CN108689481B - Ozone microbubble catalytic oxidation device and application thereof - Google Patents

Abstract

The invention belongs to sewage treatment in environmental protection engineering, and particularly relates to an ozone microbubble catalytic oxidation device and application thereof. The ozone microbubble catalytic oxidation device comprises a tower body, an ozone generator and a catalytic unit, wherein the tower body is provided with a water inlet and a water outlet, the water inlet comprises an upper water inlet and a lower water inlet which are arranged on the upper side wall and the lower side wall of the tower body, and the water outlet comprises an upper water outlet and a lower water outlet which are arranged on the upper side wall and the lower side wall of the tower body; the ozone generator conveys the gas-liquid mixture to the micro-bubble generator through the gas-liquid mixing pump, the output end of the micro-bubble generator is connected with the inlet of a circulation pipeline of the micro-bubble generator below the tower body, the catalytic unit adopts at least two layers of longitudinally spaced and horizontally arranged catalyst boxes, the catalyst boxes are arranged in the tower body through a bracket, and the outlet of the circulation pipeline of the micro-bubble generator arranged on the side wall of the tower body above the catalytic unit is connected with the gas-liquid mixing pump. The invention effectively solves the technical problems of low ozone utilization rate and the like in the prior art, and has the advantages of compact structure, high ozone utilization rate and the like.

Description

Ozone microbubble catalytic oxidation device and application thereof

Technical Field

The invention belongs to sewage treatment in environmental protection engineering, and particularly relates to an ozone microbubble catalytic oxidation device and application thereof.

Background

With the increasing development of town and industrial production, the produced urban sewage and industrial wastewater become important causes of water environment pollution. The water pollution is more serious to the threat of ecological environment and people's water safety and health. Along with the idea of harmonious and natural places, the demands and difficulties for sewage treatment technology are gradually increased.

The industrial wastewater after conventional biological treatment still contains some refractory organic matters such as phenols, benzene, cyanide, pesticides and the like, so that the COD concentration of the effluent after biological treatment is still 80-90mg/L and cannot reach the emission standard. Therefore, it is necessary to deeply treat the biologically treated effluent. In addition, some cities have developed stricter sewage discharge standards, such as 15mg/L for the first-class A standard of Beijing municipal sewage, and the COD concentration of effluent from a common urban sewage treatment plant is 30-50mg/L, which is a certain distance from reaching the Beijing municipal standard.

Ozone is a high-efficiency strong oxidant without secondary pollution, and can directly degrade organic pollutants in wastewater, however, the ozone has selectivity to the degradation of the organic pollutants, and the application of the ozone in wastewater treatment is limited. Catalytic ozonation technology utilizes a catalyst to promote ozonolysis to generate a large amount of hydroxyl radicals (OH), and can degrade most organic pollutants in water indiscriminately. Gracia et al state that ozone oxidation of humus in the presence of a metal catalyst achieved higher TOC removal rates. The catalytic ozonation technology has the advantages of high reaction speed, simplicity in operation and lower running cost. Therefore, the catalytic ozonation technology has wide application prospect in the treatment of refractory wastewater and the improvement of the biodegradability of wastewater.

In the prior art, in the ozone catalytic oxidation process of organic wastewater in the water treatment industry, ozone is only introduced into water, and after a heavy metal inducer is added, homogeneous catalytic oxidation reaction is caused, and a simple closed water tank is often only built as a reactor, so that the ozone catalytic oxidation reactor has the advantages of low ozone utilization rate, incomplete reaction, large occupied area and the like.

The ozone microbubble catalytic oxidation wastewater treatment technology is based on a common aeration disc or a titanium alloy aeration disc, and aims to provide dissolved oxygen for removing pollutants by microorganisms and improve oxygen mass transfer efficiency in aeration gas. The micro-bubbles have the advantages of large specific surface area, long residence time, high interfacial zeta potential, self-pressurization dissolution, free radical generation, mass transfer efficiency enhancement and the like. Ozone microbubble technology is adopted, so that the gas-liquid mass transfer rate of ozone and the ozone utilization efficiency are improved; at the same time, the micro-bubbles have the characteristics of shrinkage and cracking in the liquid phase, can promote the ozone to decompose and generate hydroxyl free radicals, and remarkably improve the oxidation capability of the ozone.

In recent years, the advanced treatment of industrial wastewater by adopting an ozone microbubble catalytic oxidation technology process is more studied, and a system, a method and a process are proposed from the scientific research perspective no matter from the aspects of patent literature materials or academic research materials, so that detailed discussion on specific application equipment is less. In addition, the device and the method generally adopt a plurality of aeration disc modes, and have the defects of low ozone utilization rate and the like.

The background art retrieved by the applicant includes:

patent document 201410327169.8 discloses an ozone catalytic oxidation water treatment device, and proposes a multistage ozone catalytic oxidation advanced oxidation water treatment device, wherein two solid-liquid catalysts are added. Because the common aeration disc is adopted only to realize low aeration ozone utilization rate, the liquid catalyst needs to be continuously supplied and cannot be recycled, and the solid catalytic unit does not propose an adding and replacing method.

The patent document with the application number of 201511013150.7 discloses a method and a device for catalytic oxidation of ozone, and discloses a wastewater treatment mode of multistage split catalytic oxidation, which has the defects that the basic measures for improving the ozone utilization rate are not adopted, the replacement of a catalyst is inconvenient, and the multistage communication of an ozone pipeline can be influenced by the difference of air pressure and air inlet distances and installation factors to cause uneven distribution of each stage.

Patent document 201510822328.6 discloses an ozone catalytic device, which adopts a dissolved air tank to generate bubbles in a structure, and the diameters of the bubbles are generally larger, so that the dissolved ozone can be rapidly decomposed into oxygen particularly when being influenced by metal ions, and the ozone utilization rate can not be effectively improved. The ozone tail gas of the device is not treated, so that the air is polluted and waste is caused.

Patent document 201510984211.8 discloses a tail water advanced treatment system based on heterogeneous catalytic oxidation of micro-bubble ozone, which comprises an ozone generator, a reaction column, an ozone destructor and the like. The adopted aeration mode still adopts an aeration disc mode, ozone bubbles are difficult to reach the micro-bubble degree, and the ozone utilization rate is also difficult to ensure; the catalyst unit adopts single activated carbon, and has weak adaptability to complex water quality or fluctuating water quality.

In summary, although there are many discussions and researches on catalytic oxidation of micro-bubble ozone at the present stage, the proposed micro-pore aeration mode is mainly composed of an aeration disc and an aeration head, the ozone utilization rate is low, and the oxidation capability is weak.

Disclosure of Invention

The invention aims to provide an ozone microbubble catalytic oxidation device and application thereof, which aim at the technical defects existing in the prior art, can effectively improve the ozone utilization rate, and can conveniently realize the replacement and arrangement of catalytic units according to the needs.

The invention has the following overall technical concept:

the ozone microbubble catalytic oxidation device comprises a tower body, an ozone generator for providing ozone for the tower body, and a catalytic unit for providing catalyst for the tower body, wherein the tower body is provided with a water inlet and a water outlet, the water inlet comprises an upper water inlet and a lower water inlet which are arranged above and below the side wall of the tower body, and the water outlet comprises an upper water outlet and a lower water outlet which are arranged above and below the side wall; the ozone generator conveys the mixed gas-liquid mixture to the micro-bubble generator through the gas-liquid mixing pump, the output end of the micro-bubble generator is connected with the inlet of a micro-bubble generator circulating pipeline below the tower body, the catalytic unit adopts at least two layers of longitudinally spaced and horizontally arranged catalyst boxes, the catalyst boxes are erected in the tower body through a bracket, and the outlet of the micro-bubble generator circulating pipeline arranged on the side wall of the tower body above the catalytic unit is connected with the gas-liquid mixing pump.

The application of the ozone microbubble catalytic oxidation device in sewage treatment.

The specific technical concept of the invention is as follows:

in order to improve the dissolved oxygen in the device and facilitate the treatment of sewage in the device by aerobic microorganisms, the preferred technical implementation mode is that an aeration disc is arranged below the inner part of the tower body.

In order to facilitate the evacuation of the residual water in the device, the preferred technical implementation mode is that the side wall of the bottom of the tower body is provided with an evacuation port.

In order to remove large bubbles generated by the gas-liquid mixing pump, reserving finer bubbles in the mixed liquid; the output of the gas-liquid mixing pump is connected with the input end of the micro-bubble generator through a gas-liquid separator, and the gas-liquid separator outputs the large bubbles escaping from the separated gas-liquid mixture to the gas-liquid mixing pump.

In order to observe the reaction in the tower body, and simultaneously facilitate the discharge of redundant gas in the tower body, the preferred technical scheme is that the top and the side wall of the tower body are provided with transparent windows, observation windows and exhaust valves.

In order to facilitate sampling and detection, a preferred technical implementation mode is that a sampler is arranged on the side wall of the tower body.

In order to facilitate overhauling and replacing equipment such as an aeration disc at the bottom of the tower body, the preferred technical implementation mode is that a mounting flange opening is formed in the side wall of the tower body. In order to facilitate the opening and closing of the top cover plate of the tower body, the top plate of the tower body is assembled and fixed with the tower body through quick-mounting bolts. The quick-mounting structure can be also used for structural assembly of the mounting flange opening and the tower body.

In a more preferable technical scheme, in order to further improve the utilization rate of ozone, the gas exhausted by the exhaust valve can be further recycled through a gas-liquid mixing pump.

In order to avoid the exhaust gas in the tower body from being discharged along with the effluent, the preferable technical scheme is that the upper water outlet is in an inverted U shape.

The design principle of the catalyst box is that the catalyst can be released conveniently, the sufficient contact between the catalyst and reactants can be met, and the catalyst replacement can be realized conveniently. The preferred technical implementation mode is that the catalyst box comprises a hollow cavity body formed by a sieve plate with micropores on the surface and a sealing cover on the surface of the sieve plate.

In order to facilitate the taking and placing of the catalyst box, the preferred technical implementation mode is that the sieve plates positioned on the two sides or the upper surface are fixedly provided with handles.

In order to improve the structural strength of the catalyst box, the preferred technical implementation mode is that the corners of the hollow cavity are provided with reinforcing ribs.

The microbubble generator is mainly used for improving the utilization rate of ozone, and comprises a main pipe with inlets and outlets at two ends, wherein the inlets of the main pipe are connected with the output end of the gas-liquid mixing pump, the inlets of the main pipe are connected with the output end of the gas-liquid mixing pump through a first venturi, the outlets of the main pipe are output through a second venturi, the first venturi and the second venturi comprise inlet sections, shrinkage sections, throats and diffusion sections which are sequentially connected from outside to inside, helical blades which are in the same direction as the advancing direction of materials are fixed in the main pipe, openings are formed in the helical blades, the diameters of the openings are sequentially reduced from inside to outside along the radial direction, the diameters of the openings are 0.5mm-2.5mm, the distances between adjacent openings on the same radial direction are 0.8mm-5mm, and the openings on the same circumference are distributed at equal angle intervals. The microbubble generator is designed by adopting the Venturi principle, so that the microbubble generator can be called a Venturi microbubble generator.

The main mechanism of the distribution of the open pores on the helical blade is as follows: under the action of hydraulic cyclone, the diameters of bubbles in the gas-liquid mixed solution are distributed from small to large along the radial direction close to the inner wall under the action of centrifugal force, and meanwhile, the size distribution of the openings of the spiral blades is opposite to that of the bubbles, so that the diameters of small-diameter microbubbles are maintained through the large holes, and the microbubbles with the diameters of the large bubbles undergo gradual expansion and gradual expansion when passing through the openings, so that the microbubbles can be further crushed and refined.

In order to facilitate the quick fixed assembly of the helical blade and the main pipe, the preferable technical scheme is that the distance between the inner wall of the main pipe and the outer side of the helical blade is not more than 0.3mm. The main purpose of clearance fit is to fix the outside spiral blade with the inside of the main pipe by spot welding or welding after the spiral blade is installed in place during assembly, so as to realize the positioning of the spiral blade in the main pipe.

The spiral blade has the main function that under the water flow pressure and the diversion function, the gas-liquid mixed liquid generates centrifugal force, and the diameter of the micro-bubbles is distributed from small to large along the radial direction under the centrifugal force. The small-diameter microbubbles directly flow out through the holes on the spiral blades, and the large-diameter microbubbles are further crushed through the holes on the spiral blades, so that the large-diameter microbubbles are crushed and refined. The preferable technical scheme is that the distance between the adjacent spiral blades is reduced from the inlet to the outlet of the main pipe in sequence, and the distance between the adjacent spiral blades is 200mm-50mm. With the flow of the gas-liquid mixture, the pitch of the helical blades is gradually reduced, the centrifugal force is increased, and the fine crushing effect on the microbubbles is further enhanced. Under the condition of constant total flow, the flow velocity and pressure of the gas-liquid mixed liquid are gradually increased due to the reduction of the area of the rotational flow section, and the microbubbles with larger diameters in the gas-liquid mixed liquid are also distributed along the radial direction close to the inner wall of the main pipe under the action of centrifugal force. According to the characteristics of the hydraulic cyclone, the pressure of the fluid is gradually increased along the direction approaching to the wall surface along the radial direction, and the bubbles are crushed and refined under the action of the flow velocity increase and the pressure increase. In addition, when the gas-liquid mixed solution passes through the holes of the helical blades, the gas-liquid mixed solution is subjected to gradual expansion and gradual contraction, and microbubbles with larger diameters are thinned.

In order to lead the gas-liquid mixed solution to the helical blade and improve the uniformly distributed effect of the gas-liquid mixed solution in the circumferential direction, the preferable technical scheme is that a water diversion shaft is arranged in the main pipe along the axis, the helical blade is fixed between the water diversion shaft and the inner wall of the main pipe, the distance between the inner side of the helical blade and the water diversion shaft is not more than 0.3mm, and the main purpose of clearance fit is to facilitate the welding positioning of the inner side of the helical blade and the water diversion shaft during assembly.

The more preferable technical proposal is that the end part of the water diversion shaft adjacent to the main pipe inlet is conical with the taper angle of beta, and beta is more than or equal to 10 degrees and less than or equal to 20 degrees.

In order to facilitate the connection of the micro-bubble generator and the gas-liquid mixing pump and other equipment, the preferred technical scheme is that the outer sides of the inlet sections of the first venturi tube and the second venturi tube are provided with connecting hoops. It will be apparent that other forms of connection interfaces and securing members may be employed with the connector clip without departing from the spirit of the present invention.

In order to obtain a better micro-bubble generation effect, the preferable technical implementation mode is that the flow rate of the gas-liquid mixture output by the gas-liquid mixing pump 17 is 1m/s-10m/s, and the pressure is 0.1MPa-0.5MPa.

The primary function of the first venturi tube and the second venturi tube is that the cross section diameter of the gas-liquid mixed solution is increased when passing through the diffusion section of the first venturi tube, the flow velocity is decreased, the pressure is decreased, and the micro bubbles are increased; the cross section diameter becomes smaller when passing through the diffusion section of the second venturi, the flow speed is increased, the pressure is increased, and the micro bubbles become smaller; in order to obtain the ideal diameter of the micro-bubbles, the preferable technical proposal is that the taper angles of the diffusion sections of the first venturi tube and the second venturi tube are alpha, and alpha is more than or equal to 10 degrees and less than or equal to 20 degrees.

The structure design of the open pore is mainly used for further improving the breaking effect of the micro-bubble and further refining the micro-bubble, and the preferable technical scheme is that the outer side and the inner side of the open pore are taper holes, and the corresponding taper angles are gamma 1 and gamma 2 respectively, wherein gamma 1 is more than or equal to 100 degrees and less than or equal to 160 degrees, and gamma 2 is more than or equal to 100 degrees and less than or equal to 160 degrees; the middle part of the opening 13G is a circular through hole, the aperture is phi, phi is more than or equal to 0.5mm and less than or equal to 2.5mm; the thickness of the spiral blade is delta, and delta is more than or equal to 1mm and less than or equal to 5mm. The design of the opening mainly adopts the design principle of Venturi, the size of the opening is a direct factor influencing the pressure difference between the inside and the outside of the opening, and the smaller the aperture, the larger the pressure difference, and the smaller the pressure difference. The small-aperture opening has high degree of refinement for the gas in the gas-liquid mixture, and the large-aperture opening has low degree of refinement for the gas in the gas-liquid mixture.

In order to facilitate the arrangement of the catalyst box and realize better wildness of the bracket, the preferred realization mode of the technology is that the bracket comprises a first bracket arranged at the bottom of the tower body and a second bracket longitudinally overlapped and arranged above the first bracket; the first bracket and the second bracket are formed by fixedly assembling a longitudinal supporting rod and a transverse supporting rod, the top of the first bracket is horizontally provided with an upper frustum, and the bottom of the first bracket is provided with a footing; the top and the bottom of the second bracket are horizontally provided with an upper frustum and a lower frustum which are matched in shape.

In order to facilitate the taking and placing of the support, the preferred technical implementation mode is that the support is provided with lifting lugs.

The working principle of the invention is as follows:

when in use, single-layer or multi-layer, single or multiple catalysts can be selected according to the water quality and the technological condition, common aeration discs or micro-bubble mixed liquid circulation loops are adopted for aeration, the upper water inlet and outlet or lower water inlet and upper water outlet modes are selected, and the air outlet quantity of the ozone generator is regulated according to the water quality change condition of the outlet water.

The applicant needs to say that:

in the description of the present invention, the terms "below," "above," "bottom," "top," "sidewall," "longitudinal," "horizontal," "upper surface," "both sides," "radial," "circumferential," "inner wall," "inside," and the like indicate orientations or positional relationships based on the orientation or positional relationships shown in the drawings, merely to facilitate the description of the present invention, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the invention. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

The invention has the substantial characteristics and the remarkable technical progress that:

1. the invention has compact integral structure, convenient maintenance and disassembly and convenient transportation and placement. Can be used as a catalytic oxidation treatment process for treating industrial wastewater independently, and can also be combined with other processes in series for combined treatment. The device can be used as medium-sized test equipment for sewage treatment technical research and also can be used as emergency water treatment equipment for point-type sewage sources.

2. The tower body adopts a combined catalyst box and a bracket, and the upper part and the bottom of the bracket are provided with frustum-shaped connecting nesting tables, so that the bracket is convenient to accurately and stably place in the tower body. Firstly, the catalyst support can be lifted from the top conveniently, and can be used in a single layer or combined in multiple layers, and can be taken out in a single layer or stacked in multiple layers; secondly, different catalysts can be arranged in the catalyst box according to different processes, and the catalyst box is used for catalyzing different water quality and different pollutants respectively and is superior to a single-component catalyst; and thirdly, the multi-layer arrangement of the catalyst layers can promote hydraulic disturbance, so that gas-liquid mixing and transmission are facilitated.

3. Ozone utilization rate can be further improved by adopting a microbubble generator and a circulation loop, and meanwhile, direct aeration is performed by adopting an aeration disc. Can flexibly select according to the water quality condition, the microbubble aeration mode is selected to improve the ozone utilization rate, the SS water quality is relatively high, and the traditional aeration disc aeration is selected to be suitable for relatively complex water quality.

4. The structural design of the gas-liquid separator can effectively remove large bubbles generated by the gas-liquid mixing pump and retain finer bubbles in the mixed liquid; the bubbles generated by the treatment of the microbubble generator are further refined and homogenized.

5. The water inlet and outlet of the tower body adopts two modes of upward and downward flow, namely downward flow, upward flow, namely upward flow, wherein the upper water outlet adopts an inverted U-shaped water outlet pipe, and the gas in the tower can be prevented from flowing out along with the water flow. From the process point of view, the downward flow is adopted to facilitate the full contact of gas and liquid, and the upward flow is adopted to facilitate the contact of water and the catalyst. Reasonable flow direction can be selected according to the water quality condition (for example, upward flow is selected for water quality which is easy to catalyze and has good catalysis performance, and downward flow is selected for water quality which is poor in water quality and is difficult to be oxidatively degraded).

6. The top and the side wall of the tower body are provided with transparent windows and observation windows for lighting and observing the state in the tower, and especially the requirement for adjusting micro bubbles is met.

7. The venturi design principle is utilized to design the pipeline and the opening of the micro-bubble generator, so that the thinning of the micro-bubble crusher is effectively realized. The comparative experiment proves that the technical effect of the device for treating the catalytic oxidation wastewater is obviously better than that of the existing aeration equipment.

8. The spiral blade adopts a structural design with gradually reduced spacing, so that the fine crushing effect of the microbubbles is further enhanced.

9. According to the characteristics of utilizing the hydrocyclone, the layout of the holes on the spiral blades and the hole structure designed by adopting the Venturi principle are carried out, so that the breaking and refining degree of the microbubbles is further improved, and the uniformity of the microbubbles is improved.

10. The structural design of the water diversion shaft enables the positioning and assembly of the helical blade to be more convenient, the end part of the water diversion shaft adopts a conical structural design, so that the gas-liquid mixed solution is guided to the helical blade, and the uniform distribution effect of the gas-liquid mixed solution in the circumferential direction is improved.

Drawings

Fig. 1 is a schematic view of the overall structure of the present invention.

Fig. 2 is an enlarged partial view of section i of fig. 1.

Fig. 3 is A-A view of fig. 1.

Fig. 4 is a perspective view of the present invention.

Fig. 5 is a schematic view of the structure of the catalyst case in the present invention.

Fig. 6 is a bottom view of fig. 5.

Fig. 7 is a perspective view of the catalyst case.

Fig. 8 is a schematic view of the structure of the bottom bracket in the present invention.

Fig. 9 is a top view of fig. 8.

Fig. 10 is a perspective view of the bottom bracket.

Fig. 11 is a schematic structural view of the middle bracket of the present invention.

Fig. 12 is a top view of fig. 11.

Fig. 13 is a perspective view of the middle bracket.

Fig. 14 is a schematic view showing the cooperation of the bracket and the catalyst case in the present invention.

FIG. 15 is a schematic view of the structure of a microbubble generator in the present invention.

Fig. 16 is a B-B enlarged view of fig. 15.

Fig. 17 is a schematic view of an open cell structure of a microbubble generator.

Reference numerals in the drawings are as follows:

1. a transparent window; 2. a quick-mounting bolt; 3. a tower body; 4. an upper water outlet; 5. an observation window; 6. a catalyst tank; 6A, a sieve plate; 6B, sealing; 6C, micropores; 6D, a handle; 6E, reinforcing ribs; 7. a bracket; 7A, an upper frustum; 7B, lifting eyes; 7C, a longitudinal support rod; 7D, a transverse supporting rod; 7E, footing; 7F, a lower frustum; 8. an aeration disc; 9. a lower water outlet; 10. a water inlet pipe; 11. an evacuation port; 12. a lower water inlet; 13. a microbubble generator; 13A, a connection clamp; 13B, a first venturi; 13C, helical blades; 13D, a water diversion shaft; 13E, a main pipe; 13F, a second venturi; 13G, perforating; 14. an inlet of a circulation pipeline of the microbubble generator; 15. installing a flange port; 16. an outlet of a circulation pipeline of the microbubble generator; 17. a gas-liquid mixing pump; 18. a gas-liquid separator; 19. an ozone generator; 20. an upper water inlet; 21. a tower top plate; 22. an exhaust valve; 23. a sampler.

Detailed Description

The present invention will be further described with reference to the following examples, but should not be construed as limiting the invention, and the scope of the invention is defined by the appended claims, and any equivalents thereof may be substituted according to the description without departing from the scope of the invention.

The whole structure of the embodiment is shown in the figure, wherein the ozone microbubble catalytic oxidation device comprises a tower body 3, an ozone generator 19 for providing ozone for the tower body 3, a catalytic unit for providing catalyst for the tower body 3, a water inlet and a water outlet are arranged on the tower body 3, the water inlet comprises an upper water inlet 20 and a lower water inlet 12 which are arranged above and below the side wall of the tower body 3, and the water outlet comprises an upper water outlet 4 and a lower water outlet 9 which are arranged above and below the side wall; the ozone generator 19 conveys the mixed gas-liquid mixture to the micro-bubble generator 13 through the gas-liquid mixing pump 17, the output end of the micro-bubble generator 13 is connected with the inlet 14 of the micro-bubble generator circulation pipeline below the tower body 3, the catalytic unit adopts three layers of longitudinally-spaced and horizontally-arranged catalyst boxes 6, the catalyst boxes 6 are erected in the tower body 3 through the support 7, and the outlet 16 of the micro-bubble generator circulation pipeline arranged on the side wall of the tower body 3 above the catalytic unit is connected with the gas-liquid mixing pump 17.

The application of the ozone microbubble catalytic oxidation device in sewage treatment.

An aeration disc 8 is arranged below the inner part of the tower body 3.

The side wall of the bottom of the tower body 3 is provided with an emptying port 11.

The output of the gas-liquid mixing pump 17 is connected with the input end of the micro-bubble generator 13 through a gas-liquid separator 18, and the gas-liquid separator 18 outputs the large bubbles escaped from the separated gas-liquid mixture to the gas-liquid mixing pump 17.

The top and the side wall of the tower body 3 are provided with a transparent window 1, an observation window 5 and an exhaust valve 22.

The side wall of the tower body 3 is provided with a sampler 23.

The side wall of the tower body 3 is provided with a mounting flange opening 15.

The tower top plate 21 and the tower body 3 are assembled and fixed through the quick-mounting bolts 2. The quick-mounting structure is also used for structural assembly of the mounting flange opening 15 and the tower body 3.

The gas discharged from the exhaust valve 22 is further recycled by the gas-liquid mixing pump 17.

The upper water outlet 4 is in an inverted U shape.

The catalyst box 6 comprises a hollow cavity body formed by a sieve plate 6A with micropores 6C formed in the surface, and a sealing cover 6B formed on the surface of the sieve plate 6A.

The lifting handles 6D are fixed on the screen plate 6A positioned on the two sides or the upper surface.

The corner of the hollow cavity is provided with a reinforcing rib 6E.

The microbubble generator 13 comprises a main pipe 13E, the two ends of the main pipe 13E are provided with inlets and outlets, the inlets of the main pipe 13E are connected with the output end of the gas-liquid mixing pump through a first venturi tube 13B, the outlets of the main pipe 13E are output through a second venturi tube 13F, the first venturi tube 13B and the second venturi tube 13F comprise inlet sections, shrinkage sections, throats and diffusion sections which are sequentially connected from outside to inside, helical blades 13C which are in the same direction as the advancing direction of materials are fixed in the main pipe 13E, the helical blades 13C are provided with openings 13G, the apertures of the openings 13G are sequentially reduced from inside to outside in the radial direction, the apertures are 0.5mm-2.5mm, the intervals between the adjacent openings 13G in the same radial direction are 0.8mm-5mm, and the intervals between the adjacent openings 13G in the circumferential direction are 0.8mm-5mm, and the openings 13G on the same angle are distributed at intervals on the same circumference. The microbubble generator is designed by adopting the Venturi principle, so that the microbubble generator can be called a Venturi microbubble generator.

The distance between the inner wall of the main pipe 13E and the outside of the helical blade 13C is not more than 0.3mm.

The distance between the adjacent spiral blades 13C is reduced from the inlet to the outlet of the main pipe 13E, and the distance between the adjacent spiral blades 13C is 200mm-50mm.

The main pipe 13E is internally provided with a water diversion shaft 13D along the axis, a spiral blade 13C is fixed between the water diversion shaft 13D and the inner wall of the main pipe 13E, and the distance between the inner side of the spiral blade 13C and the water diversion shaft 13D is not more than 0.3mm.

The end of the water diversion shaft 13D adjacent to the inlet of the main pipe 13E is conical with a taper angle beta which is more than or equal to 10 degrees and less than or equal to 20 degrees.

The outer sides of the inlet sections of the first venturi tube 13B and the second venturi tube 13F are provided with a connecting clamp 13A.

The flow rate of the gas-liquid mixture output by the gas-liquid mixing pump 17 is 1m/s-10m/s, and the pressure is 0.1MPa-0.5MPa.

The taper angle of the diffusion sections of the first venturi 13B and the second venturi 13F is alpha, and alpha is more than or equal to 10 degrees and less than or equal to 20 degrees.

The outer side and the inner side of the opening 13G are taper holes, the corresponding taper angles are gamma 1 and gamma 2, gamma 1 is more than or equal to 100 degrees and less than or equal to 160 degrees, gamma 2 is more than or equal to 100 degrees and less than or equal to 160 degrees; the middle part of the opening 13G is a circular through hole, the aperture is phi, phi is more than or equal to 0.5mm and less than or equal to 2.5mm; the thickness of the spiral blade 13C is delta, and delta is more than or equal to 1mm and less than or equal to 5mm.

The bracket 7 comprises a first bracket arranged at the bottom of the tower body 3 and a second bracket longitudinally overlapped and arranged above the first bracket; the first bracket and the second bracket are formed by fixedly assembling a longitudinal supporting rod 7C and a transverse supporting rod 7D, the top of the first bracket is horizontally provided with an upper frustum 7A, and the bottom of the first bracket is provided with a foot 7E; the top and the bottom of the second bracket are horizontally provided with an upper frustum 7A and a lower frustum 7F which are matched in shape.

The support 7 is provided with a lifting lug 7B.

To verify the technical effect of this example, the applicant carried out the following tests:

the applicant has verified the effect of generating micro bubbles by applying the device in this example to ozone catalytic oxidation wastewater treatment and comparing with a common aeration device, and the specific test procedure is as follows:

1. time: 2016 for 10 months to 12 months;

2. the test contents are as follows: the ozone microbubble catalytic oxidation device is applied to treatment tests of industrial wastewater;

3. test equipment: microbubble ozone catalytic oxidation integrated test equipment;

4. test water source: waste water from Jinzhou chemical park;

5. test process

(1) Catalytic oxidation by ozone;

(2) Catalyst: the original AC is added in an amount of 1/3 of the effective volume of the reactor;

(3) Hydraulic retention time is 0.5h;

(4) Aeration mode: aeration disc aeration and micro-bubble aeration.

6. Test results

(1) The COD of the water produced by adopting the aeration disc ozone aeration test is about 120mg/L, and the ozone utilization rate is 50-60%; the COD of the effluent of the equipment in the embodiment is below 30mg/L, the average ozone utilization rate is above 90.8%, and the pH of the effluent is relatively stable.

(2) The effect of treating wastewater by adopting the equipment in the embodiment is superior to the first-level A emission standard of pollutant emission standard of urban sewage treatment plant (GB 18918-2002).

Claims (20)

1. The ozone microbubble catalytic oxidation device comprises a tower body (3), an ozone generator (19) for providing ozone for the tower body (3), and a catalytic unit for providing catalyst for the tower body (3), wherein the tower body (3) is provided with a water inlet and a water outlet; the ozone generator (19) conveys the mixed gas-liquid mixture to the micro-bubble generator (13) through the gas-liquid mixing pump (17), the output end of the micro-bubble generator (13) is connected with the inlet (14) of a circulation pipeline of the micro-bubble generator below the tower body (3), the catalytic unit adopts at least two layers of longitudinally spaced and horizontally arranged catalyst boxes (6), the catalyst boxes (6) are erected in the tower body (3) through the bracket (7), and the outlet (16) of the circulation pipeline of the micro-bubble generator arranged on the side wall of the tower body (3) above the catalytic unit is connected with the gas-liquid mixing pump (17); the micro-bubble generator (13) comprises a main pipe (13E) with inlets and outlets at two ends, the inlets of the main pipe (13E) are connected with the output end of the gas-liquid mixing pump through a first venturi pipe (13B), the outlets of the main pipe (13E) are output through a second venturi pipe (13F), the first venturi pipe (13B) and the second venturi pipe (13F) sequentially comprise an inlet section, a contraction section, a throat and a diffusion section which are sequentially connected from outside to inside, helical blades (13C) which are in the same direction as the advancing direction of materials are fixed in the main pipe (13E), holes (13G) are formed in the helical blades (13C), the aperture of the holes (13G) sequentially decreases from inside to outside in the radial direction, the aperture is 0.5mm-2.5mm, the distance between the holes (13G) which are adjacent in the radial direction is 0.8mm-5mm, and the holes (13G) which are located in the same circumference are distributed at equal angle intervals.

2. The ozone microbubble catalytic oxidation device as set forth in claim 1, characterized in that an aeration disc (8) is disposed below the inside of the tower body (3).

3. The ozone microbubble catalytic oxidation device as set forth in claim 1, characterized in that the bottom side wall of the tower body (3) is provided with an evacuation port (11).

4. The ozone microbubble catalytic oxidation device as set forth in claim 1, characterized in that the output of the gas-liquid mixing pump (17) is connected to the input end of the microbubble generator (13) through a gas-liquid separator (18), and the gas-liquid separator (18) outputs the separated large bubbles escaping from the gas-liquid mixture to the gas-liquid mixing pump (17).

5. The ozone microbubble catalytic oxidation device as set forth in claim 1, characterized in that the top and side walls of the tower body (3) are provided with a transparent window (1), an observation window (5) and an exhaust valve (22).

6. The ozone microbubble catalytic oxidation device as set forth in claim 1, characterized in that the upper water outlet (4) is in an inverted U-shape.

7. The ozone microbubble catalytic oxidation device as set forth in claim 1, characterized in that the catalyst box (6) comprises a hollow cavity formed by a sieve plate (6A) with micropores (6C) on the surface, and a cover (6B) on the surface of the sieve plate (6A).

8. The ozone microbubble catalytic oxidation device as set forth in claim 7, characterized in that a handle (6D) is fixed on the screen plate (6A) on both sides or the upper surface.

9. The ozone microbubble catalytic oxidation device as set forth in claim 7, characterized in that the corners of the hollow cavity are provided with reinforcing ribs (6E).

10. Ozone microbubble catalytic oxidation device according to claim 1, characterized in that the distance between the inner wall of the main tube (13E) and the outside of the helical blades (13C) is not more than 0.3mm.

11. Ozone microbubble catalytic oxidation device according to claim 1, characterized in that the pitch of adjacent helical blades (13C) decreases in sequence from the inlet to the outlet of the main pipe (13E), the pitch of adjacent helical blades (13C) being 200-50 mm.

12. The ozone microbubble catalytic oxidation device as set forth in claim 1, characterized in that a water diversion shaft (13D) is disposed in the main pipe (13E) along the axis, a helical blade (13C) is fixed between the water diversion shaft (13D) and the inner wall of the main pipe (13E), and the distance between the inner side of the helical blade (13C) and the water diversion shaft (13D) is not greater than 0.3mm.

13. The ozone microbubble catalytic oxidation device as recited in claim 12, characterized in that the end of the water diversion shaft (13D) adjacent to the inlet of the main pipe (13E) has a conical shape with a taper angle β,10 ° β being less than or equal to 20 °.

14. The ozone microbubble catalytic oxidation device as set forth in claim 1, characterized in that a connection clip (13A) is provided outside the inlet sections of the first venturi (13B) and the second venturi (13F).

15. The ozone microbubble catalytic oxidation device as recited in any one of claims 1, 11-13, characterized in that the flow rate of the gas-liquid mixture outputted by the gas-liquid mixing pump (17) is 1m/s-10m/s, and the pressure is 0.1MPa-0.5MPa.

16. Ozone microbubble catalytic oxidation device according to any one of claims 1, 11-14, characterized in that the taper angle of the diffuser sections of the first venturi (13B) and the second venturi (13F) is α,10 ° or more α or less than 20 °.

17. The ozone microbubble catalytic oxidation device as set forth in claim 16, characterized in that the outer side and the inner side of the opening (13G) are tapered holes, and the corresponding taper angles are γ1 and γ2, respectively, and are 100 ° - γ1-160 °, and 100 ° - γ2-160 °; the middle part of the opening (13G) is a circular through hole, the aperture is phi, phi is more than or equal to 0.5mm and less than or equal to 2.5mm; the thickness of the spiral blade (13C) is delta, and delta is more than or equal to 1mm and less than or equal to 5mm.

18. The ozone microbubble catalytic oxidation device as recited in any one of claims 1-14, characterized in that the bracket (7) comprises a first bracket arranged at the bottom of the tower body (3) and a second bracket longitudinally superposed above the first bracket; the first bracket and the second bracket are formed by fixedly assembling a longitudinal supporting rod (7C) and a transverse supporting rod (7D), an upper frustum (7A) is horizontally arranged at the top of the first bracket, and a footing (7E) is arranged at the bottom of the first bracket; the top and the bottom of the second bracket are horizontally provided with an upper frustum (7A) and a lower frustum (7F) which are matched in shape.

19. The ozone microbubble catalytic oxidation device as set forth in claim 18, characterized in that lifting lugs (7B) are provided on the bracket (7).

20. Use of an ozone microbubble catalytic oxidation device according to any one of claims 1-19 in wastewater treatment.