A system and method for treating wastewater by turbulent catalytic ozonation

Abstract

The application discloses a treatment system and method for turbulent catalytic ozone oxidation of wastewater. The treatment system utilizes the strong power provided by water-gas mixing to make the fluid in the intense turbulent motion of swirling and tumbling, improves the gas-liquid-solid contact and mixing behavior, realizes the fluidization of the large-density powder catalyst, promotes the interphase mass transfer, and greatly improves the treatment efficiency of pollutants. The application can fully utilize the catalytic advantages of the ozone catalyst and the strong power provided by water-gas mixing, effectively solve the fluid dynamics inertia of the micron zero-valent iron powder as the ozone catalyst caused by the large density, and enhance the mass transfer between the solid-liquid-gas phases.

Description

Technical Field

[0001] This invention relates to a treatment system for turbulent catalytic ozone oxidation wastewater, and also to a corresponding treatment method, belonging to the field of industrial wastewater treatment technology. Background Technology

[0002] In wastewater treatment, ozone offers advantages such as high treatment efficiency, thorough oxidation, and no secondary pollution, making it widely used, particularly in industrial wastewater treatment. However, relying solely on ozone technology for industrial wastewater treatment suffers from low ozone utilization and limited treatment effectiveness. Developing ozone catalytic oxidation technology can significantly improve ozone utilization and wastewater treatment efficiency, enabling more efficient and environmentally friendly wastewater treatment. Therefore, ozone catalytic oxidation of industrial wastewater has become a research hotspot in the water treatment field in recent years.

[0003] Iron plays a crucial role in environmental chemistry. Among various environmental remediation methods, the catalytic effect of iron (Fe(II) / Fe(III) cycle activation of persulfate, Fenton treatment, iron-carbon microelectrolysis, etc.) plays an irreplaceable role in pollutant removal. Zero-valent iron (ZVFe) possesses unique advantages in ozone catalysis due to its excellent electron-donating ability, abundant surface hydroxyl groups, and surface metal redox cycle. However, due to its high density, ZVFe is often limited to use in fixed-bed permeation reactors. As the reaction occurs and time continues, the corrosion products from the ZVFe reaction accumulate in situ, causing the fixed bed to lose permeability, even clogging pipes and leading to system failure.

[0004] In existing technologies, heterogeneous catalytic ozone oxidation is a gas-liquid-solid three-phase reaction. During this reaction, ozone utilization and oxidation efficiency are significantly affected by mass transfer. Therefore, improving the mass transfer efficiency between the gas, liquid, and solid phases can effectively improve the oxidation efficiency of heterogeneous ozone catalytic oxidation. To improve the mass transfer efficiency between the gas, liquid, and solid phases, existing technologies using suspended packing water treatment systems primarily employ the following key technical means:

[0005] (1) Flotation process to remove relatively low density suspended coarse particles from wastewater;

[0006] (2) When the equipment is running, add an appropriate amount of reagent to make the impurity particles or organic matter adhere to the bubbles, so as to achieve the separation and removal of small-density particles;

[0007] (3) By using external mechanical stirring and wastewater recirculation, the internal water flow of the oxidation reactor is agitated, thereby fluidizing the catalyst and achieving ozone catalysis. However, the effectiveness of the above-mentioned techniques is limited. To solve the problem of low efficiency in ozone catalytic oxidation of wastewater and to fully utilize the catalytic performance of the ozone catalyst, suspending zero-valent iron during the reaction process is a possible solution. In this context, developing supporting reaction equipment is essential for improving the catalytic performance of the catalyst and promoting the industrial application of zero-valent iron. Summary of the Invention

[0008] In order to overcome the deficiencies in the existing technology, the primary technical problem to be solved by the present invention is to provide a treatment system for turbulent catalytic ozone oxidation of wastewater.

[0009] Another technical problem to be solved by the present invention is to provide a method for treating wastewater by turbulent catalytic ozone oxidation.

[0010] To achieve the above objectives, the present invention adopts the following technical solution:

[0011] According to a first aspect of the present invention, a treatment system for turbulent catalytic ozone oxidation of wastewater is provided, comprising a support frame, a reaction tower, and a hydrodynamic generating section; wherein,

[0012] The reaction tower includes a catalyst-filled tube, an inverted conical expanding receiving tube, a tower body, an inverted conical separation cylinder, a sedimentation tank, a fixing frame, a flow guide cylinder, and a baffle tube, all coaxially connected; wherein,

[0013] The upper end of the catalyst packing tube is connected to the small diameter end of the conical expansion receiving tube, the large diameter end of the inverted conical expansion receiving tube is connected to the lower end of the tower body, the upper end of the tower body is connected to the small diameter end of the inverted conical separation cylinder, the large diameter end of the inverted conical separation cylinder is connected to the open end of the sedimentation tank, the other end of the sedimentation tank is a closed end, and it is provided with an air outlet; the side of the sedimentation tank is provided with an upper water outlet, and the lower end of the tower body is provided with a lower water outlet;

[0014] The lower inner side of the tower body is connected to the outer edge of the fixing frame, the inner edge of the fixing frame is connected to the lower end of the guide tube, the lower opening of the guide tube extends to the inverted conical expansion bearing tube, and the upper opening of the guide tube extends into the sedimentation tank.

[0015] The upper end of the baffle tube is connected to the closed end of the sedimentation tank, and the lower end of the baffle tube extends to the upper end of the tower body; the diameter of the baffle tube is larger than the diameter of the guide tube and smaller than the diameter of the tower body; the wall of the baffle tube is located between the guide tube and the tower body.

[0016] The support frame is connected to the lower end of the tower body to support and fix the tower body.

[0017] The hydrodynamic generating section includes a conical hydrocyclone device, a circulating water pump, a metering pump, a raw water tank, an ejector, a gas flow meter, and an ozone generator; wherein,

[0018] The upper end of the conical hydrocyclone device is connected to the lower end of the catalyst filling tube, the lower end of the conical hydrocyclone device is connected to the output end of the jet injector, the gas input end of the jet injector is connected to the output end of the gas flow meter, and the input end of the gas flow meter is connected to the output end of the ozone generator.

[0019] The input end of the jet injector is connected to the output end of the circulating water pump. The input end of the circulating water pump is connected to the lower outlet of the tower body, the output end of the metering pump, and the raw water tank. The input end of the metering pump is connected to the raw water tank.

[0020] Preferably, the conical hydrocyclone device includes a cone; wherein the conical hydrocyclone device is a cylinder with a diameter greater than its height, and the cone is coaxially arranged at the bottom.

[0021] Preferably, the height of the cone is less than its base diameter, and its base diameter is less than the diameter of the conical hydrocyclone device;

[0022] The cone is provided with multiple inclined guide holes that penetrate the bottom surface and the conical surface of the cone; the inclined guide holes are all oblique cylindrical through holes, the centers of the openings of the multiple inclined guide holes are coplanar, and the line connecting the centers of adjacent openings forms a regular polygon; the central axis of the cone passes through the center of the regular polygon and is perpendicular to the plane in which the regular polygon is located.

[0023] Preferably, the catalyst filling tube is cylindrical and coaxially connected to the conical hydrocyclone device; the inverted conical expanding pipe is frustoconical with a cylindrical large-diameter end; the tower body is cylindrical; the inverted conical separation cylinder is frustoconical; and the sedimentation tank is cylindrical.

[0024] The internal region of the catalyst filling tube is the upflow zone I; the internal region of the guide tube is the flow guiding zone II; the region between the guide tube and the tower body is the downflow zone III; the region between the inverted conical separation cylinder and the baffle tube is the conical separation zone IV; and the region between the sedimentation tank and the baffle tube is the sedimentation zone V.

[0025] According to a second aspect of the present invention, a method for treating wastewater from turbulent catalytic ozone oxidation is provided, comprising the following steps:

[0026] S1: The ozone metered by the gas flow meter and the raw water metered by the metering pump are mixed in the ejector and then fed into the conical hydrocyclone device.

[0027] S2: The mixed liquid output from the jet jet passes through multiple inclined guide holes of the conical hydrocyclone device and impacts the catalyst in the catalyst filling tube;

[0028] S3: The mixed liquid is swept upwards, carrying the catalyst, and enters the rising flow zone I. After passing through the inverted conical expansion pipe, it enters the guiding flow zone II, the falling flow zone III, the conical separation zone IV, and the sedimentation zone V in sequence under the guidance of the guide tube.

[0029] S4: The density of catalyst and bubbles in the guiding zone II is greater than that in the descending zone III, and the kinematic activity of the gas-liquid-solid three-phase mixture in the guiding zone II is greater than that in the descending zone III.

[0030] Preferably, the catalyst is zero-valent iron powder with a particle size of 0.5–100 μm and a particle bulk density of 1.8–8 g / cm³. 3 Compared with existing technologies, the turbulent catalytic ozone oxidation wastewater treatment system and method provided by this invention utilizes the power source of sufficient water-gas mixing and the impact force of swirling injection to place the fluid (multiphase mixture) in a turbulent and churning state, forming a turbulent region as the main reaction site. This significantly improves the contact and mixing behavior between the gas phase (ozone), liquid phase (industrial wastewater), and solid phase (powdered catalyst), achieving fluidization of the high-density powdered catalyst, promoting mass transfer between phases, and greatly improving the treatment efficiency of pollutants. This invention can fully utilize the catalytic advantages of ozone catalysts and the powerful driving force provided by water-gas mixing, effectively solving the hydrodynamic inertia caused by the high density of micron-sized zero-valent iron powder used as an ozone catalyst, and enhancing mass transfer between solid, liquid, and gas phases. Attached Figure Description

[0031] Figure 1 This is a schematic diagram of a turbulent catalytic ozone oxidation wastewater treatment system;

[0032] Figure 2 This is a schematic diagram showing the water flow pattern and the movement path of the catalyst iron powder in the reaction tower during the turbulent catalytic ozone oxidation process for treating wastewater.

[0033] Figure 3 This is a top view of the cone-shaped hydrocyclone device;

[0034] Figure 4 yes Figure 3 Side view of the cone in the middle;

[0035] Figure 5 These are the results of removing COD from wastewater from a wastewater treatment plant using this treatment system in Examples 1 and 2.

[0036] Figure 6These are visual results of using this treatment system to remove wastewater from a sewage treatment plant in Examples 1 and 2.

[0037] Figure 7 This shows the COD removal efficiency of wastewater from a wastewater treatment plant under different reaction times.

[0038] Figure 8 This is a comparison of the reaction kinetic constants of the COD removal efficiency of wastewater from a certain sewage treatment plant under different reaction times;

[0039] Figure 9 This is a visual diagram of the wastewater treatment results at a wastewater treatment plant. In the diagram: 1-Support frame, 2-Tower body, 3-Conical hydrocyclone device, 4-Catalyst filling pipe, 5-Inverted conical expansion receiving pipe, 6-Catalyst, 7-Guide cylinder, 8-Baffle pipe, 9-Inverted conical separation cylinder, 10-Sedimentation tank, 11-Ball valve, 12-Ball valve, 13-Ball valve, 14-Gas outlet, 15-Fixed frame, 16-Cone, 17-Inclined guide hole, 18-Ozone generator, 19-Ejector, 20-Circulating water pump, 21-Metering pump, 22-Ball valve, 23-Ball valve, 24-Raw water tank, 25-Gas flow meter. Detailed Implementation

[0040] The technical solution of the present invention will now be clearly and completely described with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of the present invention. Based on the embodiments provided by the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0041] In the description of this invention, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing the invention and for simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on the invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0042] In the description of this invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0043] Example 1

[0044] Turbulence is a chaotic fluid state characterized by high Reynolds numbers and vortex pulsations, which can rapidly and effectively promote the mixing and transport of mass, momentum, and energy. Utilizing turbulence, mass transfer between the solid-liquid-gas phases can be effectively enhanced, achieving the goal of catalytic ozone treatment of wastewater and improving pollutant removal efficiency.

[0045] like Figure 1 As shown in the figure, an embodiment of the present invention provides a treatment system for turbulent catalytic ozone oxidation of wastewater, which mainly includes a reaction tower 100, a hydrodynamic forming part 200 and a support frame 1.

[0046] Inside the reaction tower 100, arranged sequentially from bottom to top along the central axis are: a catalyst packing pipe 4 at the bottom of the reaction tower 100, an inverted conical expansion receiving pipe 5, a guide cylinder 7 and a baffle tube 8 arranged coaxially inside; outside the baffle tube 8 are an inverted conical separation cylinder 9 and a sedimentation zone V at the top, with a gas outlet 14 at the very top. Ball valves 11 to 13 are installed to control the reaction circulation.

[0047] A support frame 1 is installed on the outer bottom of the reaction tower 100 to fix the entire equipment.

[0048] The hydrodynamic generating section 200 includes: a conical hydrocyclone device 3 located below the reaction tower 100; a circulating water pump 20, a metering pump 21, and a raw water tank 24 connected in sequence by pipes; and a ball valve 12 controlling the opening and closing of the hydrodynamic circulation. The raw water tank 24 stores industrial wastewater to be purified, and the metering pump 21 monitors the water flow rate. The other end of the circulating water pump 20 is an ejector 19. An ozone generator 18 is connected to the ejector 19. After the ozone and industrial wastewater mix in the ejector 19, the circulating water pump 20 provides the hydrodynamic force to drive the water-air mixture from the ejector 19 through the conical hydrocyclone device 3 into the reaction tower 100. The ball valve 11 controls the operating state of the ejector 19.

[0049] like Figures 2-4 As shown, the high-momentum water-gas mixture injected by the jet injector 19 passes through the cone 16 of the conical hydrocyclone device 3 at the bottom of the reaction tower 100 and enters the catalyst filling pipe 4. Inclined guide holes 17 are provided on the conical surface and bottom surface of the cone 16, so that the water-gas mixture is swept out obliquely upwards, forming a vortex with large energy above the conical hydrocyclone device 3.

[0050] When the ejected water-gas mixture encounters the inner walls of the catalyst filling tube 4 and the guide tube 7, and under the influence of the velocity difference between the water flow in the middle and on both sides, the direction of the vortex flow changes anisotropically, resulting in the stretching, twisting, and deformation of the vortex, and the formation of rotating vortex pairs and anti-rotating vortex pairs. Under the force of the vortex flow that continuously impacts upward at a relatively high speed and changes continuously, the zero-valent iron powder catalyst 6 is driven to rise and swirl upward with the turbulence.

[0051] The design of the conical hydrocyclone device 3 and the inclined guide hole 17 is described in detail below.

[0052] The conical hydrocyclone device 3 is a cylinder with an outer diameter of 70 mm and a height of 60 mm, with a coaxially mounted cone 16 at the bottom. The height of the cone 16 inside the device is greater than its bottom diameter, specifically a bottom diameter of 50 mm and a height of 30 mm. Four inclined guide holes 17 are formed on the cone 16. Each inclined guide hole 17 is a slanted cylindrical through-hole. The four inclined guide holes 17 are located at the center of the opening on the conical surface of the cone 16, on the same plane, and the line connecting the centers of adjacent openings forms a square. The central axis of the conical hydrocyclone device 3 passes perpendicularly through the center of this square. The openings of the inclined guide holes 17 on the bottom surface of the cone 16 are close to the bottom surface of the conical hydrocyclone device 3, receiving the water-air mixture injected by the jet injector 19. Specifically, the diameter of the inclined guide hole 17 is 6 mm.

[0053] The catalyst filling tube 4 has a diameter of 70 mm and a height of 60 mm, and is coaxial with the conical hydrocyclone device 3.

[0054] The reaction tower 100 has a total height of 320 mm. The inverted conical expanding receiving pipe 5 at the bottom of the reaction tower 100 is frustoconical, with a bottom diameter of 70 mm, a top diameter of 110 mm, and a height of 80 mm; the larger diameter end is cylindrical. The tower body 2 is cylindrical, with a diameter of 110 mm and a height of 160 mm. The upper part of the reaction tower 100 consists of an inverted conical separation cylinder 9 and a sedimentation tank 10. The inverted conical separation cylinder 9 is frustoconical, with a bottom diameter of 110 mm, a top diameter of 140 mm, and a height of 40 mm. The sedimentation tank 10 is cylindrical, with a diameter of 140 mm and a height of 40 mm.

[0055] Inside the reaction tower 100, the guide tube 7 is coaxially installed with the tower body 2, with a diameter of 70 mm and a height of 260 mm. Its bottom is 40 mm from the bottom of the inverted conical expansion receiving tube 5. The interior of the guide tube 7 is the flow guiding zone II. A baffle tube 8 is coaxially installed on the upper part of the guide tube 7. The baffle tube 8 has a diameter of 90 mm and a height of 90 mm. The exterior of the guide tube 7 is the descending flow zone III. The area inside the inverted conical separation cylinder 9 and outside the baffle tube 8 is the conical separation zone IV. The area inside the sedimentation tank 10 and outside the baffle tube 8 is the sedimentation zone V.

[0056] The catalyst packing tube 4, which is cylindrical and 70 mm in diameter and 70 mm in height, is located below the reaction tower 100. The interior is the upflow zone I.

[0057] The water-air mixture in the jet injector 19 passes through the inclined guide hole 17 of the conical hydrocyclone device 3 and impacts the catalyst 6 in the catalyst filling tube 4. The swirling sweep carries the catalyst 6 upward, forming an upflow zone I. After passing through the inverted conical expanding receiving tube 5, it enters the guide zone II under the guidance of the guide tube 7. The density of the catalyst 6 and bubbles in guide zone II is greater than that in downflow zone III, and the kinetic activity of the gas-liquid-solid three-phase mixture in guide zone II is greater than that in downflow zone III. This ensures that less catalyst 6 enters the circulating water pump 20 through the ball valve 12, preventing blockage and damage, and maximizing the utilization efficiency of the catalyst 6. The gas-liquid-solid three-phase mixture repeatedly swirls and rises within the reaction tower 100, forming a vortex turbulent effect. The flow field exhibits a turbulent state, significantly accelerating mass transfer between the three phases, prolonging the residence time of ozone gas in the system, and prompting the zero-valent iron powder, acting as a catalyst, to catalyze the production of more active oxygen species (·OH, ·O2). - , 1 O2), thereby accelerating the reduction and oxidation removal rate of pollutants in wastewater.

[0058] In the gas-liquid-solid three-phase mixture, due to its inherent physicochemical properties, ozone gas reacts and dissipates through outlet 14, while the solid-liquid mixture flows back into the descending zone III of the reaction tower along the guide tube 7. Furthermore, in the ascending zone I, the significant upward force of the water and gas phases creates a negative pressure environment between the guide tube 7 and the inverted conical expansion receiving pipe 5. Additionally, the gravity of the catalyst 6 and water facilitates the recirculation of the catalyst 6 into the ascending zone I and the guide tube 7. This continuous circulation ensures the catalyst 6 is repeatedly utilized within the reaction tower 100. Finally, the treated wastewater flows out through the inverted conical separation zone IV and sedimentation zone V, ensuring that the treated liquid exiting through ball valve 13 is clear and meets compliance standards after inspection.

[0059] The turbulent catalytic ozone oxidation water treatment system provided by this invention offers a simple and effective pathway for the industrial application of ozone catalysts made from suspended and fluidized high-density zero-valent iron powder in wastewater treatment. During the catalytic ozone reaction, catalyst 6 remains suspended in the reaction tower 100, ensuring a complete ozone reaction and preventing catalyst powder accumulation in the reaction zone. This overcomes the drawbacks of existing technologies where zero-valent iron powder, as a catalyst, has high density, is prone to accumulation over long-term use, and does not participate in the reaction. The turbulent catalytic ozone oxidation water treatment system effectively reduces catalyst loss during the reaction. Using turbulent catalytic ozone oxidation technology to treat industrial wastewater enhances mass transfer between the gas, liquid, and solid phases, improves catalyst and ozone utilization efficiency, and ultimately results in significant industrial wastewater treatment effects.

[0060] Specific reaction steps:

[0061] Commercially available micron-sized zero-valent iron powder (ZVI) was selected as catalyst 6 and placed in catalyst packing tube 4. The above reaction equipment was adjusted.

[0062] The particle size of the micron-sized zero-valent iron powder catalyst ranges from 0.5 to 100 μm, and its bulk density ranges from 1.8 to 8 g / cm³. 3 The bulk density of micron-sized iron powder varies considerably depending on its processing technology and vibration compaction, which has a certain impact on the actual catalytic effect. Specifically, 1 μm and 1.8 g / cm³ iron powder were selected. 3 ; 10 μm, 2.8 g / cm 3 ; 100 μm, 3.9 g / cm 3 50 μm, 4.2 g / cm 3 50 μm, 5.5 g / cm 3 Several different catalysts were tested, and when they passed through this device, they all formed a distinct gas-liquid-solid three-phase mixture, which could react with the wastewater to achieve the effect of catalytic oxidation of the wastewater.

[0063] First, open ball valves 11, 22, and 23, close ball valve 12, and turn on circulating water pump 20 to inject industrial wastewater from raw water tank 24 into reaction tower 100, ensuring the industrial wastewater liquid covers ball valve 12 (inlet flow rate is approximately 1 L). Then, open ball valve 12, close ball valve 22, and turn on metering pump 21.

[0064] Turn on the ozone generator 18 and adjust the ozone flow rate so that the ozone enters the pipeline through the ejector 19. After the ozone and industrial wastewater mix in the ejector 19, the gas-liquid mixture formed by the ozone and industrial wastewater is swept into the reaction tower 100 by the hydrodynamic force provided by the circulating water pump 20, passing through the ejector 19 and the conical hydrocyclone device 3 at the bottom of the reaction tower 100.

[0065] Catalyst 6, namely micron-sized zero-valent iron powder, is fluidized by the water-gas thrust of a continuously changing vortex turbulent gas-liquid mixture, forming a gas-liquid-solid three-phase mixture, and a reaction occurs.

[0066] Example 2

[0067] The industrial wastewater is sourced from a wastewater treatment plant.

[0068] like Figure 5 and Figure 6As shown, in the wastewater treatment process of a certain sewage treatment plant, the ozone flow rate of this treatment system is 0.8 L / min, the inlet flow rate of metering pump 21 is 40 ml / min, and the flow rate of circulating water pump 20 is 10 L / min. After 45 minutes of reaction, the total amount of wastewater treated is approximately 1.8 L. For comparison, the conical hydrocyclone device 3 is not installed at the bottom of the reaction tower, but other operating procedures are the same. The micron-sized zero-valent iron powder (ZVI) is a purchased industrial product.

[0069] Micron-sized zero-valent iron powder (ZVI: 1 μm, 1.8 g / cm³) was added to the device. 3 This refers to the catalytic ozone oxidation process. Without the addition of micron-sized zero-valent iron powder (ZVI), it is a typical ozone oxidation process.

[0070] The original COD of the industrial wastewater was 340 mg / L. Under the same external conditions such as ozone flow rate and reaction time, the following measures were taken and then tested:

[0071] Under non-turbulent conditions without a conical hydrocyclone device, the COD in wastewater treated by traditional ozone oxidation is 195 mg / L.

[0072] Under turbulent conditions equipped with a conical hydrocyclone device, the COD in the wastewater after traditional ozone oxidation treatment is 174 mg / L.

[0073] Add micron-sized zero-valent iron powder (ZVI: 1 μm, 1.8 g / cm³) 3 As a catalyst, under non-turbulent conditions, the COD in the wastewater treated by catalytic ozone oxidation was 158 mg / L.

[0074] Add micron-sized zero-valent iron powder (ZVI: 1 μm, 1.8 g / cm³) 3 As a catalyst, under turbulent conditions, the COD in the wastewater after catalytic ozone oxidation treatment was 118 mg / L.

[0075] Therefore, it is evident that turbulent ozone oxidation (O3) and turbulent catalytic ozone oxidation (ZVI+O3) can significantly improve the COD removal rate of wastewater. In treating wastewater from a certain sewage treatment plant, turbulent ozone oxidation (O3) improved the COD removal rate by 6% compared to ordinary ozone oxidation (O3). Turbulent catalytic ozone oxidation (ZVI+O3) improved the COD removal rate by 12% compared to ordinary catalytic ozone oxidation (ZVI+O3).

[0076] like Figure 7 and Figure 8As shown, the kinetic constants of turbulent ozone oxidation (O3) and turbulent catalytic ozone oxidation (ZVI+O3) were observed respectively. The turbulent ozone oxidation technology provided by this treatment system improves the kinetic constant by 1.07 times compared to ordinary ozone oxidation technology; the turbulent catalytic ozone oxidation technology improves the kinetic constant by 1.21 times compared to ordinary catalytic ozone oxidation technology.

[0077] Example 3

[0078] The industrial wastewater is sourced from a wastewater treatment plant.

[0079] During operation, the ozone flow rate of this treatment system is 0.8 L / min, the inlet flow rate of metering pump 21 is 40 ml / min, and the flow rate of circulating water pump 20 is 10 L / min. After 45 minutes of reaction, the total wastewater treated is approximately 1.8 L. In contrast, the conical hydrocyclone device 3 is not installed at the bottom of the reaction tower; all other operating procedures are the same. The micron-sized zero-valent iron powder (ZVI) is a purchased industrial product.

[0080] The COD results of wastewater from a wastewater treatment plant after treatment using different methods are shown in Table 1. Images illustrating the wastewater treatment effects are also included. Figure 9 As shown, turbulent ozone oxidation and turbulent catalytic ozone oxidation have a good effect on improving COD removal from wastewater.

[0081]

[0082] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them. Although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A treatment system for turbulent catalytic ozone oxidation wastewater, characterized in that: It includes a support frame, a reaction tower, and a hydrodynamic forming section; wherein, the reaction tower includes a catalyst filling pipe, an inverted conical expansion pipe, a tower body, an inverted conical separation cylinder, a sedimentation tank, a fixing frame, a flow guide cylinder, and a baffle tube, all of which are coaxially connected; The catalyst filling tube is connected at its upper end to the small diameter end of the conical expansion receiving tube, the large diameter end of the inverted conical expansion receiving tube is connected to the lower end of the tower body, the upper end of the tower body is connected to the small diameter end of the inverted conical separation cylinder, the large diameter end of the inverted conical separation cylinder is connected to the open end of the sedimentation tank, the other end of the sedimentation tank is a closed end with an air outlet; the sedimentation tank has an upper water outlet on its side, and the lower end of the tower body has a lower water outlet. The lower inner side of the tower body is connected to the outer edge of the fixing frame, the inner edge of the fixing frame is connected to the lower end of the guide tube, the lower opening of the guide tube extends to the inverted conical expansion bearing tube, and the upper opening of the guide tube extends into the sedimentation tank. The upper end of the baffle tube is connected to the closed end of the sedimentation tank, and the lower end of the baffle tube extends to the upper end of the tower body; the diameter of the baffle tube is larger than the diameter of the guide tube and smaller than the diameter of the tower body; the wall of the baffle tube is located between the guide tube and the tower body. The support frame is connected to the lower end of the tower body to support and fix the tower body. The hydrodynamic forming part includes a conical hydrocyclone device, a circulating water pump, a metering pump, a raw water tank, an ejector, a gas flow meter, and an ozone generator; The upper end of the conical hydrocyclone device is connected to the lower end of the catalyst filling tube, the lower end of the conical hydrocyclone device is connected to the output end of the jet injector, the gas input end of the jet injector is connected to the output end of the gas flow meter, and the input end of the gas flow meter is connected to the output end of the ozone generator. The input end of the jet injector is connected to the output end of the circulating water pump. The input end of the circulating water pump is connected to the lower outlet of the tower body, the output end of the metering pump, and the raw water tank. The input end of the metering pump is connected to the raw water tank. The conical hydrocyclone device includes a cone; wherein, the conical hydrocyclone device is a cylinder with a diameter greater than its height, and the cone is coaxially arranged at the bottom; The height of the cone is less than its base diameter, and its base diameter is less than the diameter of the conical hydrocyclone device; The cone is provided with multiple inclined guide holes that penetrate the bottom surface and the conical surface of the cone; the inclined guide holes are all oblique cylindrical through holes, the centers of the openings of the multiple inclined guide holes are coplanar, and the line connecting the centers of adjacent openings forms a regular polygon; the central axis of the cone passes through the center of the regular polygon and is perpendicular to the plane in which the regular polygon is located; The catalyst packed in the catalyst-filled tube (4) is zero-valent iron powder with a particle size of 0.5–100 μm and a particle bulk density of 1.8–8 g / cm³. 3 .

2. The processing system as described in claim 1, characterized in that: The catalyst filling tube is cylindrical and coaxially connected to the conical hydrocyclone device; the inverted conical expanding pipe is frustoconical with a cylindrical end at the large diameter; the tower body is cylindrical; the inverted conical separation cylinder is frustoconical; and the sedimentation tank is cylindrical. The internal region of the catalyst filling tube is the upflow zone I; the internal region of the guide tube is the flow guiding zone II; the region between the guide tube and the tower body is the downflow zone III; the region between the inverted conical separation cylinder and the baffle tube is the conical separation zone IV; and the region between the sedimentation tank and the baffle tube is the sedimentation zone V.

3. A method for treating wastewater from turbulent catalytic ozone oxidation, using the treatment system as described in claim 1, characterized in that, Includes the following steps: S1: The ozone metered by the gas flow meter and the raw water metered by the metering pump are mixed in the ejector and then fed into the conical hydrocyclone device. S2: The mixed liquid output from the jet jet passes through multiple inclined guide holes of the conical hydrocyclone device and impacts the catalyst in the catalyst filling tube; S3: The mixed liquid is swept upwards, carrying the catalyst, and enters the rising flow zone I. After passing through the inverted conical expansion pipe, it enters the guiding flow zone II, the falling flow zone III, the conical separation zone IV, and the sedimentation zone V in sequence under the guidance of the guide tube. S4: The density of catalyst and bubbles in the guiding zone II is greater than that in the descending zone III, and the kinematic activity of the gas-liquid-solid three-phase mixture in the guiding zone II is greater than that in the descending zone III.

4. The processing method as described in claim 3, characterized in that: The catalyst is zero-valent iron powder with a particle size of 0.5–100 μm and a particle volume density of 1.8–8 g / cm³. 3 .

Images