter a secondary reaction tank 200, passes through a primary tank ozone inlet regulating valve 212 after countercurrent reaction, is fully mixed with primary tank circulating water in a primary tank jet device 110 to enter a primary reaction tank 100, and is discharged after countercurrent reaction after sequentially passing through a primary tank ozone discharge regulating valve 214 and an ozone tail gas destructor 215215. The secondary tank ozone discharge regulating valve 213 is normally closed, and is automatically opened to discharge when the secondary reaction tank 200 needs to discharge or when the pressure exceeds a warning value.
Referring to fig. 2, the sewage inflow water is displayed with flow rate through a primary tank inflow flowmeter 106, and the flow rate is regulated together through a front end valve body; the primary tank liquid level transmitter 104 monitors the liquid level of the primary reaction tank 100 in real time and automatically adjusts the primary tank water outlet regulating valve 111 to control the primary tank treatment water outlet flow; the secondary tank liquid level transmitter 204 monitors the liquid level of the secondary reaction tank 200 in real time and automatically adjusts the secondary tank water outlet regulating valve 209 to control the secondary tank treated water outlet flow. The primary tank pressure transmitter 103 monitors the pressure of the primary reaction tank 100 in real time and automatically adjusts the primary tank exhaust regulating valve 214 to control the pressure of the primary reaction tank 100; the secondary tank pressure transmitter 203 monitors the secondary tank 200 pressure in real time and automatically adjusts the secondary tank exhaust gas regulating valve 213 to control the secondary tank 200 pressure.
As can be seen from the above-mentioned sewage flowing direction and ozone flowing direction, the concentration of ozone in the secondary reaction tank 200 is highest, the concentration of ozone in the secondary reaction tank 200 gradually decreases, and the sewage in the primary reaction tank 100 has a high concentration and easy treatment part COD, which is easy to react with low concentration ozone, so that the exhaust gas discharged from the exhaust regulating valve 214 of the primary reaction tank is very small, and the power consumption of the ozone generator and the exhaust gas destructor is effectively reduced to reduce the running cost. In the secondary reaction tank 200, high-concentration ozone reacts with the COD of the part which is the least difficult to treat with low concentration, so that the treatment of the COD is effectively ensured. Ozone and sewage flow in opposite directions, so that the cleaning of sewage is ensured and the ozone utilization rate is improved.
In order to more intuitively and clearly understand the advancement of the utility model, the following steps are to use the waste water generated in the production of sodium sulfate by lithium batteries in a certain factory as a material, and respectively adopt the countercurrent contact type ozone reactor of the utility model to treat the waste water and use a certain secondary ozone advanced catalytic oxidation reactor to treat the waste water:
as shown in figure 3, sodium sulfate wastewater produced by lithium batteries in a certain factory is used as a material, the sewage cod is 2200mg/L, PH and is 9-10, suspended matters are <60mg/L, the wastewater is treated by the countercurrent contact type ozone reactor, the total residence time is set to be 4 hours, wherein the primary residence time is 2 hours, and the secondary residence time is 2 hours. The first-stage water inflow cod is 2200mg/L, the first-stage water outflow cod is 1064mg/L, and the removal rate of the cod is 51.6%; the concentration of the first-stage inlet ozone is 43.5 mg/L, the concentration of the exhaust ozone is 12.1mg/L, and the utilization rate of the first-stage ozone is 72.2%; the secondary water inflow cod is 1064mg/L, the water outflow cod is 380mg/L, the secondary cod removal rate is 64.3%, and the comprehensive cod removal rate is 82.7%; the inlet concentration of the secondary ozone is 79.8mg/L, the concentration of the secondary exhaust ozone is 43.5 mg/L, the utilization rate of the secondary ozone is 45.5%, and the comprehensive ozone utilization rate is 85.8%.
The same batch of sodium sulfate wastewater is used as a material, as shown in fig. 4, the sewage cod is 2200mg/L, PH and is 9-10, suspended matters are <60mg/L, a certain secondary ozone advanced catalytic oxidation reactor is used for treating the wastewater, the total residence time is set to be 4 hours, wherein the residence time of a primary main reaction tank is 2.5 hours, and the residence time of a secondary auxiliary reaction tank is 1.5 hours. The first-stage water inflow cod is 2200mg/L, the first-stage water outflow cod is 952mg/L, and the removal rate of the cod is 56.8%; the concentration of the first-stage inlet ozone is 79.9 mg/L, the concentration of the exhaust ozone is 38.0mg/L, and the utilization rate of the first-stage ozone is 52.5%; the secondary water inflow cod is 952mg/L, the water outflow cod is 610mg/L, the secondary cod removal rate is 36.0%, and the comprehensive cod removal rate is 72.3%; the inlet concentration of the secondary ozone is 38.0mg/L, the concentration of the secondary exhaust ozone is 25.2 mg/L, the utilization rate of the secondary ozone is 33.7%, and the comprehensive ozone utilization rate is 68.5%.
As can be seen from the comparison, when the countercurrent contact type sewage ozone catalytic oxidation device provided by the utility model is used for treating the same sewage, the removal rate of cod and the utilization rate of ozone are far better than those of the existing secondary ozone advanced catalytic oxidation reactor.
In summary, the utility model adopts a double-tank countercurrent contact design, ensures stable water outlet, simultaneously ensures that the ozone with the highest concentration reacts with COD of the part which is the most difficult to treat with low concentration, and provides the highest mass transfer driving force for the pollutant of the part which is difficult to treat so as to achieve the highest removal rate; the low-concentration ozone tail gas reacts with the high-concentration easily-treated part COD to improve the ozone utilization rate, and the power consumption of an ozone generator and a tail gas destructor is effectively reduced to reduce the running cost.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this utility model belongs. The terminology used herein in the description of the utility model is for the purpose of describing particular embodiments only and is not intended to be limiting of the utility model. The term "and/or" as used herein includes any and all combinations of one or more of the associated listed items.
The above embodiments are only for illustrating the present utility model, not for limiting the present utility model, and various changes and modifications may be made by one of ordinary skill in the relevant art without departing from the spirit and scope of the present utility model, and therefore, all equivalent technical solutions are also within the scope of the present utility model, and the scope of the present utility model is defined by the claims.
Claims (10)
1. A countercurrent contact type sewage ozone catalytic oxidation device is characterized in that: the device comprises a primary reaction tank (100), a secondary reaction tank (200), a liquid conveying system and a gas conveying system, wherein the liquid conveying system and the gas conveying system are communicated with the primary reaction tank (100) and the secondary reaction tank (200) in a penetrating way;
the sewage is connected with a primary tank water inlet water distributor (102) in the primary reaction tank (100) through a pipeline, a primary tank catalyst zone (101) is arranged below the primary tank water inlet water distributor (102), and the bottom of the primary reaction tank (100) is connected with a primary tank circulating water regulating valve (107) and a primary tank water outlet regulating valve (111);
the primary tank water outlet regulating valve (111) conveys the sewage treated by the primary reaction tank (100) to a secondary tank water inlet water distributor (202) in the secondary reaction tank (200) through a secondary tank water inlet lifting pump (112), and the sewage passes through a secondary tank catalyst zone (201) in the middle of the secondary reaction tank (200) and is connected with a secondary tank circulating water regulating valve (205) and a secondary tank water outlet regulating valve (209) from the bottom through pipelines;
the gas conveying system comprises an ozone air inlet, a flowmeter and an ozone tail gas destructor (215), the ozone air inlet is sequentially connected with a secondary tank ozone air inlet flowmeter (210), a secondary tank ozone air inlet regulating valve (211) and a secondary tank jet device (208), an inlet and an outlet of the secondary tank jet device (208) are respectively connected with a secondary tank circulating water regulating valve (205) and a secondary reaction tank (200), ozone is mixed with secondary tank circulating water in the secondary tank jet device (208) and enters the secondary reaction tank (200), and after countercurrent reaction, the ozone is fully mixed with primary tank circulating water in the primary tank jet device (110) and enters the primary reaction tank (100), and after countercurrent reaction, the ozone is discharged after passing through the primary tank ozone air outlet regulating valve and the ozone tail gas destructor (215).
2. The countercurrent contact type sewage ozone catalytic oxidation device according to claim 1, wherein: the primary tank circulating water regulating valve (107) is sequentially connected with a primary tank ozone adding pump (108), a primary tank circulating water flowmeter (109) and a primary tank jet device (110); the secondary tank circulating water regulating valve (205) is sequentially connected with a secondary tank ozone adding pump (206), a secondary tank circulating water flowmeter (207) and a secondary tank jet device (208).
3. The countercurrent contact type sewage ozone catalytic oxidation device according to claim 1, wherein: a second-stage tank exhaust regulating valve (213) is further arranged between the first-stage tank ozone inlet regulating valve (212) and the second-stage reaction tank (200), and an outlet of the second-stage tank exhaust regulating valve (213) is connected with an ozone tail gas destructor (215).
4. The countercurrent contact type sewage ozone catalytic oxidation device according to claim 1, wherein: the valve, the water pump, the sensor and the flowmeter are automatically controlled by a PLC.
5. The countercurrent contact type sewage ozone catalytic oxidation device according to claim 1, wherein: the pressure of the secondary reaction tank (200) is higher than that of the primary reaction tank (100).
6. The countercurrent contact type sewage ozone catalytic oxidation device according to claim 1, wherein: the ozone tail gas destructor (215) adopts an ozone tail gas thermal destructor or an ozone tail gas catalytic destructor.
7. The counter-current contact type sewage ozone catalytic oxidation device according to claim 6, wherein: the ozone oxidation catalyst in the first-stage tank catalyst zone (101) and the second-stage tank catalyst zone (201) adopts a metal oxidant taking silicon dioxide as a carrier.
8. The countercurrent contact type sewage ozone catalytic oxidation device according to claim 1, wherein: the sewage sequentially passes through a primary tank water inlet pump (105) and a primary tank water inlet flowmeter (106) to be connected with a primary tank water inlet water distributor (102), and a secondary tank water inlet flowmeter (113) is arranged between a secondary tank water inlet lifting pump (112) and a secondary tank water inlet water distributor (202) and used for displaying flow.
9. The countercurrent contact type sewage ozone catalytic oxidation device according to claim 1, wherein: the primary reaction tank (100) and the secondary reaction tank (200) are respectively provided with a primary tank liquid level transmitter (104) and a secondary tank liquid level transmitter (204) for monitoring the liquid level of the reaction tank in real time and automatically adjusting a reaction tank water outlet regulating valve so as to control the water outlet flow of the reaction tank.
10. The countercurrent contact type sewage ozone catalytic oxidation device according to claim 1, wherein: the primary reaction tank (100) and the secondary reaction tank (200) are respectively provided with a primary tank pressure transmitter (103) and a secondary tank pressure transmitter (203) for monitoring the pressure of the reaction tank in real time and automatically adjusting an exhaust regulating valve of the reaction tank to control the pressure of the reaction tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322016198.XU CN220432498U (en) | 2023-07-29 | 2023-07-29 | Countercurrent contact type sewage ozone catalytic oxidation device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322016198.XU CN220432498U (en) | 2023-07-29 | 2023-07-29 | Countercurrent contact type sewage ozone catalytic oxidation device |
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| Publication Number | Publication Date |
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| CN220432498U true CN220432498U (en) | 2024-02-02 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202322016198.XU Active CN220432498U (en) | 2023-07-29 | 2023-07-29 | Countercurrent contact type sewage ozone catalytic oxidation device |
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| CN (1) | CN220432498U (en) |
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