Red soil nickel ore high pressure leaching slurry concentration regulation method and regulation system

Abstract

The application provides a laterite nickel ore high-pressure leaching slurry concentration regulation method and a regulation system, and belongs to the technical field of metallurgy. The laterite nickel ore high-pressure leaching slurry concentration regulation method comprises the following steps: obtaining actual concentration values and target concentration thresholds of iron ion concentration and silicon ion concentration in a circulating leaching tank; comparing the sum of the actual concentration values of the iron ion concentration and the silicon ion concentration in the circulating leaching tank with the target concentration threshold; and when the sum of the actual concentration values of the iron ion concentration and the silicon ion concentration in the circulating leaching tank is greater than the target concentration threshold, the concentration of the feed slurry of a high-pressure reaction kettle is reduced, so that the real-time regulation of the iron ion concentration and the silicon ion concentration in the slurry is realized, and a large amount of iron ions and silicon ions are prevented from being leached in the high-pressure leaching stage, so as to affect the subsequent multi-stage countercurrent washing, flocculation and precipitation effect.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of metallurgy, and particularly relates to a method and system for regulating the concentration of high-pressure leaching slurry of laterite nickel ore. BACKGROUND

[0002] Currently, in the process of laterite nickel ore hydrometallurgy, after the slurry is subjected to high-pressure leaching, cyclic leaching and multi-stage pre-neutralization, it needs to be subjected to multi-stage countercurrent washing to sufficiently wash the nickel, cobalt and manganese in the slurry bottom stream into the solution and perform solid-liquid separation. However, in actual application, the flocculation and sedimentation effect of multi-stage countercurrent washing often is not good, which is not conducive to the solid-liquid separation of the solution containing nickel, cobalt and manganese and the slag.

[0003] The poor flocculation and sedimentation effect of multi-stage countercurrent washing is due to the excessively high concentration of trivalent iron and silicon ions contained in the slurry, and the excessively high concentration of iron and silicon ions is due to the high content of iron and silicon in the batch of laterite nickel ore, thereby causing more iron and silicon ions to be leached in the high-pressure leaching stage, and the poor flocculation and sedimentation effect of multi-stage countercurrent washing. SUMMARY

[0004] The present application aims to provide a method and system for regulating the concentration of high-pressure leaching slurry of laterite nickel ore, which can solve the problem of poor flocculation and sedimentation effect of multi-stage countercurrent washing in the related art, so as to realize real-time regulation of the concentration of iron ions and silicon ions in the slurry, thereby avoiding more iron ions and silicon ions from being leached in the high-pressure leaching stage, and affecting the flocculation and sedimentation effect of subsequent multi-stage countercurrent washing.

[0005] To achieve this purpose, the present application adopts the following technical solutions:

[0006] In a first aspect, the present application provides a method for regulating the concentration of high-pressure leaching slurry of laterite nickel ore, the high-pressure leaching slurry of laterite nickel ore is contained in a cyclic leaching tank, a feed end of the cyclic leaching tank is connected with a bottom stream of a high-pressure reactor, a feed end of the high-pressure reactor is connected with a bottom stream of a thickener, and the method comprises:

[0007] obtaining actual concentration values and target concentration threshold values of the concentration of iron ions and the concentration of silicon ions in the cyclic leaching tank, wherein the target concentration threshold value is a preset value of the sum of the concentration of iron ions and the concentration of silicon ions in the cyclic leaching tank;

[0008] comparing the sum of the actual concentration values of the concentration of iron ions and the concentration of silicon ions in the cyclic leaching tank with the target concentration threshold value, and when the sum of the actual concentration values of the concentration of iron ions and the concentration of silicon ions in the cyclic leaching tank is greater than the target concentration threshold value, controlling the feed slurry concentration of the high-pressure reactor to be reduced.

[0009] In one of the embodiments, the control of the decrease of the feed slurry concentration of the high-pressure reactor includes:

[0010] obtaining the discharge slurry concentration of the thickener and a target discharge concentration value;

[0011] comparing the discharge slurry concentration with the target discharge concentration value, and when the discharge slurry concentration is equal to the target discharge concentration value, controlling the decrease of the feed slurry concentration of the high-pressure reactor to stop.

[0012] In one of the embodiments, the obtaining of the discharge slurry concentration of the thickener includes:

[0013] obtaining the feed slurry concentration, the feed slurry density, the discharge slurry density, the settling area and the discharge volume flow of the thickener, and the settling velocity of the flocculation body;

[0014] obtaining the discharge slurry concentration of the thickener based on the feed slurry concentration, the feed slurry density, the discharge slurry density, the settling area and the discharge volume flow of the thickener, and the settling velocity of the flocculation body.

[0015] In one of the embodiments, the discharge slurry concentration of the thickener is determined based on the following formula:

[0016]

[0017] wherein Vmin is the settling velocity of the flocculation body, C1 is the feed slurry concentration of the thickener, ρ1 is the feed slurry density of the thickener, C2 is the discharge slurry concentration of the thickener, ρ2 is the discharge slurry density of the thickener, S is the settling area of the thickener, and G is the discharge volume flow.

[0018] In one of the embodiments, the obtaining of the settling velocity of the flocculation body includes:

[0019] obtaining an initial settling velocity of the material in the thickener without adding the flocculation agent;

[0020] obtaining the concentration of the flocculation agent in the liquid phase of the thickener, and determining the ratio between the settling velocity of the flocculation body and the initial settling velocity based on the concentration of the flocculation agent in the liquid phase;

[0021] determining the settling velocity of the flocculation body based on the initial settling velocity and the ratio.

[0022] In one of the embodiments, the ratio between the settling velocity of the flocculation body and the initial settling velocity is determined based on the following formula:

[0023]

[0024] Wherein, C is the concentration of flocculant in the liquid phase of the thickener, a1, a2 and a3 are constants calibrated by experiments, and k is the ratio between the settling rate of the flocculation body and the initial settling rate.

[0025] In one of the embodiments, the concentration of flocculant in the liquid phase of the thickener is obtained, comprising:

[0026] The flocculant addition amount, the feed ore pulp concentration and the feed mass flow of the thickener are obtained.

[0027] Based on the flocculant addition amount, the feed ore pulp concentration and the feed mass flow of the thickener, the concentration of flocculant in the liquid phase of the thickener is determined.

[0028] In one of the embodiments, the concentration of flocculant in the liquid phase of the thickener is determined based on the following formula:

[0029] m = C x (1-C1) x V0

[0030] Wherein, m is the flocculant addition amount, C is the concentration of flocculant in the liquid phase of the thickener, C1 is the feed ore pulp concentration of the thickener, and V0 is the feed mass flow of the thickener.

[0031] In the second aspect, the application provides a laterite nickel ore high-pressure leaching ore pulp concentration regulation system, which can implement the laterite nickel ore high-pressure leaching ore pulp concentration regulation method in any of the above-mentioned schemes.

[0032] The underflow of the thickener is connected with the feed end of the high-pressure reaction kettle, and the discharge end of the high-pressure reaction kettle is connected with the circulating leaching tank.

[0033] The ion concentration acquisition device is used to acquire the actual concentration values of the iron ion concentration and the silicon ion concentration in the circulating leaching tank, and send the actual concentration values to the automatic control device.

[0034] The automatic control device is used to control the feed ore pulp concentration of the high-pressure reaction kettle to be reduced when the sum of the actual concentration values of the iron ion concentration and the silicon ion concentration in the circulating leaching tank is greater than the target concentration threshold value.

[0035] In one of the embodiments, the automatic control device is further used to acquire the discharge ore pulp concentration of the thickener, and control the feed ore pulp concentration of the high-pressure reaction kettle to stop being reduced when the discharge ore pulp concentration is equal to the target discharge concentration value.

[0036] The application has the following beneficial effects:

[0037] The method and system for regulating the concentration of high-pressure leaching slurry of laterite nickel ore provided by the application connect the underflow of the thickener with the feeding end of the high-pressure reaction kettle, connect the discharging end of the high-pressure reaction kettle with the circulating leaching tank, obtain the actual concentration value and the target concentration threshold of the iron ion concentration and the silicon ion concentration in the circulating leaching tank, and control the feeding slurry concentration of the high-pressure reaction kettle to be reduced when the sum of the actual concentration values of the iron ion concentration and the silicon ion concentration exceeds the target concentration threshold, so that the iron ion concentration and the silicon ion concentration in the slurry are regulated in real time, and more iron ions and silicon ions are prevented from being leached in the high-pressure leaching stage, thereby affecting the effect of subsequent multi-stage countercurrent washing, flocculation and precipitation. BRIEF DESCRIPTION OF DRAWINGS

[0038] Figure 1 The flowchart of an embodiment of the method for regulating the concentration of high-pressure leaching slurry of laterite nickel ore provided by the application is shown in the figure.

[0039] Figure 2 The flowchart of the method for regulating the concentration of high-pressure leaching slurry of laterite nickel ore provided by the application is shown in the figure.

[0040] Figure 3 The flowchart of the method for regulating the concentration of high-pressure leaching slurry of laterite nickel ore provided by the application is shown in the figure.

[0041] Figure 4 The flowchart of the method for regulating the concentration of high-pressure leaching slurry of laterite nickel ore provided by the application is shown in the figure.

[0042] Figure 5 The flowchart of the method for regulating the concentration of high-pressure leaching slurry of laterite nickel ore provided by the application is shown in the figure.

[0043] Figure 6 The principle block diagram of an embodiment of the system for regulating the concentration of high-pressure leaching slurry of laterite nickel ore provided by the application is shown in the figure.

[0044] In the figure:

[0045] 101, thickener; 102, high-pressure reaction kettle; 103, circulating leaching tank; 104, automatic regulation device; 105, ion concentration acquisition device. DETAILED DESCRIPTION

[0046] The application will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the application and not to limit the application. In addition, it should be noted that only the parts related to the application are shown in the drawings for the convenience of description.

[0047] In the description of the present application, unless otherwise explicitly specified and limited, the terms "connected", "connected", "fixed" should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or it can be integrated; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the internal communication of two elements or the interaction relationship between two elements. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0048] In the present application, unless otherwise explicitly specified and limited, the first feature "on" or "under" the second feature can include that the first and second features are in direct contact, or that the first and second features are not in direct contact but are in contact through another feature between them. Moreover, the first feature "on", "above" and "above" the second feature includes that the first feature is directly above and obliquely above the second feature, or only indicates that the horizontal height of the first feature is higher than that of the second feature. The first feature "below", "below" and "below" the second feature includes that the first feature is directly below and obliquely below the second feature, or only indicates that the horizontal height of the first feature is less than that of the second feature.

[0049] In the description of the present embodiment, the terms "up", "down", "left", "right" and other orientation or position relationship are based on the orientation or position relationship shown in the drawings, and are only for the convenience of description and simplification of operation, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present application. In addition, the terms "first" and "second" are only used to distinguish in the description and have no special meaning.

[0050] As shown in Figure 1 and Figure 6 The embodiment of the first aspect of the present application provides a method for regulating the concentration of high-pressure leaching slurry of laterite nickel ore. The high-pressure leaching slurry of laterite nickel ore can be contained in the circulating leaching tank 103. The feed end of the circulating leaching tank 103 is connected with the underflow of the high-pressure reaction kettle 102. The feed end of the high-pressure reaction kettle 102 is connected with the underflow of the thickener 101. The method for regulating the concentration of high-pressure leaching slurry of laterite nickel ore specifically comprises the following steps:

[0051] Step S100, obtaining the actual concentration value and the target concentration threshold of the iron ion concentration and the silicon ion concentration in the circulating leaching tank 103, wherein the target concentration threshold is a preset value of the sum of the iron ion concentration and the silicon ion concentration in the circulating leaching tank 103;

[0052] Step S200, comparing the sum of the actual concentration value of the iron ion concentration and the silicon ion concentration in the circulating leaching tank 103 with the target concentration threshold;

[0053] Step S300, when the sum of the actual concentration values of the iron ion concentration and the silicon ion concentration in the circulating leaching tank 103 is greater than the target concentration threshold, the feed slurry concentration of the high-pressure reaction kettle 102 is reduced.

[0054] In the laterite nickel ore high-pressure leaching slurry treatment process, the laterite nickel ore slurry is subjected to preliminary treatment by the thickener 101, after removing part of the liquid, the solid content of the slurry increases, and then enters the high-pressure reaction kettle 102, under high temperature and high pressure conditions, nickel, chromium, manganese and other metals in the slurry, as well as iron, silicon and other impurities are leached. The leached slurry flows into the circulating leaching tank 103.

[0055] The core of the laterite nickel ore high-pressure leaching slurry concentration control method of the embodiment is to detect the actual concentration values of the iron ion concentration and the silicon ion concentration in the circulating leaching tank 103 in real time, and then dynamically adjust the feed slurry concentration of the high-pressure reaction kettle 102, to realize accurate control of the iron ion concentration and the silicon ion concentration in the slurry, which can effectively avoid excessive leaching of iron ions and silicon ions in the high-pressure leaching process, thereby improving the separation effect of subsequent multi-stage countercurrent washing and flocculation precipitation. Specifically, first, the actual concentration values of the iron ion concentration and the silicon ion concentration in the circulating leaching tank 103 are obtained, that is, the iron ion concentration and the silicon ion concentration in the circulating leaching tank 103 are obtained in real time, which reflects the overall level of iron ions and silicon ions in the slurry. Then, the sum of the actual concentration values of the iron ion concentration and the silicon ion concentration in the circulating leaching tank 103 is compared with the preset target concentration threshold. The target concentration threshold is set according to the needs of the subsequent treatment process, for example, multi-stage countercurrent washing and flocculation precipitation, which represents the maximum leaching amount of iron ions and silicon ions allowed in the high-pressure leaching stage. If the sum of the actual concentration values of the iron ion concentration and the silicon ion concentration in the circulating leaching tank 103 exceeds the target concentration threshold, it means that the concentration of these iron ions and silicon ions in the slurry is too high and may affect the subsequent treatment effect. Finally, the feed concentration is regulated. In the case where the sum of the actual concentration values exceeds the target concentration threshold, the regulation mechanism will be started to reduce the feed slurry concentration of the high-pressure reaction kettle 102, for example, by increasing the proportion of liquid such as water added to the high-pressure reaction kettle 102, thereby diluting the slurry and reducing the leaching amount of iron ions and silicon ions in the high-pressure leaching stage.

[0056] In this way, the laterite nickel ore high-pressure leaching slurry concentration regulation method can effectively reduce the leaching of iron ions and silicon ions by timely reducing the feed slurry concentration of the high-pressure reactor 102, reduce the influence of iron ions and silicon ions on the separation effect in the subsequent treatment process, such as in the multi-stage countercurrent washing, too high iron ion and silicon ion concentration may promote the formation of colloids, affecting the solid-liquid separation. Moreover, the regulation method ensures the stability of the ion concentration in the slurry, so that the ion concentration is appropriate, which helps to maintain the efficiency and stability of the entire treatment process, reduces unnecessary process adjustment, and improves production efficiency. In the face of different batches of laterite nickel ore, the iron and silicon content may vary, and the embodiment can flexibly respond by adjusting the feed concentration of the high-pressure reactor 102 in real time, ensuring the controllability of the ion concentration in the slurry, enhancing the adaptability and flexibility, reducing the leaching of iron ions and silicon ions, and realizing real-time regulation of the iron ion concentration and silicon ion concentration in the slurry, thereby avoiding too many iron ions and silicon ions being leached in the high-pressure leaching stage, affecting the subsequent multi-stage countercurrent washing flocculation and precipitation effect, and solving the problem of poor flocculation and precipitation effect in the multi-stage countercurrent washing in the related art.

[0057] As shown in Figure 2 and Figure 6 In some embodiments, in step S300, the feed slurry concentration of the high-pressure reactor 102 is controlled to be reduced, including:

[0058] Step S310, obtaining the discharge slurry concentration of the thickener 101 and the target discharge concentration value;

[0059] Step S320, comparing the discharge slurry concentration and the target discharge concentration value;

[0060] Step S330, when the discharge slurry concentration is equal to the target discharge concentration value, the feed slurry concentration of the high-pressure reactor 102 is controlled to stop reducing.

[0061] The discharge slurry concentration of the thickener 101 is the detected concentration value of the discharge slurry of the thickener 101, which detects the solid content in the slurry, i.e. the proportion of solid particles to the total volume of the slurry, which can be but not limited to measured in real time by sensors and analysis equipment integrated in the laterite nickel ore high-pressure leaching slurry concentration regulation system.

[0062] The target discharge concentration value is pre-set according to the requirements of the metallurgical process and the needs of the subsequent process, which represents an optimal slurry concentration to improve the efficiency of the high-pressure leaching stage and optimize the subsequent flocculation and precipitation process.

[0063] Comparing the discharge slurry concentration with the target discharge concentration value means that the automatic control device 104 and other control equipment can receive the real-time discharge slurry concentration data of the thickener 101, and compare it with the preset target discharge concentration value. The comparison is completed through the built-in algorithm and logical judgment mechanism, which ensures the accuracy and real-time performance of the slurry concentration control. The detailed steps and control structure of the two value comparison process are similar to the prior art, and will not be described here.

[0064] When the discharge slurry concentration is equal to the target discharge concentration value, the control of the feed slurry concentration of the high-pressure reactor 102 stops decreasing, which means that if the comparison result shows that the discharge slurry concentration of the thickener 101 reaches the target discharge concentration value, the automatic control device 104 and other control equipment will adjust the feed slurry concentration of the high-pressure reactor 102, i.e. stop further reducing the feed slurry concentration, to maintain the concentration around the target discharge concentration value.

[0065] In this way, appropriate slurry concentration ensures efficient leaching of metals in the high-pressure reactor 102. Too high concentration may mean excessive dissolution of iron and silicon ions, affecting the subsequent flocculation and precipitation effect. Too low concentration may reduce the dissolution rate of metal ions and prolong the leaching time. By precisely controlling the discharge slurry concentration of the thickener 101, the optimal leaching conditions inside the high-pressure reactor 102 can be maintained, thereby improving the leaching efficiency and recovery rate of metals. Controlling the feed slurry concentration of the high-pressure reactor 102 to be equal to the target discharge concentration value can keep the slurry concentration within the appropriate range, avoiding excessive iron and silicon ions in the high-pressure leaching stage, which will affect the solid-liquid separation effect in the subsequent flocculation and precipitation stage. Maintaining appropriate slurry concentration helps to form more effective flocculation bodies, thereby improving the separation efficiency of metals and impurities. Real-time concentration monitoring and feedback mechanism ensures the stability and continuity of the entire system operation, reduces fluctuations in the slurry processing process, avoids production efficiency decline and inconsistent product quality caused by concentration fluctuations, reduces the need for manual intervention, and improves production efficiency and process controllability.

[0066] As shown in Figure 3 and Figure 6 In some embodiments, in step S310, the discharge slurry concentration of the thickener 101 is obtained, including:

[0067] Step S311, obtaining the feed slurry concentration, feed slurry density, discharge slurry density, settling area and discharge volume flow rate of the thickener 101, and the settling rate of the flocculation body;

[0068] Step S312, obtaining the discharge slurry concentration of the thickener 101 based on the feed slurry concentration, feed slurry density, discharge slurry density, settling area and discharge volume flow rate of the thickener 101, and the settling rate of the flocculation body.

[0069] The feed slurry concentration refers to the volume ratio of solid particles in the slurry, such as laterite nickel ore to water. This can be measured in real time using online concentration measurement equipment, such as ultrasonic densitometers and radiographic densitometers. The feed slurry density and discharge slurry density, which refer to the mass of slurry per unit volume, are affected by the ratio of solids to liquids in the slurry. Changes in density can significantly affect slurry fluidity, settling rate, and flocculation.

[0070] The settling area refers to the horizontal surface area of ​​the slurry in the thickener 101. The size of this area directly affects the speed and efficiency of slurry settling. The discharge volume flow rate refers to the volume of slurry discharged from the thickener 101 outlet per unit time, reflecting the slurry processing speed and production capacity.

[0071] The settling rate of flocs is the process by which solid particles in the slurry aggregate into larger particles by adding flocculants, thereby accelerating their settling. The settling rate is related to the processing efficiency of the thickener 101 and the concentration of the discharged slurry. Based on the above parameters and the principles of material balance and fluid dynamics, the discharge slurry concentration of the thickener 101 can be calculated. The actual discharge slurry concentration of the thickener 101 can be estimated by taking into account the differences in feed and discharge concentration, density, and flow rate, as well as the impact of the floc settling rate on slurry concentration efficiency.

[0072] With this setup, real-time slurry concentration data can be used to optimize thickener 101 operating parameters, such as the amount of flocculant added and settling time, improving slurry treatment in thickener 101 and, consequently, the subsequent leaching efficiency in autoclave 102. Accurate slurry concentration information can help automatic control device 104 adjust the feed conditions for autoclave 102, avoiding resource waste caused by excessively high concentrations or metal recovery impacted by excessively low concentrations. Precise control of slurry concentration reduces unnecessary concentration or dilution steps, saving water and energy consumption, lowering production costs, and improving slurry treatment efficiency and production line capacity.

[0073] like Figure 3 and Figure 6 As shown, in some embodiments, in step S312, the discharge slurry concentration of the thickener 101 is determined based on the following formula:

[0074]

[0075] Wherein, Vmin is the settling rate of the flocculation body, also refers to the minimum settling rate of the flocculant in the thickener 101, directly affects the concentration efficiency of the ore pulp and the concentration of the final discharge. C1 is the concentration of the feed ore pulp of the thickener 101, which can be the mass of solids per unit volume of ore pulp. ρ1 is the density of the feed ore pulp of the thickener 101, which reflects the combined density of solids and liquids in the feed. C2 is the concentration of the discharge ore pulp of the thickener 101, which represents the concentration of solids in the ore pulp after concentration. ρ2 is the density of the discharge ore pulp of the thickener 101, the density of the treated ore pulp, and the solid particles can be more concentrated. S is the settling area of the thickener 101, that is, the effective area of the solid particles in the ore pulp. G is the volume flow rate of the discharge.

[0076] It can be understood that the core purpose of adding flocculants is to improve the settling velocity of the material, and in a given thickener 101, the settling rate of the flocculation body after adding the flocculant needs to meet the above relationship in order to achieve the target discharge concentration and flow rate of the material.

[0077] The formula of the embodiment can provide a quantitative calculation model between the discharge ore pulp concentration of the thickener 101 and the settling rate of the flocculation body, and can calculate the minimum speed of the flocculation body settling in the thickener 101. The control of this speed is conducive to keeping the discharge ore pulp concentration of the thickener within the target range. By adjusting the amount of flocculant added, controlling the concentration of the feed ore pulp of the thickener, the density of the feed ore pulp, the density of the discharge ore pulp and the volume flow rate of the discharge, and adjusting the settling area of the thickener 101, it can be ensured that the settling rate of the flocculation body is within the appropriate range, thereby effectively controlling the concentration of the discharge ore pulp.

[0078] In specific operation, the automatic control device 104 can monitor the concentrations of iron ions and silicon ions in the circulating leaching tank 103 through the ion concentration acquisition device 105. When the sum of the actual concentration values of the iron ion concentration and the silicon ion concentration exceeds the preset target concentration threshold, the automatic control device 104 will start to control to reduce the discharge ore pulp concentration of the thickener 101, thereby reducing the content of iron and silicon ions in the ore pulp entering the high-pressure reaction kettle 102, improving the effect of the subsequent washing, flocculation and precipitation steps, and indirectly controlling the leaching amount of iron ions and silicon ions by adjusting the ore pulp concentration.

[0079] By monitoring Vmin and inversely calculating C2 according to the formula, the embodiment can adjust the operating conditions of the thickener 101 in real time, and ensure that the discharge ore pulp concentration meets the process requirements. The embodiment has real-time control capability, which can greatly improve the stability and efficiency of the production process, facilitate accurate control of the discharge ore pulp concentration of the thickener 101, avoid excessive iron ions and silicon ions being leached in the high-pressure leaching stage, not only improve the effect of subsequent washing and precipitation, but also reduce unnecessary use of chemical reagents, reduce production cost, improve product quality and recovery rate, reduce human operation errors, and ensure the repeatability and consistency of the process.

[0080] As shown in FIG. 11, in some embodiments, in step S311, the settling rate of the flocculation body is obtained, including: Figure 4 Figure 6 As shown in FIG. 11, in some embodiments, in step S311, the settling rate of the flocculation body is obtained, including:

[0081] Step 3111, obtaining the initial settling rate of the material in the thickener 101 without adding flocculant;

[0082] Step 3112, obtaining the concentration of the flocculant in the liquid phase of the thickener 101, and determining the ratio between the settling rate of the flocculation body and the initial settling rate based on the concentration of the flocculant in the liquid phase;

[0083] Step 3113, determining the settling rate of the flocculation body based on the initial settling rate and the ratio.

[0084] Wherein, obtaining the initial settling rate of the material in the thickener 101 without adding flocculant refers to that before the addition of flocculant, the particles in the ore slurry settle according to the natural gravity to form an initial settling rate. This rate is affected by factors such as the size, density and shape of the solid particles in the ore slurry and the viscosity of the ore slurry. Obtaining this initial settling rate can be used as a benchmark for the change of the settling rate after the addition of flocculant, helping to evaluate the effect of the flocculant and make necessary adjustments.

[0085] Obtaining the concentration of the flocculant in the liquid phase of the thickener 101 refers to that the concentration of the flocculant has a direct impact on the formation and settling rate of the flocculation body. By monitoring the actual concentration of the flocculant in the liquid phase, it can be ensured that the amount of flocculant added reaches the level required to optimize the flocculation effect, avoiding excessive or insufficient addition, thereby improving the flocculation efficiency and saving costs.

[0086] For determining the ratio between the settling rate of the flocculation body and the initial settling rate, after the addition of flocculant, the formation of flocculation body can significantly improve the settling speed of solid particles in the ore slurry, because the flocculant helps to bridge and aggregate between particles, forming larger flocculation body, and then improving the settling rate. By calculating the ratio between the settling rate of the flocculation body and the initial settling rate, the efficiency of the flocculant can be quantified, providing a basis for subsequent concentration control.

[0087] Based on the initial settling rate and the ratio, the settling rate of the flocculation body is determined, which means that after obtaining the initial settling rate and the ratio of the flocculant to improve the settling rate, the system can accurately calculate the settling rate after adding the flocculant. The settling rate directly affects the speed and efficiency of the ore slurry concentration, which is conducive to controlling the discharge ore slurry concentration of the thickener 101.

[0088] ​Thus configured, the present embodiment can significantly improve the thickening efficiency of the ore slurry in the thickener 101 by optimizing the use of flocculant, i.e., a higher concentration of ore slurry can be obtained in the same time, which helps to improve the metal recovery rate in the subsequent high-pressure leaching stage. Accurate measurement of the concentration and effect of the flocculant can help to reduce unnecessary addition of flocculant, and through real-time monitoring and adjustment of the settling rate of the flocculation body, the ore slurry thickening process can be more accurately controlled to ensure that the discharge ore slurry concentration is stably within the target discharge concentration value, which can maintain the stability and efficiency of the entire high-pressure leaching process. Controlling the concentration of the discharge ore slurry can reduce the leaching of iron, silicon and other ions in the high-pressure leaching stage, avoid their interference with the subsequent washing, flocculation and precipitation process, and help to improve the yield and product quality of the entire gold treatment process.

[0089] As shown in Figure 4 and Figure 6 Further, in step 3112, the ratio of the settling rate of the flocculation body to the initial settling rate is determined based on the following formula:

[0090]

[0091] where C is the concentration of the flocculant in the liquid phase of the thickener 101, a1, a2 and a3 are constants calibrated through experiments, reflecting the influence of the characteristics of the flocculant and the physical and chemical properties of the ore slurry on the settling rate. k is the ratio of the settling rate of the flocculation body to the initial settling rate.

[0092] The mathematical model of the present embodiment is a function based on a nonlinear relationship, which is used to quantify the influence of the flocculant concentration C on the ratio k of the settling rate of the flocculation body to the initial settling rate, indicating that there is a complex dependence relationship between the flocculant concentration and the enhanced ratio of the settling rate, rather than a simple linear increase or decrease.

[0093] At low concentrations, the flocculant promotes bridging between particles, forming flocs that increase the settling efficiency. The settling rate of the flocs, Vmin, can increase significantly with the concentration of the flocculant, C, in the liquid phase of the thickener 101. However, as the concentration increases further, the growth of k can slow down and even start to decrease at a certain point due to the weakening of the aggregation effect of the flocs, the increase in the viscosity of the slurry, or the reduction of the binding force between particles due to the influence of the flocculant itself. After calibrating the values through experiments, the model can be used to predict the expected settling rate enhancement ratio at different flocculant concentrations. This helps to determine the optimal usage concentration of the flocculant, at which the settling rate of the flocs reaches its maximum, achieving the most efficient slurry thickening and processing. Based on the relationship between the ratio k of the settling rate of the flocs to the initial settling rate and the concentration C of the flocculant in the liquid phase of the thickener 101, the amount of flocculant added can be controlled in real time to maintain the ratio k within the optimal range. In this way, not only can the efficiency of the flocculation process be ensured, but also the overuse of the flocculant can be avoided. By predicting the impact of changes in flocculant concentration on the settling rate enhancement ratio through the above model, the possible response of the system can be predicted in advance, so that timely adjustments can be made when needed. For example, if it is monitored that k starts to decrease, it means that the concentration of the flocculant may have exceeded the optimal point, and adjustments can be made by reducing the amount of addition, and vice versa.

[0094] By optimizing the use of the flocculant, the present embodiment avoids unnecessary waste and reduces processing costs. The optimization of the ratio of the settling rate of the flocs to the initial settling rate directly improves the efficiency of the slurry processing, reduces the residence time of the slurry in the thickener 101, and speeds up the entire high-pressure leaching process.

[0095] It can be understood that the initial settling rate of the material without adding the flocculant satisfies the following relationship:

[0096]

[0097] wherein Va is the initial settling rate, p3 is the material density, p0 is the liquid density, g is the acceleration of gravity, d is the average particle size of the material, and η is the initial viscosity of the feed slurry of the thickener 101 (without combining the flocculant).

[0098] With the addition of the flocculant, the settling rate of the material changes, and there is a proportional relationship between the settling rate of the material with the addition of the flocculant and the settling rate without the addition of the flocculant, k = Vmin / Va, Vmin is the settling rate of the flocs after adding the flocculant, and Va is the initial settling rate. The value of k satisfies the above relationship with the concentration of the flocculant in the liquid phase.

[0099] As Figure 5 and Figure 6As shown, in some embodiments, in step S3112, the concentration of the flocculant in the liquid phase of the thickener 101 is obtained, including:

[0100] Step S31121, obtaining the flocculant addition amount, and the feed slurry concentration and feed mass flow rate of the thickener 101;

[0101] Step S31122, determining the concentration of the flocculant in the liquid phase of the thickener 101 based on the flocculant addition amount, and the feed slurry concentration and feed mass flow rate of the thickener 101.

[0102] Wherein, obtaining the flocculant addition amount refers to recording or measuring the actual addition amount of the flocculant, which can be obtained by using a precise feeding device such as a metering pump, to ensure the accuracy of subsequent calculations and avoid poor flocculation effect caused by inaccurate addition amount.

[0103] The feed slurry concentration and the feed mass flow rate are key parameters affecting the distribution of the flocculant in the slurry. The feed slurry concentration refers to the proportion of solid content in the slurry entering the thickener 101, while the feed mass flow rate refers to the total mass of the slurry entering the thickener 101 per unit time. The feed slurry concentration and the feed mass flow rate are crucial for calculating the actual concentration of the flocculant in the liquid phase.

[0104] Based on the flocculant addition amount, the feed slurry concentration and the feed mass flow rate, the concentration of the flocculant in the liquid phase of the thickener 101 is determined. Based on the feed mass flow rate and the slurry density, the total volume of the feed slurry can be calculated. To determine the concentration of the flocculant in the liquid phase of the thickener 101, the addition amount of the flocculant needs to be combined with the total volume of the feed slurry, while considering the influence of the feed slurry concentration on the distribution of the flocculant, to determine the actual concentration of the flocculant in the liquid phase.

[0105] In this way, the embodiment accurately obtains the concentration of the flocculant in the liquid phase to ensure that the flocculant is added at an optimal concentration, avoiding insufficient or excessive addition. Optimized use not only improves the flocculation effect, but also reduces the waste of flocculant and production costs. Based on real-time data of the flocculant concentration, the addition amount of the flocculant can be dynamically adjusted to ensure that the flocculant concentration always maintains within the most effective range, which helps to avoid unstable concentration process efficiency caused by fluctuations in flocculant concentration. Precise control of the flocculant concentration helps to improve the formation speed and settling efficiency of the flocculation body, thereby accelerating the concentration process of the slurry in the thickener 101 and improving the processing capacity of the thickener 101 and the overall production efficiency of the system. Reasonable flocculant concentration ensures that the solid particles in the slurry can settle in a better form, reducing suspended solids and improving the efficiency of solid-liquid separation, which is crucial for subsequent high-pressure leaching, washing, flocculation and precipitation processes, and helps to improve the overall metal recovery rate and product quality.

[0106] As shown,Figure 5 and Figure 6 As shown in FIG. 31, in some embodiments, in step S31122, the concentration of the flocculant in the liquid phase of the thickener 101 is determined based on the following formula:

[0107] m = C x (1 - C1) x V0

[0108] where m is the amount of flocculant added, i.e., the mass of flocculant added to the thickener 101 per unit time. C is the concentration of the flocculant in the liquid phase of the thickener 101, C1 is the concentration of the feed slurry of the thickener 101, representing the volume fraction or mass fraction of solid particles in the slurry. V0 is the mass flow rate of the feed slurry of the thickener 101, i.e., the mass of slurry entering the thickener 101 per unit time.

[0109] When C1 and V0 are known and constant, the concentration C of the flocculant in the liquid phase can be controlled by adjusting the amount of flocculant added m. This formula takes into account the solid particle content C1 in the feed slurry and the total volume of feed per unit time, which is determined by V0 and C1 together, so that the calculated concentration C of the flocculant in the liquid phase is more accurate, reflecting the distribution of the flocculant in the actual liquid phase environment.

[0110] The (1 - C1) part of the formula represents the volume or mass proportion of the liquid phase in the slurry. Because in the thickener 101, the slurry is composed of solid particles and liquid, the solid particle part does not directly participate in the dissolution and distribution of the flocculant, so it is excluded when calculating the flocculant concentration in the liquid phase. By dividing m by (1 - C1) x V0, we are actually calculating the mass of flocculant per unit volume of liquid phase, i.e., the concentration C of the flocculant in the liquid phase.

[0111] By setting it this way, since the concentration of the flocculant directly affects the formation speed and size of the flocculation body, by accurately calculating the concentration of the flocculant in the liquid phase, we can ensure that the flocculant works at an optimal concentration, thereby improving the flocculation efficiency and settling rate of the solid particles in the slurry and speeding up the slurry thickening process. Using this formula, we can accurately calculate the required concentration of the flocculant in the liquid phase, avoiding excessive addition of the flocculant, reducing waste of the flocculant, and reducing production costs.

[0112] Under specific feed slurry concentration and mass flow rate, by adjusting the amount of flocculant added to control its concentration in the liquid phase, we can help maintain the stability and consistency of the entire slurry treatment process, improve the predictability and controllability of the process. By adjusting the concentration of the flocculant in the liquid phase of the thickener 101, we can optimize the viscosity and solid content of the slurry, etc., creating favorable conditions for subsequent high-pressure leaching, washing, and precipitation processes, etc., and improving overall production efficiency and metal recovery rate.

[0113] Those skilled in the art can understand that all or part of the processes of the above-mentioned embodiment methods can be completed by instructing the relevant hardware through a computer program, and the program can be stored in a computer readable storage medium. The computer readable storage medium is a disk, an optical disk, a read-only memory or a random access memory, etc.

[0114] As shown in Figures 1 to 6 The embodiment of the second aspect of the application provides a laterite nickel ore high-pressure leaching slurry concentration regulation system, which can implement the laterite nickel ore high-pressure leaching slurry concentration regulation method in any of the above-mentioned embodiments. The laterite nickel ore high-pressure leaching slurry concentration regulation system comprises a thickener 101, a high-pressure reaction kettle 102, a circulating leaching tank 103, an ion concentration acquisition device 105 and an automatic regulation device 104. The underflow of the thickener 101 is connected with the feeding end of the high-pressure reaction kettle 102, and the discharging end of the high-pressure reaction kettle 102 is connected with the circulating leaching tank 103. The ion concentration acquisition device 105 is used to acquire the iron ion concentration and the silicon ion concentration in the circulating leaching tank 103, and send the iron ion concentration and the silicon ion concentration to the automatic regulation device 104. The automatic regulation device 104 is used to control the feeding slurry concentration of the high-pressure reaction kettle 102 to be reduced when the actual concentration value of the sum of the iron ion concentration and the silicon ion concentration is greater than the target concentration threshold value.

[0115] The thickener 101 is used to preliminarily concentrate the laterite nickel ore slurry, remove excess water and increase the solid content of the slurry. The underflow of the thickener 101, i.e. the more concentrated slurry, is sent to the high-pressure reaction kettle 102, which can improve the efficiency of high-pressure leaching, because the reduced amount of water means less energy consumption for heating and pressurizing. Under high temperature and high pressure conditions, the high-pressure reaction kettle 102 promotes the leaching of metals such as nickel, cobalt and manganese in the slurry. The slurry after concentration by the thickener 101 enters the high-pressure reaction kettle 102, and the reacted slurry is sent to the circulating leaching tank 103.

[0116] As an intermediate storage and further processing device of the slurry, the circulating leaching tank 103 allows the slurry to flow therein so as to more fully leach the metal ions therein and subsequently regulate the concentration. The circulating leaching tank 103 is the sampling point of the ion concentration acquisition device 105 to obtain the concentrations of iron ions and silicon ions in the slurry. The ion concentration acquisition device 105 is responsible for real-time monitoring of the iron ion and silicon ion concentrations of the slurry in the circulating leaching tank 103, and can provide a basis for the automatic regulation device 104 to implement concentration regulation.

[0117] The automatic control device 104 receives concentration information of iron ions and silicon ions in the circulating leaching tank 103 from the ion concentration acquisition device 105. The automatic control device 104 can be, but is not limited to, a programmable logic controller. By receiving actual concentration values and target concentration thresholds, and sending electrical signals to control the concentration of the feed slurry of the high-pressure reactor, the concentration of the feed slurry of the high-pressure reactor 102 can be reduced. When the sum of the actual concentration values of the iron ions and silicon ions in the circulating leaching tank 103 exceeds the preset target concentration value, the automatic control device 104 can send electrical signals to the high-pressure reactor 102 to reduce the concentration of the feed slurry of the high-pressure reactor 102, thereby reducing the excessive generation of iron ions and silicon ions during the leaching stage.

[0118] The present embodiment preliminarily concentrates the slurry by the thickener 101, reduces the amount of water entering the high-pressure reactor 102, thereby improving the temperature and pressure conditions in the high-pressure reactor 102, which is conducive to efficient leaching of metals. The automatic control device 104 adjusts the concentration of the slurry entering the high-pressure reactor 102 according to the concentrations of iron ions and silicon ions in the circulating leaching tank 103, thereby ensuring the optimization of the subsequent multi-stage countercurrent washing, flocculation and precipitation process. Excessive concentrations of iron ions and silicon ions can interfere with the formation of flocculation bodies and affect the solid-liquid separation effect of metal ions and slag. By adjusting the concentration of the slurry, the generation of these impurity ions is reduced, the efficiency and purity of solid-liquid separation are improved, unnecessary slurry concentration adjustment is reduced, excessive leaching of iron ions and silicon ions is avoided, and the amount of chemical reagents used is reduced. Real-time monitoring and response of the automatic control device 104 make the entire slurry treatment process more stable, reduce the adverse effects caused by fluctuations in the composition of the slurry, and improve the consistency and reliability of production. The combination of the ion concentration acquisition device 105 and the automatic control device 104 enables automatic control of the system, improves the intelligent level of slurry treatment, reduces the need for manual intervention, and improves production efficiency. The red soil nickel ore high-pressure leaching slurry concentration control system realizes the optimization of slurry treatment through the fine design and mutual cooperation of various structures, improves the recovery rate of metals and the quality of products, and reduces production costs.

[0119] It can be understood that the laterite nickel ore high-pressure leaching slurry concentration regulation system provided by the present application comprises a thickener 101, a high-pressure reaction kettle 102, a circulating leaching tank 103 and an automatic regulation device 104, the underflow of the thickener 101 is connected with the feeding end of the high-pressure reaction kettle 102, the discharging end of the high-pressure reaction kettle 102 is connected with the circulating leaching tank 103, the automatic regulation device 104 detects the concentrations of iron ions and silicon ions in the circulating leaching tank 103 in real time through a detection module, and when the sum of the concentrations of iron ions and silicon ions exceeds a set threshold value, the feeding slurry concentration of the high-pressure reaction kettle 102 is controlled to be reduced, so that the concentrations of iron ions and silicon ions in the slurry are adjusted in real time, and more iron ions and silicon ions are prevented from being leached in the high-pressure leaching stage, thereby affecting the subsequent multi-stage countercurrent washing flocculation and precipitation effect.

[0120] The detection port of the ion concentration acquisition device 105 can be connected with the circulating leaching tank 103 to obtain part of the slurry in the circulating leaching tank 103, and the ion composition of the part of the slurry is analyzed to obtain the concentrations of iron ions and silicon ions. It can be easily understood that the ion concentration acquisition device 105 can adopt conventional detection equipment and other feasible detection methods in the prior art, such as a metal element analyzer, a spectrophotometer, an inductively coupled plasma mass spectrometer, etc., as long as the concentrations of iron ions and silicon ions in the slurry in the circulating leaching tank 103 can be detected.

[0121] The feeding slurry first enters the thickener 101, and the slurry is thickened in the thickener 101 based on the principle of gravity settling, and the underflow of the thickener 101 is sent to the high-pressure reaction kettle 102 to promote the leaching of nickel, cobalt and manganese in a high-temperature and high-pressure environment, and finally the slurry after leaching is sent to the circulating leaching tank 103.

[0122] The core idea of the present application is to regulate the feeding slurry concentration of the high-pressure reaction kettle 102 according to the concentrations of iron ions and silicon ions in the discharging end of the high-pressure reaction kettle 102, so as to improve the multi-stage countercurrent washing flocculation and precipitation effect.

[0123] In some embodiments, the automatic regulation device 104 is further configured to obtain the discharging slurry concentration of the thickener 101, and when the discharging slurry concentration is equal to a target discharging concentration value, the feeding slurry concentration of the high-pressure reaction kettle 102 is controlled to stop being reduced. It can be understood that the feeding slurry concentration of the high-pressure reaction kettle 102 is consistent with the discharging slurry concentration of the thickener 101, and when the discharging slurry concentration of the thickener 101 reaches the target concentration value, it indicates that the feeding slurry concentration of the high-pressure reaction kettle 102 also reaches the target concentration value.

[0124] The embodiment can improve the accuracy and real-time performance of the pulp concentration control. The step of obtaining the discharge pulp concentration by the automatic control device 104 can refer to the above embodiment. The automatic control device 104 can collect the operating parameters of the thickener 101 through the corresponding sensors and online analyzers, including the concentration, density and volume flow of the feed pulp, the density and volume flow of the discharge pulp, and the settling rate of the flocculation body in the thickener 101, and the like. The automatic control device 104 calculates the discharge pulp concentration of the thickener 101 based on the parameters of the thickener 101. The automatic control device 104 monitors the discharge pulp concentration of the thickener 101 in real time to ensure that it matches the preset target discharge concentration value. Once the concentration reaches the target value, the control device immediately responds to stop reducing the feed pulp concentration of the high-pressure reactor 102 to maintain the stability and efficiency of the entire treatment process, facilitate the accurate control of the discharge pulp concentration of the thickener 101, and avoid the situation of high or low concentration.

[0125] The high-pressure leaching pulp concentration control system and method for laterite nickel ore are described in detail above, and the principles and implementation modes of the present application are described by applying specific examples. The above embodiment is only used to help understand the method and core idea of the present application. Meanwhile, for those skilled in the art, according to the idea of the present application, the specific implementation mode and application range will be changed, and the above description should not be understood as a limitation of the present application.

[0126] Obviously, the above embodiments of the present application are only examples for clearly illustrating the present application, and are not intended to limit the implementation modes of the present application. For those skilled in the art, various obvious changes, readjustments and substitutions can be made without departing from the protection scope of the present application. It is unnecessary and impossible to enumerate all the implementation modes. Any modification, equivalent substitution and improvement within the spirit and principles of the present application should be included in the protection scope of the claims of the present application.

Claims

1. A method for controlling slurry concentration in high-pressure leaching of laterite nickel ore, characterized in that: The laterite nickel ore high-pressure leaching slurry can be contained in a circulating leaching tank, the feed end of the circulating leaching tank is connected to the underflow of the high-pressure reactor, and the feed end of the high-pressure reactor is connected to the underflow of the thickener. The laterite nickel ore high-pressure leaching slurry concentration control method includes: Obtaining actual concentration values ​​and target concentration thresholds of the iron ion concentration and the silicon ion concentration in the circulating leaching tank, wherein the target concentration threshold is a preset value of the sum of the iron ion concentration and the silicon ion concentration in the circulating leaching tank; comparing the sum of the actual concentration values ​​of the iron ion concentration and the silicon ion concentration in the circulating leaching tank with the target concentration threshold, and when the sum of the actual concentration values ​​of the iron ion concentration and the silicon ion concentration in the circulating leaching tank is greater than the target concentration threshold, controlling the feed slurry concentration of the high-pressure reactor to decrease; Controlling the feed slurry concentration of the high-pressure reactor to decrease includes: Obtaining the discharge slurry concentration and target discharge concentration value of the thickener; The discharge slurry concentration is compared with the target discharge concentration value, and when the discharge slurry concentration is equal to the target discharge concentration value, the feed slurry concentration of the high-pressure reactor is controlled to stop decreasing.

2. The method for controlling slurry concentration of laterite nickel ore high pressure leaching according to claim 1, wherein: Obtaining the discharge slurry concentration of the thickener, including: Obtaining the feed slurry concentration, feed slurry density, discharge slurry density, settling area and discharge volume flow rate of the thickener, as well as the settling rate of flocs; The discharge slurry concentration of the thickener is obtained based on the feed slurry concentration, feed slurry density, discharge slurry density, settling area and discharge volume flow rate of the thickener, and the settling rate of the flocs.

3. The method for controlling slurry concentration of laterite nickel ore high pressure leaching according to claim 2, wherein: The discharge slurry concentration of the thickener is determined based on the following formula: Where Vmin is the settling rate of flocs, C1 is the feed slurry concentration of the thickener, ρ1 is the feed slurry density of the thickener, C2 is the discharge slurry concentration of the thickener, ρ2 is the discharge slurry density of the thickener, S is the settling area of ​​the thickener, and G is the discharge volume flow rate.

4. The method for controlling slurry concentration of laterite nickel ore high pressure leaching according to claim 2, wherein: Obtain the sedimentation rate of flocs, including: Obtaining the initial settling velocity of the material in the thickener when no flocculant is added; obtaining a concentration of a flocculant in a liquid phase of the thickener, and determining a ratio between a settling velocity of the flocs and the initial settling velocity based on the concentration of the flocculant in the liquid phase; The settling rate of the flocs is determined based on the initial settling velocity and the ratio.

5. The method for controlling slurry concentration of laterite nickel ore high pressure leaching according to claim 4, characterized in that: The ratio between the settling velocity of the flocs and the initial settling velocity is determined based on the following formula: Wherein, C is the concentration of the flocculant in the liquid phase of the thickener, a1, a2 and a3 are constants calibrated by experiments, and k is the ratio between the settling velocity of the flocs and the initial settling velocity.

6. The method for controlling slurry concentration of laterite nickel ore high pressure leaching according to claim 4, characterized in that: Obtaining the concentration of the flocculant in the liquid phase of the thickener, comprising: Obtaining the amount of flocculant added, as well as the feed slurry concentration and feed mass flow rate of the thickener; The concentration of the flocculant in the liquid phase of the thickener is determined based on the amount of flocculant added, as well as the feed slurry concentration and feed mass flow rate of the thickener.

7. The method for controlling slurry concentration of laterite nickel ore high pressure leaching according to claim 6, characterized in that: The concentration of the flocculant in the liquid phase of the thickener is determined based on the following formula: m=C×(1-C1)×V0 Where m is the amount of flocculant added, C is the concentration of flocculant in the liquid phase of the thickener, C1 is the feed slurry concentration of the thickener, and V0 is the feed mass flow rate of the thickener.

8. A laterite nickel ore high pressure leaching slurry concentration control system, characterized in that: A method for controlling the concentration of a laterite nickel ore high-pressure leaching slurry according to any one of claims 1 to 7 can be implemented, wherein the laterite nickel ore high-pressure leaching slurry concentration control system comprises a thickener, a high-pressure reactor, a circulating leaching tank, an ion concentration collection device, and an automatic control device; The underflow of the thickener is connected to the feed end of the high-pressure reactor, and the discharge end of the high-pressure reactor is connected to the circulating leaching tank; The ion concentration collection device is used to collect the actual concentration values ​​of the iron ion concentration and the silicon ion concentration in the circulating leaching tank, and send the actual concentration values ​​to the automatic control device; The automatic control device is used to control the feed slurry concentration of the high-pressure reactor to decrease when the sum of the actual concentration values ​​of the iron ion concentration and the silicon ion concentration in the circulating leaching tank is greater than the target concentration threshold.

9. The laterite nickel ore high pressure leaching slurry concentration control system according to claim 8, characterized in that: The automatic control device is further used to obtain the discharge slurry concentration of the thickener, and when the discharge slurry concentration is equal to the target discharge concentration value, the feed slurry concentration of the high-pressure reactor is controlled to stop decreasing.

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