Logarithmic spiral structure-based material distribution device of efficient thickener

Abstract

The utility model belongs to the technical field of thickeners, and particularly relates to a logarithmic spiral structure-based material distribution device of a high-efficiency thickener. The utility model provides the material distribution device based on the logarithmic spiral structure of the efficient thickener, which is used for enhancing the mixing and flocculation effects. The device comprises a main body channel, an ore inlet pipe is arranged at one end of the main body channel, a discharge port is formed in the bottom of the main body channel, a flocculant adding point is arranged above the main body channel, and a dilution port is formed in the side of the main body channel. The diameter of the channel body is gradually reduced along with the end away from the ore inlet pipe.

Description

Technical Field

[0001] This utility model belongs to the field of thickener technology, specifically relating to a high-efficiency thickener based on a logarithmic spiral structure for fabric distribution. Background Technology

[0002] In modern industrial production, thickeners play a vital role in many fields such as mining, chemical industry, metallurgy, and environmental protection. Their main function is to achieve solid-liquid separation, and the application of flocculants is a key step in improving the separation efficiency of thickeners. However, there are still many problems in the flocculant distribution process of thickeners.

[0003] In traditional thickener operations, the slurry typically enters the thickener at a high flow rate. This high-speed flow creates a complex flow field, which, on the one hand, makes it difficult for the flocculant to mix quickly and evenly with the slurry after addition. Due to the rapid flow of the slurry, the flocculant may be washed away before it is fully dispersed, failing to make sufficient contact with suspended particles in the slurry, thus affecting the flocculation effect. For example, in some mineral processing steps, the slurry contains mineral particles of various sizes and densities. If the flocculant is not evenly distributed, some particles may fail to flocculate and settle effectively, thereby reducing the efficiency of the entire mineral processing flow.

[0004] On the other hand, traditional flocculant addition methods often involve single-point or small-point addition. For large thickeners, this method cannot meet the flocculant requirements of different areas within the thickener. Taking a large-scale chemical wastewater treatment thickener as an example, its processing capacity is enormous, and adding flocculant at a single or few points cannot guarantee uniform coverage of the flocculant across the entire cross-section of the thickener. This results in significant differences in flocculation effects in different areas, leading to uneven solids settling at the bottom of the thickener, which affects subsequent treatment and the stable operation of the equipment.

[0005] Furthermore, as industrial production moves towards large-scale and high-efficiency operations, higher demands are placed on the processing capacity and quality of thickeners. Existing flocculant distribution devices often exhibit significant limitations when facing complex conditions such as high-concentration slurries, high-flow-rate conditions, and complex slurry compositions. They fail to effectively ensure uniform distribution of flocculant in the slurry under various complex conditions, thus hindering the overall performance improvement of the thickener and increasing production costs and environmental pressures. Therefore, there is an urgent need for an innovative flocculant distribution device for thickeners to solve these problems, improve flocculant distribution quality and thickener efficiency, and meet the needs of modern industrial production. Utility Model Content

[0006] This invention addresses the aforementioned problems by providing a high-efficiency thickener based on a logarithmic spiral structure for fabric application, which enhances mixing and flocculation effects.

[0007] The present invention adopts the following technical solution: the present invention includes a main channel, an inlet pipe at one end of the main channel, an outlet at the bottom of the main channel, a flocculant addition point at the top of the main channel, and a dilution port at the side of the main channel. The main feature is that the main body of the channel is a logarithmic spiral-shaped channel, the diameter of the inlet pipe at the main body of the channel is the largest, and the diameter of the main body of the channel gradually decreases as it moves away from the inlet pipe.

[0008] As a preferred embodiment of this utility model, the flocculant addition points are evenly distributed above the main channel; for main channels with a maximum diameter of less than 5m, at least 3 flocculant addition points are provided; for main channels with a maximum diameter of more than 5m, at least 5 flocculant addition points are provided.

[0009] Furthermore, the flocculant addition point includes a flocculant supply pipeline, which is equipped with a flow regulating valve and a flow monitor corresponding to the main channel.

[0010] As another preferred embodiment of this utility model, the cross-section of the main channel includes a main channel with a rectangular upper cross-section, and a discharge channel with a trapezoidal cross-section below the main channel, with the discharge port located at the bottom of the discharge channel.

[0011] Furthermore, multiple flow-blocking plate assemblies are distributed in the middle of the main channel. Each flow-blocking plate assembly includes an upper plate and a lower plate, and both the upper and lower plates have through holes on their surfaces. Both the upper and lower plates are inclined.

[0012] Furthermore, the upper plate and the lower plate form an angle of 30 to 60 degrees; a gap is provided between the upper plate and the lower plate; and the end where the extension lines of the upper plate and the lower plate intersect corresponds to one end of the ore inlet pipe.

[0013] Furthermore, the through holes of the flow baffle plate gradually decrease in size starting from one end of the ore inlet pipe.

[0014] As a third preferred embodiment of this utility model, multiple dilution ports are evenly distributed on the side of the main channel; the dilution ports are connected to independent diluent supply pipelines.

[0015] As a fourth preferred embodiment of this utility model, the total area of ​​the discharge port is 1.5 times the inner diameter area of ​​the inlet pipe.

[0016] The beneficial effects of this utility model are as follows: By setting up a flow baffle, a logarithmic spiral channel, multiple flocculant addition points, a dilution port and a discharge port, this utility model effectively reduces the slurry flow rate, extends the residence time, and enhances the turbulent mixing effect, thereby achieving uniform distribution of flocculant, improving flocculation efficiency and solid-liquid separation effect, adapting to complex working conditions, improving the thickener's processing capacity and operational stability, reducing costs, and enhancing economic benefits. Attached Figure Description

[0017] Figure 1 This is a schematic diagram of the structure of this utility model.

[0018] Figure 2 This is a schematic diagram of the bottom structure of this utility model.

[0019] Figure 3 This is a top view of the present invention.

[0020] Figure 4 This is a schematic diagram of the flow baffle assembly.

[0021] Figure 5 yes Figure 3 AA sectional view.

[0022] In the attached diagram, 1 is the main channel, 11 is the main channel, 12 is the discharge channel, 2 is the flocculant addition point, 3 is the baffle plate group, 31 is the upper plate, 32 is the lower plate, 4 is the discharge port, 5 is the dilution port, and 6 is the ore inlet pipe. Detailed Implementation

[0023] This utility model includes a main channel 1, with an inlet pipe 6 at one end of the main channel 1, an outlet 4 at the bottom of the main channel 1, a flocculant addition point 2 at the top of the main channel 1, and a dilution port 5 on the side of the main channel 1. The main channel is a logarithmic spiral-shaped channel. The diameter of the inlet pipe 6 is the largest at one end of the main channel, and the diameter of the main channel gradually decreases as it moves away from the end of the inlet pipe 6.

[0024] The main channel 1 of this invention adopts a logarithmic spiral shape, constructed using a mathematical model. The channel width and maximum diameter can be determined based on the slurry volume, diameter, and flow rate, which is a conventional technique in this field. This logarithmic spiral structure enables the flocculant to form a uniform coverage trajectory within the distribution device when sprayed from the pipe. The lining of the main channel 1 can be made of a high-strength, corrosion-resistant, wear-resistant layer, such as ultra-high molecular weight polyethylene. The main channel 1 ensures uniform flow rate of the slurry within the channel, avoiding uneven distribution caused by sudden changes in flow rate.

[0025] The flocculant addition points 2 are evenly distributed above the main channel 1; for main channels 1 with a maximum diameter of less than 5m, at least 3 flocculant addition points 2 are set; for main channels 1 with a maximum diameter of more than 5m, at least 5 flocculant addition points 2 are set.

[0026] By uniformly setting multiple flocculant addition points 2 along the flow direction above the main channel 1, and setting different numbers of addition points according to different maximum diameters of the channel, the flocculant can be distributed as needed at different locations, allowing it to continuously enter the fluid system at different stages. This effectively avoids the problem of excessively high or insufficient local concentration caused by concentrated addition of flocculant at one time, thereby improving the uniformity and sufficiency of the flocculation reaction and enhancing the system's processing capacity and adaptability.

[0027] The flocculant addition point 2 includes a flocculant supply pipeline, which is equipped with a flow regulating valve and a flow monitor corresponding to the main channel 1.

[0028] By installing flow regulating valves and flow monitors on the flocculant supply pipeline, precise control and real-time monitoring of the flocculant dosage can be achieved. The addition rate can be flexibly adjusted according to changes in slurry concentration and channel location differences to avoid over- or under-dosing, thereby improving reaction efficiency and flocculant utilization. At the same time, the system automation and operational stability are enhanced, facilitating centralized control and remote adjustment.

[0029] The main channel 1 has a cross-section including a main channel 11 with a rectangular upper cross-section, and a discharge channel 12 with a trapezoidal cross-section below the main channel 11. The discharge port 4 is located at the bottom of the discharge channel 12.

[0030] By setting the cross-sectional structure of the main channel 1 to a composite form of an upper rectangle and a lower trapezoid, the upper main channel 11 can maintain a stable flow rate and ensure thorough mixing, while the lower trapezoidal structure forms a natural settling zone, which is conducive to the settling and concentration of mineral particles after flocculation. The discharge port 4 is located at the bottom, which can directly draw out the sediment, reduce the probability of blockage, improve discharge efficiency, and contribute to the efficient operation and convenient maintenance of the system as a whole.

[0031] Multiple flow-blocking plate groups 3 are arranged in the middle of the main channel 11. Each flow-blocking plate group 3 includes an upper plate 31 and a lower plate 32. Both the upper plate 31 and the lower plate 32 have through holes on their surfaces. Both the upper plate 31 and the lower plate 32 are inclined.

[0032] The upper plate 31 and the lower plate 32 form an angle of 30 to 60 degrees; a gap is provided between the upper plate 31 and the lower plate 32; one end of the extension lines of the upper plate 31 and the lower plate 32 intersects with one end of the ore inlet pipe 6.

[0033] The through holes of the flow baffle plate gradually decrease in size starting from one end of the ore inlet pipe 6.

[0034] By setting multiple inclined baffle plates 3 with through holes in the middle of the main channel 11, the upper plate 31 and the lower plate 32 together form a multi-level turbulence structure, causing the slurry to form turbulence and stratification during flow. The flow is guided through the holes to penetrate locally, while the overall streamline is deflected, thereby enhancing the mixing effect of the slurry, increasing the contact frequency and uniformity between the flocculant and mineral particles, and promoting floc formation. Setting the upper and lower baffle plates at an angle of 30-60° with gaps, and having their extension lines converge in the direction of the inlet pipe 6, can guide the fluid to form a regular guiding path and swirling zone between the plates, enhancing fluid disturbance and mixing, while avoiding the formation of dead zones or sedimentation zones, improving the flow distribution, and effectively improving the efficiency of the flocculation reaction and space utilization. By designing the flow baffle plate with the through-hole size gradually decreasing from the ore inlet, it can adapt to the trend of the fluid velocity gradually slowing down. This allows the faster flow velocity in the front section to quickly penetrate the large hole, while the lower flow velocity in the rear section is controlled to pass through the small hole. This creates a gradient turbulence and flow distribution throughout the channel, enhances the residence time and mixing uniformity of the slurry in each area, and effectively promotes the settling of large particles and the flocculation of small particles.

[0035] Multiple dilution ports 5 are evenly distributed on the side of the main channel 1; the dilution ports 5 are connected to independent diluent supply pipelines.

[0036] By uniformly setting dilution ports 5 on the side of the channel and connecting them to independent diluent supply pipes, diluent can be introduced into different areas to adjust the concentration of high-concentration slurry in stages, so that the flocculant is more evenly dispersed in the diluted system, improving the reaction rate and floc formation effect, while avoiding the risk of incomplete agglomeration or blockage caused by excessive concentration, thus enhancing the system's flexibility and stability.

[0037] The total area of ​​the discharge port 4 is 1.5 times the inner diameter area of ​​the inlet pipe 6.

[0038] By setting the total area of ​​the discharge port 4 to 1.5 times the inner diameter area of ​​the inlet pipe 6, it can be ensured that the discharge port 4 will not become a bottleneck for fluid passage during the process of the slurry passing through the main channel 1, effectively reducing the flow velocity and pressure at the outlet, preventing backflow, eddy currents and sedimentation, improving discharge efficiency and overall smoothness, and ensuring long-term continuous and stable operation of the device.

[0039] This invention achieves thorough and uniform mixing of flocculant with the slurry by reducing velocity, modifying flow pattern, and increasing residence time through internal baffles, combined with the uniform addition of flocculant at multiple top points. This ensures sufficient contact between the flocculant and suspended particles, forming superior flocs, improving solid-liquid separation efficiency, and reducing particle residue. It addresses different thickeners, slurry properties, and processing conditions, ensuring uniform flocculant distribution to meet production requirements. It enhances stability and maintainability: ensuring structural stability, easy maintenance and troubleshooting of components, stable operation, and continuous production. It strengthens flocculation and adaptability to various operating conditions, improves thickener efficiency, reduces flocculant waste and maintenance costs, and enhances economic benefits.

[0040] Example: Flow baffle assembly 3. The flow baffles inside the device are arranged in a multi-layered, inclined configuration, and are made of high-strength, wear-resistant materials (such as stainless steel, high-manganese steel, etc.). Each layer of flow baffles has several through holes of different sizes, the diameter of which gradually decreases from the end near the ore inlet to the end near the discharge outlet 4. The intersection angle between adjacent layers of flow baffles is between 30° and 60°.

[0041] When the slurry enters the device, it first comes into contact with the first layer of baffles, where some of its kinetic energy is consumed and its flow velocity decreases. Turbulence is generated as the slurry passes through the through-holes in the baffles, resulting in a more uniform particle distribution. As the slurry continues to flow, passing through multiple layers of cross-arranged baffles, its flow velocity further decreases and the flow becomes more turbulent, creating favorable conditions for thorough mixing of the flocculant and the slurry.

[0042] Multiple flocculant addition points 2 are set at the top of the main channel 1, the number of which is determined according to the diameter or side length of the thickener. For a cloth-laying device with a diameter of less than 5 meters, the number of addition points shall not be less than 3; for a cloth-laying device with a diameter of more than 5 meters, the number of addition points shall not be less than 5. These addition points are evenly distributed, forming a circumferential distribution at the top of the cloth-laying device.

[0043] Each flocculant addition point 2 is connected to an independent flocculant supply pipeline, which is equipped with a flow regulating valve and a flow monitor. The control system precisely controls the flocculant flow rate at each addition point by adjusting the flow regulating valve based on parameters such as the slurry level and concentration in the thickener, ensuring that the flocculant is evenly added to the slurry from multiple points.

[0044] Diluting ports 5 are evenly distributed on the outer side of the logarithmic spiral pipe. The number, size, and spacing of the diluting ports 5 are determined based on the feed rate, feed concentration, and the amount of water required for dilution of the thickener. For example, if the feed rate is 200 tons / hour and the feed concentration is 20%, and the slurry needs to be diluted to 10%, calculations show that 1000 cubic meters / hour of water needs to be added. According to the hydraulic equation, a dilution area with a cross-sectional area of ​​0.185 square meters needs to be designed. Then, the number and location of the diluting ports 5 are designed according to the diameter of the distribution cylinder. Each diluting port 5 is connected to an independent diluent supply pipe. The diluent can be water or other liquids compatible with flocculants and slurry.

[0045] Multiple small discharge ports 4 are provided at the bottom of the device, and the total area of ​​the discharge ports 4 is designed to be 1.5 times the area of ​​the inlet pipe 6. This structure is based on the fluid dynamics study of the mixing of slurry and flocculant in the thickener. When the area of ​​the small discharge ports 4 and the area of ​​the inlet pipe 6 meet this ratio, the flocculant can better interact with the slurry entering the thickener after being sprayed from the discharge ports 4.

[0046] It is understood that the above specific description of this utility model is only used to illustrate this utility model and is not limited to the technical solutions described in the embodiments of this utility model. Those skilled in the art should understand that modifications or equivalent substitutions can still be made to this utility model to achieve the same technical effect; as long as the use needs are met, they are all within the protection scope of this utility model.

Claims

1. A high-efficiency thickener based on a logarithmic spiral structure cloth device, comprising a main channel (1), one end of the main channel (1) is provided with a mine inlet pipe (6), the bottom of the main channel (1) is provided with a discharge port (4), the upper side of the main channel (1) is provided with a flocculating agent adding point (2), and the side of the main channel (1) is provided with a dilution port (5), characterized in that: The main channel is a logarithmic spiral-shaped channel. The diameter of the main channel is largest at one end of the ore inlet pipe (6), and gradually decreases as the end moves away from the ore inlet pipe (6).

2. The high-efficiency thickener based on the logarithmic spiral structure distributing device according to claim 1, characterized in that: The flocculant addition points (2) are evenly distributed above the main channel (1); for the main channel (1) with a maximum diameter of less than 5m, at least 3 flocculant addition points (2) are set; for the main channel (1) with a maximum diameter of more than 5m, at least 5 flocculant addition points (2) are set.

3. A high efficiency thickener based on the logarithmic spiral structure of the distribution device according to claim 2, characterized in that: The flocculant addition point (2) includes a flocculant supply pipeline, and the flocculant supply pipeline is equipped with a flow regulating valve and a flow monitor corresponding to the main channel (1).

4. The high-efficiency thickener based on the logarithmic spiral structure distributing device according to claim 1, characterized in that: The main channel (1) has a cross-section including a main channel (11) with a rectangular upper cross-section, and a discharge channel (12) with a trapezoidal cross-section below the main channel (11). The discharge port (4) is located at the bottom of the discharge channel (12).

5. A high efficiency thickener based on the logarithmic spiral clothings according to claim 4, characterized in that: Multiple flow-blocking plate groups (3) are arranged in the middle of the main channel (11). Each flow-blocking plate group (3) includes an upper plate (31) and a lower plate (32). Both the upper plate (31) and the lower plate (32) have through holes on their surfaces. Both the upper plate (31) and the lower plate (32) are inclined.

6. A high efficiency thickener based on the logarithmic spiral clothings according to claim 5, characterized in that: The upper plate (31) and the lower plate (32) form an angle of 30 to 60 degrees; a gap is provided between the upper plate (31) and the lower plate (32); one end of the extension lines of the upper plate (31) and the lower plate (32) intersects with one end of the ore inlet pipe (6).

7. A high efficiency thickener based on the logarithmic spiral clothings according to claim 5, characterized in that: The through holes of the flow baffle plate gradually decrease in size starting from one end of the ore inlet pipe (6).

8. The high-efficiency thickener based on the logarithmic spiral structure distributing device according to claim 1, characterized in that: The main channel (1) is provided with multiple dilution ports (5) evenly distributed on the side; the dilution ports (5) are connected to independent diluent supply pipelines.

9. The high-efficiency thickener based on the logarithmic spiral structure distributing device according to claim 1, characterized in that: The total area of ​​the discharge port (4) is 1.5 times the inner diameter area of ​​the inlet pipe (6).

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