Filter pressing feeding control method and system based on dry coal slime amount

Abstract

The invention discloses a filter pressing feeding control method and system based on the amount of dry coal slime, and relates to the technical field of coal slime filter pressing, and the method comprises the following steps: 1, determining the total volume of each filter chamber according to the number and size of the filter chambers of a filter press, and calculating the theoretical total mass of the dry coal slime by combining the density of the dry coal slime after filter pressing; 2, setting an allowable error range based on the theoretical total mass of the dry coal slime, and forming a target mass interval; and 3, collecting the concentration and flow signals of the ore pulp entering the filter chamber of the filter press in real time, and obtaining the real-time dry coal slurry flow according to a real-time dry coal slurry flow calculation formula. Compared with a traditional method depending on artificial experience, fixed duration or pressure peak value, the method can improve objectivity and accuracy of end point judgment, the problem that a filter cake is too thin or overpressed due to fluctuation of feeding concentration is avoided, meanwhile, a reliable basis is provided for full-process automatic control, and the method is suitable for large-scale popularization and application. The stability and the treatment efficiency of the filter pressing operation are favorably improved.

Description

Technical Field

[0001] This invention relates to the field of coal slime filter press technology, and more specifically to a filter press feed control method and system based on the amount of dry coal slime. Background Technology

[0002] The working principle of a filter press is as follows: Under the pressure of the feed pump, the slurry to be filtered is transported to each filter chamber, where solid-liquid separation is achieved using special filter cloth and other filter media. Solid particles continuously deposit on the surface of the filter cloth, gradually forming a filter cake until the filter chamber is full; the filtrate then passes through the filter cloth and is discharged. Figure 1 A schematic diagram of a chamber filter press is shown, wherein 101 represents the frame for installing the filter press, 102 represents the filter plates of the filter press, and in a tightly fitted state, there is a closed filtration chamber between adjacent filter plates, and 103 represents the filtrate outlet pipe of the filtration chamber, through which the filtrate in the filtration chamber is discharged.

[0003] Currently, filter presses are mostly operated as stand-alone automated equipment, and the determination of the feed endpoint mainly relies on the following three methods: (1) Operators observe the state of the filtrate outlet based on experience and make manual judgments based on the phenomenon of "dripping water not forming a line"; (2) Set a fixed feeding time; the feeding is considered to be over when the time is up. (3) Monitor the pressure in the feed pipeline and use the preset pressure peak as the endpoint signal.

[0004] However, all of the above methods have obvious limitations, which are analyzed in order as follows: (1) The manual observation method is greatly affected by subjective experience, and the filter press cycle of a single device can fluctuate by 20 to 30 minutes, resulting in poor process stability; (2) Fixed-time control method cannot respond to dynamic changes in feed properties (such as concentration and particle size) and has insufficient adaptability. For example, simulation shows that when the coal slime water concentration drops from 300g / L to 200g / L, the amount of dry coal slime under the same feeding time decreases by about 33%, which can easily lead to a thinner filter cake or excessive filtration. (3) The pressure peak judgment method is easily affected by changes in pipeline resistance and pump pressure fluctuations.

[0005] Regardless of which method is used, in scenarios where multiple filter presses operate in parallel, operators still need to monitor the feeding status of each device throughout the process, resulting in high labor intensity. Furthermore, this reliance on manual intervention leads to a decrease in overall system processing efficiency, hindering further improvements in production efficiency. Summary of the Invention

[0006] The purpose of this invention is to solve the problems in the prior art by proposing a filter press feed control method based on the amount of dry coal slime. By collecting the slurry concentration and flow rate signals in real time and combining them with the filter chamber volume and dry coal slime density, the method can achieve accurate feed endpoint determination based on the actual accumulated amount of dry coal slime.

[0007] To address the above problems, the present invention provides the following technical solution: The filter press feed control method based on dry coal slime quantity includes the following steps: Step 1: Determine the total volume of each filter chamber based on the number and size of the filter chambers in the filter press, and calculate the theoretical total mass of dry coal slime based on the density of the dry coal slime after filtration. Step 2: Based on the theoretical total mass of dry coal slime, set an allowable error range to form a target mass range; Step 3: Real-time acquisition of slurry concentration and flow rate signals entering the filter chamber of the filter press; calculation of real-time dry coal slime flow rate using the formula. ; Step 4: In the initial stage of filter press feeding, select several sets of scanning cycles for the control system. Real-time dry coal slime flow rate By accumulating the time, the mass of the dry coal slime entering the filter chamber of the filter press is obtained. ; Step 5: In the next scan cycle of the control system Within this scanning cycle Real-time dry coal slime flow rate corresponding to this scanning cycle Perform a product operation to obtain the scan cycle. The increase in dry coal slime within the specified volume is added to the aforementioned dry coal slime mass. In the process, the cumulative dry coal slime quality was obtained. Update the cumulative value; Step Six: Determine the cumulative dry coal slime quality after each update. If the target quality range in step two has been entered, then the filter press feeding is considered complete, and a stop feeding command is issued.

[0008] As a further aspect of the present invention: when the cumulative dry coal slime mass When the lower limit of the target quality range is reached, feed flow monitoring is initiated and a flow threshold is set; at the same time, the filtrate level is monitored through the horizontal transfer pipes set at each filtrate outlet pipe, and a level threshold is set; when the feed flow rate is continuously lower than the threshold flow rate for 30 seconds, and the filtrate level is lower than the level threshold, the stop feed command is issued.

[0009] As a further aspect of the present invention: the filter press is provided with a feed pipe connected to the mixing tank, and a drive source is provided on the feed pipe. When the drive source is working, the feed is started; otherwise, the feed is stopped.

[0010] As a further aspect of the present invention, a concentration meter and an electromagnetic flow meter are installed on the feed pipe to collect the concentration and flow rate signals of the slurry entering the filter chamber of the filter press in real time.

[0011] As a further aspect of the present invention, the horizontal transfer pipe is provided with a detection device for monitoring the filtrate level.

[0012] As a further aspect of the present invention: the formula for calculating the real-time dry coal slime flow rate is:

[0013] In the formula: Expressed as real-time dry coal slime flow rate, in t / h; C represents the feed concentration, in g / L; Q represents the feed flow rate, in m³ / h; k represents the percentage of moisture in the filter cake, with a value between 22% and 26%.

[0014] As a further aspect of the present invention: the mass of the dry coal slime The calculation formula is:

[0015] In the formula: Expressed as dry coal slime mass, in tons (t); ΔT represents the scan period of the control system, in seconds; n represents the number of groups in the scan cycle.

[0016] As a further aspect of the present invention: the cumulative dry coal slime mass The calculation formula is: / 3600 In the formula: Expressed as dry coal slime mass, in tons (t); Expressed as real-time dry coal slime flow rate, in t / h; ΔT represents the scan period of the control system, with the unit being seconds (s).

[0017] As a further aspect of the present invention: a pressure transmitter for monitoring the feed pressure is provided on the feed pipe. When the monitored feed pressure exceeds 1.2 MPa, the control system controls the drive source to stop working.

[0018] The present invention also proposes a filter press feeding system based on dry coal slime quantity, including a mixing tank, a connecting pipe at one end of the mixing tank, the other end of the connecting pipe being connected to the feed port of the drive source, the discharge port of the drive source being connected to the feed pipe, the feed pipe being connected to the filter press inlet, and a concentration meter and an electromagnetic flow meter being installed on it. It also includes a horizontal transfer pipe, which is located below multiple sets of filtrate outlet pipes and is used to receive the filtrate discharged from multiple sets of filtrate outlet pipes; the horizontal transfer pipe has a horizontal section of the pipe cavity, which can be divided into low filtrate level, medium filtrate level and high filtrate level according to the different liquid levels of the filtrate in it; the horizontal transfer pipe is equipped with an inspection device, which is used to monitor the liquid level of the filtrate.

[0019] Compared with the prior art, the present invention has the following beneficial effects: 1. This application achieves accurate endpoint determination of feed based on the actual accumulated amount of dry coal slime by real-time acquisition of slurry concentration and flow rate signals, combined with the filter chamber volume and dry coal slime density. Compared with traditional methods that rely on manual experience, fixed time periods, or pressure peaks, the method of this application can improve the objectivity and accuracy of endpoint determination, avoid problems such as thin filter cake or overpressure caused by fluctuations in feed concentration, and provide a reliable basis for full-process automated control, which helps to improve the stability and processing efficiency of filter press operation.

[0020] 2. When the cumulative dry coal slime quality approaches the lower limit of the target range, a dual-condition verification mechanism of feed flow rate and filtrate level is further introduced. This mechanism can reconfirm whether the filtration process has actually ended after the cumulative amount reaches the target. This design can effectively prevent premature or delayed shutdown due to signal delay or calculation error, improve the reliability and robustness of system control, and ensure that each filter press cycle ends at the optimal time, taking into account both efficiency and filter cake quality.

[0021] 3. By adding a pressure transmitter and setting an overpressure protection threshold of 1.2MPa, an independent safety interlock protection mechanism is introduced in addition to the main control logic based on cumulative mass. This mechanism can stop the machine in time when there is abnormal blockage in the feed pipeline or a sudden increase in pressure, effectively preventing equipment overload damage and improving the safety of system operation. Attached Figure Description

[0022] The invention will now be further described with reference to the accompanying drawings.

[0023] Figure 1 This is a front view structural diagram of a chamber filter press in the prior art; Figure 2 This is a front view structural diagram of the present invention; Figure 3 This is a front view schematic diagram of the two sets of filter plates in this invention. Figure 1 ; Figure 4This is a front view schematic diagram of the two sets of filter plates in this invention. Figure 2 .

[0024] In the diagram: 101, frame; 102, filter plate; 103, filtrate outlet pipe; 1, mixing tank; 2, coal slime slurry; 3, connecting pipe; 4, drive source; 5, concentration meter; 6, electromagnetic flow meter; 7, feed pipe; 8, detection device; 9, horizontal transfer pipe; 10, low filtrate level; 11, medium filtrate level; 12, high filtrate level; 13, pressure transmitter; 14, collection tank. Detailed Implementation

[0025] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. 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 skilled in the art without creative effort are within the scope of protection of the present invention.

[0026] Example 1: like Figures 2-4 As shown, a filter press feeding system based on dry coal slime includes a mixing tank 1, coal slime slurry 2, connecting pipe 3, drive source (e.g., pump body) 4, concentration meter 5, electromagnetic flow meter 6, feed pipe 7, frame 101, filter plate 102, filtrate outlet pipe 103, detection device 8 (patent application filed, patent number 2025105814165, entitled "A multi-stage thermal conductivity online detection device and detection method for filtrate water of a chamber coal slime filter press"), horizontal transfer pipe 9, pressure transmitter 13, and collection tank 14.

[0027] The specific connection method is as follows: one end of the connecting pipe 3 is connected to the mixing tank 1, and the other end is connected to the inlet of the drive source 4. The outlet of the drive source 4 is connected to the inlet pipe 7. Since the mixing tank 1 is usually located on the first floor of a coal preparation plant in a conventional layout, and the filter press is mostly located on the second floor or above, the drive source 4 is needed to provide power for the filter press feed. The inlet pipe 7 is connected to the filter press inlet and is equipped with a concentration meter 5 and an electromagnetic flow meter 6. The concentration meter 5 monitors the slurry feed concentration in real time, and the electromagnetic flow meter 6 monitors the slurry feed flow rate in real time. The electromagnetic flow meter 6 can measure very small flow rates (≤0.5 m³ / h). According to the principle of mass conservation, the real-time dry coal slime flow rate... It is calculated by multiplying the concentration by the flow rate.

[0028] The horizontal transfer pipe 9 is located on the roof of the floor below the filter press, so that the filtrate can flow by gravity to the circulating water tank. The collection tank 14 is located at the top of the horizontal transfer pipe 9 and below the multiple sets of filtrate outlet pipes 103, and is used to collect the filtrate discharged from the multiple sets of filtrate outlet pipes 103.

[0029] The filter press unit consists of filter plates 102 neatly arranged on the frame 101 and filter cloth on the surface of the filter plates 102. During filtration, coal slime slurry 2 is evenly distributed into each sealed filter chamber through the feed pipe 7 under the drive of the drive source 4; under the action of the feed pressure, the slurry achieves solid-liquid separation through the filter cloth: solid particles are retained in the filter chamber to form a filter cake, and the filtrate is discharged through the filtrate outlet pipe 103. This filter cake formation can be achieved by... Figures 3 to 4 To express, Figure 4 The black clusters in the image represent the filter cake.

[0030] Example 2: A method for controlling filter press feed based on dry coal slime quantity includes the following steps: Step 1: Based on the number and dimensions of the filter chambers in the filter press, determine the total volume of each chamber. Then, considering the density of the dried coal slime after filtration, calculate the theoretical total mass of the dried coal slime. Example as follows: Specifically: the filter plate 102 of the filter press has a fixed size (e.g., 1500mm × 1500mm), and the effective filtration area (A) of a single filter chamber is constant (which can be estimated based on the size of the filter plate 102 or provided by the manufacturer, e.g., A = 2.1 m²). 2 The filter chamber design thickness (d) is fixed (e.g., d = 0.032m, i.e., 32mm). The total number of filter plates P can be adjusted according to production conditions (e.g., P = 80 pieces). The formula for calculating the volume of a single filter chamber is: (1) The number of filter chambers Z is determined by the total number of filter plates P, and the calculation formula is: (2) If there are 79 filter chambers, the total volume of the filter chambers can be calculated by combining formulas (1) and (2): (3) Under stable operating conditions, the density of the coal slime after pressure filtration changes little, assumed to be 1450 kg / m³. 3 The formula for calculating the total filter cake weight m in one filter press cycle is as follows: (4) According to formula (4), the total filter cake weight m obtained by the filter press in one filter press working cycle is 7.6978t, which is the theoretical total mass of dry coal slime.

[0031] Step 2: Based on the theoretical total mass of dry coal slime, set an allowable error range to form a target mass interval. Taking an allowable error range of ±3% as an example, the resulting target mass interval is 7.4669t-7.9287t.

[0032] Step 3: The concentration and flow rate of the slurry entering the filter chamber of the filter press are collected in real time using the concentration meter 5 and electromagnetic flow meter 6. The real-time dry coal slime flow rate is obtained according to the real-time dry coal slime flow rate calculation formula. Specifically, the formula for calculating the real-time dry coal slime flow rate is: (5) In the formula: Expressed as real-time dry coal slime flow rate, in t / h; C represents the feed concentration, in g / L; Q represents the feed flow rate, with units of m³ / h.

[0033] To take into account the effect of filter cake moisture on dry coal slime flow rate Due to the influence of moisture, a moisture correction term is introduced into formula (5), resulting in the corrected formula: (6) In the formula: k represents the percentage of moisture in the filter cake, which ranges from 22% to 26%.

[0034] Step 4: In the initial stage of filter press feeding, select several sets of scanning cycles for the control system. Real-time dry coal slime flow rate By accumulating the time, the mass of the dry coal slime entering the filter chamber of the filter press is obtained. Specifically, the quality of dry coal slime The calculation formula is: (7) In the formula: Expressed as dry coal slime mass, in tons (t); ΔT represents the scan period of the control system, in seconds; n represents the number of groups in the scan cycle.

[0035] Step 5: In the next scan cycle of the control system Within this scanning cycle Real-time dry coal slime flow rate corresponding to this scanning cycle Perform a product operation to obtain the scan cycle. The increase in dry coal slime within the specified volume is added to the aforementioned dry coal slime mass. In the process, the cumulative dry coal slime quality was obtained. In each subsequent scan cycle, the obtained increase in dry coal slime is added to the cumulative dry coal slime mass of the previous scan cycle. Upgrade to update the cumulative value; Step Six: Determine the cumulative dry coal slime quality after each update. If the target quality range in step two has been entered, then the filter press feed is considered complete, and the control system issues a stop feed command, causing drive source 4 to stop working.

[0036] The filter press feed control method based on dry coal slime quantity proposed in this application has the following advantages compared with the endpoint control methods such as manual observation, fixed duration, or pressure peak judgment relied upon by conventional filter presses: (1) Achieve precise and quantitative endpoint determination, significantly improving control stability and consistency. Traditional manual observation methods ("a drop doesn't form a line") rely on operator experience, are highly subjective, and result in fluctuations of up to 20-30 minutes in a single filter press cycle, leading to poor stability. This method calculates and accumulates the actual dry coal slime mass entering the filter press chamber in real time and compares it with a theoretical target range calculated based on chamber volume and coal slime density, achieving complete quantification and objectivity in endpoint determination. This feed control method fundamentally eliminates the influence of human error, ensuring the accuracy and repeatability of endpoint determination for each filter press cycle, resulting in a highly stable production process.

[0037] (2) It has dynamic self-adaptability and effectively overcomes the interference of fluctuations in feed properties.

[0038] The fixed feed duration method ignores changes in key parameters such as feed concentration and particle size. When the concentration of coal slime slurry 2 fluctuates (e.g., from 300 g / L to 200 g / L), it can lead to a deviation of approximately 33% in the dry coal slime processing volume, resulting in filter cakes that are too thin or over-pressurized. The core control of this method is the accumulation of dry coal slime mass, rather than a fixed time. During the filter press feeding process, regardless of changes in feed concentration, the system continuously accumulates the actual amount of solids passing through until the preset quality target is reached. Therefore, the feed control method of this application can automatically adapt to dynamic changes in feed properties, ensuring that each batch of filter cake reaches the expected fullness (dry basis mass), improving the adaptability of the process and the uniformity of product quality.

[0039] (3) It has strong anti-interference ability, direct and reliable judgment logic, and low misjudgment rate.

[0040] The method based on peak feed pressure is susceptible to interference from factors such as changes in pipeline resistance, pump performance fluctuations, and valve opening. On-site pressure fluctuations often reach 0.2-0.5 MPa, leading to a false endpoint error rate exceeding 15%. This method directly monitors and calculates the slurry concentration and flow rate, two parameters that have a direct and clear physical correlation with the final product (dry coal slime) yield. Through formula... The dry coal slime flow rate is calculated, and the cumulative mass is obtained through discrete integration. This method is not affected by pressure fluctuations within complex pipeline systems, which fundamentally improves the reliability and robustness of the judgment.

[0041] (4) Laying the foundation for achieving full-process automation and centralized intelligent monitoring.

[0042] Conventional methods, even with partial automation, still require manual assistance in judgment or parameter setting. When multiple devices operate in parallel, this results in high labor intensity for operators, and manual intervention reduces overall system efficiency. This method, through real-time data acquisition, automatic calculation, and logical judgment, achieves closed-loop automatic control of the entire process from material input to endpoint determination. It not only frees up manpower, making it possible for one person to monitor multiple devices, but also generates standardized, transmissible real-time data (such as cumulative dry coal slime mass). This provides a solid data foundation and interface conditions for seamlessly integrating individual "standalone automation" equipment into a centralized control system (DCS / SCADA), conducting big data analysis, optimizing scheduling, and performing predictive maintenance, thereby further improving the overall production efficiency and management intelligence level of the plant.

[0043] Example 3: This embodiment, based on Embodiment 2, designs a flow rate-dry coal slime quantity linkage judgment logic to improve the reliability of the feed endpoint judgment. The details are as follows: (1) The horizontal transfer pipe 9 has a horizontal section of the cavity, which can be divided into low filtrate level 10, medium filtrate level 11 and high filtrate level 12 based on the different liquid levels of the filtrate in it. In the initial feeding stage, no filter cake is formed in the filter chamber, and the discharge of filtrate water is relatively large, so the high filtrate level 12 is formed in the horizontal transfer pipe 9; as the filter cake gradually forms, the discharge of filtrate water decreases, and the liquid level gradually drops to the medium filtrate level 11; when the "dripping water not forming a line" endpoint state is reached by traditional manual observation, the low filtrate level 10 is formed in the horizontal transfer pipe 9, and at this time the detection device 8 can detect that the liquid level is lower than the detection liquid surface.

[0044] (2) When the cumulative dry coal slime mass When the lower limit of the target mass range is reached (taking the target mass range in step two above as an example, the lower limit is 7.4669t), the feed flow rate monitoring is activated and a flow rate threshold (e.g., 1.0 m³ / h) is set. At the same time, the filtrate level is monitored through the horizontal transfer pipe 9 set at each filtrate outlet pipe 103, and a level threshold (e.g., the aforementioned filtrate low level 10, or a level below the filtrate low level 10) is set.

[0045] If the feed flow rate remains below the threshold flow rate for 30 seconds, and the filtrate level is below the level threshold, while the dry coal slime volume increases stagnantly or extremely slowly, a stop feed command will be issued.

[0046] Example 4: This embodiment improves upon Embodiment 2 or Embodiment 3 by proposing an abnormal operating condition handling mechanism: A pressure transmitter 13 is installed on the feed pipe 7. During the feeding cycle, the pressure transmitter 13 monitors the feed pressure in real time. When the feed pressure exceeds 1.2 MPa, the drive source 4 is automatically cut off and an alarm is triggered. Simultaneously, a dry coal slime quantity fluctuation warning (>±5% / min) is set. When a sudden change in feed concentration, pipe blockage, or downstream scraper conveyor / belt conveyor malfunction is detected, the unloading procedure is locked, and fault information is pushed to the intelligent terminal via an audible and visual alarm to ensure equipment and personnel safety.

[0047] The foregoing has provided a detailed description of one embodiment of the present invention, but this description is merely a preferred embodiment and should not be construed as limiting the scope of the invention. All equivalent variations and modifications made within the scope of the claims of this invention should still fall within the patent coverage of this invention.

Claims

1. A method for controlling the feed of filter press based on the amount of dry coal slime, characterized in that, Includes the following steps: Step 1: Determine the total volume of each filter chamber based on the number and size of the filter chambers in the filter press, and calculate the theoretical total mass of dry coal slime based on the density of the dry coal slime after filtration. Step 2: Based on the theoretical total mass of dry coal slime, set an allowable error range to form a target mass range; Step 3: Real-time acquisition of slurry concentration and flow rate signals entering the filter chamber of the filter press; calculation of real-time dry coal slime flow rate using the formula. ; Step 4: In the initial stage of filter press feeding, select several sets of scanning cycles for the control system. Real-time dry coal slime flow rate By accumulating the time, the mass of the dry coal slime entering the filter chamber of the filter press is obtained. ; Step 5: In the next scan cycle of the control system Within this scanning cycle Real-time dry coal slime flow rate corresponding to this scanning cycle Perform a product operation to obtain the scan cycle. The increase in dry coal slime within the specified volume is added to the aforementioned dry coal slime mass. In the process, the cumulative dry coal slime quality was obtained. Update the cumulative value; Step Six: Determine the cumulative dry coal slime quality after each update. If the target quality range in step two has been entered, then the filter press feeding is considered complete, and a stop feeding command is issued.

2. The filter press feed control method based on dry coal slime quantity according to claim 1, characterized in that, When the cumulative dry coal slime quality When the lower limit of the target quality range is reached, feed flow monitoring is initiated and a flow threshold is set; at the same time, the filtrate level is monitored through the horizontal transfer pipes set at each filtrate outlet pipe, and a level threshold is set; when the feed flow rate is continuously lower than the threshold flow rate for 30 seconds, and the filtrate level is lower than the level threshold, the stop feed command is issued.

3. The filter press feed control method based on dry coal slime quantity according to claim 1, characterized in that, The filter press is equipped with a feed pipe that is connected to the mixing tank, and the feed pipe is equipped with a drive source. When the drive source is working, the feed will start; otherwise, the feed will stop.

4. The filter press feed control method based on dry coal slime quantity according to claim 3, characterized in that, A concentration meter and an electromagnetic flow meter are installed on the feed pipe to collect the concentration and flow rate signals of the slurry entering the filter chamber of the filter press in real time.

5. The filter press feed control method based on dry coal slime quantity according to claim 2, characterized in that, The horizontal transfer pipe is equipped with a detection device for monitoring the filtrate level.

6. The filter press feed control method based on the amount of dry coal slime according to any one of claims 1-5, characterized in that, The formula for calculating the real-time dry coal slime flow rate is as follows: In the formula: Expressed as real-time dry coal slime flow rate, in t / h; C represents the feed concentration, in g / L; Q represents the feed flow rate, in m³ / h; k represents the percentage of moisture in the filter cake, with a value between 22% and 26%.

7. The filter press feed control method based on the amount of dry coal slime according to any one of claims 1-5, characterized in that, The mass of the dry coal slime The calculation formula is: In the formula: Expressed as dry coal slime mass, in tons (t); ΔT represents the scan period of the control system, in seconds; n represents the number of groups in the scan cycle.

8. The filter press feed control method based on the amount of dry coal slime according to any one of claims 1-5, characterized in that, The cumulative dry coal slime mass The calculation formula is: / 3600 In the formula: Expressed as dry coal slime mass, in tons (t); Expressed as real-time dry coal slime flow rate, in t / h; ΔT represents the scan period of the control system, with the unit being seconds (s).

9. The filter press feed control method based on dry coal slime quantity according to claim 3, characterized in that, The feed pipe is equipped with a pressure transmitter for monitoring the feed pressure. When the monitored feed pressure exceeds 1.2 MPa, the control system controls the drive source to stop working.

10. A filter press feeding system based on dry coal slime quantity, characterized in that, It includes a mixing tank (1), one end of which is provided with a connecting pipe (3), the other end of which is connected to the feed port of the drive source (4), the discharge port of the drive source (4) is connected to a feed pipe (7), the feed pipe (7) is connected to the inlet of the filter press, and a concentration meter (5) and an electromagnetic flow meter (6) are installed on it. It also includes a horizontal transfer pipe (9), which is located below the multiple sets of filtrate outlet pipes (103) and is used to receive the filtrate discharged from the multiple sets of filtrate outlet pipes (103); the horizontal transfer pipe (9) has a horizontal section of the pipe cavity, which can be divided into low filtrate level (10), medium filtrate level (11) and high filtrate level (12) based on the different liquid levels of the filtrate in it; an inspection device (8) is provided on the horizontal transfer pipe (9), and the detection device (8) is used to monitor the liquid level of the filtrate.

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