Heterogeneous catalysis super oxidation wall-breaking deep dehydration treatment system and method for sludge

Abstract

The invention discloses a sludge heterogeneous catalysis super oxidation wall-breaking deep dehydration treatment system which comprises an ozone generation device, a heterogeneous micro-nano bubble mixed flow feeding device, a uniform mixing reaction tank, a uniform mixing tempering system and a high-pressure dehydration system, a dispersing device, a sludge distributing device, a first-stage catalytic oxidation reaction zone and a second-stage catalytic oxidation reaction zone are arranged in 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 an ejector, and the mixing and conditioning system comprises a material mixing device and a dosing device. The high-pressure dehydration system comprises a high-pressure plate frame dehydration device, a squeezing water tank and a sewage treatment device. The high-flow-state sludge and ozone form ozone mixed-phase flow in the jet device, and the ozone mixed-phase flow is jetted into the uniform mixing reaction tank; ozone and sludge are mixed to generate super catalytic oxidation reaction, and sludge cell walls and EPS are deeply destroyed and decomposed; and tempering and thickening the wall-broken slurry by a uniform mixing and tempering system, and carrying out mud-water separation by a high-pressure plate frame dehydration device to obtain high-concentration organic wastewater and low-content cement cakes.

Description

Technical Field

[0001] This invention relates to the field of activated sludge treatment technology, and in particular to a sludge multiphase catalytic super oxidation cell wall disruption deep dewatering treatment system and method. Background Technology

[0002] In the current field of activated sludge treatment in wastewater treatment plants, poor dewatering performance is one of the key bottlenecks restricting the efficient disposal of sludge. Existing technologies commonly employ mechanical dewatering methods such as plate and frame filter presses and centrifugation to improve sludge dewatering efficiency. However, due to the dense structure of numerous microbial cells and extracellular polymeric substances (EPS) in the sludge, which encapsulate a large amount of water, conventional mechanical conditioning is insufficient to effectively disrupt the cell structure, making it difficult to release water. To address this issue, Fenton and ozone oxidation technologies have been introduced in recent years for the sludge pretreatment stage. The principle is to utilize the strong oxidizing properties of ozone to disrupt the cell walls and EPS structure, releasing intracellular and adsorbed water, thereby improving dewatering performance. Currently, some sludge conditioning equipment based on ozone treatment has appeared on the market. This typically uses an ozone generator in conjunction with a reaction tank, introducing ozone into the sludge through aeration for oxidation. While such equipment is simple in process, it generally suffers from low ozone mass transfer efficiency, long reaction time, high energy consumption, and insufficient ozone utilization. Specifically, uneven ozone supply leads to localized ozone accumulation or short-circuiting 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 stability of the overall treatment effect. Low dissolved ozone concentration and efficiency result in a large amount of ozone escaping without participating in the reaction, wasting gas resources and potentially burdening exhaust gas treatment and posing safety hazards. Catalysts are prone to passivation and failure, hindering the full utilization of ozone's oxidizing capacity. The lack of effective mixing and agitation mechanisms within the reactor causes sludge to settle or aggregate, making it difficult for ozone to penetrate the sludge flocs, resulting in low overall cell disruption efficiency and unsatisfactory dewatering improvement. Furthermore, traditional devices often fail to optimize reactor structure for sludge characteristics, leading to uneven ozone distribution, insufficient localized oxidation, and limited overall cell disruption, making it difficult to achieve efficient and energy-saving dewatering improvements. These shortcomings severely limit the widespread application of ozone technology in deep sludge dewatering.

[0003] Therefore, there is an urgent need to develop a new ozone oxidation sludge treatment system that can efficiently transfer mass, enhance the cell wall breaking effect of ozone, and improve dewatering performance.

[0004] This invention addresses key technical problems in existing sludge treatment technologies and devices, such as poor cell wall breaking and dewatering performance, low mass transfer efficiency, uneven ozone supply, low dissolved concentration, slow catalytic reaction, and uneven sludge reaction. By innovatively designing the reactor structure and process parameters, and combining them with multiphase catalytic materials, the invention significantly enhances the destructive effect of ozone on sludge cell walls and EPS, thereby achieving a significant improvement in sludge dewatering performance. Summary of the Invention

[0005] The technical problem to be solved by this invention is to address the problems of poor sludge cell wall breaking and dewatering, low ozone mass transfer efficiency, uneven ozone supply, low dissolved concentration, slow catalytic reaction, and uneven sludge reaction in the existing technologies. This invention proposes a multiphase catalytic super oxidation cell wall breaking and deep dewatering treatment system for sludge. By optimizing the design of the high-efficiency reactor structure and combining it with multiphase catalytic materials, the system significantly enhances the destructive effect of ozone on sludge cell walls and EPS, achieving a significant improvement in sludge dewatering performance. Furthermore, it is equipped with integrated conditioning and dewatering technology equipment to achieve deep dewatering and volume reduction of sludge.

[0006] The technical solution adopted in this invention is: A sludge multiphase catalytic super oxidation cell wall breaking deep dewatering treatment system includes an ozone generator, a multiphase micro-nano bubble mixing feed device, a homogenizing reaction tank, a homogenizing conditioning system, and a high-pressure dewatering system. The homogenizing reaction tank is equipped with a dispersion device, a sludge feeding device, a primary catalytic oxidation reaction zone, and a secondary catalytic oxidation reaction zone, arranged sequentially from bottom to top. 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, the outlet end extends into the inlet end of the pressurized mixing pipe and is interconnected, the ozone inlet is opened on the side wall of the inlet end of the pressurized mixing pipe, and the outlet end is connected to the dispersion device; the ozone inlet is connected to the ozone generator; the highly fluid sludge from the homogenized reaction tank and ozone form an ozone mixed flow in the ejector and are injected into the homogenized reaction tank through the dispersion device in a high-pressure jet manner; The homogenization and conditioning system includes a mixing device and a dosing device; the mixing device includes a mixing silo, an overflow silo, a bipolar settling inclined plate device, a double-spiral mixing device, and a sludge discharge device. The overflow silo is installed at the top of the mixing silo, the bipolar settling inclined plate device is installed in the upper middle part of the mixing silo, the double-spiral mixing device is installed at the inlet of the mixing silo and connected to the sludge discharge pipeline of the homogenization reaction tank, and the sludge discharge device is installed at the bottom of the mixing silo; the dosing device is connected to the double-spiral mixing device. The high-pressure dewatering system includes a high-pressure plate and frame dewatering device, a pressing water tank, and a wastewater treatment device. The feed pipe of the high-pressure plate and frame dewatering device is connected to the sludge discharge device of the mixing device. The pressing water tank is connected to the high-pressure plate and frame dewatering device to pressurize water into the diaphragm plate pressing chamber. The drain pipe of the high-pressure plate and frame dewatering device is connected to the wastewater treatment device. The overflow chamber is connected to the wastewater treatment device through an overflow pipe.

[0007] Further optimization involves the following: 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 to serve as an ozone intake channel and 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.

[0008] Further optimization involves filling both the primary and secondary catalytic oxidation reaction zones with Mn-Fe-C micro-electrolysis composite catalytic materials.

[0009] Further optimization involves providing a backwashing device in the turbulent mixing zone. This backwashing device 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.

[0010] Further optimization includes a main pipe, branch pipes, sub-branch pipes, and a dispersing nozzle. The main pipe and branch pipes are horizontally arranged. The main pipe is connected to the discharge end of the pressurized mixing pipe. The branch pipes are arranged vertically or parallel to the main pipe and are connected to it. The sub-branch pipes are vertically arranged above the branch pipes and are connected to them. The dispersing nozzle is fixedly installed above the sub-branch pipes. 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 sub-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] Further optimization involves installing internal support structures in the upper and lower parts of the primary and secondary catalytic oxidation reaction zones, respectively. The internal support structures include a fine grid, a coarse grid, a baffle plate layer, and a fixed support layer arranged sequentially from near to far.

[0012] Further optimization involves the following: the double-helix mixing device includes a cylindrical body and a helical shaft rotatably disposed at the center of the cylindrical body. The upper and lower sections of the helical shaft are designed as right-handed helical sections and the middle section as left-handed helical sections, or the upper and lower sections are designed as left-handed helical sections and the middle section as right-handed helical sections, thereby forming a double-helix structure.

[0013] In a further optimization, the mixing device also includes a conical dispersing structure fixedly installed at the bottom of the double-helix mixing device, the diameter of which gradually increases from top to bottom.

[0014] Further optimization involves the following: the opposite bipolar settling inclined plate device includes two layers of settling inclined plates spaced apart at the top and bottom, with the inclination directions of the two layers of settling inclined plates being opposite to each other; both layers of settling inclined plates are located above the outlet of the double helix mixing device.

[0015] Accordingly, this invention also proposes a method for deep dewatering of sludge through multiphase catalytic super oxidation, employing the aforementioned system. The method includes the following steps: A high concentration of oxygen (200-250 mg / L) is generated by an ozone generator and introduced into a multiphase micro-nano bubble mixing feed device through an ozone inlet. Simultaneously, a high-fluidity sludge is pumped from the turbulent mixing zone of a homogenizing reaction tank into the multiphase micro-nano bubble mixing feed device via a high-pressure feed pump. The high-fluidity sludge and ozone form an ozone mixed flow in an ejector and are injected into the homogenizing reaction tank through a dispersion device using a high-pressure jet. In the homogenization reaction tank, ozone is further mixed and contacted with the sludge in the tank, and then passes through the primary catalytic oxidation reaction zone and the secondary catalytic oxidation reaction zone in sequence. It fully contacts the multiphase coupled catalytic material to create a strong oxidation environment and generate a super catalytic oxidation reaction, which deeply destroys and decomposes the sludge cell wall and EPS, thereby releasing intracellular water and adsorbed water. After the sludge is broken down, it is transported to a homogenization and conditioning system for conditioning and thickening, and then to a high-pressure plate and frame dewatering device for mud-water separation. Finally, high-concentration organic wastewater and low-cement cake are obtained, realizing the deep dewatering and volume reduction treatment of sludge.

[0016] The beneficial effects of this invention are: 1. The sludge multiphase catalytic super oxidation cell-wall breaking and deep dewatering treatment system of the present invention integrates an ozone generator, a multiphase micro-nano bubble mixing feed device, a homogenizing reaction tank, a tail gas treatment device, a homogenizing conditioning system, and a high-pressure plate and frame dewatering device. It can economically and efficiently achieve sludge ozone catalytic oxidation cell-wall breaking and deep dewatering and volume reduction treatment. The overall process system is tightly connected, the integrated process is highly operable, the equipment structure is reasonable, the modular design is compact, and it occupies a small area.

[0017] 2. The homogenizing reactor 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. This increases the reaction time and enables the high-concentration dissolved ozone to be fully mixed and contacted with the sludge in stages, achieving efficient catalytic oxidation and cell wall disruption. 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 materials at the bottom 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 concentration in the mixed materials, while the high-flow-rate feeding method increases the mixing disturbance of the multiphase materials, achieving thorough mixing of ozone and sludge and providing a favorable environment for the subsequent catalytic oxidation and cell wall disruption 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.

[0018] 3. 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.

[0019] 4. The multiphase micro-nano bubble mixing and feeding device is integrated and simplified, saving energy and reducing consumption. It eliminates the need for a dedicated nano bubble generator. Through the efficient integration of pipelines and jet injectors, it realizes gas-liquid mixing, microbubble generation and high-pressure injection in one integrated manner. It has a simple structure, low failure rate and low maintenance cost, and has great value for engineering application and large-scale promotion.

[0020] 5. 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.

[0021] 6. 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 eliminates the risk of catalyst clogging and passivation, thus improving the overall efficiency of ozone catalytic oxidation.

[0022] 7. 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.

[0023] 8. The homogenization and conditioning system employs a double-helix mixing device, combined with an Archimedes spiral flow guide structure. Under conditions without external power, it utilizes the turbulent tumbling of the fluid within the double-helix structure to achieve thorough and uniform mixing of sludge and modifier. Simultaneously, it possesses energy-dissipating and flow-stabilizing functions, effectively avoiding eddies and short-circuiting during the mixing process, ensuring the uniformity and efficiency of the conditioning reaction. This significantly improves the flocculation and agglomeration capacity of the fine, dispersed sludge after cell wall disruption, laying the foundation for subsequent deep dewatering. Therefore, it can achieve highly efficient homogenization and non-powered modification and conditioning of cell wall-broken sludge, significantly improving flocculation and settling performance.

[0024] 9. The homogenization and conditioning system is equipped with an anti-polar settling inclined plate device to achieve multi-stage barrier and secondary settling and thickening of fine sludge particles. Addressing the technical challenges of small, lightweight, easily floating, and difficult-to-settle particles in broken-cell sludge, the system employs an upper and lower two-stage anti-polar settling inclined plate device to form a tiered interception and energy dissipation settling mechanism: the first-stage inclined plate blocks large flocs from floating and promotes settling; small particles that have not fully settled continue to rise to the second-stage inclined plate, extending the agglomeration and growth time, achieving a dynamic thickening process of "settling, growing, and then settling again," significantly improving the sludge solid phase recovery rate, reducing the supernatant SS value, and enhancing thickening efficiency and sludge solids content.

[0025] 10. The high-pressure dewatering system adopts high-pressure diaphragm hydraulic pressing technology, breaking through the pressure bottleneck of traditional pneumatic pressing and achieving deep dewatering of sludge with ultra-low moisture content. This invention uses a hydraulically driven high-pressure diaphragm plate and frame system to apply a high-pressure pressing force of ≥2MPa, which is far higher than the pressure limit of conventional pneumatic pressing. This effectively overcomes the resistance to the removal of capillary water and bound water in sludge, achieving rapid and deep solid-liquid separation of sludge, and finally obtaining a low-moisture cake with a moisture content of less than 50%. This greatly improves the volume reduction effect and meets the high standards for sludge resource utilization and harmless treatment. Attached Figure Description

[0026] 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.

[0027] Figure 1 This is a schematic diagram of the overall structure of the sludge multiphase catalytic super oxidation cell wall breaking deep dewatering treatment system of the present invention; Figure 2 yes Figure 1 The diagram shows the connection of the multiphase micro / nano bubble mixing feeder, the homogenizing reaction tank, and the tail gas treatment device in the system shown. Figure 3 This is a schematic diagram of the homogenization reaction vessel; Figure 4 This is a schematic diagram of the structure of a multiphase micro / nano bubble mixing and feeding device; Figure 5 This is a schematic diagram of the overall structure of the jet injector in a multiphase micro / nano bubble mixing feed device; Figure 6 This is a schematic diagram of the overall structure of the slurry inlet filtration device of the multiphase micro-nano bubble mixing feed device; Figure 7 yes Figure 6 A partial structural cross-sectional view of the slurry inlet filtration device shown. Figure 8 This is a schematic diagram of the dispersion device, where (a) is a top view and (b) is a front view; Figure 9 yes Figure 8 A schematic diagram of the dispersion nozzle of the dispersion device shown; Figure 10 yes Figure 9 A schematic diagram of the structure of the fixing nut for the dispersion nozzle shown; Figure 11 This is a schematic diagram of the internal support structure of the tower; Figure 12yes Figure 11 A schematic diagram of the fixed support layer of the tower's internal support structure; Figure 13 yes Figure 11 A schematic diagram of the baffle plate layer of the tower's internal support structure. Figure 14 This is a schematic diagram showing the connection between the homogeneous mixing and conditioning system and the high-pressure plate and frame dewatering device; Figure 15 This is a schematic diagram of the mixing device in a homogeneous mixing and conditioning system; Figure 16 This is a schematic diagram of the structure of the double-helix mixing device in a homogenization and conditioning system.

[0028] In the diagram: 100, Ozone generator; 101, Air compressor; 102, Oil-gas separator; 103, Air tank; 104, Dryer; 105, Air drying device; 106, Oxygen generator; 107, Ozone generator; 108, Cooling system; 109, Air inlet pipe; 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; 500. Homogenizing and conditioning system; 501. Mixing device; 5011. Mixing silo; 5012. Overflow silo; 5013. Opposite bipolar settling inclined plate device; 5014. Double helix mixing device; 50141. Right helix section; 50142. Left helix section; 5015. Conical dispersion structure; 5016. Sludge discharge device; 502. Dosing device; 503. Dosing pump; 504. Dosing pipeline; 505. Overflow pipe; 506. Sludge supply pump; 507. Feed pipeline; 600. High-pressure plate and frame dewatering device; 601. Pressing water tank; 602. Water pump; 603. Pressing water pipe; 604. Return water pipe; 605. Drainage pipe; 606. Sewage treatment device; 607. Mud cake. Detailed Implementation

[0029] 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.

[0030] 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.

[0031] 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.

[0032] 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.

[0033] like Figure 1As shown, a preferred embodiment of the present invention provides a sludge multiphase catalytic super oxidation cell wall breaking deep dewatering treatment system, including an ozone generator 100, a multiphase micro-nano bubble mixing feed device 200, a homogenizing reaction tank 300, a tail gas treatment device 400, a homogenizing conditioning system 500, and a high-pressure plate and frame dewatering device 600.

[0034] Ozone generator 100 is used to generate high-concentration ozone (200-250 mg / L) to provide an ozone source for the entire treatment system.

[0035] The multiphase micro / nano bubble mixing feeder 200, the homogenizing reaction tank 300, and the tail gas treatment device 400 together constitute the following: Figure 2 The sludge ozone cell disruption high-efficiency turbulent flow homogenization reaction device shown is used to improve ozone dissolution efficiency and enhance the homogenization effect of sludge, ozone and catalyst.

[0036] like Figure 3 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.

[0037] like Figure 4-5As 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.

[0038] Combination Figure 2 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.

[0039] The mixed sludge slurry after cell wall disruption is then conditioned and thickened in a 500-stage homogenization and conditioning system, such as... Figure 14-15 As shown, the homogenization and conditioning system 500 includes a mixing device 501 and a dosing device 502. The mixing device 501 includes a mixing silo 5011, an overflow silo 5012, a bipolar settling inclined plate device 5013, a double-helix mixing device 5014, a conical dispersion structure 5015, and a sludge discharge device 5016. The overflow silo 5012 is installed at the top of the mixing silo 5011. The bipolar settling inclined plate device is installed in the upper middle part of the mixing silo 5011. The double-helix mixing device 5014 is installed at the inlet of the mixing silo 5011 and is connected to the sludge discharge pipe 302. The conical dispersion structure 5015 is fixedly installed at the bottom of the double-helix mixing device 5014, and the diameter of the conical dispersion structure 5015 gradually increases from top to bottom. The sludge discharge device 5016 is installed at the bottom of the mixing silo 5011. The dosing device 502 is connected to the top of the double helix mixing device 5014 via the dosing pump 503 and the dosing pipeline 504.

[0040] After conditioning and thickening, the mixed sludge slurry undergoes sludge-water separation via a high-pressure dewatering system. (See also...) Figure 14 The high-pressure dewatering system includes a high-pressure plate and frame dewatering device 600, a pressing water tank 601, and a wastewater treatment device 606. The feed pipe of the high-pressure plate and frame dewatering device 600 is connected to the sludge discharge device 5016 of the mixing device 501. The pressing water tank 601 is connected to the high-pressure plate and frame dewatering device 600 through a water pump 602 and a pressing water pipe 603 to press press water into the diaphragm plate pressing chamber. The drain pipe 605 of the high-pressure plate and frame dewatering device 600 is connected to the wastewater treatment device 606. The overflow chamber 5012 is connected to the wastewater treatment device 606 through an overflow pipe 505.

[0041] The sludge multiphase catalytic super oxidation cell-wall breaking deep dewatering treatment system of the present invention uses an ozone generator 100 to produce high-concentration ozone (200-250 mg / L) to provide an 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 a 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 mixed 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-scale bubbles and increasing the dissolved ozone concentration in the sludge. In the homogenizing reaction tank 300, ozone further mixes and contacts the sludge inside the tank. After passing through two catalytic oxidation reaction zones, it comes into full contact with the supporting multiphase composite catalytic materials, which can rapidly catalyze the reaction of ozone molecules 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 the sludge cell walls and extracellular polymers and other flocculent substances, thereby releasing intracellular water and adsorbed water, thus improving dewatering performance. After the sludge has been broken down, it is discharged to the double helix mixing device 5014 through the sludge discharge pipe 302. At the same time, the dosing device 502 introduces modifiers (such as filter aids and flocculants) into the double helix mixing device 5014 through the dosing pump 503 and the dosing pipe 504. The modifiers and broken sludge are fully homogenized, modified and conditioned, and dispersed from the bottom of the double helix mixing device 5014 into the mixing bin 5011, where they rapidly flocculate, agglomerate and settle. Some small particles rise in the mixing bin 5011, undergo secondary sedimentation and thickening through the energy dissipation and blocking effect of the counter-rotating bipolar settling inclined plate device 5013, and are then discharged to the high-pressure plate and frame dewatering device 600 via the sludge discharge device 5016. Meanwhile, the low-solids-content water overflows through the counter-rotating bipolar settling inclined plate device 5013 into the overflow bin 5012, and is then discharged to the tailwater treatment device via the overflow pipe 505. The thickened sludge is transported by the sludge supply pump 506 and the feed pipe 507 to the diaphragm plate and frame system of the high-pressure plate and frame dewatering device 600. Once the diaphragm chamber is full of sludge, the slurry feeding stops and the valve is closed. At the same time, the water pump 602 is started to pressurize the water in the pressing water tank 601 into the pressing chamber of the diaphragm plate through the pressing water pipe 603, and press quickly to achieve rapid solid-liquid separation of sludge. The filtrate is discharged from the drain pipe 605 at the bottom of the filter plate to the sewage treatment device 606, and at the same time, a sludge cake 607 with low water content (water content less than 50%) is formed.

[0042] Further optimization, such as Figure 1As shown, the ozone generator 100 includes an air compressor 101, an oil-gas separator 102, an air storage tank 103, a dryer 104, an air cooling and drying device 105, an oxygen generator 106, an ozone generator 107, and a cooling system 108. The air compressor 101 provides a certain volume of air at a certain pressure. Before entering the air storage tank 103, the air passes through the oil-gas separator 102 to remove oily substances mixed in during air compression, thus purifying the air. The compressed air in the air storage tank 103 first passes through the dryer 104 to remove condensed moisture from the air compression process, and then continues to enter the air cooling and drying device 105 for cooling and drying, resulting in clean and dry air. The pretreated clean air enters the oxygen generator 106 to separate and produce high-concentration oxygen. After being deeply dried by the dryer 104, it enters the ozone generator 107. The oxygen is converted into ozone through high-voltage discharge and connected to the ozone inlet 2035 through the inlet pipe 109, providing a high-concentration ozone source for subsequent processes. Cooling system 108 is used to cool ozone generator 107.

[0043] Further optimization, such as Figure 6 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 7 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.

[0044] During the material extraction process of the high-pressure feed pump 202, the material in the slurry inlet pipe 201 forms a high-speed suction flow, and the sludge is continuously drawn in through the gaps of the spherical filter cover 2041. As the sludge enters, a certain fluid dynamic is formed, which drives the spherical filter cover 2041 to perform a non-powered rotational motion. In this process, large particles of impurities and flocculent matter can be thrown away and filtered out, while the uniform, high-fluidity fine-particle sludge passes through the gaps of the spherical filter cover 2041, which can effectively ensure the homogeneity of the jet liquid phase source and avoid clogging of the feed pipe. This design can effectively solve the problem of conventional filter screen clogging.

[0045] 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.

[0046] 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.

[0047] Further optimization involves controlling the feeding pressure of the high-pressure feed pump 202 between 200kPa and 500kPa to generate a high jet.

[0048] 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.

[0049] 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.

[0050] Further optimization, such as Figure 2 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.

[0051] Further optimization, such as Figure 8 As 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.

[0052] Further optimization, such as Figure 9As 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.

[0053] Further optimization, such as Figure 10 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.

[0054] 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.

[0055] 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.

[0056] Further optimization, such as Figure 2-3 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.

[0057] For further optimization, please refer to [link / reference]. Figure 11 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.

[0058] For further optimization, please refer to [link / reference]. Figure 12 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.

[0059] For further optimization, please refer to [link / reference]. Figure 13 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.

[0060] 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.

[0061] For further optimization, please refer to [link / reference]. Figure 16 The double-helix mixing device 5014 includes a cylindrical body and a helical shaft rotatably disposed at the center of the cylindrical body. The upper and lower sections of the helical shaft are designed as right-hand helical sections 50141, and the middle section is designed as a left-hand helical section 50142, thereby forming a double-helix structure. This structure can increase the internal turbulence of the slurry. In other embodiments, the upper and lower sections of the helical shaft can also be designed as left-hand helical sections 50142, and the middle section as right-hand helical sections 50141.

[0062] Further optimized, the opposite bipolar settling inclined plate device 5013 includes two layers of settling inclined plates arranged at an upper and lower interval, with the inclination directions of the two layers of settling inclined plates being opposite to each other. Both layers of settling inclined plates are located above the outlet of the double helix mixing device 5014.

[0063] As the modifier and the cell-wall-breaking sludge are spirally conveyed along the guide channel, they tumble and roll within the double-helix structure, achieving non-powered mixing and energy dissipation, before finally being discharged at low speed from the bottom outlet. The bottom outlet is equipped with a conical dispersion structure 5015, which enables rapid and uniform dispersion of the modified and mixed sludge, increases the settling of flocculent particles, and improves the efficiency and quality of sludge flocculation and thickening.

[0064] Meanwhile, the upper layer is equipped with an anti-polarity settling inclined plate device 5013 to dissipate energy, improve the settling velocity of agglomerated sludge, reduce the suspended solids (SS) value in the supernatant, and reduce the solids content. Compared with ordinary sludge agglomerates, the sludge particles after cell wall disruption are fine and dispersed, with a lower specific gravity, making them easy to suspend but difficult to settle. Conventional single-stage sedimentation inclined plates are difficult to efficiently achieve the settling and flocculation of fine sludge particles. When the mixed sludge is discharged from the bottom of the double-helix mixing device 5014, the sludge flocs have not yet agglomerated and grown large enough, and are easily disturbed and turned upwards during the feeding process. They first encounter the lower first-stage settling inclined plate, which hinders most of the flocs from continuing to float. As the particles continue to agglomerate and grow, they sink. However, some small-diameter sludge agglomerates, as they continue to rise through the first-stage settling inclined plate, encounter the upper second-stage sedimentation inclined plate. The sludge agglomerates are obstructed from rising, prolonging the particle agglomeration and growth time, which in turn increases the particle size of the sludge agglomerates, thus achieving the settling of large particles.

[0065] Further optimization resulted in a spacing of 30mm-50mm between the two settlement inclined plates, with an inclination angle of 45°-60°.

[0066] Further optimization involves designing the bottom of the mixing silo 5011 as a funnel structure, with the bottom end of the funnel structure connected to the sludge discharge device 5016. The sludge discharge device 5016 includes a sludge discharge pipe and a solenoid valve mounted on the sludge discharge pipe.

[0067] Further optimization has been achieved by adding filter aids and flocculants to the dosing device 502.

[0068] Further optimization is achieved by the high-pressure plate and frame dewatering device 600, which is also equipped with a return water pipe 604 connected to the pressing water tank 601. After pressing, the pressing water flows back to the pressing water tank 601 through the return water pipe 604 for recycling, and occupies a small area.

[0069] Further optimization involves the water pump 602 pressurizing the water in the pressing water tank 601 to over 2 MPa, and then delivering it to the diaphragm pressing chamber of the high-pressure plate and frame dewatering device 600. This diaphragm hydraulic pressing provides a high pressure of over 2 MPa, overcoming the problem of insufficient pressure in conventional pneumatic pressing and achieving rapid pressing.

[0070] Accordingly, this invention also proposes a method for deep dewatering of sludge through multiphase catalytic super oxidation, employing the aforementioned system. The method includes the following steps: Ozone generator 100 produces high-concentration oxygen of 200-250 mg / L, which is introduced into multiphase micro-nano bubble mixed feed device 200 through ozone inlet 2035. At the same time, high-fluidity sludge is pumped from the turbulent mixing zone 310 of homogenizing reaction tank 300 into multiphase micro-nano bubble mixed feed device 200 through high-pressure feed pump 202. The high-fluidity sludge and ozone form ozone mixed flow in ejector 203 and are injected into homogenizing reaction tank 300 through dispersion device 304 in the form of high-pressure jet. In the homogenizing reaction tank 300, ozone is further mixed and contacted with the sludge in the tank, and then passes through the primary catalytic oxidation reaction zone 309 and the secondary catalytic oxidation reaction zone 311 in sequence. It fully contacts the multiphase coupled catalytic material to create a strong oxidation environment and generate a super catalytic oxidation reaction, which deeply destroys and decomposes the sludge cell wall and EPS, thereby releasing intracellular water and adsorbed water. The mixed sludge slurry after cell wall breaking is transported to the homogenization and conditioning system 500 for conditioning and thickening, and then transported to the high-pressure plate and frame dewatering device 600 for sludge-water separation, finally obtaining high-concentration organic wastewater and low-cement cake, realizing deep dewatering and volume reduction treatment of sludge.

[0071] 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.

[0072] 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.

[0073] 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 sludge multiphase catalytic super oxidation cell-wall breaking deep dewatering treatment system, characterized in that, Includes an ozone generator, a multiphase micro-nano bubble mixing feeder, a homogenizing reaction tank, a homogenizing conditioning system, and a high-pressure dehydration system; The homogenizing reaction tank is equipped with a dispersion device, a sludge feeding device, a primary catalytic oxidation reaction zone, and a secondary catalytic oxidation reaction zone, arranged sequentially from bottom to top. 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, the outlet end extends into the inlet end of the pressurized mixing pipe and is interconnected, the ozone inlet is opened on the side wall of the inlet end of the pressurized mixing pipe, and the outlet end is connected to the dispersion device; the ozone inlet is connected to the ozone generator; the highly fluid sludge from the homogenized reaction tank and ozone form an ozone mixed flow in the ejector and are injected into the homogenized reaction tank through the dispersion device in a high-pressure jet manner; The homogenization and conditioning system includes a mixing device and a dosing device; the mixing device includes a mixing silo, an overflow silo, a bipolar settling inclined plate device, a double-spiral mixing device, and a sludge discharge device. The overflow silo is installed at the top of the mixing silo, the bipolar settling inclined plate device is installed in the upper middle part of the mixing silo, the double-spiral mixing device is installed at the inlet of the mixing silo and connected to the sludge discharge pipeline of the homogenization reaction tank, and the sludge discharge device is installed at the bottom of the mixing silo; the dosing device is connected to the double-spiral mixing device. The high-pressure dewatering system includes a high-pressure plate and frame dewatering device, a pressing water tank, and a wastewater treatment device. The feed pipe of the high-pressure plate and frame dewatering device is connected to the sludge discharge device of the mixing device. The pressing water tank is connected to the high-pressure plate and frame dewatering device to pressurize water into the diaphragm plate pressing chamber. The drain pipe of the high-pressure plate and frame dewatering device is connected to the wastewater treatment device. The overflow chamber is connected to the wastewater treatment device through an overflow pipe.

2. The sludge multiphase catalytic super oxidation cell disruption deep dewatering treatment system 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 multiphase catalytic super oxidation cell-wall breaking deep dewatering treatment system 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.

4. The sludge multiphase catalytic super oxidation cell disruption deep dewatering treatment system 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.

5. The sludge multiphase catalytic super oxidation cell wall disruption deep dewatering treatment system according to claim 1, characterized in that, The dispersing device includes a main pipe, branch pipes, sub-branch pipes, and dispersing nozzles. The main pipe and branch pipes are horizontally arranged. The main pipe is connected to the discharge end of the pressurized mixing pipe. The branch pipes are arranged vertically or parallel to the main pipe and are connected to it. The sub-branch pipes are vertically arranged above the branch pipes and are connected to them. The dispersing nozzles are fixedly installed above the sub-branch pipes. The dispersing nozzles include 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 sub-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 compression elastic elements and sealing balls. 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 dispersing disc is fixed above the fixing nut and has a gap with the outlet of the fixing nut.

6. The sludge multiphase catalytic super oxidation cell disruption deep dewatering treatment system 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.

7. The sludge multiphase catalytic super oxidation cell disruption deep dewatering treatment system according to claim 1, characterized in that, The double-helix mixing device includes a cylindrical body and a helical shaft rotatably disposed at the center of the cylindrical body. The upper and lower sections of the helical shaft are designed as right-handed helical sections and the middle section is designed as left-handed helical sections, or the upper and lower sections are designed as left-handed helical sections and the middle section is designed as right-handed helical sections, thereby forming a double-helix structure.

8. The sludge multiphase catalytic super oxidation cell-wall breaking deep dewatering treatment system according to claim 1, characterized in that, The mixing device also includes a conical dispersing structure fixedly installed at the bottom of the double-helix mixing device, the diameter of which gradually increases from top to bottom.

9. The sludge multiphase catalytic super oxidation cell disruption deep dewatering treatment system according to claim 1, characterized in that, The opposite bipolar settling inclined plate device includes two layers of settling inclined plates arranged at an upper and lower interval, with the inclination directions of the two layers of settling inclined plates being opposite to each other; both layers of settling inclined plates are located above the outlet of the double helix mixing device.

10. A method for deep dewatering of sludge through multiphase catalytic super-oxidation and cell wall disruption, characterized in that, The method using the system according to any one of claims 1-9 includes the following steps: A high concentration of oxygen (200-250 mg / L) is generated by an ozone generator and introduced into a multiphase micro-nano bubble mixing feed device through an ozone inlet. Simultaneously, a high-fluidity sludge is pumped from the turbulent mixing zone of a homogenizing reaction tank into the multiphase micro-nano bubble mixing feed device via a high-pressure feed pump. The high-fluidity sludge and ozone form an ozone mixed flow in an ejector and are injected into the homogenizing reaction tank through a dispersion device using a high-pressure jet. In the homogenization reaction tank, ozone is further mixed and contacted with the sludge in the tank, and then passes through the primary catalytic oxidation reaction zone and the secondary catalytic oxidation reaction zone in sequence. It fully contacts the multiphase coupled catalytic material to create a strong oxidation environment and generate a super catalytic oxidation reaction, which deeply destroys and decomposes the sludge cell wall and EPS, thereby releasing intracellular water and adsorbed water. After the sludge is broken down, it is transported to a homogenization and conditioning system for conditioning and thickening, and then to a high-pressure plate and frame dewatering device for mud-water separation. Finally, high-concentration organic wastewater and low-cement cake are obtained, realizing the deep dewatering and volume reduction treatment of sludge.

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