Sludge ozone wall breaking efficient turbulent flow uniform mixing reaction device

Abstract

The invention discloses a sludge ozone wall breaking efficient turbulent flow uniform mixing reaction device which comprises a uniform mixing reaction tank, a dispersing device, a sludge distributing device, a first-stage catalytic oxidation reaction area and a second-stage catalytic oxidation reaction area are arranged in the uniform mixing reaction tank from bottom to top, and the sludge distributing device is communicated with a sludge inlet pipeline of the uniform mixing reaction tank; the multiphase micro-nano bubble mixed flow feeding device comprises a slurry inlet pipe, a high-pressure feeding pump and a jet device, the feeding end of the slurry inlet pipe is communicated with the turbulent flow mixing area, the slurry outlet end of the slurry inlet pipe is communicated with the high-pressure feeding pump, and the jet device comprises an ozone inlet, a conical feeding connector and a pressurized flow mixing pipe. The feeding end of the conical feeding connector is communicated with a discharging port of the high-pressure feeding pump, the discharging end of the conical feeding connector extends into and is communicated with the feeding end of the pressurized flow mixing pipe, an ozone inlet is formed in the side wall of the feeding end of the pressurized flow mixing pipe, and the discharging end of the pressurized flow mixing pipe is communicated with the dispersing device. The sludge wall breaking rate and the organic matter dissolution rate are remarkably improved, and the method has the advantages of being high in treatment efficiency, stable in operation, capable of saving energy and reducing consumption and the like.

Description

Technical Field

[0001] This invention relates to the field of activated sludge and wastewater treatment technology, and in particular to a high-efficiency ozone-induced cell disruption and homogenization reaction device for sludge. Background Technology

[0002] With the acceleration of urbanization and industrialization, the amount of sludge generated during wastewater treatment is increasing daily, making sludge treatment and resource utilization a crucial aspect of environmental governance. Ozone catalytic oxidation technology, due to its high efficiency and lack of secondary pollution, is widely used in sludge cell disruption to achieve cell breakdown and release of organic matter. However, existing sludge ozone catalytic oxidation technologies still face numerous technical bottlenecks in practical applications, severely restricting their treatment efficiency and widespread adoption. Currently, there is a lack of specialized equipment for sludge conditioning reactions using ozone. Typically, reaction tanks from wastewater treatment processes are used in conjunction with ozone generators, introducing ozone into the sludge through aeration for oxidation. While this type of equipment is simple, it generally suffers from low ozone mass transfer efficiency, long reaction times, high energy consumption, and insufficient ozone utilization. The main problems are as follows: ozone has low solubility in water, especially in sludge, leading to low mass transfer efficiency and a large amount of ozone being wasted without participating in the reaction; uneven ozone aeration during feeding causes localized accumulation or short-circuiting of ozone within the reactor, preventing sufficient contact with the sludge and resulting in over-oxidation in some areas while under-reacting in others, severely impacting the overall treatment effect; a single sludge feeding method easily leads to uneven material distribution within the reactor, affecting reaction stability; insufficient mixing of sludge and ozone results in inadequate contact and limited reaction rate; furthermore, the unreasonable distribution of heterogeneous catalyst materials within the reactor easily leads to localized accumulation or loss, making it difficult to achieve efficient utilization of catalytic sites and further weakening the catalytic oxidation effect; the lack of an effective mixing and disturbance mechanism within the reactor causes sludge to easily settle or form aggregates, making it difficult for ozone to penetrate the sludge flocs, resulting in low overall cell disruption efficiency and unsatisfactory dewatering improvement. Summary of the Invention

[0003] This invention addresses key technical problems in existing technologies, such as low ozone mass transfer efficiency during sludge cell disruption, uneven ozone supply, low dissolved concentration, slow catalytic reaction, and uneven sludge reaction. It provides a high-efficiency turbulent mixing reactor for sludge ozone cell disruption. By optimizing the internal flow field structure of the reactor, designing a multi-channel, multi-phase feeding system, and introducing high-efficiency turbulent components, the turbulent mixing is enhanced, significantly increasing the contact frequency and reaction probability of sludge, ozone, and catalyst. Simultaneously, by employing multiphase catalytic materials and using catalytic material immobilization and uniform distribution technology, the catalyst is ensured to function stably and efficiently in the reaction zone, significantly improving the ozone's destructive effect on sludge cell walls and achieving a significant improvement in sludge dewatering performance.

[0004] The technical solution adopted in this invention is: A high-efficiency turbulent mixing and homogenizing reaction device for sludge ozone cell disruption includes a multiphase micro-nano bubble mixing and feeding device and a homogenizing reaction tank. The homogenizing reaction tank is arranged from bottom to top as follows: a dispersion device, a sludge feeding device, a primary catalytic oxidation reaction zone, and a secondary catalytic oxidation reaction zone. The sludge feeding device is connected to the sludge inlet pipe of the homogenizing reaction tank. A multiphase feeding mixing zone is formed between the bottom of the homogenizing reaction tank and the primary catalytic oxidation reaction zone. A turbulent mixing zone is formed between the primary and secondary catalytic oxidation reaction zones. A discharge zone is formed above the secondary catalytic oxidation reaction zone, and the discharge zone is equipped with a sludge discharge pipe and a waste gas pipe. The multiphase micro-nano bubble mixing and feeding device includes... The system includes a slurry inlet pipe, a high-pressure feed pump, and an ejector. The inlet end of the slurry inlet pipe is connected to the turbulent mixing zone, and the outlet end is connected to the inlet of the high-pressure feed pump. The ejector includes an ozone inlet, a conical feed connector, and a pressurized mixing pipe. The inlet end of the conical feed connector is connected to the outlet of the high-pressure feed pump, and the outlet end of the conical feed connector extends into and is connected to the inlet end of the pressurized mixing pipe. The ozone inlet is located on the side wall of the inlet end of the pressurized mixing pipe, and the outlet end of the pressurized mixing pipe is connected to the dispersing device. High-fluidity sludge from the homogenizing reactor and ozone form an ozone mixed flow in the ejector and are injected into the homogenizing reactor through the dispersing device in a high-pressure jet manner.

[0005] In the above scheme, the discharge end of the conical feed connector has a tapered conical structure to form a pressurization zone; a gap is left between the outer wall of the discharge end of the conical feed connector and the inner wall of the feed end of the pressurized mixing pipe as an ozone intake channel and to form a negative pressure zone; the pressurized mixing pipe includes a tapering section and a diffusion section along the fluid flow direction, the tapering section forms a high-pressure jet zone, and the diffusion section forms a mixed-flow diffusion zone.

[0006] In the above scheme, the multiphase micro-nano bubble mixing and feeding device further includes a slurry inlet filtration device. The slurry inlet end of the slurry inlet pipe is connected to the slurry inlet filtration device. The slurry inlet filtration device includes a spherical filter cover, a rotating connecting pipe, a rotating bearing, and a fixed connecting pipe. The spherical filter cover is fixed to one end of the rotating connecting pipe. The rotating connecting pipe is connected to the fixed connecting pipe through the rotating bearing. The fixed connecting pipe is fixedly connected to the slurry inlet end of the slurry inlet pipe.

[0007] In the above scheme, both the primary catalytic oxidation reaction zone and the secondary catalytic oxidation reaction zone are filled with Mn-Fe-C micro-electrolysis composite catalytic material.

[0008] In the above scheme, the turbulent mixing zone is equipped with a backwashing device, which is connected to an external high-pressure clean water or high-pressure air device to remove impurities adhering to the surface of the catalyst materials in the primary catalytic oxidation reaction zone and the secondary catalytic oxidation reaction zone.

[0009] In the above scheme, the dispersing device includes a main pipe, a branch pipe, a sub-branch pipe, and a dispersing nozzle. The main pipe and the branch pipe are arranged horizontally. The main pipe is connected to the discharge end of the pressurized mixing pipe. The branch pipe is arranged vertically or parallel to the main pipe and is connected to the main pipe. The sub-branch pipe is arranged vertically above the branch pipe and is connected to the branch pipe. The dispersing nozzle is fixedly installed above the sub-branch pipe.

[0010] In the above scheme, the dispersing nozzle includes a limiting nut, a fixing nut, and a conical dispersing disc arranged sequentially from bottom to top. The lower end of the limiting nut is fixedly connected to the branch pipe, and the upper end of the limiting nut is fixedly connected to the lower end of the fixing nut. The inner cavities of the limiting nut and the fixing nut are equipped with a compression elastic element and a sealing ball. The lower end of the inner cavity of the limiting nut is designed with a limiting step. The sealing ball is pre-tightened downward by the compression elastic element and pre-pressed at the limiting step to form a seal and prevent the upper sludge slurry from flowing back. The conical dispersing disc is fixed above the fixing nut and has a gap with the outlet of the fixing nut.

[0011] In the above scheme, the upper outlet of the fixing nut is designed as a flared structure, and the inner wall of the flared structure is provided with several vertical slurry discharge holes along the circumference, which are connected to the inner cavity to increase the cross-sectional area of ​​the channel.

[0012] In the above scheme, the multiphase feed mixing zone, the primary catalytic oxidation reaction zone, the secondary catalytic oxidation reaction zone, and the discharge zone are all equipped with inspection ports.

[0013] In the above scheme, the upper and lower parts of the primary catalytic oxidation reaction zone and the secondary catalytic oxidation reaction zone are respectively equipped with tower support structures. The tower support structures include a fine grid, a coarse grid, a baffle plate layer and a fixed support layer arranged from near to far.

[0014] The beneficial effects of this invention are: 1. The sludge ozone cell-wall breaking and high-efficiency turbulent mixing reaction device of the present invention includes a multiphase micro-nano bubble mixing feed device and a mixing reaction tank. The mixing reaction tank is designed with a multiphase synchronous feeding and mixing method, allowing the mixed materials to pass through a multiphase feeding mixing zone, a primary catalytic oxidation reaction zone, a turbulent mixing zone, a secondary catalytic oxidation reaction zone, and a discharge zone, respectively. This increases the reaction time and allows for the staged achievement of thorough mixing and contact between high-concentration dissolved ozone and sludge, resulting in efficient catalytic oxidation and cell-wall breaking. During the accelerated homogenization process in the turbulent mixing zone, some sludge enters the multiphase micro-nano bubble mixing feed device as a liquid phase source, which is beneficial for the upward circulation of bottom materials and simultaneously increases the ozone dissolution rate. The multiphase mixing feed device forms microbubble ozone in a high-pressure jet structure, integrating ozone into the sludge solution in the form of micro-nano bubbles. This increases the ozone dissolution concentration in the mixed materials. Simultaneously, the high-flow-rate feeding method increases the mixing turbulence of the multiphase materials, achieving thorough mixing of ozone and sludge, providing a favorable environment for the subsequent catalytic oxidation and cell-wall breaking stage. This invention effectively solves key technical problems such as uneven mixing, limited mass transfer, and low catalytic efficiency in traditional reaction tanks, significantly improving sludge cell wall breakage rate and organic matter dissolution rate. It has advantages such as high treatment efficiency, stable operation, and energy saving and consumption reduction, providing an innovative technical path for sludge resource utilization treatment, and has good application prospects and promotion value.

[0015] 2. The multiphase micro / nano bubble mixed-flow feeding device: After being pressurized and accelerated by a high-pressure feed pump, the slurry enters the ejector, achieving an innovative jet-driven and gas-liquid mixing mechanism. A conical structure is designed in the pressurization zone within the ejector cavity to compress the high-velocity slurry, forming a high-pressure jet. This jet enters the high-pressure jet zone while simultaneously creating a localized negative pressure zone within the cavity, efficiently providing an ozone intake channel. The ozone feed maintains a certain pressure to ensure a sufficient supply of ozone gas. In the mixed-flow diffusion zone within the ejector cavity, the sudden increase in the tank diameter causes intense turbulence in the high-jet slurry, promoting rapid mixing of ozone gas with the high-jet sludge and generating micro / nano bubble ozone, further increasing the dissolved ozone concentration in the mixture. This device has no mechanical rotating structure, resulting in a low failure rate and reducing the need for a dedicated nanobubble generator. Furthermore, employing a pure fluid dynamics design without mechanical moving parts, it utilizes high flow rates for self-cleaning, fundamentally avoiding the risk of clogging in high-suspended-solids systems, ensuring stable and reliable operation.

[0016] 3. The multiphase micro-nano bubble mixing and feeding device integrates simplification and energy saving, eliminating the need for a dedicated nano bubble generator. Through the efficient integration of pipelines and ejectors, it achieves gas-liquid mixing, microbubble generation, and high-pressure injection in one integrated system. It has a simple structure, low failure rate, and low maintenance cost, making it highly valuable for engineering applications and large-scale promotion.

[0017] 4. The dispersion nozzle is designed with a threaded connection to the branch pipe for easy maintenance. A conical dispersion disc at the top increases the material distribution area, while a certain gap (2-3mm) at the outlet ensures smooth discharge of sludge. This invention incorporates a unidirectional anti-backflow structure in the dispersion nozzle design to prevent sludge backflow. To ensure smooth passage of the mixed slurry through the fixing nut into the tank, multiple discharge holes are added to the fixing nut, increasing the channel cross-sectional area. Simultaneously, the upper outlet is designed with a funnel-shaped structure, instantly increasing the flow area when the high-pressure jet slurry is discharged, allowing for rapid dispersion. Combined with the conical dispersion disc, this creates a large material dispersion area, enabling efficient diffusion of ozone-containing materials into the sludge, increasing the contact area between ozone and sludge, and improving ozone catalytic oxidation efficiency.

[0018] 5. The turbulent mixing zone design effectively reduces the risk of uneven and incomplete single-stage catalytic oxidation reactions, which could lead to unreacted ozone being released from the tank and wasting costs. Regular backwashing effectively removes risks such as catalyst clogging and passivation, thus improving the overall efficiency of ozone catalytic oxidation.

[0019] 6. The internal support structure effectively ensures good flowability while confining and blocking heterogeneous catalytic particles, and increases turbulence in the slurry during its ascent. On the one hand, the turbulence-dispersing plates help the sludge-ozone mixture pass evenly through the coarse and fine grids, allowing it to smoothly enter the next zone. On the other hand, the grid's interception confines the catalyst material within the primary and secondary catalytic oxidation reaction zones, ensuring effective reaction space for the catalytic material. Attached Figure Description

[0020] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0021] Figure 1 This is a schematic diagram of the overall structure of the sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device of the present invention; Figure 2 yes Figure 1 A schematic diagram of the homogenizing reaction vessel of the apparatus shown; Figure 3 yes Figure 1 A schematic diagram of the multiphase micro / nano bubble mixing feed device shown. Figure 4 yes Figure 3 A schematic diagram of the overall structure of the jet injector in the multiphase micro / nano bubble mixing feed device shown. Figure 5 yes Figure 3 A schematic diagram of the overall structure of the slurry inlet filtration device of the multiphase micro-nano bubble mixing feed device shown. Figure 6 yes Figure 5 A partial structural cross-sectional view of the slurry inlet filtration device shown. Figure 7 yes Figure 1 The diagram shows the structure of the dispersion device, where (a) is a top view and (b) is a front view; Figure 8 yes Figure 7 A schematic diagram of the dispersion nozzle of the dispersion device shown; Figure 9 yes Figure 8 A schematic diagram of the structure of the fixing nut for the dispersion nozzle shown; Figure 10 yes Figure 1 A schematic diagram of the tower support structure of the device shown. Figure 11 yes Figure 10 A schematic diagram of the fixed support layer of the tower's internal support structure; Figure 12 yes Figure 10 The diagram shows the structure of the baffle plate layer in the tower's internal support structure.

[0022] In the diagram: 200, Multiphase micro / nano bubble mixing and feeding device; 201, Slurry inlet pipe; 202, High-pressure feed pump; 203, Ejector; 2031, Pressurization zone; 2032, High-pressure jet zone; 2033, Negative pressure zone; 2034, Mixed flow diffusion zone; 2035, Ozone inlet; 2036, Conical feed connector; 2037, Pressurized mixing pipe; 204, Slurry inlet filtration device; 2041, Spherical filter cover; 2042, Rotary connecting pipe; 2043, Rotary bearing; 2044, Fixed connecting pipe; 2045, Bearing sealing plate; 300. Homogenizing reaction vessel; 301. Sludge inlet pipe; 302. Sludge discharge pipe; 303. Exhaust gas pipe; 304. Dispersion device; 3041. Branch pipe; 3042. Main pipe; 30421. Connecting flange pipe; 3043. Branch pipe; 3044. Dispersion nozzle; 30441. Conical dispersion disc; 30442. Fixing nut; 304421. Slurry discharge hole; 304422. Trumpet-shaped structure; 30443. Support frame; 30444. Limiting nut; 3044 5. Blocking ball; 30446. Compression elastic element; 3045. Support frame; 305. Sludge distribution device; 306. Internal support structure of the tower; 3061. Fixed support layer; 3062. Baffle plate layer; 3063. Coarse grid; 3064. Fine grid; 307. Backwashing device; 308. Multiphase feed mixing zone; 309. Primary catalytic oxidation reaction zone; 310. Baffle mixing zone; 311. Secondary catalytic oxidation reaction zone; 312. Discharge zone; 313. Inspection port; 400. Exhaust gas treatment device. Detailed Implementation

[0023] To make the objectives, technical solutions, and advantages of this invention clearer, the invention will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative and not intended to limit the invention.

[0024] It should be noted that the illustrations provided in the embodiments of the present invention are only schematic representations of the basic concept of the present invention. Therefore, the drawings only show the components related to the present invention and are not drawn according to the number, shape and size of the components in actual implementation. In actual implementation, the form, quantity and proportion of each component can be arbitrarily changed, and the layout of the components may also be more complex.

[0025] In this invention, it should also 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 this application and 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 this application. Furthermore, the terms "first" and "second" are used only for descriptive and distinguishing purposes and should not be construed as indicating or implying relative importance.

[0026] Furthermore, it should be noted that the features of the various embodiments of the present invention can be combined or integrated in whole or in part, and as those skilled in the art will understand, they can interact and operate in different ways. Each embodiment can be implemented independently of each other or in association with one another.

[0027] like Figure 1 As shown, a sludge ozone cell-wall breaking and high-efficiency turbulent flow homogenizing reaction device is used to improve ozone dissolution efficiency and enhance the homogenization effect of sludge, ozone, and catalyst. The sludge ozone cell-wall breaking and high-efficiency turbulent flow homogenizing reaction device includes a multiphase micro-nano bubble mixing feed device 200 and a homogenizing reaction tank 300.

[0028] like Figure 2 As shown, the homogenizing reaction tank 300 is arranged from bottom to top as follows: a dispersing device 304, a sludge spreading device 305, a primary catalytic oxidation reaction zone 309, and a secondary catalytic oxidation reaction zone 311. The sludge spreading device 305 is connected to the sludge inlet pipe 301 of the homogenizing reaction tank 300. A multiphase feed mixing zone 308 is formed between the bottom of the homogenizing reaction tank 300 and the primary catalytic oxidation reaction zone 309. The dispersing device 304 and the sludge spreading device 305 are arranged in the multiphase feed mixing zone 308. A turbulent mixing zone 310 is formed between the primary catalytic oxidation reaction zone 309 and the secondary catalytic oxidation reaction zone 311. A discharge zone 312 is formed above the secondary catalytic oxidation reaction zone 311. The discharge zone 312 is provided with a sludge discharge pipe 302 and a waste gas pipe 303. High-fluidity sludge is thoroughly mixed with ozone in the multiphase feed mixing zone 308, undergoes catalytic oxidation in the primary catalytic oxidation reaction zone 309, is accelerated for homogenization in the turbulent mixing zone 310, and then enters the secondary catalytic oxidation reaction zone 311 for deep cell disruption. Finally, it is discharged to the overflow zone 312. This structure increases the reaction time, enabling high-concentration dissolved ozone to be fully mixed and contacted with the sludge in stages, achieving efficient catalytic oxidation and cell disruption. During the accelerated homogenization process in the turbulent mixing zone 310, some sludge enters the multiphase micro / nano bubble mixing feed device 200 as a liquid source, which facilitates the upward circulation of bottom materials and simultaneously increases the ozone dissolution rate.

[0029] like Figure 3-4As shown, the multiphase micro-nano bubble mixed feeding device 200 includes a slurry inlet pipe 201, a high-pressure feed pump 202, and an ejector 203. High-fluidity sludge with a moisture content of about 98% enters the device through the slurry inlet pipe 201. The slurry outlet of the slurry inlet pipe 201 is connected to the feed port of the high-pressure feed pump 202 through a flange pipe, and the discharge port of the high-pressure feed pump 202 is connected to the ejector 203. The jet injector 203 includes an ozone inlet 2035, a conical feed connector 2036, and a pressurized mixing pipe 2037. The feed end of the conical feed connector 2036 is connected to the discharge port of the high-pressure feed pump 202. The discharge end of the conical feed connector 2036 extends into the feed end of the pressurized mixing pipe 2037 and is connected to it. An ozone inlet 2035 is opened on the side wall of the feed end of the pressurized mixing pipe 2037. The discharge end of the pressurized mixing pipe 2037 is connected to the dispersion device 304. The discharge end of the conical feed connector 2036 has a tapered conical structure to form a pressurization zone 2031; a gap is left between the outer wall of the discharge end of the conical feed connector 2036 and the inner wall of the feed end of the pressurized mixing pipe 2037 as an ozone intake channel and to form a negative pressure zone 2033; the pressurized mixing pipe 2037 includes a tapering section and a diffusion section along the fluid flow direction, the tapering section forms a high-pressure jet zone 2032, and the diffusion section forms a mixed flow diffusion zone 2034. High-fluidity sludge is accelerated and pressurized by a high-pressure feed pump 202 and enters the ejector 203. In the pressurization zone 2031 within the ejector 203 chamber, the high-velocity sludge is compressed to form a high-pressure jet, which enters the high-pressure jet zone 2032. Simultaneously, a localized negative pressure is created in the negative pressure zone 2033 within the chamber. The negative pressure zone 2033 is connected to the ozone inlet 2035, which supplies an ozone source. Ozone gas rapidly mixes with the high-jet sludge, generating micro-nano bubble ozone, further increasing the dissolved ozone concentration in the mixture. In the mixed-flow diffusion zone 2034 within the ejector 203 chamber, the tank diameter suddenly increases, causing violent turbulence in the high-jet sludge. This promotes rapid mixing of ozone gas with the high-jet sludge, generating micro-nano bubble ozone, further increasing the dissolved ozone concentration in the mixture. Finally, the ozone mixed-phase flow is discharged as a high-pressure jet through the outlet end of the pressurized mixing pipe 2037. The device has no mechanical rotating structure, has a low failure rate, and reduces the need for a dedicated nanobubble generator.

[0030] Combination Figure 1 Activated sludge is uniformly injected into the multiphase feed mixing zone 308 through the sludge inlet pipe 301 and the sludge distribution device 305 at the bottom of the tank, quickly filling the multiphase feed mixing zone 308. Simultaneously, high-flow-rate sludge from the homogenizing reactor 300 and ozone form an ozone mixed flow in the ejector 203 and are injected into the mixing reactor via the dispersion device 304 in a high-pressure jet manner, ensuring thorough mixing and contact with the sludge in the multiphase feed mixing zone 308. This high-flow-rate feeding method increases the mixing disturbance of the multiphase flow materials, achieving thorough mixing of ozone and sludge, and providing a favorable environment for the subsequent catalytic oxidation and cell disruption stage.

[0031] A high-concentration ozone generator (not shown) produces high-concentration ozone (200-250 mg / L) to provide the ozone source for the entire system. A multiphase micro / nano bubble mixing feed device 200 integrates ozone into the sludge solution in the form of micro / nano bubbles, which are then introduced into the homogenizing reaction tank 300 via a high-pressure jet. The multiphase micro / nano bubble mixing feed device 200 is connected to the ozone source and the homogenizing reaction tank 300. Utilizing the high-pressure jet homogenizing principle, high-concentration ozone is first introduced into the highly fluid sludge with a water content of approximately 98%. Under the high-speed multiphase flow environment within the chamber, the ozone and sludge are thoroughly mixed, breaking the ozone bubbles into micro / nano-sized bubbles and increasing the dissolved ozone concentration in the sludge. In the homogenization reaction tank 300, ozone is further mixed and contacted with the sludge inside the tank. After passing through two catalytic oxidation reaction zones, it comes into full contact with the matching multiphase composite catalytic materials. This allows ozone molecules to rapidly catalyze the reaction to generate strong oxides such as hydroxyl radicals (·OH), creating a strong oxidizing environment. Under the combined action of ozone and strong oxides such as hydroxyl radicals (·OH), a super catalytic oxidation reaction is generated, which deeply destroys and decomposes flocculent substances such as sludge cell walls and extracellular polymers, thereby releasing intracellular water and adsorbed water and improving dewatering performance.

[0032] Further optimization, such as Figure 5 As shown, the multiphase micro / nano bubble mixed-flow feeding device 200 also includes a slurry inlet filter device 204. The slurry inlet end of the slurry inlet pipe 201 is connected to the slurry inlet filter device 204 through a flange pipe. The high-fluidity sludge is first uniformly fed through the slurry inlet filter device 204, and then transported to the slurry inlet pipe 201 to enter the device. Figure 6 As shown, the slurry inlet filtration device 204 includes a spherical filter cover 2041, a rotating connecting pipe 2042, a rotating bearing 2043, a fixed connecting pipe 2044, and a bearing sealing plate 2045. The spherical filter cover 2041 is fixed to one end of the rotating connecting pipe 2042, and the rotating connecting pipe 2042 is connected to the fixed connecting pipe 2044 through the rotating bearing 2043. The spherical filter cover 2041 can rotate freely, and the fixed connecting pipe 2044 is fixedly connected to the inlet end of the slurry inlet pipe 201. The spherical filter cover 2041 is a spherical structure formed by rotating and arranging multiple curved bending plates. Adjacent curved bending plates maintain a certain angle and gap, serving as a sludge slurry channel. The bearing sealing plate 2045 is fixed to the rotating connecting pipe 2042 by screw connection, forming a seal for the rotating bearing 2043.

[0033] During the material extraction process by the high-pressure feed pump 202, the material in the slurry inlet pipe 201 forms a high-speed suction flow, continuously drawing in sludge, which enters through the gaps in the spherical filter cover 2041. As the sludge enters, a certain fluid dynamic is created, causing the spherical filter cover 2041 to rotate without power. This process effectively removes and filters out large particles and flocculent matter, while the uniform, highly fluid, fine-particle sludge passes through the gaps in the spherical filter cover 2041, effectively ensuring the homogeneity of the jet liquid phase source and preventing blockage of the feed pipe. This design effectively solves the problem of conventional filter screen clogging.

[0034] Further optimization involves integrating the discharge end of the conical feed connector 2036 with the feed end of the pressurized mixing pipe 2037 via a threaded connection, employing a detachable connection for easy maintenance. The ozone inlet 2035 is fixedly welded to the pressurized mixing pipe 2037.

[0035] Further optimization is needed. Unlike conventional sewage venturi jet pumps, this structure requires a smaller gap in the negative pressure zone 2033, while the ozone inlet pipe needs to maintain a certain pressure to supply sufficient ozone gas. Excessive pressure, however, can damage the negative pressure zone 2033 and reduce the mixing effect. Therefore, the gap width of the negative pressure zone 2033 in this application is 3mm-5mm. By precisely controlling the gap size, a stable local negative pressure is ensured while avoiding a decrease in suction capacity due to an excessively wide gap or blockage due to an excessively narrow gap. The inlet pressure of the ozone inlet 2035 is controlled between 50kPa and 100kPa. Ozone gas is efficiently drawn in through the inlet under negative pressure and undergoes initial shear dispersion in the high-pressure jet zone 2032.

[0036] Further optimization involves controlling the feeding pressure of the high-pressure feed pump 202 between 200kPa and 500kPa to generate a high jet.

[0037] Further optimization involves the pressurized mixing pipe 2037 comprising, sequentially along the fluid flow direction, a converging section, a first cylindrical section, a diffuser section, and a second cylindrical section. The first cylindrical section extends the energy transfer distance of the high-pressure jet zone 2032, forming a stable high-pressure jet and preventing turbulence caused by sudden diffusion of the inner diameter from disrupting the stability of the flow field in the high-pressure jet zone 2032. The second cylindrical section stabilizes the flow field of the mixture generated in the mixing and diffusion zone 2034, forming a stable high-pressure jet material that is smoothly discharged through the outlet end.

[0038] Further optimization involves filling both the primary catalytic oxidation reaction zone 309 and the secondary catalytic oxidation reaction zone 311 with multiphase composite catalytic materials, primarily manganese + iron + carbon (Mn-Fe-C) micro-electrolysis composite catalytic materials. This creates an iron-carbon micro-electrolysis environment, spontaneously forming countless tiny "micro-batteries" without an external power source, thereby generating highly oxidizing substances to degrade pollutants. During the iron-carbon micro-electrolysis process, the iron anode continuously releases Fe²⁺. + Fe² + It can catalyze the decomposition of ozone (O3) to generate highly oxidizing and non-selective hydroxyl radicals (·OH). Simultaneously, the manganese + iron + carbon (Mn-Fe-C) micro-electrolysis composite catalytic material uses carbon materials as a carrier to adsorb and enrich pollutants and ozone. Manganese and iron form a synergistic catalytic system on the surface, promoting electron transfer through multi-valence state conversion, efficiently activating ozone to generate hydroxyl radicals and non-radical active species. This achieves heterogeneous catalytic oxidation with wide pH adaptability, avoiding the dependence of traditional processes on acidic and alkaline environments while significantly improving the degradation efficiency and stability of organic matter.

[0039] Further optimization, such as Figure 1 As shown, the main function of the turbulent mixing zone 310 is to address the uneven sludge flow caused by the random distribution of the catalytic material when sludge passes through the primary catalytic oxidation reaction zone 309, which reduces the effective catalytic contact area. The turbulent mixing zone 310, located between the primary and secondary catalytic oxidation reaction zones 309 and 311, collects the sludge in this area and redisperses it evenly before it enters the secondary catalytic oxidation reaction zone 311, thus improving the efficiency of the catalytic zone. A backwashing device 307 is installed in the turbulent mixing zone 310, connected to an external high-pressure water or high-pressure air system, to remove impurities adhering to the surface of the catalytic materials in the primary and secondary catalytic oxidation reaction zones 309 and 311. Regular aeration cleaning with high-pressure water or high-pressure air removes impurities from the surface of the catalytic materials, preventing sludge blockage and subsequent degradation of catalytic material performance. This design can effectively reduce the risk of ozone being discharged from the tank unreacted due to uneven and incomplete single-stage catalytic oxidation reaction, resulting in cost waste. Regular backwashing can effectively remove risks such as catalyst blockage and passivation, thereby improving the overall efficiency of ozone catalytic oxidation.

[0040] Further optimization, such as Figure 7As shown, the dispersion device 304 includes a main pipe 3042, a branch pipe 3043, a sub-branch pipe 3041, and a dispersion nozzle 3044. The main pipe 3042 and branch pipe 3043 are horizontally arranged, covering the cross-section of the tank, and are fixed to the support frame 3045 at the bottom of the reaction tank by U-shaped hinges to ensure stability and firmness during the feeding process. The main pipe 3042 is connected to the outlet end of the pressurized mixing pipe 2037 via a connecting flange pipe 30421. The branch pipe 3043 is arranged vertically or parallel to the main pipe 3042 and is connected to it. The sub-branch pipe 3041 is vertically arranged above the sub-branch pipe 3043 and is connected to it. The dispersion nozzle 3044 is fixedly installed above the sub-branch pipe 3041. The mixture in the main pipe 3042 is distributed to the branch pipe 3043 and sprayed out from the dispersion nozzle 3044.

[0041] Further optimization, such as Figure 8As shown, the dispersion nozzle 3044 includes a limiting nut 30444, a fixing nut 30442, and a conical dispersion disc 30441 arranged sequentially from bottom to top. The lower end of the limiting nut 30444 is threadedly connected to the branch pipe 3041, and the upper end of the limiting nut 30444 is threadedly connected to the lower end of the fixing nut 30442. A compression elastic element 30446 and a sealing ball 30445 are installed inside the cavities of the limiting nut 30444 and the fixing nut 30442. A limiting step is designed at the lower end of the inner cavity of the limiting nut 30444. The sealing ball 30445 is pre-tightened downwards at the limiting step by the compression elastic element 30446, forming a seal to prevent backflow of the upper sludge slurry. The conical dispersion disc 30441 is fixed above the fixing nut 30442 by a support 30443, which can increase the material distribution area. It should be kept 2-3 cm away from the outlet of the fixing nut 30442. A mm gap ensures smooth spraying of sludge material. Since the dispersing nozzle 3044 is located at the bottom of the tank, the tank is filled with sludge during normal operation, resulting in high pressure at the bottom. To prevent sludge backflow during feeding stops, this invention incorporates a unidirectional anti-backflow structure in the dispersing nozzle 30444 to prevent sludge backflow. The fixing nut 30442 and the limiting nut 30444 are connected by threads to form a single unit, confining the sealing ball 30445 and the compression elastic element 30446 within a limited space and creating a certain pre-tightening force. A limiting step is designed at the lower end of the inner cavity of the limiting nut 30444. The sealing ball 30445, under the pre-tightening force provided by the compression elastic element 30446, pre-presses downwards against the limiting step at the lower end of the inner cavity of the limiting nut 30444, forming a seal and preventing backflow of the upper sludge slurry. During normal feeding, the mixture is conveyed under high pressure from bottom to top through branch pipe 3041 to limit nut 30444, which lifts the sealing ball 30445. The material continues to be conveyed upwards and is ejected under high pressure from the upper outlet of fixed nut 30442. When feeding stops, the sealing ball 30445 is quickly reset by the pre-tightening force provided by the compressed elastic element 30446, sealing the channel and preventing slurry backflow. The sealing ball 30445 can be made of steel ball, and the compressed elastic element 30446 can be made of compression spring.

[0042] Further optimization, such as Figure 9 As shown, the upper outlet of the fixing nut 30442 is designed as a funnel-shaped structure 304422. When the high-pressure jet slurry is discharged, it instantly increases the flow area, allowing it to be rapidly sprayed out. Combined with the conical dispersion disc 30441, this forms a larger material dispersion area, enabling efficient diffusion of ozone-containing materials into the sludge, increasing the contact area between ozone and sludge, and improving ozone catalytic oxidation efficiency. To ensure that the mixed slurry can smoothly pass through the fixing nut 30442 into the tank, this invention adds multiple slurry discharge holes 304421 to the fixing nut 30442, increasing the channel cross-sectional area.

[0043] Further optimization has been achieved by making the sludge feeding device 305 have the same structure as the dispersion device 304, which can quickly realize the feeding of activated sludge.

[0044] Further optimizations include the installation of inspection ports 313 in the multiphase feed mixing zone 308, the primary catalytic oxidation reaction zone 309, the secondary catalytic oxidation reaction zone 311, and the discharge zone 312, facilitating inspection and maintenance.

[0045] Further optimization, such as Figure 1-2 As shown, in order to divide the tank into zones, it is necessary to ensure good flowability while restricting and blocking heterogeneous catalytic particle materials and increasing turbulence of the slurry during the upward process. Therefore, tower support structures 306 need to be installed in the upper and lower parts of the primary catalytic oxidation reaction zone 309 and the secondary catalytic oxidation reaction zone 311, respectively.

[0046] For further optimization, please refer to [link / reference]. Figure 10 The internal support structure 306 includes a fine grid 3064, a coarse grid 3063, a baffle plate layer 3062, and a fixed support layer 3061 arranged sequentially from near to far (relative to the catalytic oxidation reaction zone). The coarse grid 3063 has a porous structure with a pore size ranging from 5mm to 10mm; the fine grid 3064 has a fine pore structure with a pore size ranging from 3mm to 5mm. On the one hand, the baffle plate layer 3062 can evenly disperse the sludge-ozone mixture through the coarse grid 3063 and the fine grid 3064, allowing it to smoothly enter the next zone (such as the primary catalytic oxidation reaction zone 309). On the other hand, due to the interception of the grid, the catalyst material is placed within the primary catalytic oxidation reaction zone 309 and the secondary catalytic oxidation reaction zone 311, ensuring effective reaction space for the catalyst material.

[0047] For further optimization, please refer to [link / reference]. Figure 11 The fixed support layer 3061 is designed as a double-ten support frame. The members of the double-ten support frame can be designed as a prefabricated and detachable structure, which is beneficial for the maintenance and repair of the internal structure of the tank. The components can be connected by bolts. The fixed support layer 3061 is fixed to the inner wall of the tank and is fixedly connected to the baffle layer 3062.

[0048] For further optimization, please refer to [link / reference]. Figure 12 The 3062 baffle plate layer is designed as a corrugated bent baffle structure, consisting of several spaced corrugated bent plates and reinforcing ribs (i.e., six plates arranged along the chord length in the figure) welded together as a single structure. Its main function is to disturb and uniformly guide the passing sludge to the next area. To increase component strength and minimize weld seams to avoid overall structural deformation, the reinforcing ribs are designed with inlay grooves, allowing the corrugated bent plates to be directly inlaid and fixed. Only electric welding is required at the upper joint, effectively reducing weld seams, preventing overall structural deformation, and increasing component strength.

[0049] Further optimization includes a tail gas treatment device 400 for the sludge ozone cell disruption high-efficiency turbulent mixing reaction device. The residual waste gas in the tank is discharged from the top of the tank and collected in the tail gas treatment device 400 to achieve residual ozone destruction and detoxification treatment.

[0050] It should be noted that, depending on the implementation needs, the various steps / components described in this application can be broken down into more steps / components, or two or more steps / components or parts of the operation of steps / components can be combined into new steps / components to achieve the purpose of this invention.

[0051] The order of the steps in the above embodiments does not imply the order of execution. The execution order of each process should be determined by its function and internal logic, and should not constitute any limitation on the implementation process of the embodiments of this application.

[0052] It should be understood that those skilled in the art can make improvements or modifications based on the above description, and all such improvements and modifications should fall within the protection scope of the appended claims.

Claims

1. A high-efficiency turbulent flow homogenization reaction device for sludge ozone cell disruption, characterized in that, This includes a multiphase micro / nano bubble mixing feeder and a homogenizing reaction vessel; The homogenizing reaction tank is arranged from bottom to top as follows: a dispersion device, a sludge feeding device, a primary catalytic oxidation reaction zone, and a secondary catalytic oxidation reaction zone. The sludge feeding device is connected to the sludge inlet pipe of the homogenizing reaction tank. A multiphase feeding mixing zone is formed between the bottom of the homogenizing reaction tank and the primary catalytic oxidation reaction zone. A turbulent mixing zone is formed between the primary catalytic oxidation reaction zone and the secondary catalytic oxidation reaction zone. A discharge zone is formed above the secondary catalytic oxidation reaction zone. The discharge zone is equipped with a sludge discharge pipe and an exhaust gas pipe. The multiphase micro / nano bubble mixed-flow feeding device includes a slurry inlet pipe, a high-pressure feed pump, and an ejector. The inlet end of the slurry inlet pipe is connected to the turbulent mixing zone, and the outlet end is connected to the inlet of the high-pressure feed pump. The ejector includes an ozone inlet, a conical feed connector, and a pressurized mixing pipe. The inlet end of the conical feed connector is connected to the outlet of the high-pressure feed pump, and the outlet end of the conical feed connector extends into and is connected to the inlet end of the pressurized mixing pipe. The ozone inlet is opened on the side wall of the inlet end of the pressurized mixing pipe, and the outlet end of the pressurized mixing pipe is connected to the dispersion device. The highly fluid sludge from the homogenizing reaction tank and ozone form an ozone mixed flow in the ejector and are injected into the homogenizing reaction tank through the dispersion device in a high-pressure jet manner.

2. The sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device according to claim 1, characterized in that, The discharge end of the conical feed connector has a tapered cone structure to form a pressurization zone; a gap is left between the outer wall of the discharge end of the conical feed connector and the inner wall of the feed end of the pressurized mixing pipe as an ozone intake channel and to form a negative pressure zone; the pressurized mixing pipe includes a tapering section and a diffusion section along the fluid flow direction, the tapering section forming a high-pressure jet zone, and the diffusion section forming a mixed-flow diffusion zone.

3. The sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device according to claim 1, characterized in that, The multiphase micro / nano bubble mixing feed device also includes a slurry inlet filtration device. The slurry inlet end of the slurry inlet pipe is connected to the slurry inlet filtration device. The slurry inlet filtration device includes a spherical filter cover, a rotating connecting pipe, a rotating bearing, and a fixed connecting pipe. The spherical filter cover is fixed to one end of the rotating connecting pipe. The rotating connecting pipe is connected to the fixed connecting pipe through the rotating bearing. The fixed connecting pipe is fixedly connected to the slurry inlet end of the slurry inlet pipe.

4. The sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device according to claim 1, characterized in that, Both the primary and secondary catalytic oxidation reaction zones are filled with Mn-Fe-C micro-electrolysis composite catalytic materials.

5. The sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device according to claim 1, characterized in that, The turbulent mixing zone is equipped with a backwashing device, which is connected to an external high-pressure clean water or high-pressure air device to remove impurities adhering to the surface of the catalytic materials in the primary and secondary catalytic oxidation reaction zones.

6. The sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device according to claim 1, characterized in that, The dispersing device includes a main pipe, a branch pipe, a sub-branch pipe, and a dispersing nozzle. The main pipe and the branch pipe are arranged horizontally. The main pipe is connected to the discharge end of the pressurized mixing pipe. The branch pipe is arranged vertically or parallel to the main pipe and is connected to the main pipe. The sub-branch pipe is arranged vertically above the branch pipe and is connected to the branch pipe. The dispersing nozzle is fixedly installed above the sub-branch pipe.

7. The sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device according to claim 6, characterized in that, The dispersion nozzle includes a limiting nut, a fixing nut, and a conical dispersion disc arranged sequentially from bottom to top. The lower end of the limiting nut is fixedly connected to the branch pipe, and the upper end of the limiting nut is fixedly connected to the lower end of the fixing nut. The inner cavities of the limiting nut and the fixing nut are equipped with a compression elastic element and a sealing ball. The lower end of the inner cavity of the limiting nut is designed with a limiting step. The sealing ball is pre-tightened downward by the compression elastic element and pre-presses against the limiting step to form a seal and prevent the upper sludge slurry from flowing back. The conical dispersion disc is fixed above the fixing nut and has a gap with the outlet of the fixing nut.

8. The sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device according to claim 7, characterized in that, The upper outlet of the fixing nut is designed as a flared structure. Several vertical slurry discharge holes are arranged circumferentially on the inner wall of the flared structure and communicate with the inner cavity to increase the cross-sectional area of ​​the channel.

9. The sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device according to claim 1, characterized in that, Inspection ports are provided in the multiphase feed mixing zone, the primary catalytic oxidation reaction zone, the secondary catalytic oxidation reaction zone, and the discharge zone.

10. The sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device according to claim 1, characterized in that, The upper and lower parts of the primary catalytic oxidation reaction zone and the secondary catalytic oxidation reaction zone are respectively equipped with internal support structures. The internal support structures include a fine grid, a coarse grid, a baffle plate layer and a fixed support layer arranged from near to far.

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