Efficient chemical wastewater treatment device

Abstract

The utility model discloses an efficient chemical wastewater treatment device, which relates to the technical field of wastewater treatment, and comprises a circular reaction cylinder, a mixing module is arranged in the circular reaction cylinder, the mixing module comprises a first conical spiral pipe and a second conical spiral pipe, the axis of the first conical spiral pipe is the same as that of the second conical spiral pipe, and the axis of the second conical spiral pipe is the same as that of the first conical spiral pipe. The spiral directions of the first conical spiral pipe and the second conical spiral pipe are opposite, spiral lines of the first conical spiral pipe and the second conical spiral pipe are conical spiral lines with large upper portions and small lower portions, and outlets of the first conical spiral pipe and the second conical spiral pipe are opposite. According to the device, through spiral hedging and mixing of the mixing modules in the circular reaction cylinder, accurate matching of flow field characteristics and a reaction stage is realized, the contradiction between colloid destabilization rapid reaction characteristics in the early stage of flocculation mixing and long-time scale of traditional mixing equipment is effectively solved, the fine particle destabilization efficiency and the effluent quality are improved, and the device is suitable for industrial production. And the cost of the subsequent chemical wastewater whole process is effectively reduced.

Description

Technical Field

[0001] This utility model relates to the field of wastewater treatment technology, specifically to a high-efficiency chemical wastewater treatment device. Background Technology

[0002] With the rapid development of the chemical industry, the amount of chemical wastewater generated is increasing daily. Chemical wastewater has a complex composition, often containing pollutants such as heavy metals, organic matter, and acids and alkalis. If discharged directly without effective treatment, it will cause serious pollution to the soil, water bodies, and other ecological environments, endangering human health. In the entire process of chemical wastewater treatment, the flocculation device, as a key link between pretreatment and main treatment, directly affects the load of subsequent processes and the quality of effluent.

[0003] Flocculation is a process in which chemicals are added to water to disrupt the stability of colloidal particles, causing them to aggregate into larger flocs and settle. Flocculation devices use mechanical stirring and other methods to mix the chemicals with the wastewater, forming flocs to achieve solid-liquid separation. Currently, insufficient mixing uniformity and inadequate dispersion of fine particles are the core technical problems in the flocculation process. Traditional stirring or hydraulic devices are limited by flow field distribution and energy input, easily resulting in dead zones or uneven turbulence, with low-velocity areas at the edges forming mixing blind zones. Furthermore, insufficient turbulence intensity leads to chemical dispersion particle sizes >100μm. A single addition of chemicals causes a sudden increase in local concentration, far exceeding the critical concentration required for colloid destabilization. Excessive chemicals form "clusters" that adsorb onto the surface of large particles, hindering contact with fine particles. This causes the already destabilized fine particles to recharge and disperse, reducing dispersion efficiency.

[0004] The rapid reaction characteristics (10-60 seconds) of colloid destabilization are fundamentally contradictory to the long time scale (2-10 minutes) of traditional mixing equipment. This leads to a kinetic mismatch where "the reaction is completed but the mixing is not finished" or "the reaction is delayed even though the mixing has just begun." This causes the formed micro-flocs to break down under high shear force. In addition, the high viscosity and low temperature of the water further weaken the turbulence intensity, ultimately resulting in poor mixing uniformity and insufficient destabilization efficiency of fine particles. As a result, fine particles are difficult to settle due to lack of aggregation. The impact extends from the failure of chemical wastewater effluent to the increase in the overall process cost. Undestabilized particles directly lead to insufficient removal of suspended solids and turbidity, exacerbating the load on subsequent sedimentation and membrane treatment. At the same time, it forces an increase in the input of reagents and energy consumption, forming a vicious cycle of "poor effect - high cost". Utility Model Content

[0005] The purpose of this invention is to provide a high-efficiency chemical wastewater treatment device. Through a mixing module, chemical wastewater and reagents are mixed within a circular reaction tank using a spiral tube. This design incorporates both axial and tangential velocity differences to create a three-dimensional turbulent flow field. Furthermore, the device features a three-stage flocculation structure design: a cylinder-ring-cylinder configuration. By combining different tank shapes and mixing methods, the device achieves precise matching between flow field characteristics and reaction stages. It offers multiple advantages, including high mixing efficiency, shear control, and compact space. This effectively resolves the contradiction between the rapid destabilization reaction characteristics of colloids in the initial stage of flocculation mixing and the long-term nature of traditional mixing equipment. It improves the destabilization efficiency of fine particles and the quality of the effluent, effectively reducing the overall cost of the subsequent chemical wastewater treatment process. The device combines high technical efficiency with economic efficiency.

[0006] This objective is achieved using the following technical solution:

[0007] A high-efficiency chemical wastewater treatment device includes a circular reaction cylinder. A mixing module is provided inside the circular reaction cylinder. The mixing module includes a first conical spiral tube and a second conical spiral tube. The first and second conical spiral tubes have the same axis, but their spiral directions are opposite. The spiral lines of the first and second conical spiral tubes are conical spirals with a larger upper diameter and a smaller lower diameter. The outlets of the first and second conical spiral tubes are opposite to each other. Chemical wastewater and reagents flow out of the first and second conical spiral tubes respectively and then mix against each other. The clockwise and counterclockwise spiral tubes generate clockwise and counterclockwise spiral water flows, respectively. The spiral lines with a larger upper diameter and a smaller lower diameter increase the fluid velocity along the flow direction, greatly increasing the Reynolds number. At the same time, the centrifugal force generated by the clockwise and counterclockwise spirals greatly increases the radial velocity of the fluid, forming a complex turbulent flow field. The counter-current mixing process causes the liquid velocity gradient G to far exceed the critical value required for colloid destabilization, disrupting the double electric layer on the particle surface in a very short time. This highly matches the reaction window for colloid destabilization. Simultaneously, when the two opposing helical streams are ejected, their momentum cancels each other out, generating a violent vortex. The collision kinetic energy is significantly increased compared to traditional stirring, enabling the colloidal particles to complete effective collision destabilization in a very short time, avoiding the hydrolytic failure of reagents caused by mixing lag in traditional equipment. In addition, the vortex center generated by the counter-current mixing forms a low-pressure zone, continuously entraining the surrounding fluid. This causes the reagent and wastewater to undergo a "shear-break-entrainment-remixing" cycle in the mixing zone, effectively improving the mixing uniformity.

[0008] Compared to existing devices, which primarily use mechanical agitation (such as paddle or turbine mixers) or static mixers (such as tubular mixers) to mix chemical wastewater and chemicals, this device struggles to ensure that the hydrolysis products of the coagulant are rapidly and evenly distributed throughout the water body. In the initial stages of flocculation, colloidal particles need to fully contact and destabilize with the coagulant within a very short time. However, due to the limitations of the mixing equipment, the coagulant is unevenly distributed in the water. In some areas, the concentration of the coagulant is too high, leading to localized overreaction, while in other areas, the concentration is insufficient, and the colloidal particles are not fully destabilized, resulting in incomplete flocculation. Furthermore, traditional agitation suffers from uneven flow field characteristics, characterized by "high turbulence near the blades and low velocity in the far field." Undestabilized fine particles, due to their small size and low settling velocity, cannot be effectively removed by subsequent sedimentation tanks. This leads to insufficient removal of suspended solids and turbidity, increasing subsequent treatment costs.

[0009] This invention utilizes turbulent vortices generated by the opposing of forward and reverse spiral flows. The high velocity gradient G value generated by the opposing of forward and reverse spiral flows compresses the mixing time to (10-30) seconds, precisely matching the destabilization reaction time. This avoids the hydrolysis and failure of the reagents, greatly improving the destabilization efficiency. At the same time, the combined effect of spiral centrifugal force and opposing impulse greatly enhances the uniformity of the flow field within the circular reaction cylinder, improving the mixing efficiency and destabilization effect, reducing the amount of reagents used, and lowering the energy consumption and cost of the entire process.

[0010] Furthermore, the helix angles of the first and second conical helical tubes are between 15° and 30°. The helix angle is an important parameter affecting the fluid mixing effect. When the helix angle is small, the tangential velocity component is too small, the rotational motion of the fluid along the tube wall is weak, making it difficult to form a stable helical flow. The Reynolds number of the outflowing liquid is low, and the degree of irregular movement of the fluid particles is low, resulting in insufficient mixing uniformity. The flow field at the outlet is not fully developed, the effective mixing length is insufficient, the shear force is unevenly distributed along the tube length, and the velocity gradient G value at the outlet section is low, which cannot effectively break the double layer on the surface of colloidal particles, thus reducing the destabilization efficiency of fine particles. When the helix angle is large, the Reynolds number of the outflowing liquid is high. Although it is in a vigorous turbulent region, the fluctuation range of the turbulent dissipation rate is large, the turbulent uniformity of the mixing zone is reduced, the velocity gradient G value at the outlet section is too large, the molecular chain breakage rate of the polymer agent increases, the shear strength is out of control, and the agent is prone to failure. A suitable helix angle achieves the best balance between turbulence uniformity and shear strength, making it an optimal solution that takes into account both technical and economic factors, and laying the foundation for outlet hedging mixing.

[0011] Furthermore, the aspect ratios of both the first and second conical solenoids are between 10 and 12. The aspect ratio determines the residence time of the fluid within the solenoid and the degree of flow field development. When the aspect ratio is too small, the fluid does not fully develop into a stable helical flow, resulting in insufficient turbulence intensity and uneven outlet velocity distribution. When the aspect ratio is too large, the fluid residence time within the pipe is too long, which may lead to turbulence attenuation due to frictional resistance, a surge in energy consumption, and excessive drag loss. A suitable aspect ratio allows the fluid sufficient time to complete the helical flow development and maintain a turbulent state before the outlet, resulting in more uniform momentum exchange during counter-current.

[0012] Furthermore, the first and second conical spiral tubes have outward-flaring tapers. This outward taper increases the tube diameter along the pipe length, causing the fluid velocity to decrease. This ensures that the Reynolds number Re remains in the vigorous turbulence region throughout the entire tube length, avoiding the decrease in turbulence intensity caused by velocity decay in traditional straight pipes. The taper of both the first and second conical spiral tubes is between 1.2 and 1.5. Too small a taper results in excessively rapid velocity decay within the spiral tube, leading to insufficient turbulence intensity; too large a taper results in a large outlet jet diffusion angle, dispersing energy over a larger space during collision, reducing the velocity gradient G at the outlet section, and lowering the collision efficiency between the agent and particles. A suitable taper ensures precise matching between the centrifugal force field gradient and the energy gradient required for particle destabilization, improving mixing uniformity and destabilization efficiency.

[0013] Furthermore, it also includes an annular reaction cylinder, which comprises an inner cylinder wall, an outer cylinder wall, and an annular bottom plate. The annular bottom plate is located between the inner and outer cylinder walls. The annular reaction cylinder is aligned with the axis of the circular reaction cylinder. Driven by a liquid level difference, the mixed liquid inside the circular reaction cylinder flows freely from the top into the coaxial annular reaction cylinder. The area enclosed by the inner cylinder wall, outer cylinder wall, and annular bottom plate forms an annular stirring zone. The diameter of the inner cylinder wall is smaller than the diameter of the circular reaction cylinder. The annular reaction cylinder is located vertically below the circular reaction cylinder. The flocculation reaction follows a three-stage process: rapid destabilization → floc growth → compaction and maturation. The three-stage structure achieves precise control through spatial partitioning. The circular reaction cylinder area is the rapid mixing zone, utilizing a high-shear mixing mechanism to achieve instantaneous dispersion of the reagent and chemical wastewater, corresponding to the rapid destabilization requirement in the initial stage of flocculation. The annular stirring zone is the flocculation reaction zone, providing medium-intensity stirring through side-wall stirring or a folded plate structure, promoting the aggregation of destabilized particles into flocs, matching the mid-stage requirement of floc growth. The second cylindrical zone is a slow flocculation zone, which uses low-intensity stirring or no stirring. The floc maturation is completed by relying on the kinetic energy of the fluid itself, avoiding floc breakage caused by high-intensity shearing. The synergistic effect of staged mixing improves flocculation efficiency, reduces reagent waste, and lowers the energy consumption of the device.

[0014] Furthermore, the inner cylinder wall diameter is between 0.4 and 0.6 times the outer cylinder wall diameter. The inner cylinder wall diameter is the diameter of the inner cylinder in the annular structure, and the outer cylinder wall diameter is the diameter of the outer cylinder in the annular structure. The diameter ratio of the inner ring to the outer ring directly determines the flow state of the fluid in the annular region. If the diameter ratio is too large, the annular gap will be too small, and the fluid will form a narrow slit flow in the annular region. The narrow slit flow leads to insufficient turbulence development and a decrease in destabilization efficiency. If the diameter ratio is too small, the annular region will be close to a large-diameter single cylinder. The fluid in the annular region is prone to forming eccentric vortices, with high-shear and low-shear regions coexisting, disrupting the symmetry of the flow field, and causing mixing turbulence.

[0015] Furthermore, the annular reaction cylinder is equipped with a side-wall agitator and a liquid addition device. The asymmetric stirring of the side-wall agitator eliminates the traditional defects of high flow velocity near the wall and low flow velocity in the center of the annular zone, improving flow velocity uniformity and avoiding mixing dead zones. The liquid addition device is used to add the reagent to the annular stirring zone. After the chemical wastewater and reagent are initially mixed, the reagent is added again, avoiding excessive reagent addition during the initial mixing and matching the stage requirements of the flocculation reaction. The discharge check valve of the liquid addition device is located within the flow field action area of ​​the side-wall agitator, which is within the rotation trajectory of the agitator blades. The reagent discharge port is located within the rotation trajectory of the agitator blades, which can quickly complete the dispersion of the reagent, significantly improving the uniformity of the reagent concentration distribution in the annular zone and ensuring that all particles have an equal probability of contact with the reagent.

[0016] Furthermore, there are at least two sidewall agitators, which are evenly distributed circumferentially on the outer cylinder wall. The composite flow field generated by multiple agitators has stronger anti-interference ability and ensures the uniformity of the flow field.

[0017] Furthermore, it also includes a tank body, the bottom of which is equipped with a sludge discharge pipe, and a solenoid valve is installed on the sludge discharge pipe to promptly remove sludge and maintain an efficient environment for flocculation reaction.

[0018] Compared with the prior art, the high-efficiency chemical wastewater treatment device provided by this utility model has the following beneficial effects:

[0019] 1. This utility model provides a high-efficiency chemical wastewater treatment device. By using the high velocity gradient G value generated by the opposing spiral flow at the outlets of the forward and reverse spiral pipes, it effectively solves the contradiction between the rapid reaction characteristics of colloidal destabilization in the early stage of flocculation and mixing and the long mixing time of traditional mixing equipment. This improves the destabilization efficiency of fine particles and the quality of effluent, and effectively reduces the cost of the entire subsequent chemical wastewater treatment process. It combines technical efficiency with engineering economy.

[0020] 2. This utility model provides a high-efficiency chemical wastewater treatment device. Through a three-stage flocculation structure design of cylinder-ring-cylinder, and by combining different tank shapes and mixing methods, it achieves precise matching of flow field characteristics and reaction stages, and has multiple advantages such as mixing efficiency, shear control and compact space. Attached Figure Description

[0021] The accompanying drawings, which are provided to further illustrate the embodiments of the present invention and constitute a part of the present invention, do not constitute a limitation thereof.

[0022] Figure 1 This is a front view of the structure of this utility model;

[0023] Figure 2 This is a schematic diagram of the hybrid module structure of this utility model;

[0024] Figure 3 This is a schematic diagram of the annular reaction cylinder structure of this utility model;

[0025] Figure 4 This is a top view of the structure of this utility model;

[0026] Among them, 1-tank body, 2-first conical spiral tube, 3-second conical spiral tube, 4-circular reaction cylinder, 5-annular reaction cylinder, 51-inner cylinder wall; 52-outer cylinder wall, 53-annular bottom plate; 6-first cylindrical area, 7-annular stirring area, 8-second cylindrical area, 9-side wall mixer, 10-limiting moving block, 11-rotating rod, 12-piston rod, 13-cylinder, 14-plunger, 15-cylinder body, 16-feed check valve, 17-discharge check valve, 18-sludge discharge pipe, 19-solenoid valve. Detailed Implementation

[0027] To better understand the above-mentioned objectives, features, and advantages of this utility model, the present utility model will be further described in detail below with reference to the accompanying drawings and specific embodiments. It should be noted that, where there is no conflict, the embodiments of this utility model and the features within them can be combined with each other.

[0028] Many specific details are set forth in the following description in order to provide a full understanding of the present invention. However, the present invention may also be implemented in other ways different from those described herein. Therefore, the scope of protection of the present invention is not limited to the specific embodiments disclosed below.

[0029] Example 1

[0030] like Figure 1 and Figure 2The diagram illustrates a high-efficiency chemical wastewater treatment device, comprising a circular reaction cylinder 4. The circular reaction cylinder 4 contains a mixing module, which includes a first conical spiral tube 2 and a second conical spiral tube 3. Chemical wastewater is introduced into either the first or second conical spiral tube, while a reagent is introduced into the other conical spiral tube. The first and second conical spiral tubes 2 and 3 have the same axis, but their spiral directions are opposite. The spiral lines of the first and second conical spiral tubes 2 and 3 are conical spirals with a larger upper diameter and a smaller lower diameter. The outlets of the first and second conical spiral tubes 2 and 3 are opposite to each other. In the outlet region of the first and second conical spiral tubes 2 and 3, the wastewater spiral flow and the reagent spiral flow meet at the outlet, forming a three-dimensional turbulent field. This achieves efficient mixing and enhanced reaction of the fluids. The mixed liquid then converges within the circular reaction cylinder, with the first and second conical spiral tubes 2 and 3 immersed in the mixed liquid. The entrainment effect of the fluids at the outlets of the first and second conical spiral tubes 2 and 3 drives the surrounding liquid to mix, achieving rapid blending.

[0031] In some embodiments, the helix angle of the first conical helical tube 2 and the second conical helical tube 3 is between 15° and 30°.

[0032] In some embodiments, the taper of the first conical spiral tube 2 and the second conical spiral tube 3 is outward, and the taper of both the first conical spiral tube 2 and the second conical spiral tube 3 is between 1.2 and 1.5.

[0033] Example 2

[0034] Based on Example 1, such as Figure 1 and Figure 3As shown, it also includes an annular reaction cylinder 5, which includes an inner cylinder wall 51, an outer cylinder wall 52, and an annular bottom plate 53. The annular bottom plate 53 is located between the inner cylinder wall 51 and the outer cylinder wall 52. The area enclosed by the inner cylinder wall 51, the outer cylinder wall 52, and the annular bottom plate 53 is an annular stirring zone 7. The diameter of the inner cylinder wall 51 is smaller than the diameter of the circular reaction cylinder 4. The annular reaction cylinder 5 and the circular reaction cylinder 4 have the same axis. The annular reaction cylinder 5 is located vertically below the circular reaction cylinder 4. As chemical wastewater and reagents are introduced into the circular reaction cylinder 4, they fall freely from the top and converge into the coaxial... The annular reaction cylinder 5 and the circular reaction cylinder 4 form the first cylindrical zone 6. Below the annular reaction cylinder 5, the tank 1 forms the second cylindrical zone 8. Chemical wastewater and reagents are mixed in a spiral counter-current manner in the first cylindrical zone 6, and then flow into the annular stirring zone 7 for further stirring and flocculation. The flocculated material falls through the central circular hole of the annular zone to the second cylindrical zone 8 for further growth and sedimentation. The three-stage flocculation mechanism of the first cylindrical zone 6, the annular stirring zone 7, and the second cylindrical zone 8 adopts the concept of graded treatment, dividing the flocculation process into three stages, thereby achieving efficient flocculation treatment of chemical wastewater.

[0035] In some embodiments, the diameter of the inner cylinder wall 51 is between 0.4 and 0.6 times the diameter of the outer cylinder wall 52.

[0036] In some embodiments, the annular reaction cylinder 5 is equipped with a side wall stirrer 9 and a liquid addition device. The liquid addition mechanism can take many forms, such as quantitative liquid addition by weighing or liquid addition by rotating a screw to push the material.

[0037] This embodiment preferably provides a liquid addition device, including a limiting moving block 10, a rotating rod 11, a piston rod 12, a cylinder 13, a plunger 14, a cylinder body 15, a feed check valve 16, and a discharge check valve 17. The plunger 14 is fitted inside the cylinder body 15. The feed check valve 16, the discharge check valve 17, and the plunger 14 close the cylinder body 15. The cylinder 13 is connected to the plunger 14. Activating the cylinder 13 causes the plunger 14 to move axially back and forth within the cylinder body 15. When the plunger 14 moves backward, the cylinder body... As the internal space of cylinder 15 increases, the feed check valve 16 opens, and the agent is drawn into cylinder 15. When plunger 14 moves forward, the internal space of cylinder 15 decreases, and discharge check valve 17 opens. The feed check valve 16 of the liquid addition device is connected to the agent storage tank, and the agent is added into the annular stirring zone 7. The limiting moving block 10 is threaded onto the rotating rod 11. When the rotating rod 11 rotates around its own axis, the rotational motion is converted into the axial linear motion of the moving block using the thread. The piston rod 12 is connected to cylinder 13, making the moving distance of piston rod 12 adjustable, thereby further controlling the moving distance of plunger 14 to achieve quantitative liquid addition. The discharge check valve 17 of the liquid addition device is located within the flow field action area of ​​the side wall mixer 9, which is within the rotation trajectory of the blades of the side wall mixer 9.

[0038] In some embodiments, such as Figure 4 As shown, there are at least two sidewall mixers 9, which are evenly distributed circumferentially on the outer cylinder wall 52.

[0039] In some embodiments, the system also includes a tank body 1, the bottom of which is provided with a mud discharge pipe 18, and a solenoid valve 19 is provided on the mud discharge pipe 18.

[0040] Although preferred embodiments of the present invention have been described, those skilled in the art, upon learning the basic inventive concept, can make other changes and modifications to these embodiments. Therefore, the appended claims are intended to be interpreted as including the preferred embodiments as well as all changes and modifications falling within the scope of the present invention.

[0041] Obviously, those skilled in the art can make various modifications and variations to this utility model without departing from its spirit and scope. Therefore, if these modifications and variations fall within the scope of the claims of this utility model and their equivalents, this utility model also intends to include these modifications and variations.

Claims

1. A high-efficiency chemical wastewater treatment device, characterized in that, The device includes a circular reaction cylinder (4), which contains a mixing module. The mixing module includes a first conical spiral tube (2) and a second conical spiral tube (3). The first conical spiral tube (2) and the second conical spiral tube (3) have the same axis, and the spiral directions of the first conical spiral tube (2) and the second conical spiral tube (3) are opposite. The spiral lines of the first conical spiral tube (2) and the second conical spiral tube (3) are conical spiral lines with a larger upper diameter and a smaller lower diameter. The outlets of the first conical spiral tube (2) and the second conical spiral tube (3) are opposite to each other.

2. The high-efficiency chemical wastewater treatment device according to claim 1, characterized in that, The helix angle of the first conical helical tube (2) and the second conical helical tube (3) is between 15° and 30°.

3. The high-efficiency chemical wastewater treatment device according to claim 1, characterized in that, The length-to-diameter ratio of the first conical spiral tube (2) and the second conical spiral tube (3) is between 10 and 12.

4. The high-efficiency chemical wastewater treatment device according to claim 1, characterized in that, The first conical spiral tube (2) and the second conical spiral tube (3) have outward taper, and the taper of the first conical spiral tube (2) and the second conical spiral tube (3) is between 1.2 and 1.

5.

5. The high-efficiency chemical wastewater treatment device according to claim 1, characterized in that, It also includes an annular reaction cylinder (5), which includes an inner cylinder wall (51), an outer cylinder wall (52) and an annular bottom plate (53). An annular bottom plate (53) is provided between the inner cylinder wall (51) and the outer cylinder wall (52). The area enclosed by the inner cylinder wall (51), the outer cylinder wall (52) and the annular bottom plate (53) is an annular stirring zone (7). The diameter of the inner cylinder wall (51) is smaller than the diameter of the circular reaction cylinder (4). The annular reaction cylinder (5) is on the same axis as the circular reaction cylinder (4). The annular reaction cylinder (5) is located vertically below the circular reaction cylinder (4).

6. The high-efficiency chemical wastewater treatment device according to claim 5, characterized in that, The diameter of the inner cylinder wall (51) is between 0.4 and 0.6 times the diameter of the outer cylinder wall (52).

7. The high-efficiency chemical wastewater treatment device according to claim 5, characterized in that, The annular reaction cylinder (5) is equipped with a side wall agitator (9).

8. The high-efficiency chemical wastewater treatment device according to claim 7, characterized in that, The annular reaction cylinder (5) is equipped with a liquid addition device, which is used to add the agent to the annular stirring zone (7). The discharge check valve (17) of the liquid addition device is located in the flow field action area of ​​the side wall mixer (9), which is within the blade rotation trajectory of the side wall mixer (9).

9. The high-efficiency chemical wastewater treatment device according to claim 7, characterized in that, There are at least two sidewall mixers (9), which are evenly distributed circumferentially on the outer cylinder wall (52).

10. The high-efficiency chemical wastewater treatment device according to claim 1, characterized in that, It also includes a tank body (1), the bottom of which is provided with a mud discharge pipe (18), and a solenoid valve (19) is provided on the mud discharge pipe (18).

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