Self-splitting opposed-jet gas-liquid mixing system and use thereof

Abstract

The present invention provides a self-splitting opposed-jet gas-liquid mixing system and a use thereof. The system comprises a gas-liquid supply unit, a mixing unit, and a treatment unit which are sequentially communicated in a fluid flow direction, wherein the mixing unit comprises square-shaped flow splitting opposed-jet pipes, each flow splitting opposed-jet pipe comprises an inlet section in communication with the gas-liquid supply unit, a flow splitting section for splitting into two branch flows a gas-liquid flow flowing in from the inlet section, a flow combining section for combining the two branch flows and creating an opposed jet, and an outlet section in communication with the treatment unit, and the pipe diameters of each inlet section and each outlet section are equal. In the system, an opposed jet of gas-liquid flows is created in pipes by means of a plurality of square-shaped flow splitting pipes in combination with pump pressure, resulting in self-shearing of bubbles, the gas-liquid mixing time is short, the efficiency is high, and the number of micro-bubbles in a mixed product is large. Moreover, devices in the system are easy to mount, little space is occupied, and low subsequent maintenance costs are required, and thus the system has good market prospects.

Description

A self-diverting and counter-current gas-solution mixing system and its application Technical Field

[0001] This invention relates to the field of gas-solution mixing equipment, and more particularly to a self-diverting and counter-current gas-solution mixing system and its application. Background Technology

[0002] For over a century, dissolved air flotation (DAF) has been widely used in wastewater treatment. The DAF process generates fine bubbles. Hydrophobic particles leave the liquid, where adsorbed bubbles concentrate or filter waste (molecules, colloids, or large particles). Waste is selectively absorbed from the bubble surface; the separation efficiency depends largely on the number and volume of bubbles, and partly on differences in surface activity. Traditional wastewater treatment systems have the following significant drawbacks: 1. They occupy a huge amount of space, greatly increasing production and operating costs; 2. The output (bubble density and flow rate) cannot respond instantly to the input parameters (air supply and pump speed), lacking production flexibility.

[0003] Based on the above technical problems, the inventor applied for a patent on June 27, 2016 [CN106115834B], which discloses a multi-stage aeration generator and a sewage treatment method, including a generator body, a pressure monitoring device installed on the generator body, a venturi nozzle, a capillary tube and a concentric tube, wherein one end of the capillary tube is connected to the venturi nozzle and the other end is connected to the concentric tube.

[0004] This patented technology, through a combination of a multi-stage aerator, venturi nozzle, and concentric tube, can provide continuous and stable very fine foam, and can immediately adjust the output in response to changes in input operating parameters. It is used to regulate air feed and pump speed to generate appropriate foam density and size for subsequent treatment. However, it still has the following drawbacks in practical applications: the capillary tube structure, due to its small pore size and high density, can cause some obstruction to the gas-liquid mixture during use, affecting the stability of the flow pressure. After a period of use, the capillary pores may also become clogged, causing further obstruction. At the same time, the subsequent maintenance of the capillary tube will still require a large cost. The air intake of the venturi nozzle will also lead to unstable flow pressure, requiring a long pipeline to stabilize the pressure, which will also occupy a large space, thus limiting its long-term use. Summary of the Invention

[0005] The purpose of this invention is to address the shortcomings and deficiencies of existing technologies by providing a self-diverting and counter-current gas-solid mixing system and its application. This system uses a multi-segment loop-shaped diversion pipeline in conjunction with pump pressure to achieve gas-solid reaction in the pipeline, resulting in self-cutting of bubbles. The gas-solid mixing time is short and the efficiency is high, with a high amount of microbubbles in the mixed product. At the same time, the system itself is simple to install, occupies little space, and has low subsequent maintenance costs, thus having good market prospects.

[0006] To achieve the above objectives, the technical solution adopted by the present invention is: a self-diverting and counter-fluidizing gas-solid mixing system, comprising a gas-solid feeding unit, a mixing unit, and a processing unit connected sequentially along the fluid flow direction. The mixing unit includes a loop-shaped diverting and counter-fluidizing pipe, which includes an inlet section connected to the gas-solid feeding unit, a diversion section for dividing the gas-solid flowing in from the inlet section into two branches, a parallel flow section for merging the two branches and forming counter-fluidizing flow, and an outlet section connected to the processing unit. The diameters of the inlet section and the outlet section are equal.

[0007] Furthermore, the diversion section and the parallel flow section are mutually symmetrical three-way structures. The diversion section includes a first diversion trunk, a first diversion branch and a second diversion branch. One end of the first diversion trunk is connected to the gas-solid feed unit, and the other end is connected to the first diversion branch and the second diversion branch respectively.

[0008] The parallel flow section includes a first parallel flow trunk line, a first parallel flow branch line, and a second parallel flow branch line. The first branch line is connected to the first parallel flow branch line, and the second branch line is connected to the second parallel flow branch line. The ends of the first parallel flow branch line and the second parallel flow branch line that are away from the branch line section are connected to one end of the first parallel flow trunk line. The other end of the first parallel flow trunk line is connected to the processing unit.

[0009] Furthermore, the pipe diameters of the first branch and the second branch satisfy the following:

[0010] The sum of the flow rates of the first branch and the second branch is equal to the flow rate of the inlet section;

[0011] The flow rate refers to the amount of gaseous solution that passes through the pipeline within the designed time period.

[0012] Furthermore, the gas-liquid feeding unit includes a gas input pipe, a liquid input pipe, and a pressurizing device; both the gas input pipe and the liquid input pipe are connected to the input end of the pressurizing device, and the output end of the pressurizing device is connected to the mixing unit.

[0013] Furthermore, the pressurizing device is a centrifugal dissolved air pump, a gear dissolved air pump, or a screw dissolved air pump. The centrifugal dissolved air pump is suitable for situations where the gas-solid solution processing volume is small. When the gas-solid solution processing volume is large, the centrifugal dissolved air pump may experience cavitation interruption due to structural limitations, leading to unstable pressure and affecting the mixing effect. The gear dissolved air pump is suitable for situations where there are few liquid impurities and few particulate matter in the liquid. When there are many liquid impurities and many particulate matter in the liquid, the gear dissolved air pump will experience obvious lag or even jamming. Therefore, according to the site design requirements, it can be replaced with a screw dissolved air pump that will not experience cavitation interruption, lag, or jamming, but has a higher cost.

[0014] Furthermore, a pressure monitoring module is provided between the pressurizing device and the mixing unit. The pressure monitoring module includes a pressure sensor and a pressure display device. The pressure sensor is used to detect the output pressure of the pressurizing device. The pressure sensor is electrically connected to the pressure display device. The pressure sensor can sense the pressure data formed by the fluid in the device and feed it back to the pressure display device to remind the operator.

[0015] Another object of the present invention is to provide a wastewater treatment method using the above-described gas-solution mixing system, comprising the following steps:

[0016] S1. Air and wastewater are pressurized through the gas-solution feeding unit to form a gas-solution and then fed into the mixing unit;

[0017] S2. Under the action of the diversion and counter-fluid pipe in the mixing unit, the gas-solid solution is first diverted to form two branches, and then the two branches are made to counter-fluidize each other, cutting and breaking the air bubbles in the gas-solid solution before being fed into the processing unit.

[0018] The S3 gas solution is filtered and treated as wastewater through the flotation tank of the treatment unit.

[0019] Furthermore, in step S2, the diversion and flushing pipes in the mixing unit are connected front and rear in the mixing unit. The gas-solid mixture enters the inlet section of the diversion and flushing pipe. When the gas-solid mixture passes through the diversion section at a set flow rate under the pressure of the pressurizing device in S1, the three-way structure of the diversion section will disrupt the spiral flow formed by the gas-solid mixture in the first diversion trunk, causing it to be evenly diverted into the first and second diversion branches respectively. This ensures that the sum of the flow rates in the first and second diversion branches equals the flow rate at the inlet section. The flow rate is interpreted as one unit. The amount of gas-solid solution passing through the pipeline under a specified pressure within a given time period; when the gas-solid solution from the first branch and the second branch merges into the first parallel branch and the second parallel branch respectively, the gas-solid solution in the parallel section will form two opposing gas-solid solutions. During the opposing process, the bubbles in the two gas-solid solutions are cut by the bubbles themselves and the impurity particles carried by the gas-solid solution, forming microbubbles, which then enter the next branch opposing pipe to form a second cutting, and so on until the outlet section of the last branch opposing pipe outputs a fully mixed gas-solid solution.

[0020] Furthermore, in step S2, the mixing unit is connected to the processing unit in step S3 at the outlet section of the last component diversion and flushing pipe. The processing unit includes a spraying device and an air flotation cylinder. The gas-solid solution after passing through the mixing unit flows to the air flotation cylinder through the spraying device.

[0021] Furthermore, in step S3, the spraying device is equipped with a valve to eliminate excessive turbulent water flow. A separation chamber is set in the middle of the spraying device, and an air release pipe is set at the top of the separation chamber to discharge excessive suspended gas and undissolved bubbles, so as to avoid affecting the interception quality.

[0022] The beneficial effects of this invention are: the system replaces the capillary aeration device with a self-diverting counter-fluidized pipeline, which ensures the gas-solid mixing effect while preventing clogging and reducing operating and maintenance costs. At the same time, the improved structure of the flotation tank effectively reduces the gaps between bubbles and prevents adhering substances from falling off. It has good application results in sewage treatment, effectively reducing subsequent drug administration costs and improving the decontamination effect. It also has good application prospects in other fields. Attached Figure Description

[0023] The accompanying drawings, which are provided to further illustrate the invention and form part of this application, are not intended to limit the scope of the invention.

[0024] Figure 1 is a schematic diagram of a gas-solution mixing system.

[0025] Figure 2 is a schematic diagram of the treatment unit of the gas-solution mixing system in the wastewater treatment method.

[0026] Wherein: 11 is the gas inlet, 12 is the liquid inlet, 13 is the pressurization device, 14 is the pressure monitoring module, 2 is the mixing unit, 21 is the diversion flushing pipe, 3 is the treatment unit, 31 is the flotation tank, and 32 is the spraying device. Detailed Implementation

[0027] The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of the present invention.

[0028] In the description of this invention, it should be noted that the terms "vertical," "upper," "lower," "horizontal," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0029] In the description of this invention, it should also be noted that, unless otherwise explicitly specified and limited, the terms "set," "install," "connect," and "link" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0030] As shown in Figure 1-2, a self-diverting and counter-fluidizing gas-solid mixing system includes a gas-solid feeding unit, a mixing unit 2, and a processing unit 3 connected sequentially along the fluid flow direction. The mixing unit 2 includes a loop-shaped diverting and counter-fluidizing pipe 21. The diverting and counter-fluidizing pipe 21 includes an inlet section connected to the gas-solid feeding unit, a diversion section for dividing the gas-solid flowing in from the inlet section into two branches, a parallel flow section for merging the two branches and forming counter-fluidizing flow, and an outlet section connected to the processing unit 3. The diameters of the inlet section and the outlet section are equal.

[0031] Furthermore, the diversion section and the parallel flow section are mutually symmetrical three-way structures. The diversion section includes a first diversion trunk, a first diversion branch and a second diversion branch. One end of the first diversion trunk is connected to the gas-solid feed unit, and the other end is connected to the first diversion branch and the second diversion branch respectively.

[0032] The parallel flow section includes a first parallel flow trunk line, a first parallel flow branch line, and a second parallel flow branch line. The first branch line is connected to the first parallel flow branch line, and the second branch line is connected to the second parallel flow branch line. The ends of the first parallel flow branch line and the second parallel flow branch line that are away from the branch line are connected to one end of the first parallel flow trunk line. The other end of the first parallel flow trunk line is connected to the processing unit 3.

[0033] When the gas-solid mixture from the first branch and the second branch merges into the first parallel branch and the second parallel branch respectively, the gas-solid mixture in the parallel section will form two opposing gas-solid mixtures. During the opposing process, the bubbles in the two gas-solid mixtures are cut by the bubbles themselves and the impurity particles carried by the gas-solid mixture, forming microbubbles. These microbubbles then enter the next branch opposing pipe 21 to form a second cutting, and so on until the fully mixed gas-solid mixture is output from the outlet section of the last branch opposing pipe 21.

[0034] In specific implementation, the pipe diameters of the first branch and the second branch satisfy the following:

[0035] The sum of the flow rates of the first branch and the second branch is equal to the flow rate of the inlet section;

[0036] The flow rate refers to the amount of gaseous solution that passes through the pipeline within the designed time period.

[0037] The closer the included angle between the first parallel main road and the first parallel branch road and the second parallel branch road of the parallel section is to 90°, the greater the impact force formed by the relative collision of gas and liquid in the first parallel branch road and the second parallel branch road, and the better the cutting effect.

[0038] In a specific implementation, the gas-liquid feeding unit includes a gas input pipe, a liquid input pipe, and a pressurizing device; both the gas input pipe and the liquid input pipe are connected to the input end of the pressurizing device, and the output end of the pressurizing device is connected to the mixing unit.

[0039] In specific implementation, the pressurizing device 13 is a centrifugal dissolved air pump, a gear dissolved air pump, or a screw dissolved air pump. The centrifugal dissolved air pump is suitable for situations where the gas-solid solution processing volume is small. When the gas-solid solution processing volume is large, the centrifugal dissolved air pump may experience cavitation interruption due to structural limitations, leading to unstable pressure and affecting the mixing effect. The gear dissolved air pump is suitable for situations where there are few liquid impurities and few particulate matter in the liquid. When there are many liquid impurities and many particulate matter in the liquid, the gear dissolved air pump will experience obvious lag or even jamming. Therefore, according to the site design requirements, it can be replaced with a screw dissolved air pump that will not experience cavitation interruption, lag, or jamming, but has a higher cost.

[0040] In a specific implementation, a pressure monitoring module 14 is provided between the pressurizing device 13 and the mixing unit 2. The pressure monitoring module 14 includes a pressure sensor and a pressure display device. The pressure sensor is used to detect the output pressure of the pressurizing device 13. The pressure sensor is electrically connected to the pressure display device. The pressure sensor can sense the pressure data formed by the fluid in the device and feed it back to the pressure display device to remind the operator to pay attention.

[0041] Another object of the present invention is to provide a wastewater treatment method using the above-described gas-solution mixing system, comprising the following steps:

[0042] S1. Air and wastewater are pressurized through the gas-solution feeding unit to form a gas-solution and then fed into the mixing unit 2;

[0043] S2. Under the action of the diversion and counter-flushing pipe 21 in the mixing unit, the gas-solid solution is first divided into two branches, and then the two branches are made to counter-fluidize each other, cutting and breaking the bubbles in the gas-solid solution before being fed into the processing unit 3.

[0044] In actual operation, the diversion and flushing pipe 21 set in the mixing unit in step S2 is connected before and after in the mixing unit 2. The gas-solid enters the inlet section of the diversion and flushing pipe 21. When the gas-solid passes through the diversion section at a set flow rate under the pressure of the pressurizing device 13 in S1, the three-way structure of the diversion section will cause the spiral flow formed by the gas-solid in the first diversion trunk to be dispersed, so that it is evenly diverted into the first diversion branch and the second diversion branch respectively, and ensures that the sum of the flow rates in the first diversion branch and the second diversion branch is equal to the flow rate of the inlet section. The flow rate is interpreted as the amount of gas-solid passing through the pipe under a specified pressure per unit time. When the gas-solid from the first diversion branch and the second diversion branch merges into the first parallel branch and the second parallel branch respectively and enters the first parallel trunk, the gas-solid in the parallel section will form The two gas-solution streams collide and are cut by the bubbles themselves and the impurity particles carried by the gas-solution streams, forming microbubbles. These microbubbles then enter the next set of flow-through counter-current pipes 21 for a second cut, and so on until the fully mixed gas-solution stream is output from the outlet section of the last set of flow-through counter-current pipes 21. Since the mixing unit 2 is composed of conventional pipes without complex components, a higher pump pressure can be set. According to Henry's Law (pB = kx, BxB), when the equilibrium liquid pressure pB is fixed, the higher the pump pressure, the higher the constant kx, B, and the higher the gas solubility xB will be. The pipes of the mixing unit 2 are sufficient to withstand a flow pressure of nearly 1000 bar. According to Henry's Law, the higher the pump pressure, the higher the gas solubility xB will be, providing a higher upper limit for gas solubility.

[0045] S3. The gas-solid mixture is filtered and treated as wastewater through the flotation tank 31 of the treatment unit 3.

[0046] In actual operation, the mixing unit in step S2 is connected to the processing unit in step S3 at the outlet section of the last component diversion and flushing pipe. The processing unit includes a spraying device and an air flotation cylinder. The gas-solid solution after passing through the mixing unit flows to the air flotation cylinder through the spraying device. The top of the air flotation cylinder is provided with an inclined plate. The inclined plate acts to gradually reduce the horizontal surface area of ​​the top of the air flotation cylinder, squeezing the microbubbles released by the spraying device and reducing the gaps between the bubbles during the rise of the microbubbles. Due to the high-speed movement of water molecules and air molecules in different directions in the gas-solid solution, large-scale microbubbles will form charged particles. The integrated charged bubbles change the surface tension of the water to help adsorb colored groups and some hydrophilic colloids. Reducing the gaps between the bubbles helps to prevent the adhering substances (suspended solids SS, organic pollutants COD, etc.) from falling off, and at the same time reduces the cost of adding chemicals (polyaluminum chloride PAC, polyacrylamide PAM, etc.) in subsequent treatment stages.

[0047] In actual operation, the spraying device 32 in step S3 is equipped with a valve to eliminate excessive turbulent water flow. A separation chamber is set in the middle of the spraying device 32, and an air release pipe is set at the top of the separation chamber to discharge excessive suspended gas and undissolved bubbles to avoid affecting the interception quality. If the gas solubility is sufficient, the valve can be removed to ensure the gas-solid release flow rate.

[0048] In one embodiment, a dyeing and finishing plant used the old-style dissolved air flotation (i.e., using a pressure dissolved air tank for gas-liquid mixing) mentioned in the background art for wastewater treatment to remove non-hydrophilic pollutants (such as surfactants, detergents, etc.) from the dyeing and finishing wastewater. The final effect is that the size of the foam can be reduced to 1-10 micrometers, and the air solubility reaches 10-15% molar fraction. Static flotation is performed using a solid-liquid separation tank. After treatment, the chemical oxygen demand (COD) of the product is reduced from 3000 mg / L to less than 800 mg / L. Due to factors such as fewer bubbles, taking the treatment of 1 cubic meter of wastewater per hour as an example, a solid-liquid separation tank with a capacity of 1.5 cubic meters is required for static flotation, which occupies a large space.

[0049] In another embodiment, a dyeing and finishing plant adopted a multi-stage aerator and a wastewater treatment method as described in the patent [CN106115834B] mentioned in the background art. This method removes non-hydrophilic pollutants (such as surfactants, detergents, etc.) from the dyeing and finishing wastewater. The pumping design pressure is set at 10 bar, and the operating liquid temperature is 25-30°C. The final effect is that the size of the foam can be reduced to 1-10 micrometers, the air solubility can be increased to 15-25% mole fraction, and the chemical oxygen demand (COD) of the treated product is reduced from 3000 mg / L to less than 500 mg / L. However, there is a clogging problem. After nearly 4 months of long-term operation, dirt gradually accumulates in the gap between the capillaries and capillary tubes, resulting in significant clogging and reduced efficiency. The capillary tubes need to be replaced, resulting in certain downtime and maintenance costs.

[0050] In another embodiment, a dyeing and bleaching plant adopted the wastewater treatment method of the present invention using a self-diverting counter-fluidized air-solution mixing system to remove non-hydrophilic pollutants (such as surfactants, detergents, etc.) from the dyeing and bleaching wastewater. The design pressure of the pump was set at 10 bar, and the operating liquid temperature was 25-30°C. The final effect achieved was that the size of the foam could be reduced to 1-10 micrometers, the air solubility could be increased to 15-25% mole fraction, and the chemical oxygen demand (COD) of the treated product was reduced from 3000 mg / L to less than 500 mg / L. No problems requiring shutdown for maintenance, such as clogging, were observed during a period of long-term operation of more than 6 months. At the same time, the start-up cost of the equipment was reduced by 40%, the operating cost of the air flotation equipment, such as pump electricity costs, was reduced by 30%, and the subsequent treatment cost, such as subsequent AAO dosing costs, was reduced by 50%. Furthermore, the shedding rate of the adhering substances (polluting and bleaching wastewater particles, etc.) in the air flotation tank was greatly reduced, and the separation effect was effectively improved in conjunction with the scraper.

[0051] In summary, this invention ensures effective gas-liquid mixing while preventing clogging and reducing operating costs. Furthermore, the improved flotation tank structure effectively reduces gaps between bubbles, preventing the shedding of adhering substances and lowering equipment footprint and maintenance costs. It demonstrates excellent performance in wastewater treatment, effectively reducing subsequent drug administration costs and improving decontamination efficiency. It also shows promising application prospects in other fields, such as gas-gas mixing, gas-liquid mixing, and liquid-liquid mixing.

[0052] Although embodiments of the invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the appended claims and their equivalents.

Claims

1. A self-diverting and counter-current gas-solution mixing system, comprising a gas-solution feeding unit, a mixing unit, and a processing unit connected sequentially along the fluid flow direction, characterized in that: The mixing unit includes a loop-shaped diversion and flushing pipe, which includes an inlet section connected to the gas-solution supply unit, a diversion section for dividing the gas-solution flowing in from the inlet section into two branches, a parallel flow section for merging the two branches and forming a flushing, and an outlet section connected to the processing unit. The diameters of the inlet section and the outlet section are equal.

2. The self-diverting and counter-current gas-solution mixing system according to claim 1, characterized in that: The diversion section and the parallel flow section are symmetrical three-way structures. The diversion section includes a first diversion trunk, a first diversion branch and a second diversion branch. One end of the first diversion trunk is connected to the gas-solid feed unit, and the other end is connected to the first diversion branch and the second diversion branch respectively. The parallel flow section includes a first parallel flow trunk line, a first parallel flow branch line, and a second parallel flow branch line. The first branch line is connected to the first parallel flow branch line, and the second branch line is connected to the second parallel flow branch line. The ends of the first parallel flow branch line and the second parallel flow branch line that are away from the branch line section are connected to one end of the first parallel flow trunk line. The other end of the first parallel flow trunk line is connected to the processing unit.

3. The self-diverting and counter-current gas-solution mixing system according to claim 2, characterized in that: The pipe diameters of the first branch and the second branch satisfy the following: The sum of the flow rates of the first branch and the second branch is equal to the flow rate of the inlet section; The flow rate refers to the amount of gaseous solution that passes through the pipeline within the designed time period.

4. The self-diverting and counter-current gas-solution mixing system according to claim 1, characterized in that: The gas-liquid feeding unit includes a gas input pipe, a liquid input pipe, and a pressurizing device; both the gas input pipe and the liquid input pipe are connected to the input end of the pressurizing device, and the output end of the pressurizing device is connected to the mixing unit.

5. A self-diverting and counter-current gas-solution mixing system according to claim 4, characterized in that: The pressurizing device is a centrifugal dissolved air pump, a gear dissolved air pump, or a screw dissolved air pump.

6. The self-diverting and counter-current gas-solution mixing system according to claim 4, characterized in that: A pressure monitoring module is provided between the pressurizing device and the mixing unit. The pressure monitoring module includes a pressure sensor and a pressure display device. The pressure sensor is used to detect the output pressure of the pressurizing device, and the pressure sensor and the pressure display device are electrically connected.

7. The application of the gas-solution mixing system according to any one of claims 1-6 in a wastewater treatment method, characterized in that, The steps are as follows: S1. Air and wastewater are pressurized through the gas-solution feeding unit to form a gas-solution and then fed into the mixing unit; S2. Under the action of the diversion and counter-fluid pipe in the mixing unit, the gas-solid solution is first diverted to form two branches, and then the two branches are made to counter-fluidize each other, cutting and breaking the air bubbles in the gas-solid solution before being fed into the processing unit. The S3 gas solution is filtered and treated as wastewater through the flotation tank of the treatment unit.

8. A wastewater treatment method according to claim 7, characterized in that: In step S2, the mixing unit is connected to the processing unit in step S3 at the outlet section of the last component diversion and flushing pipe. The processing unit includes a spraying device and an air flotation cylinder. The gas-solid mixture after passing through the mixing unit flows to the air flotation cylinder through the spraying device.

9. A wastewater treatment method according to claim 7, characterized in that: In step S3, the spraying device is equipped with a valve, a separation chamber is set in the middle of the spraying device, and an air release pipe is set at the top of the separation chamber.

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