CN111422971A - Fountain catalytic ozonation reaction system - Google Patents
Fountain catalytic ozonation reaction system Download PDFInfo
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- CN111422971A CN111422971A CN202010380131.2A CN202010380131A CN111422971A CN 111422971 A CN111422971 A CN 111422971A CN 202010380131 A CN202010380131 A CN 202010380131A CN 111422971 A CN111422971 A CN 111422971A
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- 230000003197 catalytic effect Effects 0.000 title claims abstract description 44
- 238000006385 ozonation reaction Methods 0.000 title claims abstract description 33
- 238000006243 chemical reaction Methods 0.000 claims abstract description 135
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 90
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 74
- 239000003054 catalyst Substances 0.000 claims abstract description 41
- 239000007921 spray Substances 0.000 claims abstract description 36
- 239000002351 wastewater Substances 0.000 claims abstract description 36
- 238000009826 distribution Methods 0.000 claims abstract description 23
- 239000007788 liquid Substances 0.000 claims abstract description 18
- 239000000945 filler Substances 0.000 claims abstract description 17
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 5
- 238000012856 packing Methods 0.000 claims description 10
- 239000003595 mist Substances 0.000 claims description 3
- 230000008030 elimination Effects 0.000 claims 1
- 238000003379 elimination reaction Methods 0.000 claims 1
- 238000007254 oxidation reaction Methods 0.000 description 13
- 230000003647 oxidation Effects 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- 238000012546 transfer Methods 0.000 description 7
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- 238000005273 aeration Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 238000005507 spraying Methods 0.000 description 6
- 230000035484 reaction time Effects 0.000 description 5
- 238000004065 wastewater treatment Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000012827 research and development Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000009303 advanced oxidation process reaction Methods 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004043 dyeing Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000007639 printing Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 230000003670 easy-to-clean Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000014759 maintenance of location 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
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 229910000314 transition metal oxide Inorganic materials 0.000 description 1
- 239000011800 void material Substances 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
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
- 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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/30—Nature of the water, waste water, sewage or sludge to be treated from the textile industry
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- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention relates to a spray type catalytic ozonation reaction system, which comprises at least one reaction tower, a water inlet pipe, a water outlet pipe, an ozone distribution pipe and an exhaust pipe, wherein the reaction tower is a filler spray tower and comprises a filler section with a catalyst, the water inlet pipe is connected to the reaction tower to introduce wastewater into the reaction system, the water outlet pipe is connected to the reaction tower to discharge wastewater from the reaction system, the ozone distribution pipe is connected to the reaction tower to introduce ozone into the reaction system, the exhaust pipe is connected to the reaction tower to discharge residual ozone and gas after catalytic reaction from the reaction system, and the flow direction of the wastewater in the filler section of the reaction tower is opposite to the flow direction of the ozone in the filler section of the reaction tower to realize gas-water countercurrent contact reaction. According to the spray type catalytic ozonation reaction system, the reaction area is increased through the spray mode, the contact area between ozone and a catalyst is larger, the ozone can penetrate through a liquid film more easily to reach the surface of the catalyst, and the ozone is distributed more quickly and easily in a gaseous state.
Description
Technical Field
The invention relates to wastewater treatment, in particular to a spray type catalytic ozonation reaction system.
Background
Along with the rapid development of industrial and agricultural industries in China, toxic or difficultly-degraded organic substances in water are more and more, and how to treat the substances and improve the treatment effect becomes a more concerned subject in the water treatment industry. Advanced Oxidation Process (AOP), wherein the Oxidation process taking hydroxyl radicals as main oxidants in the water treatment process is called AOP process, ozone catalytic Oxidation is a common Advanced Oxidation technology, has the advantages of simple operation process, easily obtained reactants, no need of complex equipment, environmental friendliness and the like, is gradually applied to various wastewater treatment projects such as chemical engineering, dyes, pesticides and the like, and has good application prospect. The ozone catalytic oxidation has wide application prospect in treating chemical wastewater, printing and dyeing wastewater and the like, particularly in advanced wastewater treatment due to the unique superiority.
Ozone advanced oxidation is an important method for removing organic pollutants in water treatment technology, and can degrade a plurality of organic matters and improve the biodegradation performance of the organic matters. When the ozone process is used for treating industrial wastewater, the technical keys of the ozone gas production cost, the ozone mixing uniformity in water, the contact reaction between ozone and pollutants, the overall utilization efficiency of the ozone gas and the like need to be considered. Therefore, the design of a reactor which is beneficial to the diffusion of ozone gas in wastewater and can fully mix reaction substrates has important significance for improving the sewage treatment efficiency, reducing the process cost and realizing the characteristic of catalyzing the ozone function. At present, however, research and development on ozone catalytic oxidation are mostly focused on the research and development of catalysts, research and development and improvement on ozone catalytic oxidation reactors are less, and the existing ozone catalytic oxidation reactor has low catalyst bed voidage and low ozone utilization rate; meanwhile, the problems that the gas, the liquid and the solid are difficult to separate, the catalyst is difficult to recycle, the backwashing operation is complex, the effect is poor and the like exist.
The reactor for catalyzing ozone in the prior art is mainly in a fluidized bed form or a fixed bed form, and has the advantages of high manufacturing cost, large equipment volume, high transportation cost, easy blockage, suspended matter problem in effluent, troublesome catalyst replacement and higher cost.
The existing ozone catalytic oxidation reaction tower generally adopts a bubble tower form to carry out gas-liquid contact reaction, namely ozone gas is diffused into bubbles through a gas aeration pipe or an aeration disc and then is released into wastewater of a tower body, and gas-water mixing is carried out in the tower, so that mass transfer between gas and liquid is realized, and degradation reaction of pollutants is generated. Two key problems with bubble column type reactors are that the size of the gas bubbles needs to be reduced to increase the mass transfer efficiency, thereby increasing the contact area between the ozone gas and the wastewater. This requires the use of a microporous aeration disk to disperse the incoming ozone gas into fine bubbles, which can easily clog and require frequent cleaning. Secondly, in order to improve the mass transfer rate of the ozone, higher ozone concentration is needed or the height of the tower is increased to improve the partial pressure of the ozone so as to increase the mass transfer driving force, and higher liquid level in the reactor needs to be maintained. However, the air supply pressure of the ozone generator is only 1.2 kg at most, namely 12 m of water depth, which limits the continuous increase of the height of the ozone catalytic oxidation reaction tower. That is to say, the current catalytic system has the problems of long reaction time, large catalyst filling amount, serious catalyst loss condition, high requirement on ozone aeration, high requirement on micro bubbles, high tower height, realization of increasing partial pressure of ozone to improve mass transfer of ozone and the like.
Disclosure of Invention
The invention provides a spray type catalytic ozonation reaction system, aiming at solving the problems that a catalytic ozonation reaction system in the prior art is easy to block, an aeration head is not easy to clean, the ozone utilization rate is not high, the reaction time is long, the tower height is limited and the like.
The invention provides a spray type catalytic ozonation reaction system which comprises at least one reaction tower, a water inlet pipe, a water drain pipe, an ozone distribution pipe and an exhaust pipe, wherein the reaction tower is a filler spray tower and comprises a filler section with a catalyst, the water inlet pipe is connected to the reaction tower to introduce wastewater into the reaction system, the water drain pipe is connected to the reaction tower to discharge wastewater from the reaction system, the ozone distribution pipe is connected to the reaction tower to introduce ozone into the reaction system, the exhaust pipe is connected to the reaction tower to discharge residual ozone and gas after catalytic reaction from the reaction system, and the flow direction of the wastewater in the filler section of the reaction tower is opposite to the flow direction of the ozone in the filler section of the reaction tower to realize gas-water countercurrent contact reaction.
Preferably, the reaction tower comprises a spraying section positioned above the packing section, a water distribution device used for enabling the wastewater to form fine liquid drops and fog drops is arranged in the spraying section, and the water distribution device is connected with the water inlet pipe.
Preferably, the reaction tower comprises a demisting section positioned above the spraying section, and the demisting section is connected with an exhaust pipe.
Preferably, a demister for removing liquid droplets and fog droplets entrained in the gas is arranged in the demisting section.
Preferably, the reaction tower comprises an air inlet section positioned below the packing section, and the air inlet section is connected with the ozone distribution pipe.
Preferably, the reaction tower comprises a water tank section located below the gas inlet section, the water tank section being connected to a drain pipe.
Preferably, the water trough section is connected to the water inlet pipe by a circulation pump.
Preferably, the spray type catalytic ozonation reaction system comprises a first reaction tower and a second reaction tower which are connected in series, a water inlet pipe is connected to the first reaction tower to introduce wastewater into the reaction system, a water outlet pipe is connected to the second reaction tower to discharge wastewater from the reaction system, an ozone gas distribution pipe is connected to the second reaction tower to introduce ozone into the reaction system, an exhaust pipe is connected to the first reaction tower to discharge residual ozone and gas after catalytic reaction from the reaction system, and the flow direction of wastewater and the flow direction of ozone realize gas-water countercurrent contact reaction in the spray type catalytic ozonation reaction system.
Preferably, the air inlet section of the first reaction tower is communicated with the exhaust pipe of the second reaction tower.
Preferably, the water tank section of the first reaction tower is connected with the water inlet pipe of the second reaction tower through a circulating pump.
According to the spray type catalytic ozonation reaction system, the reaction area is increased through the spray type, the contact area between the ozone and the catalyst is larger, the ozone can penetrate through the liquid film to reach the surface of the catalyst more easily, the ozone is distributed more quickly and easily in the gaseous state, and the catalyst is not immersed in the wastewater and only forms a very thin liquid film on the surface of the catalyst. According to the spray type catalytic ozonation reaction system, under the condition that the pH value of wastewater does not need to be adjusted, the ozone catalyst is used as a filler, the wastewater infiltrates the catalyst, and a very thin liquid film is formed on the surface of the catalyst, so that the reaction system has a very large reaction specific surface area, and ozone introduced from the lower part easily penetrates through the liquid film and reaches the surface of the catalyst, is converted into hydroxyl radicals HO & lt- & gt under the action of the catalyst, and quickly reacts with organic matters in the wastewater. The catalytic ozonation reaction system has the advantages of high reaction speed, full reaction, high ozone utilization rate, short effective reaction time and hydraulic retention time, stable quality of treated effluent, convenience in catalyst replacement, simple ozone gas supply mode, convenience in system operation and maintenance and the like, solves the problem of tower height limitation, and can increase the tower height properly in an area with limited land.
Drawings
FIG. 1 is a schematic diagram of a spray catalytic ozonation reaction system according to a preferred embodiment of the present invention;
fig. 2 is a schematic diagram of a spray catalytic ozonation reaction system according to another preferred embodiment of the present invention.
Detailed Description
The preferred embodiments of the present invention will be described in detail below with reference to the accompanying drawings.
Example 1
As shown in fig. 1, a spray type catalytic ozonation reaction system according to a preferred embodiment of the present invention includes a reaction tower 1, a water inlet pipe 2, a water outlet pipe 3, an ozone distribution pipe 4, and an air outlet pipe 5, wherein the reaction tower 1 is a packed spray tower, the water inlet pipe 2 is connected to the reaction tower 1 to introduce wastewater into the reaction system, the water outlet pipe 3 is connected to the reaction tower 1 to discharge wastewater from the reaction system, the ozone distribution pipe 4 is connected to the reaction tower 1 to introduce ozone into the reaction system, the air outlet pipe 5 is connected to the reaction tower 1 to discharge ozone from the reaction system, and a flow direction of wastewater in the reaction tower 1 is opposite to a flow direction of ozone in the reaction tower 1.
The reaction tower 1 comprises a demisting section 11, a spraying section 12, a packing section 13, an air inlet section 14 and a water tank section 15 which are sequentially arranged from top to bottom, wherein the spraying section 12, the packing section 13 and the air inlet section 14 are arranged between the demisting section 11 at the top and the water tank section 15 at the bottom.
A demister 111 is arranged in the demisting section 11, and liquid drops and fog drops carried in the gas entering the demisting section 11 are removed through the demister 111. The top of the demisting section 11 is connected with an exhaust pipe 5, and the reacted gas and residual ozone are discharged from the reaction tower 1 through the exhaust pipe 5. In this embodiment, the exhaust pipe 5 is connected to the ozone destructor through a blower to ensure that the discharge concentration of ozone meets the discharge requirement.
A water distribution device 121 is arranged in the spraying section 12, the water distribution device 121 is connected with the water inlet pipe 2, and wastewater enters the reaction tower 1 through the water inlet pipe 2 and the water distribution device 121 to form countless fine liquid drops and fog drops. The residual ozone from the filler section 13 rises into the spray section 12 to be in intimate mixing contact with the droplets and mist droplets to continue the reaction.
The catalyst 131 is fixed in the packing section 13, the wastewater from the water distribution device 121 is uniformly sprayed on the catalyst 131, the ozone from the air inlet section 14 rises to the packing section 13 in the form of a liquid film on the surface of the catalyst 131, the gas and the water are in reverse contact, the ozone is fully reacted on the surface of the catalyst 131, and the ozone is converted into hydroxyl radicals HO & lt- & gt under the action of the catalyst 131 and rapidly reacts with organic matters in the wastewater. It should be understood that the catalyst 131 may be an iron-based catalyst, a transition metal oxide catalyst, a noble metal catalyst, a catalyst supported on ceramsite, a catalyst supported on alumina, or a catalyst supported on activated carbon. The form of the catalyst 131 is not particularly limited, and may be in the form of a sphere, an amorphous form, a honeycomb form, a shaving form, a raschig ring, a pall ring, or the like suitable for a packed column. Of course, larger specific surface area is better, so that the reaction area is large, the void ratio is high, the blockage probability is low, and a smaller gas-water ratio design can be used, so that the wastewater treatment capacity is increased. Obviously, the spray-type catalytic ozonation reaction system provided by the invention forms a large liquid film surface on the surface of the catalyst filler, creates a good gas-liquid contact area, and has a rapid reaction.
The air inlet section 14 is connected with the ozone distributing pipe 4, and ozone is introduced into the reaction tower 1 through the ozone distributing pipe 4, quickly fills the space of the air inlet section 14 and then uniformly rises to the filling section 13. Compared with the microporous aeration disc in the prior art, the air distribution pipe has larger aperture and is not easy to block.
The bottom of the water tank section 15 is connected with a drain pipe 3, and the wastewater from the air inlet section 14 can be discharged outside through the drain pipe 3 after entering the water tank section 15. In this embodiment, the water tank section 15 is connected to the water inlet pipe 2 via the circulation pump 6, so that circulating water can be pumped from the water tank section 15 via the circulation pump 6 and introduced into the reaction tower 1 together with wastewater.
According to the spray type catalytic ozonation reaction system, the reaction system is not filled with water any more, the reaction is only carried out on the surface of the catalyst filler, and the resistance of the catalytic ozonation reaction tower with unit height is greatly reduced. In addition, the existing reaction towers are required to be relatively high, generally at least more than 6 meters, and some of the existing reaction towers reach 10 meters, because the concentration of ozone in a gas supply source is relatively low (the highest is 10-15%, which is caused by the current ozone generator technology), in order to improve the mass transfer efficiency, a relatively high reactor height needs to be designed to increase the partial pressure of ozone so as to improve the mass transfer of ozone, but the actual height of a catalyst layer is limited, namely an effective reaction area is not high. Correspondingly, the spray type catalytic ozonation reaction system does not need a higher tower height, the height of a common spray tower can be only 4-6 m, the air supply pressure is not required, a little pressure such as 0.05 kg can be used for introducing ozone, and the air can move along with the air flow direction when water and air are contacted, so that the resistance loss of the air passing through the packing layer is not more than 0.04 kg, and the air inlet pressure is more than 0.05 kg. In the area with limited land, the tower height can be increased to reduce the land occupation.
Taking secondary biochemical effluent of a sewage treatment station of a certain printing and dyeing mill, wherein the COD is 140 mg/L, the chroma is 100, and the aniline is 4mg/l, adopting a spray tower form, the filler is an iron-based catalyst, the reaction time is 10min, and O is3The dosage is 80mg/l, COD after catalytic oxidation reaction is 58 mg/L, chroma is 16, aniline is not detected, COD removal rate is more than 50%, effluent quality reaches experimental expectation, meanwhile, a conventional tower reactor with a completely immersed catalyst is adopted, the catalyst is still an iron-based catalyst, O3The catalytic oxidation reaction time is 30min, O3The dosage is 100mg/l, COD after catalytic oxidation reaction is 60 mg/L, chroma is 20, aniline is not detected, and COD removal rate is more than 50%.
Example 2
As shown in fig. 2, the spray type catalytic ozonation reaction system according to another preferred embodiment of the present invention includes a first reaction tower 1A, a second reaction tower 1B, a water inlet pipe 2 ', a water outlet pipe 3', an ozone distribution pipe 4 'and an air outlet pipe 5' connected in series, wherein the water inlet pipe 2 'is connected to the first reaction tower 1A to introduce wastewater into the reaction system, the water outlet pipe 3' is connected to the second reaction tower 1B to discharge wastewater from the reaction system, the ozone distribution pipe 4 'is connected to the second reaction tower 1B to introduce ozone into the reaction system, and the air outlet pipe 5' is connected to the first reaction tower 1A to discharge ozone from the reaction system, which can further improve ozone utilization ratio and pollutant degradation degree with respect to embodiment 1, and can be used for wastewater treatment requirements of higher emission standards. In this embodiment, the first reaction tower 1A and the second reaction tower 1B are both two-phase countercurrent packing reaction towers, and the specific structure of the reaction tower 1A is the same as that of the reaction tower 1 of embodiment 1, and is not described herein again, and only different parts are described below.
The air inlet section 14 of the first reaction tower 1A is communicated with the exhaust pipe 5B of the second reaction tower 1B, and the exhaust tail gas collected from the exhaust pipe 5B of the second reaction tower 1B still contains unreacted ozone, and the unreacted ozone enters the first reaction tower 1A through the air inlet section 14A for reaction.
The water tank section 15A of the first reaction tower 1A is connected to the water inlet pipe 2B of the second reaction tower 1B by the circulation pump 7, so that the circulating water pumped from the water tank section 15A of the first reaction tower 1A by the circulation pump 7 and the circulating water pumped from the water tank section 15B of the second reaction tower 1B by the circulation pump 6B are introduced into the second reaction tower 1B together.
The above embodiments are merely preferred embodiments of the present invention, which are not intended to limit the scope of the present invention, and various changes may be made in the above embodiments of the present invention. All simple and equivalent changes and modifications made according to the claims and the content of the specification of the present application fall within the scope of the claims of the present patent application. The invention has not been described in detail in order to avoid obscuring the invention.
Claims (10)
1. The utility model provides a fountain catalytic ozonation reaction system, characterized in that, this fountain catalytic ozonation reaction system includes at least one reaction tower, the inlet tube, the drain pipe, ozone gas distribution pipe and exhaust pipe, wherein, the reaction tower is the filler spray tower and includes the filler section that has the catalyst, the inlet tube is connected in the reaction tower in order to introduce waste water into reaction system, the drain pipe is connected in the reaction tower in order to discharge waste water from reaction system, ozone gas distribution pipe is connected in the reaction tower in order to introduce ozone into reaction system, the exhaust pipe is connected in the reaction tower in order to discharge residual ozone and the gas after the catalytic reaction from reaction system, the flow direction of waste water in the filler section of reaction tower is opposite with the flow direction of ozone in the filler section of reaction tower in order to realize the gas-water countercurrent contact reaction.
2. The spray-type catalytic ozonation reaction system according to claim 1, wherein the reaction tower comprises a spray section located above the packing section, a water distribution device for forming fine liquid droplets and fog droplets in the wastewater is arranged in the spray section, and the water distribution device is connected with the water inlet pipe.
3. The spray catalytic ozonation reaction system of claim 2, wherein the reaction tower comprises a demisting section located above the spray section, and the demisting section is connected with the exhaust pipe.
4. The spray catalytic ozonation reaction system of claim 3, wherein a demister for removing liquid droplets and mist droplets entrained in the gas is disposed in the mist elimination section.
5. The spray catalytic ozonation reaction system according to claim 1, wherein the reaction tower comprises an air inlet section located below the packing section, and the air inlet section is connected with the ozone distribution pipe.
6. The spray catalytic ozonation reaction system of claim 5, wherein the reaction tower comprises a water tank section located below the gas inlet section, and the water tank section is connected with a drain pipe.
7. The spray catalytic ozonation reaction system of claim 6, wherein the water tank section is connected to the water inlet pipe by a circulation pump.
8. The spray catalytic ozonation reaction system of claim 1, comprising a first reaction tower and a second reaction tower connected in series, wherein the water inlet pipe is connected to the first reaction tower to introduce wastewater into the reaction system, the water outlet pipe is connected to the second reaction tower to discharge wastewater from the reaction system, the ozone distribution pipe is connected to the second reaction tower to introduce ozone into the reaction system, the air outlet pipe is connected to the first reaction tower to discharge residual ozone and gas after catalytic reaction from the reaction system, and the flow direction of wastewater and the flow direction of ozone realize gas-water countercurrent contact reaction in the spray catalytic ozonation reaction system.
9. The spray catalytic ozonation reaction system of claim 8, wherein the air inlet section of the first reaction tower is communicated with the exhaust duct of the second reaction tower.
10. The spray catalytic ozonation reaction system of claim 8, wherein the water tank section of the first reaction tower is connected with the water inlet pipe of the second reaction tower through a circulating pump.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113929204A (en) * | 2021-11-11 | 2022-01-14 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced ultra-efficient wastewater ozone treatment device and treatment method |
| CN115353188A (en) * | 2022-08-18 | 2022-11-18 | 浙江树人学院 | Catalytic ozonation rotational flow purification device |
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Cited By (3)
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| CN113929204A (en) * | 2021-11-11 | 2022-01-14 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced ultra-efficient wastewater ozone treatment device and treatment method |
| CN115353188A (en) * | 2022-08-18 | 2022-11-18 | 浙江树人学院 | Catalytic ozonation rotational flow purification device |
| CN115353188B (en) * | 2022-08-18 | 2023-06-13 | 浙江树人学院 | Catalytic ozonation cyclone purification device |
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