A micro-nano bubble oxidation reaction device for sewage treatment

Abstract

The application discloses a kind of micro-nano bubble oxidation reaction devices for sewage treatment, it is related to sewage treatment technical field, including: bearing frame;Cylindrical reaction tower is fixed on bearing frame by both sides;Transportation steady flow device is set in the inside lowermost of cylindrical reaction tower;Bubble generating device is fixed above transportation steady flow device;Self-pressurized circulating unit is vertically distributed with multiple, located above bubble generating device, and is fixedly connected with the inner wall of cylindrical reaction tower;Gas-liquid separation device is set in the inside uppermost of cylindrical reaction tower;Drainage pipeline is connected with the top of gas-liquid separation device and external sink;Tail gas discharge pipe is connected with the top of cylindrical reaction tower and external ozone destructor.The application comprehensively prolongs bubble residence time, improves ozone utilization rate and mass transfer efficiency, reduces tail gas ozone content and operating cost.

Description

Technical Field

[0001] This invention relates to the field of wastewater treatment technology, and more specifically, to a micro / nano bubble oxidation reaction device for wastewater treatment. Background Technology

[0002] Currently, ozone catalytic oxidation technology has been initially industrialized in the deep treatment of recalcitrant wastewater, and some progress has been made in ozone oxidation process conditions, with the effects of factors such as pH, ozone dosage, and reaction time on the degradation efficiency of organic matter preliminarily clarified. However, in the application of ozone catalytic oxidation technology, existing micro-nano bubble devices mostly use perforated tubes or micropores for aeration, resulting in large and unevenly distributed bubble particles, low ozone solubility, and high ozone content in the exhaust gas. The bubbles have a short residence time in the reactor, with an ozone utilization rate of only 40%–55%, and lack a recycling structure, with gas escaping immediately after passing through, making deep oxidation difficult to achieve. Furthermore, the gas-liquid separation effect is poor, and unreacted ozone is easily leaked with the effluent or exhaust gas, increasing environmental risks and operating costs. Therefore, it is necessary to provide a micro-nano bubble oxidation reactor for wastewater treatment to solve the problems mentioned in the background technology. Summary of the Invention

[0003] To achieve the above objectives, the present invention provides the following technical solution: a micro / nano bubble oxidation reaction device for wastewater treatment, comprising:

[0004] Support frame;

[0005] The cylindrical reaction tower is fixed to the supporting frame on both sides;

[0006] The flow stabilizing device is located at the bottom of the interior of the cylindrical reaction tower;

[0007] A bubble generator is fixed above the conveying and stabilizing device;

[0008] Multiple self-pressurized circulation units are vertically distributed above the bubble generator and are fixedly connected to the inner wall of the cylindrical reaction tower.

[0009] The gas-liquid separation device is located at the top inside the cylindrical reaction tower;

[0010] Drainage pipes connect the top of the gas-liquid separator to the external water tank;

[0011] The exhaust pipe connects the top of the cylindrical reaction tower to the external ozone destructor.

[0012] Furthermore, preferably, the current stabilizing device includes:

[0013] The sludge discharge pipe is fixed at the bottom end cap of the cylindrical reaction tower;

[0014] A conical guide bucket is installed inside the cylindrical reaction tower, with its lower opening connected to the sludge discharge pipe;

[0015] A porous flow equalization plate is located above the conical guide bucket and is fixedly connected to the inner wall of the cylindrical reaction tower on all four sides. It has multiple circular holes.

[0016] The water inlet pipe is connected to the side wall of the cylindrical reaction tower and is located between the conical guide bucket and the porous flow equalization plate;

[0017] The baffle plate, tilted downwards, is welded to the outlet of the inlet pipe.

[0018] Furthermore, preferably, the bubble generating device includes:

[0019] The micro-nano bubble generating disk is located directly above the porous flow equalization plate, coaxially arranged with the porous flow equalization plate, and has an annular gap between it and the inner wall of the cylindrical reaction tower.

[0020] Support columns, arranged in a ring, are arranged in multiple ways to connect the top of the porous flow equalization plate and the bottom of the micro-nano bubble generating disk.

[0021] The anti-impact plate, in the shape of a ring, is fixed on the outside of the micro-nano bubble generating disk;

[0022] The ozone inlet pipe passes through the wall of the cylindrical reaction tower and connects to the bottom gas distribution pipe flange of the micro-nano bubble generating disk.

[0023] Furthermore, preferably, the self-pressure circulation unit includes:

[0024] A conical gas collecting assembly is positioned above the bubble generator and is fixedly connected to the inner wall of the cylindrical reaction tower.

[0025] The gas collection pipe is fixedly connected to the top center of the conical gas collection assembly, and its lower part extends into the interior of the conical gas collection assembly;

[0026] Connecting pipe fittings are fixed to the top of the gas collecting pipe;

[0027] Multiple guide pipes are arranged in a ring. The top of the guide pipe is fixedly connected to the connecting pipe fitting through a pipe, and the bottom passes through the conical gas collection assembly. A pressure valve is installed inside the guide pipe.

[0028] The diffusion defoaming component is installed corresponding to the flow guide tube and fixed at the bottom of the flow guide tube.

[0029] Furthermore, preferably, the conical gas collection assembly includes:

[0030] A conical gas collecting hood is installed above the bubble generator, with an opening at the top center for connection to the gas collecting pipe;

[0031] The support feet are arranged in a ring, with multiple feet connected to the bottom edge of the conical gas collecting hood and the inner wall of the cylindrical reaction tower.

[0032] Multiple guide ribs are arranged in a ring and fixed to the inner wall of the conical gas collection hood;

[0033] The high-pressure air chamber is located between the opening and the guide rib of the conical air collecting hood, and the bottom of the air collecting pipe is located inside the high-pressure air chamber.

[0034] Furthermore, preferably, there is a gap between the bottom edge of the conical gas collecting hood and the inner wall of the cylindrical reaction tower, and the gap between the bottom edge of the conical gas collecting hood and the inner wall of the cylindrical reaction tower gradually decreases from bottom to top in multiple self-pressurized circulation units.

[0035] Furthermore, preferably, the diffusion defoaming component includes:

[0036] The diffuser head is a tapered flared part that is fixed to the bottom of the guide tube;

[0037] Multiple bubble-breaking fins are provided, which are distributed in a cross pattern, and the center of the intersection of multiple bubble-breaking fins coincides with the central axis of the diffuser head;

[0038] The double-toothed ring has toothed channels on both the inner and outer sides and is fixed in the middle of the bubble-breaking fin.

[0039] An auxiliary microporous plate is fixed to the bottom of the diffuser head, with its inner side in contact with the bubble-breaking fins.

[0040] Furthermore, preferably, the gas-liquid separation device includes:

[0041] An inverted conical gas-liquid separation hood is positioned above the self-pressurized circulation unit, with an opening at the center of its bottom.

[0042] The fasteners are arranged in a ring and are fixedly connected to the bottom edge of the inverted conical gas-liquid separation hood and the inner wall of the cylindrical reaction tower.

[0043] An annular crushing grid is fixed to the outer wall of an inverted conical gas-liquid separator.

[0044] Furthermore, as a preferred embodiment, the inlet end of the drainage pipe is in contact with the inner wall of the inverted conical gas-liquid separator, and the bottom of the pipe is higher than the position of the annular crushing grid.

[0045] Compared with the prior art, the beneficial effects of the present invention are:

[0046] In this invention, by setting up multiple self-pressurized circulation units with progressively smaller intervals between the bottom edge of the conical gas collection hood and the tower wall, multi-stage relay capture and recycling of bubbles is achieved, significantly extending the residence time of bubbles in the reaction tower and improving the contact efficiency between ozone and pollutants.

[0047] By ensuring that the bottom of the gas collecting pipe always extends into the high-pressure gas chamber and remains above the liquid level, and by using the pressure valve inside the guide pipe, self-pressure driven transport of pure gas phase is achieved, avoiding energy loss caused by water mixing into the guide pipe and ensuring the continuous and stable circulation process.

[0048] By using a diffuser, cross-distributed bubble-breaking fins, a double-toothed ring with toothed channels on both the inner and outer sides, and a step-by-step shearing structure with an auxiliary microporous plate, the high-speed continuous airflow is forcibly redispersed into nano-sized bubbles, which greatly increases the gas-liquid contact surface area and enhances ozone mass transfer and free radical generation.

[0049] By setting up an inverted conical gas-liquid separation hood and an annular crushing grid fixed on its outer wall, the escaped microbubbles are sheared and crushed for the last time and the residual ozone is released, which facilitates the collection of residual ozone and timely discharge along the tail gas emission pipe at the top of the tower.

[0050] By setting up a conical guide bucket, a porous flow equalization plate, and an annular anti-scouring plate, uniform distribution of influent and directional sedimentation of sludge are achieved. At the same time, the rising water flow is prevented from scouring the bubble surface, maintaining the scale stability of the initial micro-nano bubbles and ensuring the long-term efficient operation of the device. Attached Figure Description

[0051] Figure 1 This is a schematic diagram of the overall structure of a micro-nano bubble oxidation reactor for wastewater treatment.

[0052] Figure 2 A front cross-sectional view of a micro / nano bubble oxidation reactor for wastewater treatment;

[0053] Figure 3 A side cross-sectional view of a micro / nano bubble oxidation reactor for wastewater treatment;

[0054] Figure 4 A schematic diagram of the conveyor flow stabilization device and the bubble generator;

[0055] Figure 5 This is a schematic diagram of the self-pressure circulation unit structure;

[0056] Figure 6 This is a schematic diagram of the conical gas collection assembly structure;

[0057] Figure 7 This is a schematic diagram of the diffusion defoaming component structure;

[0058] Figure 8 This is a schematic diagram of a gas-liquid separation device.

[0059] In the diagram: 1. Support frame; 2. Cylindrical reaction tower; 3. Conveying and stabilizing device; 4. Bubble generator; 5. Self-pressurized circulation unit; 6. Gas-liquid separator; 7. Drainage pipe; 8. Tail gas emission pipe; 31. Sludge discharge pipe; 32. Conical guide hopper; 33. Porous flow equalization plate; 34. Water inlet pipe; 35. Guide plate; 41. Micro-nano bubble generator; 42. Support column; 43. Anti-impact plate; 44. Ozone inlet pipe ; 51. Conical gas collection assembly; 52. Gas collection pipe; 53. Connecting pipe fittings; 54. Flow guide pipe; 55. Diffusion and bubble breaking assembly; 61. Inverted conical gas-liquid separation hood; 62. Fixing component; 63. Annular crushing grid; 511. Conical gas collection hood; 512. Support foot; 513. Flow guide rib; 514. High-pressure gas chamber; 551. Diffuser head; 552. Bubble breaking fins; 553. Double toothed ring; 554. Auxiliary microporous plate. Detailed Implementation

[0060] Please see Figures 1 to 8 In this embodiment of the invention, a micro / nano bubble oxidation reactor for wastewater treatment includes:

[0061] Support frame 1;

[0062] The cylindrical reaction tower 2 is fixed to the supporting frame 1 by both sides;

[0063] The flow stabilizing device 3 is located at the bottom of the interior of the cylindrical reaction tower 2;

[0064] The bubble generator 4 is fixed above the conveying and stabilizing device 3;

[0065] Multiple self-pressurized circulation units 5 are vertically distributed and located above the bubble generator 4, and are fixedly connected to the inner wall of the cylindrical reaction tower 2.

[0066] The gas-liquid separation device 6 is located at the top inside the cylindrical reaction tower 2;

[0067] Drainage pipe 7 connects the top of the gas-liquid separator 6 to the external water tank;

[0068] The exhaust pipe 8 connects the top of the cylindrical reaction tower 2 to the external ozone destroyer.

[0069] In this embodiment, the conveying and stabilizing device 3 includes:

[0070] The sludge discharge pipe 31 is fixed at the bottom end cap of the cylindrical reaction tower 2;

[0071] A conical guide bucket 32 ​​is installed inside the cylindrical reaction tower 2, with its lower opening connected to the sludge discharge pipe 31;

[0072] The porous flow equalization plate 33 is located above the conical flow guide hopper 32 and is fixedly connected to the inner wall of the cylindrical reaction tower 2 on all four sides. It has multiple round holes.

[0073] The water inlet pipe 34 is connected to the side wall of the cylindrical reaction tower 2 and is located between the conical guide bucket 32 ​​and the porous flow equalization plate 33;

[0074] The guide plate 35 is tilted downwards and welded to the outlet of the inlet pipe 34.

[0075] In other words, wastewater enters the cylindrical reaction tower 2 through the inlet pipe 34. At the outlet of the inlet pipe 34, the downward-sloping guide plate 35 guides the wastewater to impact the inner wall of the conical guide bucket 32 ​​in a downward direction. The impact consumes the kinetic energy of the incoming water and converts it into radial diffusion. The wastewater flows evenly to all sides along the slope of the conical guide bucket 32 ​​and then turns back upward. During this process, large particles of silt or suspended solids carried in the wastewater settle due to gravity and slide down the slope of the conical guide bucket 32 ​​to the bottom opening. The sludge is periodically discharged through the sludge discharge pipe 31 to prevent sludge accumulation from affecting subsequent treatment. The returned wastewater continues to flow upward through the porous flow equalization plate 33. The multiple circular holes on the porous flow equalization plate 33 cut the rising water flow into multiple fine jets, eliminating large-scale eddies and local high-speed zones, so that the water flow is evenly distributed throughout the entire tower cross section, forming a stable piston flow moving upward. The conical guide bucket 32 ​​is located below the porous flow equalization plate 33, and its lower opening is connected to the sludge discharge pipe 31 to ensure the stability of the bottom flow field.

[0076] In this embodiment, the bubble generating device 4 includes:

[0077] The micro-nano bubble generating disk 41 is located directly above the porous flow equalization plate 33, coaxially arranged with the porous flow equalization plate 33, and has an annular gap between it and the inner wall of the cylindrical reaction tower 2.

[0078] Support columns 42 are arranged in a ring, with multiple columns connecting the top of the porous flow equalization plate 33 and the bottom of the micro-nano bubble generating disk 41;

[0079] The anti-impact plate 43 is ring-shaped and fixed on the outside of the micro-nano bubble generating disk 41;

[0080] The ozone inlet pipe 44 passes through the wall of the cylindrical reaction tower 2 and is connected to the bottom gas distribution pipe flange of the micro-nano bubble generating plate 41.

[0081] In other words, ozone gas passes through the ozone inlet pipe 44 through the tower wall and connects to the gas distribution pipe flange at the bottom of the micro-nano bubble generating plate 41, entering the generating plate evenly. The micro-nano bubble generating plate 41 is located directly above the porous flow equalization plate 33, and the two are coaxially arranged with an annular gap between them and the tower wall. Ozone is squeezed out from the micropores of the generating plate to form initial micro-nano bubbles. Multiple support columns 42 are distributed in an annular pattern to stably support the generating plate on the porous flow equalization plate 33, ensuring its levelness. Driven by the rising water flow, the bubbles move upward. The anti-impact plate 43 is fixed in an annular shape on the outside of the micro-nano bubble generating plate 41. Its annular structure effectively blocks the high-speed rising water flow from below from directly scouring the plate surface, reducing the merging of bubbles near the plate surface, thereby maintaining the micro-nano scale of the bubbles. Since the water flow flows upward from the annular gap between the generating plate and the tower wall, some micro bubbles move directly upward with the water flow, passing through the self-pressure circulation unit 5 of this stage, while most bubbles continue to rise with the water flow and enter the self-pressure circulation unit 5.

[0082] In this embodiment, the self-pressure circulation unit 5 includes:

[0083] The conical gas collecting assembly 51 is positioned above the bubble generating device 4 and is fixedly connected to the inner wall of the cylindrical reaction tower 2.

[0084] The gas collecting pipe 52 is fixedly connected to the top center of the conical gas collecting assembly 51, and its lower part extends into the interior of the conical gas collecting assembly 51.

[0085] Connecting fitting 53 is fixed to the top of gas collecting pipe 52;

[0086] Multiple guide pipes 54 are arranged in a ring. The top of the guide pipe is fixedly connected to the connecting pipe 53 through a pipe, and the bottom passes through the conical gas collection assembly 51. A pressure valve is provided inside the guide pipe 54.

[0087] The diffusion defoaming component 55 is correspondingly provided to the guide tube 54 and is fixed at the bottom of the guide tube 54.

[0088] In other words, the rising gas-liquid mixture first encounters the first-stage conical gas collection component 51. The conical gas collection component 51 guides the bubbles to gather towards the center of the top of the cover, preventing the bubbles from escaping directly along the cover wall. As the bubbles continuously flow in and accumulate, they form a high-pressure gas chamber 514 and enter the gas collection pipe 52. After entering the top of the gas collection pipe 52, they are distributed to multiple annularly distributed guide pipes 54 via connecting pipes 53. Each guide pipe 54 is equipped with a pressure valve. Under continuous operation, the gas chamber pressure is stable above the opening threshold of the pressure valve. The pressure valve automatically maintains a slightly open state, allowing the gas to pass through continuously. The high-pressure gas flows downward at high speed under the pressure difference, passes through and enters the diffusion bubble breaking component 55. Under the shearing action of the diffusion bubble breaking component 55, micro-nano bubbles are reformed and injected into the water body below the conical gas collection component 51. These newly generated micro-nano bubbles mix with the rising sewage again and continue to participate in the oxidation reaction.

[0089] In a preferred embodiment, the guide pipes 54 and the diffusion bubble breaking components 55 in the two adjacent self-pressure circulation units 5 are staggered, which increases the dispersion of bubbles in the cross section of the tower, making the bubble capture and redispersion of each level more balanced, and further improving the mixing uniformity of ozone and sewage and the overall oxidation efficiency.

[0090] In this embodiment, the conical gas collection assembly 51 includes:

[0091] A conical gas collecting hood 511 is installed above the bubble generating device 4, and has an opening at the top center that connects to the gas collecting pipe 52.

[0092] Support feet 512 are arranged in a ring and multiple of them are connected to the bottom edge of the conical gas collecting hood 511 and the inner wall of the cylindrical reaction tower 2.

[0093] The guide ribs 513 are arranged in a ring and are fixed on the inner wall of the conical gas collection hood 511.

[0094] The high-pressure air chamber 514 is located between the opening of the conical air collecting hood 511 and the guide rib 513, and the bottom of the air collecting pipe 52 is located inside the high-pressure air chamber 514.

[0095] In other words, the rising gas-liquid mixture first encounters the first-stage conical gas collecting hood 511. The conical gas collecting hood 511 is fixedly connected to the inner wall of the tower by multiple support feet 512, and there is an annular gap between its bottom edge and the inner wall of the tower (the gap is largest in the first stage, for example, 15 mm). Most of the bubbles move upward along the inner wall of the conical gas collecting hood 511 under the influence of buoyancy and rising water flow. The annularly distributed guide ribs 513 on the inner wall further guide the bubbles to gather towards the center of the top of the hood, preventing the bubbles from escaping directly along the hood wall. As bubbles continue to flow in, a high-pressure gas chamber 514 gradually forms in the area below the center of the top of the conical gas collecting hood 511, located between the opening and the guide ribs 513. Due to the accumulation of bubbles, the pressure in the gas chamber continues to rise, forcing the liquid level inside the hood to drop slightly, but the bottom of the gas collecting pipe 52... The part is always inserted into the high-pressure gas chamber 514 and kept above the liquid surface to ensure that only gas can enter the gas collecting pipe 52 and water will not mix in. The gas in the high-pressure gas chamber 514 enters the top of the gas collecting pipe 52 through the gas collecting pipe 52, and is then distributed to multiple annularly distributed guide pipes 54 through the connecting pipe fitting 53. Under the action of air pressure, the pressure valve inside each guide pipe 54 automatically keeps a slightly open state, allowing the gas to pass through continuously. The high-pressure gas flows downward at high speed under the pressure difference drive, passes through the conical gas collecting hood 511 and enters the diffusion and bubble breaking assembly 55.

[0096] In this embodiment, there is a gap between the bottom edge of the conical gas collecting hood 511 and the inner wall of the cylindrical reaction tower 2, and the gap between the bottom edge of the conical gas collecting hood 511 and the inner wall of the cylindrical reaction tower 2 in the multiple self-pressure circulation units 5 from bottom to top gradually decreases.

[0097] In other words, the micro- and nano-bubbles that are not captured in the first stage escape upward with the water flow through the annular gap between the bottom edge of the conical gas collecting hood 511 and the tower wall, and enter the second stage region. The annular gap between the second-stage conical gas collecting hood 511 and the tower wall is smaller, so the interception efficiency is higher. The trapped bubbles form a high-pressure gas chamber 514, repeating the above-mentioned capture-pressurization-guidance-redispersion process, and the gas is sprayed downward to the area below the second-stage conical gas collecting hood 511. The third stage has the smallest annular gap and the highest interception efficiency. The gas is sprayed to the area below the third-stage conical gas collecting hood 511. Through the three-stage relay, the micro- and nano-bubbles are recycled, reducing the loss of ozone from the exhaust gas and improving the ozone utilization rate. It should be noted that some bubbles generated by the micro- and nano-bubble generating disk 41 escape upward along the gap between the conical gas collecting hood 511 and the cylindrical reaction tower 2, and some bubbles generated by the diffusion bubble breaking component 55 also escape upward. Thus, each self-pressurized circulation unit 5 has enough bubbles to maintain the generation of the high-pressure gas chamber 514.

[0098] In this embodiment, the diffusion defoaming component 55 includes:

[0099] The diffuser head 551 is a tapered flared part, which is fixed to the bottom of the guide tube 54;

[0100] Multiple bubble-breaking fins 552 are provided and are distributed in a cross pattern, and the center of the intersection of multiple bubble-breaking fins 552 coincides with the central axis of the diffuser head 551;

[0101] The double-toothed ring 553 has toothed channels on both the inner and outer sides and is fixed in the middle of the bubble-breaking fin 552;

[0102] The auxiliary microporous plate 554 is fixed to the bottom of the diffuser head 551, and its inner side is attached to the bubble-breaking fin 552.

[0103] In other words, the high-speed gas first enters the diffuser head 551 (conical flare), where the increased cross-sectional area slightly reduces the airflow velocity and restores the pressure, which is beneficial for subsequent shearing. Subsequently, the gas passes through multiple cross-distributed bubble-breaking fins 552, which cut the airflow into multiple fine streams. The center of intersection of the multiple bubble-breaking fins 552 coincides with the central axis of the diffuser head 551, ensuring a symmetrical distribution of the airflow. The segmented airflow then impacts the double-toothed ring 553, which has toothed channels on both its inner and outer sides. The gas undergoes a double shearing action when passing through the gaps between the teeth. Finally, the gas passes through the auxiliary microporous plate 554, where tiny holes force the gas into micro-nano bubbles. These bubbles are then injected from the outlet of the diffuser head 551 into the water below the conical gas collection hood 511. These newly generated micro-nano bubbles mix again with the rising sewage and continue to participate in the oxidation reaction.

[0104] In this embodiment, the gas-liquid separation device 6 includes:

[0105] An inverted conical gas-liquid separation hood 61 is positioned above the self-pressurized circulation unit 5, with an opening at the center of its bottom.

[0106] The fasteners 62 are arranged in a ring and are fixedly connected to the bottom edge of the inverted conical gas-liquid separation hood 61 and the inner wall of the cylindrical reaction tower 2.

[0107] An annular crushing grid 63 is fixed on the outer wall of an inverted conical gas-liquid separator 61.

[0108] In other words, the tiny bubbles escaping from the top-level (third-level) self-pressurized circulation unit 5 rise with the water flow and first come into contact with the outer wall of the inverted conical gas-liquid separator 61. Under the action of buoyancy, the bubbles move upward along the outer wall of the inverted conical gas-liquid separator 61. When they pass through the annular crushing grid 63 fixed on the outer wall of the inverted conical gas-liquid separator 61, they are further sheared and crushed by the grid edges, so that the residual ozone gas is released from the microbubbles. These gases continue to rise to the top of the cylindrical reaction tower 2, are discharged through the tail gas emission pipe 8, and are sent to the external ozone destroyer for treatment.

[0109] In this embodiment, the water inlet end of the drainage pipe 7 is in contact with the inner wall of the inverted conical gas-liquid separator 61, and the bottom of the pipe is higher than the position of the annular crushing grid 63.

[0110] In other words, after deep treatment, the clean water gathers at the top of the tower and enters the interior of the hood through the opening at the center of the bottom of the inverted conical gas-liquid separation hood 61. The water inlet end of the drain pipe 7 is in contact with the inner wall of the inverted conical gas-liquid separation hood 61, and the bottom of the pipe is higher than the position of the annular crushing grid 63, maintaining the water level at the annular crushing grid 63, ensuring that the ozone bubbles at the escape point can be broken, releasing the ozone gas from the microbubbles, and then discharging it. The clean water is continuously discharged to the external water tank through the drain pipe 7, completing the sewage treatment process.

[0111] In a preferred embodiment, before the device forms a complete cycle, wastewater to be treated is first injected into the cylindrical reaction tower 2 through the inlet pipe 34. When the wastewater enters, it is guided by the guide plate 35 and impacts the inner wall of the conical guide bucket 32 ​​downwards, so that the water is evenly dispersed and avoids direct impact on the porous flow equalization plate 33. At the same time, the settling effect of the conical guide bucket 32 ​​is used to deposit large particles of silt or suspended matter in the wastewater at the bottom of the bucket. The deposited sludge is periodically discharged through the sludge discharge pipe 31. As the water level rises, the wastewater is evenly rectified through multiple holes on the porous flow equalization plate 33 to form a stable upward flow, preventing excessive local flow velocity or eddies. When the water level rises to the top of the guide ribs 513 on the inner wall of the conical gas collection hood 511 in the lowest (first stage) self-pressurized circulation unit 5, the area below the center of the top of the conical gas collection hood 511 (i.e., the high-pressure gas chamber 514) is completely filled with water. At this time, the ozone is introduced through the ozone inlet pipe 4. 4. Ozone gas is injected into the micro / nano bubble generating disk 41, which generates a large number of micro / nano-sized bubbles. These bubbles move with the rising water flow. Due to the annular gap between the bottom edge of the conical gas collecting hood 511 and the inner wall of the cylindrical reaction tower 2, some extremely small bubbles escape upwards along this gap. However, most bubbles, guided by the guide ribs 513, gather along the inner wall of the conical gas collecting hood 511 towards the high-pressure gas chamber 514 at the top center. Bubbles continuously flow in, gradually forming a high-pressure gas chamber 514 below the top of the hood. The pressure in the gas chamber forces the liquid level inside the hood to drop until the bottom of the gas collecting pipe 52 is always exposed inside the gas chamber (above the liquid level), creating conditions for gas to enter the gas collecting pipe 52. Before the gas chamber pressure reaches the set threshold, the pressure valve inside the guide pipe 54 remains closed, preventing gas from flowing out, thus causing the gas chamber pressure to continue to rise until it reaches the opening pressure of the pressure valve (e.g., 0.05~0.10). (MPa), the pressure valve adopts a spring-type or pilot-operated structure, which automatically opens only when the pressure exceeds the set value, ensuring that the air chamber has sufficient driving head. After the air chamber of the first-stage self-pressure circulation unit 5 is established and the pressure valve is prepared to open, sewage and ozone continue to be injected, so that the water level rises to the second-stage and third-stage self-pressure circulation units 5. Each unit repeats the above process in sequence. The bubbles are trapped, forming a high-pressure air chamber 514, the bottom of the gas collecting pipe 52 is exposed to the air chamber, and the pressure valve is ready to open. At this point, the device has completed the start-up and entered the continuous working state.

[0112] In practice, wastewater first enters the cylindrical reaction tower 2 through the inlet pipe 34. Guided by the downward-sloping guide plate 35 at the outlet of the inlet pipe 34, it impacts the inner wall of the conical guide bucket 32 ​​in a downward direction. The kinetic energy is consumed and converted into radial diffusion. The wastewater flows evenly around the conical guide bucket 32 ​​and then turns upward. Large particles of silt or suspended matter carried in the wastewater settle due to gravity and slide down the conical guide bucket 32 ​​to the bottom opening and are periodically discharged through the sludge discharge pipe 31. The returned wastewater continues to flow upward through the porous flow equalization plate 33. The multiple round holes on the porous flow equalization plate 33 cut the rising water flow into multiple fine jets, eliminating large-scale eddies and local high-speed zones, forming a stable piston flow moving upward. At the same time, ozone gas flows upward through the ozone inlet pipe. 44 passes through the tower wall and connects to the flange of the gas distribution pipe at the bottom of the micro-nano bubble generating plate 41, uniformly entering the interior of the micro-nano bubble generating plate 41, and is squeezed out from the micropores to form initial micro-nano bubbles. The annular anti-impact plate 43 on the outside of the micro-nano bubble generating plate 41 prevents the rising water flow from directly scouring the plate surface, maintaining the micro-nano scale of the bubbles. The rising gas-liquid mixture first encounters the conical gas collecting component 51 in the first-stage self-pressure circulation unit 5. Most of the bubbles move upward along the inner wall of the conical gas collecting hood 511. The annularly distributed guide ribs 513 on the inner wall further guide the bubbles to gather towards the center of the top of the hood. As the bubbles continue to pour in, a high-pressure gas chamber 514 gradually forms in the area below the center of the top of the conical gas collecting hood 511, between the opening and the guide ribs 513. The bottom of the gas collecting pipe 52 begins to... The gas finally extends into the high-pressure gas chamber 514 and remains above the liquid surface, ensuring that only gas enters the gas collecting pipe 52. The gas enters the connecting pipe 53 through the top of the gas collecting pipe 52 and is distributed to multiple annularly distributed guide pipes 54. Each guide pipe 54 is equipped with a pressure valve. Under continuous operation, the gas chamber pressure is stabilized above the opening threshold of the pressure valve, and the pressure valve automatically remains slightly open. Driven by the pressure difference, the high-pressure gas flows downward at high speed, passes through the conical gas collecting hood 511 and enters the diffusion and bubble breaking assembly 55. The high-speed gas first enters the conical flared diffuser head 551, where the increased cross-sectional area slightly reduces the airflow velocity. Subsequently, it passes through multiple cross-distributed bubble breaking fins 552, which cut the airflow into multiple fine streams. The divided airflow then impacts the double toothed ring 55. 3. The inner and outer toothed channels of the double-toothed ring 553 perform double shearing on the gas, which is then forced into micro-nano bubbles by the auxiliary microporous plate 554. These bubbles are then injected into the water below the conical gas collecting hood 511 from the outlet of the diffuser head 551, where they mix again with the rising sewage. The extremely small bubbles that are not captured by the first stage escape upward with the water flow through the annular gap between the bottom edge of the conical gas collecting hood 511 and the tower wall, entering the second-stage self-pressurized circulation unit 5. The annular gap between the second-stage conical gas collecting hood 511 and the tower wall is even smaller, resulting in higher interception efficiency. The process of capture-pressurization-guidance-redispersion is repeated, and the gas is injected downward below the second-stage hood. The third-stage annular gap is the smallest, resulting in the highest interception efficiency. The gas is injected below the third stage, and the micro-nano bubbles are recycled through a three-stage relay.The tiny bubbles escaping from the top-level self-pressurized circulation unit 5 rise with the water flow, first contacting the outer wall of the inverted conical gas-liquid separator 61. Under buoyancy, they move upwards along the outer wall and are further sheared and broken by the edges of the annular crushing grid 63 fixed to the outer wall of the inverted conical gas-liquid separator 61. This releases residual ozone gas from the microbubbles, which rise to the top of the cylindrical reaction tower 2 and are discharged through the exhaust pipe 8 and sent to an external ozone destroyer for further treatment. The treated water gathers at the top of the tower and enters the interior of the separator through the opening at the center of the bottom of the inverted conical gas-liquid separator 61. The treated water is then continuously discharged to an external water tank through the drainage pipe 7, completing the wastewater treatment process.

[0113] The above description is merely a preferred embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any equivalent substitutions or modifications made by those skilled in the art within the scope of the technology disclosed in the present invention, based on the technical solution and inventive concept of the present invention, should be covered within the scope of protection of the present invention.

Claims

1. A micro / nano bubble oxidation reaction device for wastewater treatment, characterized in that: include: Support frame (1); The cylindrical reaction tower (2) is fixed to the supporting frame (1) on both sides; The flow stabilizing device (3) is located at the bottom of the interior of the cylindrical reaction tower (2); A bubble generator (4) is fixed above the conveying and stabilizing device (3); Multiple self-pressurized circulation units (5) are vertically distributed above the bubble generator (4) and are fixedly connected to the inner wall of the cylindrical reaction tower (2). The gas-liquid separation device (6) is located at the top inside the cylindrical reaction tower (2); Drainage pipe (7) connects the top of the gas-liquid separator (6) and the external water tank; The exhaust pipe (8) connects the top of the cylindrical reaction tower (2) to the external ozone destroyer.

2. The micro / nano bubble oxidation reactor for wastewater treatment according to claim 1, characterized in that: The conveying and stabilizing device (3) includes: The sludge discharge pipe (31) is fixed at the bottom end cap of the cylindrical reaction tower (2); A conical guide bucket (32) is installed inside the cylindrical reaction tower (2), with its lower opening connected to the sludge discharge pipe (31); A porous flow equalization plate (33) is located above the conical guide bucket (32) and is fixedly connected to the inner wall of the cylindrical reaction tower (2) on all four sides. It has multiple round holes. The water inlet pipe (34) is connected to the side wall of the cylindrical reaction tower (2) and is located between the conical guide bucket (32) and the porous flow equalization plate (33); The guide plate (35) is tilted downward and welded to the outlet of the inlet pipe (34).

3. The micro / nano bubble oxidation reactor for wastewater treatment according to claim 2, characterized in that: The bubble generating device (4) includes: The micro-nano bubble generating disk (41) is located directly above the porous flow equalization plate (33), is coaxially arranged with the porous flow equalization plate (33), and has an annular gap between it and the inner wall of the cylindrical reaction tower (2). Support columns (42) are arranged in a ring, with multiple columns connecting the top of the porous flow equalization plate (33) and the bottom of the micro-nano bubble generating disk (41); An anti-impact plate (43) is ring-shaped and fixed on the outside of the micro-nano bubble generating disk (41); The ozone inlet pipe (44) passes through the tower wall of the cylindrical reaction tower (2) and is connected to the bottom gas distribution pipe flange of the micro-nano bubble generating plate (41).

4. The micro / nano bubble oxidation reactor for wastewater treatment according to claim 1, characterized in that: The self-pressure circulation unit (5) includes: The conical gas collecting assembly (51) is positioned above the bubble generating device (4) and is fixedly connected to the inner wall of the cylindrical reaction tower (2); The gas collecting pipe (52) is fixedly connected to the top center of the conical gas collecting assembly (51), and its lower part extends into the interior of the conical gas collecting assembly (51); Connecting fitting (53) is fixed to the top of the gas collecting pipe (52); Multiple guide pipes (54) are arranged in a ring. The top is fixedly connected to the connecting pipe fitting (53) through a pipe, and the bottom passes through the conical gas collection assembly (51). A pressure valve is provided inside the guide pipe (54). The diffusion defoaming component (55) is set in correspondence with the guide tube (54) and fixed at the bottom of the guide tube (54).

5. The micro / nano bubble oxidation reactor for wastewater treatment according to claim 4, characterized in that: The conical gas collection assembly (51) includes: A conical gas collecting hood (511) is set above the bubble generating device (4), and an opening connected to the gas collecting pipe (52) is provided at the center of the top. Support feet (512) are arranged in a ring and are connected to the bottom edge of the conical gas collecting hood (511) and the inner wall of the cylindrical reaction tower (2); The flow guide ribs (513) are arranged in a ring and are fixed on the inner wall of the conical gas collection hood (511); The high-pressure air chamber (514) is located between the opening of the conical air collecting hood (511) and the guide rib (513), and the bottom of the air collecting pipe (52) is located inside the high-pressure air chamber (514).

6. The micro / nano bubble oxidation reactor for wastewater treatment according to claim 5, characterized in that: There is a gap between the bottom edge of the conical gas collecting hood (511) and the inner wall of the cylindrical reaction tower (2), and the gap between the bottom edge of the conical gas collecting hood (511) and the inner wall of the cylindrical reaction tower (2) in the multiple self-pressure circulation units (5) from bottom to top gradually decreases.

7. The micro / nano bubble oxidation reactor for wastewater treatment according to claim 5, characterized in that: The diffusion debubbling component (55) includes: The diffuser head (551) is a tapered flared part, fixed to the bottom of the guide tube (54); Multiple bubble-breaking fins (552) are provided, which are distributed in a cross pattern, and the center of the intersection of multiple bubble-breaking fins (552) coincides with the central axis of the diffuser head (551); The double-toothed ring (553) has toothed channels on both the inner and outer sides and is fixed in the middle of the bubble-breaking fin (552); An auxiliary microporous plate (554) is fixed to the bottom of the diffuser head (551), and its inner side is attached to the bubble-breaking fin (552).

8. The micro / nano bubble oxidation reactor for wastewater treatment according to claim 1, characterized in that: The gas-liquid separation device (6) includes: An inverted conical gas-liquid separation hood (61) is set above the self-pressurized circulation unit (5), with an opening at the center of the bottom; The fasteners (62) are arranged in a ring and are fixedly connected to the bottom edge of the inverted conical gas-liquid separation hood (61) and the inner wall of the cylindrical reaction tower (2); An annular crushing grid (63) is fixed on the outer wall of an inverted conical gas-liquid separator (61).

9. The micro / nano bubble oxidation reactor for wastewater treatment according to claim 8, characterized in that: The inlet end of the drainage pipe (7) is in contact with the inner wall of the inverted conical gas-liquid separator (61), and the bottom of the pipe is higher than the position of the annular crushing grid (63).

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