Multistage enhanced mixed micro vortex flocculation device

Abstract

The present application relates to the technical field of water treatment, and particularly relates to a multi-stage reinforced mixed micro-vortex flocculation device. The multi-stage reinforced mixed micro-vortex flocculation device comprises a mixing unit and a flocculation unit arranged in series, the mixing unit comprises an outer cylinder, an inner cylinder, a flow guide assembly, a flow disturbance assembly, a mixing and stirring assembly and the like, a first mixing area is formed at the junction of a first accommodating cavity and a second accommodating cavity in the outer cylinder, a second mixing area is formed in a third accommodating cavity, and a third mixing area is formed between the inner wall of the first cylinder and the outer wall of the inner cylinder; the flocculation unit comprises a shell with a fourth accommodating cavity and at least one set of flocculation units arranged in the fourth accommodating cavity. The multi-stage reinforced mixed micro-vortex flocculation device has a compact and simple overall structure, can improve the flocculation reaction flow field, strengthen the flocculation reaction power, greatly improve the mixed flocculation reaction effect and efficiency, reduce the demand for coagulants, shorten the flocculation reaction time, and improve the sedimentation performance of flocs while promoting the mixing mass transfer.

Description

Technical Field

[0001] This invention relates to the field of water treatment technology, specifically to a multi-stage enhanced mixing micro-vortex flocculation device. Background Technology

[0002] Coagulation is one of the most core and commonly used processes in water treatment, combining mixing and flocculation. The mixing process involves fully and uniformly dispersing the coagulant into the water body. The effluent from the mixing process then enters the flocculation process, where, under external force, tiny particles and reagent molecules in the raw water collide and come into contact with each other. Through a combination of factors including pressure double layer, adsorption-electrochemical neutralization, adsorption bridging, network compensation-sweeping, and Brownian motion, these particles continuously aggregate and form larger, denser flocs, thereby separating and removing pollutants from the raw water. The uniformity of coagulant mixing in the raw water significantly impacts the flocculation effect, while favorable hydraulic conditions in the flocculation process also greatly promote the contact and collision between micro-flocs.

[0003] Flocculation processes are divided into hydraulic flocculation and mechanical flocculation. Among hydraulic flocculation processes, baffle flocculation is the most widely used. Baffle flocculation utilizes multiple sets of baffles installed in the pool to create vortices in the water flow, creating a turbulent and swirling flow pattern to achieve particle collision and floc growth. Baffle flocculation has advantages such as good flocculation effect, short flocculation time, small footprint, no energy consumption, and low operating cost. In engineering, the average G-value of the flocculation pool, calculated using Camp theory and formulas, is generally used to characterize the turbulence intensity of the water flow in the flocculation pool. However, the average G-value only represents the spatial average energy dissipation rate and cannot reflect the local energy dissipation rate of the flow field. Modern flocculation theory proposes using vortex G-values ​​instead of average G-values ​​to more accurately characterize the flocculation effect. Kolmgoroff's micro-vortex theory proposes that the larger the vortex G-value, the smaller the vortex size generated in the fluid; conversely, the smaller the vortex G-value, the larger the vortex size generated. When the vortex size is close to the floc size, the flocculation reaction is most complete and the flocculation effect is optimal. When the vortex size exceeds this value, the turbulence of the water flow is insufficient to provide the energy required for flocculation. Conversely, when the vortex size is below this value, excessive water flow shear force will shear and break up the flocs. Studies have shown that the initial formation size and later formation size of the flocs are respectively 1×10 -5 m and 6×10 -4 The vortex size of the flocculation tank is approximately 1 × 10 m, meaning the vortex size ranges from 1 × 10 m. -5 m gradually increases to 6×10 -4 The flocculation effect is best at m. In traditional folded plate flocculation tanks, the vortex size of the relative folded plate section and the parallel folded plate section is basically concentrated at 1×10. -4 Up to 2×10 -4 Between m, and the initial size of the flocculent is 1×10. -5 The relatively large size of m limits its ability to improve the efficiency and effectiveness of the initial flocculation reaction.

[0004] In current coagulation processes, there is another type that uses forced recirculation of sludge from the sedimentation zone to the flocculation zone to enhance the coagulation effect. A typical example is the high-density sedimentation tank. The high-density sedimentation tank consists of mechanical mixing, mechanical flocculation, inclined tube sedimentation, sludge thickening, and a sludge recirculation and discharge system. The sludge recirculation system forces a portion of the sludge from the sedimentation zone back to the flocculation zone. A lift-type mixer and a guide tube are installed in the flocculation zone, causing the influent with added coagulant and the recirculated sludge to continuously circulate within the flocculation zone. This increases the sludge concentration for the flocculation reaction, improves the probability of floc collision, increases the removal rate of small flocs, provides floc nuclei for the reaction, and increases the density and settling performance of the flocs, resulting in more stable effluent quality. However, this process cannot sort the recirculated sludge flocs to remove silt and larger, denser flocs, preventing them from settling in the flocculation tank. Such flocs not only do not improve the flocculation effect but will also deposit and harden at the bottom of the tank over long-term operation, affecting the effective flocculation volume and retention time.

[0005] In summary, there is an urgent need for a device with a simplified structure and high flocculation reaction efficiency to solve the problems existing in the current technology. Summary of the Invention

[0006] The purpose of this invention is to provide a multi-stage enhanced mixing micro-vortex flocculation device with a simplified structure and high flocculation reaction efficiency. The specific technical solution is as follows:

[0007] A multi-stage enhanced mixing micro-vortex flocculation device includes a mixing unit and a flocculation unit arranged in series. The mixing unit includes an outer cylinder, an inner cylinder, a turbulence-inducing component, a mixing and stirring component, a first water inlet, a sludge inlet, and a first sludge outlet. The outer cylinder includes a first cylinder and a second cylinder arranged in series from top to bottom. The first cylinder includes a first receiving cavity with a lower opening, and the second cylinder includes a second receiving cavity with an upper opening and communicating with the first receiving cavity. A first mixing region is formed at the junction of the first and second receiving cavities, and a first water inlet for tangential feeding is provided at this junction. The system includes a sludge inlet; an outlet zone at the top of the first receiving cavity; a first sludge accumulation zone at the bottom of the second receiving cavity; a sludge outlet connected to the first sludge accumulation zone; an inner cylinder disposed within the first receiving cavity, located between the outlet zone and the first mixing zone; the inner cylinder including a third receiving cavity with openings at both the top and bottom, forming a second mixing zone within the third receiving cavity; a mixing and stirring assembly partially disposed within the second mixing zone; a third mixing zone formed between the inner wall of the first cylinder and the outer wall of the inner cylinder, with the turbulence-inducing assembly disposed within the third mixing zone.

[0008] The flocculation unit includes a shell with a fourth receiving cavity and at least one set of flocculation units disposed in the fourth receiving cavity; the fourth receiving cavity is connected to the effluent zone, and a second effluent outlet is provided on the other side of the shell opposite to the effluent zone; a second sludge accumulation zone is provided at the lower part of the fourth receiving cavity, and a second sludge discharge outlet is provided on the shell that is connected to the second sludge accumulation zone.

[0009] Preferably, the sludge inlet is positioned such that the first inlet is rotated 90° circumferentially around the first mixing area; a dosing pipe is provided on the pipeline connected to the first inlet; the outer cylinder of the mixing unit and the shell of the flocculation unit share the same side wall, and the fourth receiving cavity is connected to the effluent area through a notch on the side wall; or, the outer cylinder of the mixing unit has a first effluent outlet on its side wall, and the shell has a second inlet connected to the fourth receiving cavity on its side wall, and the second inlet is connected to the effluent area through the first effluent outlet.

[0010] Preferably, a flow guiding component is provided in the first receiving cavity and located between the first mixing region and the second mixing region; the flow guiding component includes an annular flow guiding component and a conical flow guiding component, the annular flow guiding component is disposed on the inner wall of the first receiving cavity, the conical flow guiding component is located in the middle part of the first receiving cavity, and the gap between the annular flow guiding component and the conical flow guiding component forms a flow channel.

[0011] Preferably, the aerodynamic component includes multiple first aerodynamic plates spaced apart circumferentially along the inner cylinder, each first aerodynamic plate including multiple folded plates arranged in series; adjacent first aerodynamic plates have the same structure or are mirror images of each other; or, the aerodynamic component includes multiple second aerodynamic plates spaced apart circumferentially along the inner cylinder, each second aerodynamic plate including a connecting rod and multiple barbs arranged along the length of the connecting rod; the barbs on adjacent second aerodynamic plates are symmetrically arranged or staggered vertically.

[0012] Preferably, the mixing assembly includes a power source, a mixing shaft, and lifting mixing blades. The power source is disposed on the outer cylinder. The connecting end of the mixing shaft is connected to the output end of the power source, and its free end is inserted into the second mixing region. The lifting mixing blades are located in the second mixing region and are disposed on the free end of the mixing shaft.

[0013] Preferably, the first water inlet and / or sludge inlet is provided with a diversion device; the diversion device includes an arc-shaped diversion plate for dispersing the water flow from the first water inlet and / or sludge inlet.

[0014] Preferably, the system further includes a cutting assembly disposed within the second mixing region; the cutting assembly includes multiple cutting strips, the connecting ends of the cutting strips being connected to the inner wall of the second mixing region, and the free ends of the cutting strips being inclined upwards; the cutting strips are arranged at an angle of 45°-75° to the inner wall surface of the second mixing region.

[0015] Preferably, along the water flow direction, the flocculation unit includes a first flocculation section, a second flocculation section, and a third flocculation section arranged sequentially; the first flocculation section includes at least two first flocculation plates arranged at intervals, each first flocculation plate including a connecting plate connected sequentially with a wave crest forming at the connection point, adjacent connecting plates being arranged at an angle α, and the wave crests of two adjacent first flocculation plates being arranged facing each other; a first flocculation channel is formed between two adjacent first flocculation plates;

[0016] The second flocculation section includes at least two second flocculation plates spaced apart. Each second flocculation plate includes a connecting plate that is connected sequentially and forms a wave crest at the connection point. Adjacent connecting plates are arranged at an angle α, and the wave crests of two adjacent second flocculation plates have the same orientation. A second flocculation channel is formed between two adjacent first flocculation plates.

[0017] The third flocculation section includes at least two third flocculation plates spaced apart, the third flocculation plates being straight plates and / or curved plates; a third flocculation channel is formed between two adjacent third flocculation plates.

[0018] Preferably, the first flocculation section and / or the second flocculation section are further provided with a micro vortex assembly; the micro vortex assembly includes one or multiple micro vortex elements spaced apart along the water flow direction; the micro vortex elements include a top micro vortex plate, a middle micro vortex plate, and a bottom micro vortex plate arranged in parallel and each provided with vortex flow holes, wherein the opening ratio of the vortex flow holes on the top micro vortex plate is P1, the opening ratio of the vortex flow holes on the middle micro vortex plate is P2, and the opening ratio of the vortex flow holes on the bottom micro vortex plate is P3, and P1 > P2 > P3; the value range of P1 is 35%-45%, the value range of P2 is 30%-40%, and the value range of P3 is 25%-35%.

[0019] Preferably, the diameters of the vortex flow holes on the top, middle, and bottom microvortex plates within a single microvortex component are all the same; a single microvortex component may have one middle microvortex plate or at least two middle microvortex plates arranged in parallel; the diameter range of the vortex flow holes is 50–150 mm; along the water flow direction, the diameter of the vortex flow holes in the microvortex component increases sequentially.

[0020] The application of the technical solution of the present invention has the following beneficial effects:

[0021] (1) The multi-stage enhanced mixing micro-vortex flocculation device of the present invention includes a mixing unit and a flocculation unit arranged in series. The mixing unit includes an outer cylinder, an inner cylinder, a flow guiding component, a flow turbulence component, a mixing and stirring component, etc. A first mixing region is formed at the junction of the first and second accommodating cavities in the outer cylinder, and a water inlet and a sludge inlet for feeding in a tangential manner are provided at the junction. A first sludge accumulation region is formed in the lower part of the second accommodating cavity. The inner cylinder is disposed in the first accommodating cavity, and a second mixing region is formed in the third accommodating cavity. The mixing and stirring component is disposed in the second mixing region to provide upward power for the flow of fluid in the second mixing region. The flow guiding component is disposed in the first accommodating cavity and located between the first and second mixing regions. A third mixing region is formed between the inner wall of the first cylinder and the outer wall of the inner cylinder, and the flow turbulence component is disposed in the third mixing region. The flocculation unit includes a shell with a fourth accommodating cavity and at least one set of flocculation units disposed in the fourth accommodating cavity. A second sludge accumulation region is provided in the lower part of the fourth accommodating cavity, and a second sludge discharge port communicating with the second sludge accumulation region is provided on the shell. The water to be treated first enters the mixing unit for treatment. Under the multi-stage mixing action of swirling mixing in the first mixing zone, mechanical mixing in the second mixing zone, micro-vortex mixing in the third mixing zone, and circulating flow mixing in the second and third mixing zones, the water to be treated, coagulant, and returned sludge undergo sufficient contact and collision. The reagents and sludge are recycled, which helps to improve the mixing reaction effect and efficiency, strengthen the mixing process's resistance to shock loads, reduce the amount of reagents added, and lower operating costs. The fully mixed water directly and quickly enters the flocculation unit. Under the combined action of baffles, swirling flow, and micro-vortexes, the turbulence intensity in the water can be increased, providing sufficient reaction power for floc collision, aggregation, and growth. A large number of micro-vortices of various scales can be generated, increasing the capture rate of small flocs and the utilization rate of coagulant, providing the most suitable hydraulic conditions for each stage of the flocculation reaction. It can also provide a large number of floc nuclei for the flocculation reaction, improving flocculation density and settling performance. Thorough mixing of the water to be treated, coagulant, and returned sludge is a prerequisite for ensuring flocculation effect. Good hydraulic conditions and sufficient reaction kinetics are key to ensuring flocculation effect. The device has a compact and simplified overall structure. While promoting mixing and mass transfer, it improves the flocculation reaction flow field and enhances the flocculation reaction kinetics, which can significantly improve the mixing and flocculation reaction effect and efficiency, reduce the demand for coagulant, shorten the flocculation reaction time, and improve the sedimentation performance of flocs.

[0022] (2) A first mixing zone is set in the lower middle part of the outer cylinder of the mixing unit, a second mixing zone and a third mixing zone are set in the upper middle part of the outer cylinder, and an outlet zone is set in the upper part of the outer cylinder. The water flows from bottom to top. The water to be treated, coagulant and sludge all enter the first mixing zone in a clockwise direction along the circumference tangent of the outer cylinder. The influent and return sludge with high flow velocity form a horizontal vortex in the first mixing zone. The components in the first mixing zone are relatively complex. Wastewater is mixed through swirling and centrifugal forces, while its components are separated and sorted. Large particles and heavy materials are centrifuged and transferred to the bottom sludge accumulation zone, while smaller, lighter components flow into the top second and third mixing zones to continue the reaction. This effectively reduces the participation of ineffective substances in the mixing reaction, improving mixing efficiency, increasing the utilization rate of coagulants, and preventing the deposition and caking of silt and sludge flocs in the system. The returned sludge provides numerous floc nuclei for mixing and flocculation, significantly increasing the probability of particle collisions, improving the density of flocs, and enhancing floc settling performance. Sludge accumulation zones are located at the bottom of the mixing and flocculation units to facilitate the separation of large particles and heavy materials to these zones and their discharge from the system.

[0023] (3) The present invention also includes a flow guiding component, which includes an annular flow guiding unit and a conical flow guiding unit. The flow guiding component separates the first mixing area located below from the second and third mixing areas located above into two relatively independent reaction zones, which do not affect or interfere with each other, ensuring the optimal conditions and efficient operation of each mixing area. At the same time, it can precisely control the water flow in the second and third mixing areas to promote the formation of circulating flow and reduce the ineffective energy dissipation of the mechanical circulating mixing system.

[0024] (4) In this invention, the turbulence component includes multiple folded turbulence components spaced apart circumferentially along the inner cylinder, or the turbulence component includes multiple barbed turbulence components spaced apart circumferentially along the inner cylinder. Through the unique structure of the turbulence component, a large number of micro-vortices with a scale close to flocs are generated in the water flow or the water flow velocity vector is continuously changed, creating a strong turbulence state, providing sufficient turbulence intensity, increasing and strengthening the collision between particles, coagulants and return sludge in the water flow, and further enhancing the mixing effect; at the same time, the energy provided by the mechanical circulation mixing system is fully used for the mixing reaction, and the energy is also efficiently utilized again.

[0025] (5) The mixing and stirring assembly in this invention includes a power source, a stirring shaft, and lifting stirring blades. In addition to its mechanical mixing function, the mixing and stirring assembly in the second mixing zone provides sufficient power for the water flow from the first mixing zone into the second and third mixing zones, as well as for the circulation within each mixing zone. Simultaneously, by adjusting the operating frequency and speed of the mixing and stirring assembly, the required circulating water flow rate and the flow velocity in the third mixing zone can be ensured, thereby improving the capture of small flocs, enhancing the mixing effect, and increasing the resistance to shock loads. Furthermore, the lifting stirring blades can break up larger floc particles in the water flow, cutting them and forming smaller flocs with a relatively uniform particle size. This creates more floc nuclei that can effectively participate in subsequent flocculation reactions, effectively increasing contact collision coagulation and netting effects, improving the subsequent flocculation reaction effect, increasing the removal rate of small particles and flocs in the water, and improving the settling performance of the flocs. At the same time, by adjusting the speed of the mixing and stirring assembly, the particle size distribution of the small floc nuclei can be optimized and controlled, further enhancing the improvement effect on subsequent flocculation reactions.

[0026] (6) In this invention, a diversion device is provided on the first water inlet and / or sludge inlet. The diversion device can disperse the incoming water flow in the height direction, so as to form a vortex in the entire height direction of the first mixing area, improve the effective utilization rate of the internal volume of the device, and at the same time avoid the ineffective consumption of kinetic energy and the destruction of the vortex in the first mixing area when the incoming water flow is directly mixed with the internal vortex.

[0027] (7) The second mixing area of ​​the present invention is also provided with a cutting component, which includes multiple cutting strips. The unique cutting component, combined with the mixing and stirring component, further cuts the larger flocs.

[0028] (8) The flocculation unit in this invention includes a first flocculation section, a second flocculation section and a third flocculation section arranged in sequence. The first flocculation section is a relatively folded plate structure, the second flocculation section is a parallel folded plate structure and the third flocculation section is a straight plate or arc plate structure. A micro vortex component is provided in the first flocculation section and / or the second flocculation section. After the water enters the flocculation unit, it flows up and down in sequence and continuously passes through the micro vortex unit. The up and down flow causes the flocs in the water to have initial collisions and contacts. Then, through the swirling effect generated by the continuous expansion and contraction of the folded plate, the flocs quickly coagulate and grow. Furthermore, the collision and coagulation are further enhanced under the action of the micro vortex generated by the micro vortex component. The combined effects of flow deflection, swirling flow, and micro-eddies generated by the water flow improve the hydraulic conditions of the flocculation reaction inside the device, increase the turbulence intensity of the water flow, and provide sufficient reaction power for floc collision, aggregation, and growth. At the same time, the large number of micro-eddies generated can promote the collision and aggregation of residual micro-flocs in the water, increase the capture rate of micro-flocs and the utilization rate of coagulants, and further improve the flocculation reaction effect and efficiency.

[0029] (9) Setting up flocculation units with smaller pore size and opening ratio in the relatively folded plate section and in the parallel folded plate section can form micro vortices with relatively small scale, relatively large turbulent energy and relatively strong disturbance in the relatively folded plate section and micro vortices with relatively large scale, relatively small turbulent energy and relatively weak disturbance in the parallel folded plate section. This provides the best flocculation hydraulic conditions for each flocculation stage, maximizes the fit with the microscopic mechanism of floc growth, can greatly improve the flocculation reaction efficiency and effect, reduce flocculation time and reduce the amount of flocculant added.

[0030] In addition to the objectives, features, and advantages described above, the present invention has other objectives, features, and advantages. The invention will now be described in further detail with reference to the figures. Attached Figure Description

[0031] The accompanying drawings, which form part of this application, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an undue limitation of the invention. In the drawings:

[0032] Figure 1 This is a schematic diagram of the structure of the multi-stage enhanced hybrid micro-vortex flocculation device in an embodiment of the present invention;

[0033] Figure 2 yes Figure 1 Top view;

[0034] Figure 3 yes Figure 1 Schematic diagram of the structure of the hybrid unit;

[0035] Figure 4 yes Figure 1 Cross-sectional view of the first mixed region in the middle;

[0036] Figure 5 yes Figure 1 Cross-sectional view of the central spoiler component when it is a single folded plate spoiler;

[0037] Figure 6 yes Figure 5 A partial schematic diagram of the unfolded single component of the central folding plate airflow disturbance;

[0038] Figure 7 yes Figure 1 Cross-sectional view of the central spoiler component when it is a single barbed spoiler piece;

[0039] Figure 8 yes Figure 7 A partial schematic diagram of the unfolded single component of the central folding plate airflow disturbance;

[0040] Figure 9 This is a schematic diagram of the combined structure of the inner cylinder and the cutting assembly;

[0041] Figure 10 yes Figure 1 A schematic diagram of the unfolded structure of the diversion device in the diagram;

[0042] Figure 11 yes Figure 1 A schematic diagram of the micro-vortex unit located in the first flocculation section;

[0043] Figure 12 yes Figure 11 A schematic diagram of the unfolded structure of the top microvortex plate in the image;

[0044] Figure 13 yes Figure 11 A schematic diagram of the unfolded structure of the central microvortex plate;

[0045] Figure 14 yes Figure 11 A schematic diagram of the unfolded structure of the bottom microvortex plate;

[0046] Among them, 1. Mixing unit, 1.1 Outer cylinder, 1.1.1 First cylinder, 1.1.2 Second cylinder, 1.1.3 Movable cover plate, 1.2 Inner cylinder, 1.2.1 Upper cylinder, 1.2.2 Lower cylinder; 1.3 Flow guiding assembly, 1.3.1 Annular flow guiding component, 1.3.2 Conical flow guiding component; 1.4 Flow turbulence assembly, a. First turbulence plate, a1. Baffle plate; b. Second turbulence plate, b1. Connecting rod, b2, barbs; 1.5, Mixing and stirring assembly, 1.5.1, Power source, 1.5.2, Stirring shaft, 1.5.3, Lifting and stirring blades; 1.6, Cutting assembly, 1.6.1, Cutting strips; 1.7, First water inlet; 1.8, Sludge inlet; 1.9, First water outlet; 1.10, First sludge outlet; 1.11, Dosing pipe; 1.12, Upper support frame; 1.13, Lower support frame; 1.14, Divider 1. Flow device; 2. Flocculation unit, 2.1. Shell, 2.2. Flocculation component, 2.2.1. First flocculation plate, 2.2.2. Second flocculation plate, 2.2.3. Third flocculation plate, 2.3. Side wall, 2.4. Second outlet, 2.5. Second sludge outlet, 2.6. Micro-vortex component, 2.6.1. Top micro-vortex plate, 2.6.2. Middle micro-vortex plate, 2.6.3. Bottom micro-vortex plate, 2.6.4. Support pipe 2.6.5 Extension plate; 2.6.6 Bolt hole; 3. Main sludge discharge pipe; E. Micro vortex forming hole; F. Bend line; H1. First mixing zone; H2. Second mixing zone; H3. Third mixing zone; H4. Effluent zone; H5. First sludge aggregation zone; H6. Second sludge aggregation zone; H7. First flocculation channel; H8. Second flocculation channel; H9. Third flocculation channel; H10. Flow channel; H11. Effluent channel. Detailed Implementation

[0047] The embodiments of the present invention will be described in detail below with reference to the accompanying drawings. However, the present invention can be implemented in many different ways as defined and covered by the claims.

[0048] Example:

[0049] A multi-stage enhanced hybrid micro-vortex flocculation device includes a mixing unit 1 and a flocculation unit 2 arranged in series, as detailed below:

[0050] The mixing unit 1 includes an outer cylinder 1.1, an inner cylinder 1.2, a flow guiding assembly 1.3, a flow turbulence assembly 1.4, a mixing and stirring assembly 1.5, a cutting assembly 1.6, a first water inlet 1.7, a sludge inlet 1.8, a first water outlet 1.9, a first sludge outlet 1.10, and a dosing pipe 1.11. See details below. Figures 1-14 Details are as follows:

[0051] The outer cylinder 1.1 includes a first cylinder 1.1.1 and a second cylinder 1.1.2 connected in series from top to bottom. The first cylinder 1.1.1 includes a first receiving cavity with an opening at the lower end, and the second cylinder 1.1.2 includes a second receiving cavity with an opening at the upper end and communicating with the first receiving cavity. A first mixing region H1 is formed at the junction of the first receiving cavity and the second receiving cavity, and a first water inlet 1.7 and a sludge inlet 1.8 for tangential feeding are provided at this junction. See details. Figure 1 and Figure 3 In this embodiment, the first cylinder 1.1.1 is a cylindrical body, which is constructed by chamfering the four corners of the inside of the cylinder using bricks and plain concrete, ultimately building a cylindrical body with a diameter of 3m and a total height of 5.65m inside. The top of the first cylinder 1.1.1 has an opening, which is sealed with a movable cover plate 1.1.3. The second cylinder 1.1.2 is a frustum cylinder, with the same inner diameter at its upper end as that of the first cylinder 1.1.1, and the inner diameter at its bottom being 0.6-0.8 times that of its top. The bottom of the second cylinder is sealed.

[0052] The first inlet 1.7 and the sludge inlet 1.8, which adopt a tangential feeding method, are specifically positioned such that the sludge inlet 1.8 is located 90° circumferentially around the first mixing zone H1, with the inlet 1.7 being the same as the first inlet 1.7. See details... Figure 2 and Figure 4A dosing pipe 1.11 is installed on the pipeline connected to the first inlet 1.7 (the dosing pipe is located near the first inlet). The water to be treated, coagulant, and sludge all enter the first mixing zone H1 in a clockwise direction along the circumferential tangent of the outer cylinder 1.1. Utilizing the high flow velocity of the influent and the returned sludge, a horizontal vortex is formed in the first mixing zone H1, mixing the influent, coagulant, and sludge. Unreacted reagent molecules in the returned sludge, as well as unbound sites on the flocs, can participate in the mixing reaction again, realizing the secondary utilization of the reagent and the resource recovery of the sludge.

[0053] In this preferred embodiment, the first water inlet 1.7 and the sludge inlet 1.8 are further provided with a diversion device 1.14, which includes an arc-shaped diversion plate, as detailed in [link to documentation]. Figure 2 , Figure 4 and Figure 10 The connecting end of the arc-shaped diversion plate is fixedly connected to the inner wall of the first mixing zone H1. The free end of the arc-shaped diversion plate is cantilevered, and the distance between the free end of the arc-shaped diversion plate and the inner wall of the first mixing zone H1 is 1 / 2 to 2 / 3 of the diameter of the corresponding first inlet 1.7 or sludge inlet 1.8. The height of the arc-shaped diversion plate is 3 times the diameter at that point. The vertical center of the diversion device 1.14 is aligned with the center line of the corresponding first inlet 1.7 or sludge inlet 1.8. The specific principle is: control the inlet water and sludge inlet directions to be clockwise or counterclockwise, and control the flow velocity of the inlet water and sludge inlet to be ≥1.5m / s, forming a swirling flow on a horizontal plane in the first mixing zone, constructing a swirling mixing zone, and mixing the inlet water, coagulant and sludge for the first time through the swirling action. The diversion device 1.14 disperses the water flow entering the first mixing zone H1 in the height direction, causing a vortex to form throughout the entire height direction of the first mixing zone H1, improving the effective utilization rate of the internal volume of the device, and at the same time avoiding the ineffective consumption of kinetic energy and the destruction of the vortex when the incoming water flow is directly mixed with the internal vortex.

[0054] The inner cylinder 1.2 is disposed within the first receiving cavity and located below the water outlet zone H4. The inner cylinder 1.2 includes a third receiving cavity with openings at both the top and bottom, forming a second mixing region H2 within the third receiving cavity. The mixing and stirring assembly 1.5 is partially disposed within the second mixing region H2 to provide upward force for the flow of fluid within the second mixing region H2. In this embodiment, the inner cylinder 1.2 includes an upper cylinder 1.2.1 and a lower cylinder 1.2.2 arranged in series. The upper cylinder is a cylindrical cylinder, and the lower cylinder is a frustum cylinder that is narrower at the top and wider at the bottom (i.e., a flared structure that is narrower at the top and wider at the bottom). The inner diameter of the cylindrical cylinder is the same as the inner diameter of the upper end of the frustum cylinder. The cylindrical inner cavity of the upper cylinder and the frustum inner cavity of the lower cylinder form the third receiving cavity. The mixing and stirring assembly 1.5 is partially located within the upper cylinder 1.2.1, and the turbulence-inducing assembly 1.4 is disposed at the same height as the upper cylinder 1.2.1 on its outer wall. In this embodiment, the central axes of the outer cylinder 1.1 and the inner cylinder 1.2 overlap. Specifically, the first accommodating cavity, the second accommodating cavity, and the third accommodating cavity are arranged along the same central axis. The diameter of the inner cylinder 1.2 is always smaller than the diameter of the outer cylinder 1.1, and the inner cylinder 1.2 is installed in the upper-middle position inside the outer cylinder 1.1.

[0055] The inner wall of the inner cylinder 1.2 is fully covered with cutting components 1.6, each of which includes multiple cutting strips 1.6.1, as detailed below. Figure 1 , Figure 3 and Figure 9 The connecting end of the cutting strip 1.6.1 is connected to the inner wall of the second mixing region H2, and its free end is inclined upward. The included angle β between the cutting strip 1.6.1 and the inner wall of the second mixing region H2 is set at 45°-75°. In this embodiment, the multiple cutting strips 1.6.1 are composed of numerous fine needles arranged in a disordered manner. One end of the fine needle is connected and fixed to the inner wall of the inner cylinder 1.2, and the other end is inclined upward at a 60° angle to the vertical. The length L of the fine needle is 1 / 8 to 1 / 6 of the diameter and does not exceed 200mm. When larger floc particles in the water flow collide with the cutting component 1.6 during their ascent, they will be cut into smaller flocs.

[0056] The mixing and stirring assembly 1.5 is located at the central axis of the upper cylinder 1.2.1, and includes a power source 1.5.1, a stirring shaft 1.5.2, and lifting and stirring blades 1.5.3, as detailed below. Figure 1 , Figure 2 and Figure 3The power source 1.5.1 is mounted on the outer cylinder 1.1 (in this embodiment, the power source 1.5.1 is mounted on the movable cover plate 1.1.3); the connecting end of the stirring shaft 1.5.2 is connected to the output end of the power source 1.5.1, and its free end is inserted into the second mixing zone H2; the lifting stirring blade 1.5.3 is located in the second mixing zone H2 and is mounted on the free end of the stirring shaft 1.5.2. The lifting stirring blade 1.5.3 can be a single layer or two or more layers spaced apart along the height direction of the stirring shaft 1.5.2. In this embodiment, the power source 1.5.1 consists of a motor and a reducer, and the lifting stirring blade 1.5.3 is located in the middle of the inner cylinder 1.2. Under the stirring and lifting action generated by the mixing and agitating assembly 1.5, the water flows from bottom to top inside the inner cylinder 1.2 (i.e., within the second mixing zone H2), flows out from the top, passes through the third mixing zone H3 from top to bottom, and returns to the bottom of the inner cylinder 1.2 to re-enter the second mixing zone H2, forming a circulating flow. The mechanical mixing and lifting action of the mixing and agitating assembly 1.5 performs a second mixing of the influent, coagulant, and sludge, providing sufficient power for the mixing reaction and circulating flow. This ensures the circulating water volume and the water flow velocity in the third mixing zone H3, improves the mixing effect and mass transfer efficiency, extends the mixing reaction time, and enhances the device's resistance to shock loads. The rotation speed of the power source of the mixing and agitating assembly 1.5 can be adjusted according to the actual mixing effect, making it suitable for different influent water volumes and qualities.

[0057] The lifting and stirring blades 1.5.3 in the second mixing zone H2 can also break up larger floc particles in the water flow. Combined with the cutting component 1.6, these larger flocs are cut into smaller flocs of similar size, forming more floc nuclei that can effectively participate in subsequent flocculation reactions. This effectively increases contact collision agglomeration and trapping effects, improving the subsequent flocculation effect, increasing the removal rate of small particles and flocs in the water, and improving the settling performance of the flocs. Simultaneously, by adjusting the rotation speed of the power source 1.5.1, the particle size distribution of the small floc nuclei can be optimized and controlled to further enhance the improvement effect on subsequent flocculation reactions.

[0058] The upper end of the inner cylinder 1.2 is mounted on the upper part of the inner wall of the first receiving cavity via an upper support frame 1.12, and the lower end of the inner cylinder 1.2 is mounted on the lower part of the inner wall of the first receiving cavity via a lower support frame 1.13. See details. Figure 3In this preferred embodiment, the upper support frame 1.12 and the lower support frame 1.13 are each made of eight channel steels evenly arranged along the axial direction of the cross-section of the outer cylinder 1.1. The two ends of the channel steels are welded to the inner wall of the outer cylinder 1.1 and the outer wall of the inner cylinder 1.2, respectively, firmly fixing the inner cylinder 1.2 within the device. The upper end of the upper support frame 1.12 is flush with the upper end of the upper cylinder 1.2.1 within the inner cylinder 1.2, and the lower end of the lower support frame 1.13 is flush with the lower end of the upper cylinder 1.2.1 within the inner cylinder 1.2.

[0059] A third mixing region H3 is formed between the inner wall of the first cylinder 1.1.1 and the outer wall of the inner cylinder 1.2, and the turbulence-inducing component 1.4 is disposed within the third mixing region H3. In this embodiment, the third mixing region H3 is an annular flow channel formed between the outer wall of the inner cylinder 1.2 and the inner wall of the outer cylinder 1.1. The turbulence-inducing component 1.4 is uniformly distributed within this annular flow channel, and the filling height of the turbulence-inducing component 1.4 is consistent with that of the upper cylinder 1.2.1 in the inner cylinder 1.2. The two ends of the turbulence-inducing component 1.4 are respectively fixed to the outer wall of the inner cylinder 1.2 and the inner wall of the outer cylinder 1.1 by welding or expansion bolts. As the water flows from top to bottom through the turbulence-inducing component 1.4, it can cause disturbance in the water flow, creating a turbulent hydraulic flow state. Through micro-eddies and turbulence, the collision between particles, coagulants, and return sludge in the water flow is increased and enhanced, resulting in a third mixing.

[0060] The turbulence-disrupting component 1.4 has two structural options, as follows:

[0061] The first type: The turbulence assembly 1.4 includes multiple first turbulence plates a spaced apart circumferentially along the inner cylinder 1.2. Each first turbulence plate includes multiple folded plates a1 arranged in series. See details. Figure 5 and Figure 6 The two adjacent first baffles a have the same structure or are mirror images of each other. In this embodiment, the first baffles a are all arranged vertically, and the connection points (i.e., plate peaks) of the folded plates a1 in the two adjacent first baffles a are arranged opposite each other, dividing the annular flow channel into multiple fan-shaped relative folded plate flow channels. Under the action of the relative folded plates, the water flow can form numerous micro-vortices of various sizes inside, which can effectively improve the collision and coagulation between particles, agents, and flocs. The height of the folded plates is the same as the height of the equal-diameter part of the inner cylinder. The two ends are fixed to the outer wall of the inner cylinder and the inner wall of the outer cylinder of the device by welding or expansion bolts. The specific specifications, the included angle between the folded plates, and the number of installations are determined according to the actual size of the device. It is advisable to control the average flow velocity of each fan-shaped flow channel to be ≥0.4m / s to ensure sufficient turbulence intensity and improve the mixing effect.

[0062] The second type: The turbulence assembly 1.4 includes multiple second turbulence plates b spaced circumferentially along the inner cylinder 1.2. Each second turbulence plate b includes a connecting rod b1 and multiple spikes b2 arranged along the length of the connecting rod. See details. Figure 7 and Figure 8 The barbs b2 on adjacent second spoiler bs are symmetrically arranged or staggered vertically. In this embodiment, the connecting rod b1 is round steel, and the barbs b2 are angle steel. Specifically, the second spoiler b is composed of multiple barbs b2 arranged equidistantly in a vertical direction, with all corners of the barbs b2 facing upwards. The ends of two adjacent barbs b2 are welded and fixed by connecting rods b1 of the same length. Multiple sets of second spoiler bs are evenly arranged along the circumferential axis of the cross section of the outer cylinder 1.1. The height of the second spoiler b is consistent with the height of the upper cylinder 1.2.1 in the inner cylinder. Since the connecting rods b1 and barbs b2 in each set of second spoiler b are already firmly welded, each set of second spoiler b only needs to be connected and fixed to the outer wall of the inner cylinder 1.2 and the inner wall of the outer cylinder 1.1 through the two ends of the top barbs b2 respectively. The second baffle plate continuously alters the velocity and direction of the water flow, increasing turbulence intensity and thus enhancing collisions between particles, chemicals, and flocs, promoting particle coagulation. Furthermore, the two adjacent angle steel elements are staggered in height to further agitate the water flow using the second baffle plate. The specific specifications of the angle steel, the included angle between the angle steel elements, and the number of elements are determined based on the size of the device. It is advisable to control the average flow velocity through the baffle assembly to ≥0.4 m / s to ensure sufficient turbulence intensity and improve mixing efficiency.

[0063] The flow guiding component 1.3 is disposed within the first receiving cavity and located between the first mixing region H1 and the second mixing region H2. In this embodiment, the second mixing region H2 is located above the first mixing region H1 and is separated by the flow guiding component 1.3. The flow guiding component 1.3 includes an annular flow guiding element 1.3.1 and a conical flow guiding element 1.3.2, as detailed below. Figure 1 and Figure 3The annular flow guide component 1.3.1 is disposed on the inner wall of the first receiving cavity, and the conical flow guide component 1.3.2 is located in the middle of the first receiving cavity, with the gap between the annular flow guide component 1.3.1 and the conical flow guide component 1.3.2 forming a flow channel H10. More preferably, the annular flow guide component 1.3.1 is arranged circumferentially along the inner wall of the outer cylinder 1.1, and the conical flow guide component 1.3.2 is disposed directly below the inner cylinder 1.2. The bottom surfaces of the annular flow guide component 1.3.1 and the conical flow guide component 1.3.2 are both horizontal and at the same elevation, with their center points overlapping. The annular flow guide component 1.3.1 is fixedly connected to the inner wall of the outer cylinder 1.1, and its cross-section is wedge-shaped, with the thicker side connected to the inner wall of the outer cylinder 1.1. The conical guide element 1.3.2 is positioned at the center of the annular guide element 1.3.1. Its height matches the thickness of the annular guide element 1.3.1, and its bottom circular radius matches the width of the annular guide element 1.3.1. The width of the annular gap formed with the annular guide element 1.3.1 matches both the width and the bottom circular radius of the annular guide element 1.3.1. Water from the first mixing zone H1 passes through the annular gap (i.e., the flow channel H10) in the middle of the guide assembly 1.3 from the top and enters the bottom of the second mixing zone H2. After mixing with the circulating flow in the second mixing zone H2, it enters the hydraulic circulation mixing process. The guide assembly 1.3 separates the first mixing zone H1 and the second mixing zone H2 into two relatively independent reaction zones, which do not affect or interfere with each other, thus improving the reaction efficiency of each mixing zone. Simultaneously, the hydraulic flow state of the second mixing zone H2 can be precisely controlled to guide the formation of the circulating flow and reduce the ineffective consumption of water head and electrical energy. The specific mechanism is as follows: After the downward flow of water in the third mixing zone collides with the annular guide component 1.3.1, it is blocked by the annular guide component 1.3.1 and forced to change direction under the flow adjustment effect of the component's inclined surface. It flows obliquely downward through the annular gap and converges towards the conical guide component 1.3.2. During the process, it mixes with the flow from the first mixing zone flowing upward from the annular gap and adjusts its direction again to oblique upward, reaching the upper part of the conical component and the bottom of the inner cylinder. Under the flow adjustment effect of the inclined surface of the conical guide component 1.3.2 and the lifting effect of the mixing and stirring component, it enters the inner cylinder and enters the circulating flow.

[0064] The upper part of the first receiving cavity forms a water outlet area H4. In this embodiment, the water outlet area H4 is located on top of the second mixing area H2 and the third mixing area H3.

[0065] The lower part of the second receiving cavity forms a first sludge accumulation zone H5, and the first sludge discharge outlet 1.10 is connected to the first sludge accumulation zone H5. The swirling current generated by the first mixing zone H1 settles heavier particles such as silt and sand in the raw water, as well as silt or heavier flocs in the returned sludge, into the first sludge accumulation zone H5. At the same time, larger flocs formed in the second mixing zone H2 and the third mixing zone H3 slowly fall into the first mixing zone H1 and will also settle into the first sludge accumulation zone H5 under the action of the swirling current. They are then discharged through the timed discharge device at the first sludge discharge outlet 1.10 to remove larger impurities in the water to be treated, reduce the ineffective consumption of coagulants, and avoid silt deposition in the subsequent flocculation tank.

[0066] The flocculation unit 2 is detailed in [reference needed]. Figure 1 It includes a shell 2.1 with a fourth receiving cavity and at least one set of flocculation units 2.2 disposed in the fourth receiving cavity; the outer cylinder 1.1 of the mixing unit 1 and the shell 2.1 of the flocculation unit 2 share the same side wall 2.3, and the fourth receiving cavity communicates with the effluent zone H4 through a notch provided on the side wall 2.3, as detailed in [link to details]. Figure 1 and Figure 2 In addition, the mixing unit and flocculation unit can also have another structure, in which the outer cylinder and the shell are not on the same wall, and the mixing unit has a first outlet 1.9 on the side wall of the outer cylinder. See [link to relevant documentation]. Figure 3 The shell 2.1 has a second inlet on its side wall that connects to the fourth accommodating cavity. The second inlet is connected to the outlet area H4 via the first outlet 1.9. In this embodiment, the second inlet and the second outlet 2.4 are arranged sequentially along the water flow direction. The lower part of the fourth accommodating cavity has a second sludge accumulation area H6, and the shell 2.1 has a second sludge outlet 2.5 that connects to the second sludge accumulation area H6. The flocculation unit is 14m long, 6m wide, and 5.65m high. There are 4 sets of flocculation units 2.2, each set of flocculation units 2.2 operates independently. A main sludge discharge pipe 3 is set below the flocculation unit. The first sludge outlet 1.10 and the second sludge outlet 2.5 are both connected to the main sludge discharge pipe 3, used to collect and discharge floc particles that settle to the bottom of the tank during the mixing and flocculation reaction process.

[0067] The flocculation unit 2.2 includes a first flocculation section, a second flocculation section, and a third flocculation section arranged sequentially. See also Figure 1 and Figure 2 Along the water flow direction, the flocculation unit 2.2 includes a first flocculation section, a second flocculation section, and a third flocculation section arranged sequentially. Each set of flocculation sections is 1.5m wide, and its structure is as follows:

[0068] The first flocculation section (i.e., the relative folding plate section) includes at least two first flocculation plates 2.2.1 (four plates are shown here) spaced apart. Each first flocculation plate 2.2.1 includes a connecting plate a connected sequentially with a wave crest formed at the connection point. Adjacent connecting plates a are arranged at an angle α, and the wave crests of two adjacent first flocculation plates 2.2.1 are oriented opposite to each other. A first flocculation channel H7 is formed between two adjacent first flocculation plates 2.2.1.

[0069] The second flocculation section (i.e., the parallel folded plate section) includes at least two second flocculation plates 2.2.2 (three are shown here) spaced apart. Each second flocculation plate 2.2.2 includes a connecting plate that is sequentially connected and forms a wave crest at the connection point. Adjacent connecting plates are arranged at an angle α, and the wave crests of two adjacent second flocculation plates 2.2.2 have the same orientation. A second flocculation channel H8 is formed between two adjacent first flocculation plates 2.2.1. The wave crest of the last first flocculation plate 2.2.1 in the first flocculation section and the wave crest of the first second flocculation plate 2.2.2 in the second flocculation section are arranged parallel to each other.

[0070] The third flocculation section includes at least two third flocculation plates 2.2.3 spaced apart (five plates are shown here), each third flocculation plate 2.2.3 being a straight plate and / or an arc-shaped plate (a straight plate is shown in the figure); a third flocculation channel H9 is formed between two adjacent third flocculation plates 2.2.3. A water outlet channel H11 is formed between the last third flocculation plate in the third flocculation section and the shell 2.1, and the second water outlet 2.4 is connected to the water outlet channel H11.

[0071] In this embodiment, the inner wall of the shell 2.1, the first flocculation channel H7, the second flocculation channel H8, the third flocculation channel H9, and the inner wall of the shell 2.1 are sequentially connected to form six N-shaped channels arranged in series.

[0072] In this embodiment, the first and second flocculation sections are further provided with micro-vortex components; the micro-vortex components include one or multiple micro-vortex elements 2.6 spaced apart along the water flow direction. In this embodiment, both the first and second flocculation sections are provided with two micro-vortex elements. See details. Figure 11 , Figure 12 , Figure 13 and Figure 14The micro-vortex component 2.6 comprises a top micro-vortex plate 2.6.1, a middle micro-vortex plate 2.6.2, and a bottom micro-vortex plate 2.6.3 arranged side-by-side, each equipped with vortex flow holes. The top, middle, and bottom micro-vortex plates 2.6.1, 2.6.2, and 2.6.3 are arranged in parallel with a spacing of 100mm. Twelve support tubes 2.6.4 are welded between the top and middle micro-vortex plates 2.6.1 and between the middle and bottom micro-vortex plates 2.6.2 and 2.6.3, respectively. Each support tube has a diameter of 20mm, a wall thickness of 2mm, and a length of 100mm. The support tubes 2.6.4 are arranged around the perimeter and center of the micro-vortex component 2.6 to securely connect the three micro-vortex plates and to support them, preventing significant deformation. The top micro vortex plate 2.6.1 and the bottom micro vortex plate 2.6.3 extend outward by 100mm in the width direction to form extension plates 2.6.5. Four bolt holes 2.6.6 with a diameter of φ20 are evenly opened on each extension plate 2.6.5. The two extension plates 2.6.5 at both ends of the same vortex plate are bent 90° outward along the bending line F to the outside of the micro vortex single piece 2.6. Each set of micro vortex single pieces 2.6 contains a total of four extension plates 2.6.5. The micro vortex single piece 2.6 is fixed to the partition walls on both sides by these four extension plates 2.6.5 and the corresponding expansion bolts.

[0073] The top micro-vortex plate 2.6.1 has an opening ratio of P1 for the vortex flow holes, the middle micro-vortex plate 2.6.2 has an opening ratio of P2 for the vortex flow holes, and the bottom micro-vortex plate 2.6.3 has an opening ratio of P3 for the vortex flow holes, where P1 > P2 > P3; the value of P1 ranges from 35% to 45%, the value of P2 ranges from 30% to 40%, and the value of P3 ranges from 25% to 35%. Further preferred:

[0074] Two sets of micro-vortex elements 2.6 are installed between the first and second first flocculation plates 2.2.1, and between the second and third first flocculation plates 2.2.1. The micro-vortex forming holes E on these micro-vortex elements 2.6 all have a diameter of φ60mm. Specifically, 114 holes are evenly distributed on the top micro-vortex plate 2.6.1 in the direction of water flow, with an opening rate of approximately 35%. See details... Figure 12 The central micro-vortex plate 2.6.2 has 105 uniformly spaced holes, with an opening rate of approximately 30%. See details. Figure 13 The bottom micro-vortex plate 2.6.3 has 95 uniformly spaced holes, with an opening rate of approximately 25%. The average opening rate of this micro-vortex component is 30%. See details. Figure 14 .

[0075] Two sets of micro-vortex elements 2.6 are installed between the third first flocculation plate 2.2.1 and the fourth first flocculation plate 2.2.1, and between the fourth first flocculation plate 2.2.1 and the first second flocculation plate 2.2.2. The micro-vortex forming holes E on these micro-vortex elements 2.6 all have a diameter of φ80mm. Specifically, in the direction of water flow, the top micro-vortex plate 2.6.1 has 86 holes evenly distributed, with an opening rate of approximately 45%; the middle micro-vortex plate 2.6.2 has 76 holes evenly distributed, with an opening rate of approximately 40%; and the bottom micro-vortex plate has 67 holes evenly distributed, with an opening rate of approximately 35%. The average opening rate on the micro-vortex elements 2.6 is 40%. See details... Figure 14 .

[0076] Two sets of micro-vortex elements 2.6 are provided between the first and second second flocculation plates 2.2.2 and between the second and third second flocculation plates 2.2.2. The micro-vortex forming holes E on these micro-vortex elements 2.6 all have a diameter of φ100mm. Specifically, in the direction of water flow, the top micro-vortex plate 2.6.1 has 67 holes evenly distributed, with an opening rate of approximately 55%; the middle micro-vortex plate 2.6.2 has 57 holes evenly distributed, with an opening rate of approximately 50%; and the bottom micro-vortex plate 2.6.3 has 48 holes evenly distributed, with an opening rate of approximately 45%. The average opening rate of the micro-vortex elements 2.6 is 50%.

[0077] In this embodiment, the micro-vortex forming holes E at different positions on the micro-vortex plate of the same micro-vortex unit 2.6 have the same aperture, which can form micro-vortices with basically consistent size. By controlling the aperture size, it is beneficial to increase the number of effective micro-vortices. The number of micro-vortex forming holes E along the water flow direction in each set of micro-vortex units 2.6 gradually decreases, and the opening ratio gradually decreases. When the water flows through the micro-vortex unit 2.6, the flow velocity gradually increases, forming a gradually increasing turbulence intensity gradient, which provides sufficient reaction power for the gradually growing flocs and improves the floc collision and flocculation reaction efficiency.

[0078] In this embodiment, the aperture and average porosity of the micro-vortex unit 2.6 arranged sequentially along the water flow direction gradually increase. This allows for the formation of relatively small-scale micro-vortices with relatively large turbulent energy in the first flocculation stage, and relatively large-scale micro-vortices with relatively small turbulent energy in the second flocculation stage. This provides optimal flocculation hydraulic conditions for each flocculation stage, maximally matching the microscopic mechanism of floc growth, significantly improving flocculation reaction efficiency and effect, reducing flocculation time, and lowering the amount of flocculant added.

[0079] The water treatment process of the multi-stage enhanced mixing micro-vortex flocculation device in this embodiment is as follows: raw water, coagulant, and returned sludge enter the lower middle part of mixing unit 1 from the first inlet 1.7, dosing pipe 1.11, and sludge inlet 1.8, respectively. They undergo multi-stage enhanced mixing reactions in the first mixing zone H1, the second mixing zone H2, and the third mixing zone H3. After sufficient mixing and mass transfer, the multiphase components in the water to be treated flow into flocculation unit 2 from the top outlet zone H4, the first outlet 1.9, and the second inlet (not marked). Then, they pass through the first flocculation section containing the first flocculation plate 2.2.1 and micro-vortex element 2.6, the second flocculation section containing the second flocculation plate 2.2.2 and micro-vortex element 2.6, and the third flocculation section containing the third flocculation plate 2.2.3 for enhanced flocculation, forming larger, denser flocs with good settling performance. The flocs then flow out from the second outlet 2.4 located in the lower middle part of the shell and enter the subsequent sedimentation treatment process. The silt and larger dense flocs carried in the mixing and flocculation units settle naturally into the first sludge aggregation zone H5 and the second sludge aggregation zone H6, respectively, and are periodically discharged through the main sludge discharge pipe 3.

[0080] The effect of applying the technical solution of this embodiment is:

[0081] I. The multi-stage enhanced mixing micro-vortex flocculation device of the present invention includes a mixing unit and a flocculation unit arranged in series. The mixing unit includes an outer cylinder, an inner cylinder, a flow guiding component, a flow turbulence component, a mixing and stirring component, etc. A first mixing region is formed at the junction of a first receiving cavity and a second receiving cavity in the outer cylinder, and a water inlet and a sludge inlet for tangential feeding are provided at the junction. A first sludge accumulation region is formed in the lower part of the second receiving cavity. The inner cylinder is disposed in the first receiving cavity, and a second mixing region is formed in the third receiving cavity. The mixing and stirring component is disposed in the second mixing region to provide upward power for the flow of fluid in the second mixing region. The flow guiding component is disposed in the first receiving cavity and located between the first mixing region and the second mixing region. A third mixing region is formed between the inner wall of the first cylinder and the outer wall of the inner cylinder, and the flow turbulence component is disposed in the third mixing region. The flocculation unit includes a shell with a fourth receiving cavity and at least one set of flocculation units disposed in the fourth receiving cavity. A second sludge accumulation region is provided in the lower part of the fourth receiving cavity, and a second sludge discharge port communicating with the second sludge accumulation region is provided on the shell. The water to be treated first enters the mixing unit for treatment. Under the multi-stage mixing action of swirling mixing in the first mixing zone, mechanical mixing in the second mixing zone, micro-vortex mixing in the third mixing zone, and circulating flow mixing in the second and third mixing zones, the water to be treated, coagulant, and returned sludge undergo sufficient contact and collision. The reagents and sludge are recycled, which helps to improve the mixing reaction effect and efficiency, strengthen the mixing process's resistance to shock loads, reduce the amount of reagents added, and lower operating costs. The fully mixed water directly and quickly enters the flocculation unit. Under the combined action of baffles, swirling flow, and micro-vortexes, the turbulence intensity in the water can be increased, providing sufficient reaction power for floc collision, aggregation, and growth. A large number of micro-vortices of various scales can be generated, increasing the capture rate of small flocs and the utilization rate of coagulant, providing the most suitable hydraulic conditions for each stage of the flocculation reaction. It can also provide a large number of floc nuclei for the flocculation reaction, improving flocculation density and settling performance. Thorough mixing of the water to be treated, coagulant, and returned sludge is a prerequisite for ensuring flocculation effect. Good hydraulic conditions and sufficient reaction kinetics are key to ensuring flocculation effect. The device has a compact and simplified overall structure. While promoting mixing and mass transfer, it improves the flocculation reaction flow field and enhances the flocculation reaction kinetics, which can significantly improve the mixing and flocculation reaction effect and efficiency, reduce the demand for coagulant, shorten the flocculation reaction time, and improve the sedimentation performance of flocs.

[0082] II. A first mixing zone is set in the lower middle part of the outer cylinder of the mixing unit, and a second and third mixing zone are set in the upper middle part of the outer cylinder. An outlet zone is set in the upper part of the outer cylinder, and the water flows from bottom to top. The water to be treated, coagulant, and sludge all enter the first mixing zone in a clockwise direction along the circumference tangent of the outer cylinder. Utilizing the high flow velocity of the influent and the return sludge, a horizontal vortex is formed in the first mixing zone. The components in the first mixing zone are relatively complex. Wastewater is mixed through swirling and centrifugal forces, while its components are separated and sorted. Large particles and heavy materials are centrifuged and transferred to the bottom sludge accumulation zone, while smaller, lighter components flow into the top second and third mixing zones to continue the reaction. This effectively reduces the participation of ineffective substances in the mixing reaction, improving mixing efficiency, increasing the utilization rate of coagulants, and preventing the deposition and caking of silt and sludge flocs in the system. The returned sludge provides numerous floc nuclei for mixing and flocculation, significantly increasing the probability of particle collisions, improving the density of flocs, and enhancing floc settling performance. Sludge accumulation zones are located at the bottom of the mixing and flocculation units to facilitate the separation of large particles and heavy materials to these zones and their discharge from the system.

[0083] III. The mixing and stirring assembly in this invention includes a power source, a stirring shaft, and lifting and stirring blades. In addition to its mechanical mixing function, the mixing and stirring assembly in the second mixing zone provides sufficient power for the upward flow of water from the first mixing zone into the second and third mixing zones, as well as for the circulation within each mixing zone. Simultaneously, by adjusting the operating frequency and rotation speed of the mixing and stirring assembly, the required circulating water flow rate and the flow velocity in the third mixing zone can be ensured, thereby improving the capture of small flocs, enhancing the mixing effect, and increasing resistance to shock loads. Furthermore, the lifting and stirring blades can break up larger floc particles in the water flow, cutting them into smaller flocs of similar size, forming more floc nuclei that can effectively participate in subsequent flocculation reactions. This effectively increases contact collision coagulation and trapping effects, improving the subsequent flocculation reaction effect, increasing the removal rate of small particles and flocs in the water, and improving the settling performance of the flocs. At the same time, by adjusting the rotation speed of the mixing and stirring assembly, the particle size distribution of the small floc nuclei can be optimized and controlled to further enhance the improvement effect on subsequent flocculation reactions.

[0084] Fourth, a turbulence-inducing component is installed in the third mixing zone. The unique structure of the turbulence-inducing component causes a large number of micro-eddies with a scale close to that of flocs to be generated in the water flow or continuously changes the water flow velocity vector, creating a strong turbulent state, providing sufficient turbulence intensity, increasing and strengthening the collision between particles, coagulants and return sludge in the water flow, and further enhancing the mixing effect; at the same time, the energy provided by the mechanical circulation mixing system is fully used for the mixing reaction, and the energy is also used efficiently again.

[0085] V. In this embodiment, a diversion device is provided. The diversion device can disperse the water flow entering the mixing unit in the height direction, so as to form a vortex in the entire height direction of the first mixing area, improve the effective utilization rate of the internal volume of the mixing unit, and at the same time avoid the ineffective consumption of kinetic energy and the destruction of the vortex when the inlet water flow is directly mixed with the internal vortex.

[0086] VI. In this embodiment, the flocculation unit is combined with the micro-vortex unit, which enables the internal water flow of the flocculation unit to generate a combined effect of deflection, swirling, and micro-vortex. The deflection effect causes initial collisions and contact between the flocs in the water, with a narrow range and low frequency. Then, the swirling effect generated by the continuous expansion and contraction of the deflectors causes the flocs to rapidly aggregate and grow, with a wider range and higher frequency. Finally, the micro-vortex effect generated by the enhanced micro-vortex flocculation device increases the turbulence intensity of the water flow, providing sufficient reaction power for floc collision, aggregation, and growth. At the same time, the large number of micro-vortices generated can promote the collision and aggregation of remaining small flocs in the water, increasing the capture rate of small flocs and the utilization rate of coagulant. The combined effect of deflection, swirling, and micro-vortex provided by the device can significantly improve the reaction power of flocculation, increase the turbulence intensity of the water flow, take into account the flocculation of flocs of all sizes, improve the flocculation reaction effect and efficiency, reduce the amount of coagulant added, and shorten the flocculation reaction time.

[0087] VII. A reinforced micro-vortex flocculation device with smaller pore size and opening ratio is installed in both the relatively folded plate section and the parallel folded plate section. This creates micro-vortices with relatively small scale, relatively large turbulent energy, and relatively strong disturbance in the relatively folded plate section, and relatively large scale, relatively small turbulent energy, and relatively weak disturbance in the parallel folded plate section. This provides optimal flocculation hydraulic conditions for each flocculation stage, maximally matching the microscopic mechanism of floc growth, significantly improving flocculation reaction efficiency and effect, reducing flocculation time, and lowering flocculant dosage. Individual micro-vortex devices offer excellent flocculation effect and high reaction efficiency. Custom-made complete sets are available to adapt to reactors of various sizes, facilitating on-site installation. Furthermore, the reactor components are less prone to sludge accumulation and clogging, minimizing inspection and maintenance workload.

[0088] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A multi-stage enhanced hybrid micro-vortex flocculation device, characterized in that, It includes a mixing unit (1) and a flocculation unit (2) arranged in series; The mixing unit (1) includes an outer cylinder (1.1), an inner cylinder (1.2), a turbulence assembly (1.4), a mixing and stirring assembly (1.5), a first water inlet (1.7), a sludge inlet (1.8), and a first sludge outlet (1.10). The outer cylinder (1.1) includes a first cylinder (1.1.1) and a second cylinder (1.1.2) connected in series from top to bottom. The first cylinder (1.1.1) includes a first receiving cavity with an opening at the lower end, and the second cylinder (1.1.2) includes a second receiving cavity with an opening at the upper end and communicating with the first receiving cavity. A first mixing region (H1) is formed at the junction of the first receiving cavity and the second receiving cavity, and a first water inlet (1.7) and a sludge inlet (1.8) for tangential feeding are provided at the junction. The upper part of the first cavity forms an outlet zone (H4); the lower part of the second cavity forms a first sludge accumulation zone (H5), and the first sludge outlet (1.10) is connected to the first sludge accumulation zone (H5); the inner cylinder (1.2) is disposed in the first cavity, and the inner cylinder (1.2) is located between the outlet zone (H4) and the first mixing zone (H1). The inner cylinder (1.2) includes a third cavity with openings at both the top and bottom, and a second mixing zone (H2) is formed in the third cavity; a mixing and stirring assembly (1.5) is partially disposed in the second mixing zone (H2); a third mixing zone (H3) is formed between the inner wall of the first cylinder (1.1.1) and the outer wall of the inner cylinder (1.2), and the turbulence shroud assembly (1.4) is disposed in the third mixing zone (H3); The flocculation unit (2) includes a shell (2.1) having a fourth receiving cavity and at least one set of flocculation units (2.2) disposed in the fourth receiving cavity; the fourth receiving cavity is connected to the effluent zone (H4), and a second effluent outlet (2.4) is provided on the other side of the shell (2.1) opposite to the effluent zone; a second sludge accumulation zone (H6) is provided at the lower part of the fourth receiving cavity, and a second sludge discharge outlet (2.5) is provided on the shell (2.1) connected to the second sludge accumulation zone (H6); A flow guiding component (1.3) is provided within the first receiving cavity and between the first mixing region (H1) and the second mixing region (H2). The flow guiding assembly (1.3) includes an annular flow guiding element (1.3.1) and a conical flow guiding element (1.3.2). The annular flow guiding element (1.3.1) is disposed on the inner wall of the first receiving cavity, and the conical flow guiding element (1.3.2) is located in the middle part of the first receiving cavity. The gap between the annular flow guiding element (1.3.1) and the conical flow guiding element (1.3.2) forms a flow passage (H10). Along the direction of water flow, the flocculation unit includes a first flocculation section, a second flocculation section and a third flocculation section arranged in sequence. The first flocculation section is a relatively folded plate structure, the second flocculation section is a parallel folded plate structure, and the third flocculation section is a straight plate or arc-shaped plate structure. The first flocculation section and / or the second flocculation section are further provided with micro vortex components; the micro vortex components include one or multiple micro vortex elements (2.6) arranged at intervals along the water flow direction.

2. The multi-stage enhanced hybrid micro-vortex flocculation device according to claim 1, characterized in that, The sludge inlet (1.8) is positioned such that the first water inlet (1.7) is rotated 90° circumferentially around the first mixing zone (H1). A dosing pipe (1.11) is provided on the pipeline connected to the first water inlet (1.7). The outer cylinder (1.1) of the mixing unit (1) and the shell (2.1) of the flocculation unit (2) share the same side wall (2.3). The fourth receiving cavity is connected to the water outlet area (H4) through a notch provided on the side wall (2.3). Alternatively, the outer cylinder (1.1) of the mixing unit (1) is provided with a first water outlet (1.9) on its side wall, and the shell (2.1) is provided with a second water inlet connected to the fourth receiving cavity on its side wall. The second water inlet is connected to the water outlet area (H4) through the first water outlet (1.9).

3. The multi-stage enhanced hybrid micro-vortex flocculation device according to claim 1, characterized in that, The turbulence assembly (1.4) includes multiple first turbulence plates (a) arranged circumferentially along the inner cylinder (1.2), and each first turbulence plate (a) includes multiple folded plates (a1) arranged in series; adjacent first turbulence plates (a) have the same structure or are mirror images of each other. Alternatively, the spoiler assembly (1.4) includes multiple second spoilers (b) spaced circumferentially along the inner cylinder (1.2), each second spoiler (b) including a connecting rod (b1) and multiple spikes (b2) arranged along the length of the connecting rod; the spikes (b2) on two adjacent second spoilers (b) are symmetrically arranged or staggered vertically.

4. The multi-stage enhanced hybrid micro-vortex flocculation device according to claim 1, characterized in that, The mixing assembly (1.5) includes a power source (1.5.1), a stirring shaft (1.5.2), and lifting stirring blades (1.5.3). The power source (1.5.1) is mounted on the outer cylinder (1.1). The connecting end of the stirring shaft (1.5.2) is connected to the output end of the power source (1.5.1), and its free end is inserted into the second mixing zone (H2). The lifting stirring blades (1.5.3) are located in the second mixing zone (H2) and are mounted on the free end of the stirring shaft (1.5.2).

5. The multi-stage enhanced hybrid micro-vortex flocculation device according to claim 1, characterized in that, The first water inlet (1.7) and / or sludge inlet (1.8) are provided with a diversion device (1.14); the diversion device (1.14) includes an arc-shaped diversion plate for dispersing the water flow of the first water inlet (1.7) and / or sludge inlet (1.8).

6. The multi-stage enhanced hybrid micro-vortex flocculation device according to claim 1, characterized in that, It also includes a cutting component (1.6) disposed within the second mixing region (H2); The cutting assembly (1.6) includes multiple cutting strips (1.6.1), the connecting end of the cutting strip is connected to the inner wall of the second mixing region (H2), and the free end of the cutting strip is inclined upward; the cutting strip is set at an angle of 45°-75° with the inner wall surface of the second mixing region (H2).

7. The multi-stage enhanced hybrid micro-vortex flocculation device according to any one of claims 1-6, characterized in that, The first flocculation section includes at least two first flocculation plates (2.2.1) spaced apart. Each first flocculation plate (2.2.1) includes a connecting plate that is connected sequentially and forms a wave crest at the connection point. Adjacent connecting plates are arranged at an angle α, and the wave crests of two adjacent first flocculation plates (2.2.1) are oriented opposite to each other. A first flocculation channel (H7) is formed between two adjacent first flocculation plates (2.2.1). The second flocculation section includes at least two second flocculation plates (2.2.2) spaced apart. Each second flocculation plate (2.2.2) includes a connecting plate that is connected sequentially and forms a wave crest at the connection point. Adjacent connecting plates are arranged at an angle α, and the wave crests of two adjacent second flocculation plates (2.2.2) have the same orientation. A second flocculation channel (H8) is formed between two adjacent first flocculation plates (2.2.1). The third flocculation section includes at least two third flocculation plates (2.2.3) spaced apart, the third flocculation plates (2.2.3) being straight plates and / or curved plates; a third flocculation channel (H9) is formed between two adjacent third flocculation plates (2.2.3).

8. The multi-stage enhanced hybrid micro-vortex flocculation device according to claim 1, characterized in that, The micro vortex component (2.6) includes a top micro vortex plate (2.6.1), a middle micro vortex plate (2.6.2), and a bottom micro vortex plate (2.6.3) arranged in parallel and each having vortex flow holes. The opening ratio of the vortex flow holes on the top micro vortex plate (2.6.1) is P1, the opening ratio of the vortex flow holes on the middle micro vortex plate (2.6.2) is P2, and the opening ratio of the vortex flow holes on the bottom micro vortex plate (2.6.3) is P3, and P1 > P2 > P3; the value range of P1 is 35%-45%, the value range of P2 is 30%-40%, and the value range of P3 is 25%-35%.

9. The multi-stage enhanced hybrid micro-vortex flocculation device according to claim 8, characterized in that, The vortex flow holes on the top microvortex plate (2.6.1), middle microvortex plate (2.6.2), and bottom microvortex plate (2.6.3) within a single microvortex component (2.6) are all of the same diameter; a single microvortex component (2.6) may have one middle microvortex plate (2.6.2) or at least two middle microvortex plates (2.6.2) arranged in parallel; the diameter of the vortex flow holes ranges from 50 to 150 mm; along the water flow direction, the diameter of the vortex flow holes in the microvortex component increases sequentially.

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