Leachate deironing device

Abstract

The utility model discloses a lixivium deironing device which comprises a feeding assembly, a first deironing assembly, a second deironing assembly, a third deironing assembly, a fourth deironing assembly and a fourth deironing assembly, wherein the feeding assembly comprises a lixivium feeding pipe, a hydrogen peroxide feeding pipe, a first steam pipe and a first neutralizer feeding pipe; the pipeline mixer is provided with a first inlet, a second inlet and a mixed outlet, the pipeline mixer is arranged in the vertical direction, the first inlet is formed in the side wall face of the pipeline mixer and located in the upper portion of the pipeline mixer, the second inlet is formed in the upper end of the pipeline mixer, the mixed outlet is formed in the lower end of the pipeline mixer, and the first inlet is connected with a leachate feeding pipe; the second inlet is connected with a hydrogen peroxide feeding pipe; the first steam pipe, the first neutralizer feeding pipe and the mixed outlet are respectively communicated with the first reaction tank; the thickener is used for solid-liquid separation, and the outlet end of the first reaction tank is connected with the inlet end of the thickener. According to the utility model, hydrogen peroxide is used for deironing the leachate, and the problem of low utilization rate during deironing of hydrogen peroxide in the prior art is solved.

Description

Technical Field

[0001] The utility model relates to the technical field of lithium battery recycling, in particular to a leaching liquid iron removal device. Background Art

[0002] In the wet recycling process of lithium batteries, copper is brought in from the waste lithium battery powder. During the leaching process of the battery powder, copper will also dissolve in the leachate. The industry usually uses the iron powder replacement method to remove copper from the leachate. This method is very effective, but it also introduces iron ions into the leachate. Iron is the most common and most harmful impurity in the leachate. They not only affect the normal progress of the leaching process, but also affect the quality of the next process product. Therefore, the removal of iron impurities is very important in the field of lithium battery recycling.

[0003] In the commonly used lithium battery material recycling process, the method of removing iron from the leachate is to use hydrogen peroxide to oxidize the iron ions in the leachate after copper removal, and then add a neutralizer to adjust the pH value to hydrolyze and precipitate the iron ions in the leachate to achieve the purpose of iron removal. Hydrogen peroxide has good oxidizing properties, does not introduce other metal ions, and does not produce new substances. It is very friendly to the battery material industry, which has very strict control of impurity ions.

[0004] The existing method is usually to directly pass the hydrogen peroxide pipeline into the solution of the iron removal reaction tank. The temperature of the reaction tank is usually above 65°C. In addition, the slow stirring speed makes it impossible for the hydrogen peroxide to be quickly mixed and evenly distributed in the reaction tank. It will escape with the water vapor, resulting in extremely low hydrogen peroxide utilization, causing a lot of waste, and increasing production costs. If the front-end hydrogen peroxide feeding pump fails, it may also cause the slurry in the reaction tank to siphon back to the hydrogen peroxide storage tank, affecting production safety. Some companies use a ring distributor at the bottom of the tank to add hydrogen peroxide. Although it can make the hydrogen peroxide mixed more evenly in the reaction tank, the slag produced during the iron removal process will cause the distributor to scale and clog. It is necessary to frequently clean the tank and dismantle the distributor for cleaning, which increases labor costs and seriously affects production efficiency. If the front-end hydrogen peroxide feeding pump fails, it may also cause the slurry in the reaction tank to siphon back to the hydrogen peroxide storage tank, affecting production safety. Utility Model Content

[0005] The utility model aims to solve at least one of the technical problems existing in the prior art. To this end, the utility model provides a device for removing iron from a leaching liquid.

[0006] The solution of the utility model to solve the technical problem is:

[0007] A leachate iron removal device, comprising:

[0008] A feed assembly, comprising a leachate feed pipe, a hydrogen peroxide feed pipe, a first steam pipe and a first neutralizer feed pipe;

[0009] A pipeline mixer, provided with a first inlet, a second inlet and a mixing outlet, the pipeline mixer is arranged in a vertical direction, the first inlet is arranged on the side wall surface of the pipeline mixer and is located at the upper part of the pipeline mixer, the second inlet is arranged at the upper end of the pipeline mixer, the mixing outlet is arranged at the lower end of the pipeline mixer, the first inlet is connected to the leachate feed pipe, and the second inlet is connected to the hydrogen peroxide feed pipe;

[0010] a first reaction tank, wherein the first steam pipe, the first neutralizing agent feed pipe and the mixing outlet are respectively connected to the first reaction tank;

[0011] A thickener is used for solid-liquid separation, and the outlet end of the first reaction tank is connected to the inlet end of the thickener.

[0012] The utility model has at least the following beneficial effects: after the leachate and hydrogen peroxide react under the regulation of appropriate temperature and pH, the iron ions in the leachate can be precipitated, and then the leachate is de-ironized by solid-liquid separation through a thickener. During the whole process, no additional new substances are generated, and no other metal particles are introduced, which meets the high requirements of the battery material industry for the control of impurity ions; the leachate and hydrogen peroxide are pre-mixed before entering the first reaction tank, which can avoid the situation that the hydrogen peroxide is not evenly mixed with the leachate in the first reaction tank and then overflows and escapes with the steam; in the pipeline mixer, the mixing temperature of the leachate and hydrogen peroxide is low, which can prevent the problem of hydrogen peroxide overflowing and escaping, reduce the amount of hydrogen peroxide used, and improve the utilization rate of hydrogen peroxide; and because the pipeline mixer is provided, the hydrogen peroxide storage tank at the front end can be protected. Even if the hydrogen peroxide feeding pump at the front end fails, the mixture in the first reaction tank will not be siphoned into the hydrogen peroxide storage tank, thereby improving the safety of production.

[0013] As a further improvement of the above technical solution, the outlet end of the leachate feed pipe is arranged along the tangent direction of the side wall of the pipeline mixer. Such an arrangement allows the leachate to flow along the extension direction of the leachate feed pipe and enter the pipeline mixer along the tangent direction of the side wall of the pipeline mixer, while the hydrogen peroxide is vertically fed from the top of the pipeline mixer, and the two materials form a vortex in the pipeline mixer, further improving the degree of mixing of the hydrogen peroxide and the leachate.

[0014] As a further improvement of the above technical solution, the outlet end of the first steam pipe, the outlet end of the first neutralizer feed pipe and the mixed outlet are all located at the upper part of the first reaction tank, and the leaching liquid iron removal device also includes a first lifting pipe, the inlet end of the first lifting pipe extends to the bottom of the first reaction tank, and a first discharge pipe is provided at the upper part of the first lifting pipe, the outlet end of the first discharge pipe extends out of the first reaction tank and is connected to the inlet end of the thickener.

[0015] Such an arrangement allows the leachate to flow out after the leachate has reacted completely in the first reaction tank, thereby preventing the leachate from leaving the first reaction tank directly after entering the first reaction tank, thereby improving the iron removal effect of the first reaction tank on the leachate.

[0016] As a further improvement of the above technical solution, a first regulating valve is provided on the leachate feed pipe, and the first regulating valve is used to control the flow rate of the leachate entering the pipeline mixer. A second regulating valve is provided on the hydrogen peroxide feed pipe, and the second regulating valve is used to control the flow rate of the hydrogen peroxide entering the pipeline mixer.

[0017] The first regulating valve and the second regulating valve can control the ratio of the leachate and the hydrogen peroxide entering the pipeline mixer, thereby avoiding the situation where insufficient hydrogen peroxide causes incomplete iron removal reaction of the leachate or excessive hydrogen peroxide causes waste.

[0018] As a further improvement of the above technical solution, the first reaction tank is provided with a first thermometer, the first thermometer is used to obtain the temperature of the mixed liquid in the first reaction tank, and the first steam pipe is provided with a third regulating valve, the third regulating valve is configured to control the flow of the first steam pipe according to the detected temperature of the first thermometer. Through the coordinated use of the first thermometer and the third regulating valve, the temperature in the first reaction tank can be adjusted by controlling the steam consumption, so as to ensure that the temperature in the first reaction tank is maintained within a preset range, thereby ensuring the smooth progress of the reaction.

[0019] As a further improvement of the above technical solution, the first discharge pipe is provided with a first pH detection component, and the first neutralizer feed pipe is provided with a fourth regulating valve, and the fourth regulating valve is configured to control the flow of the first neutralizer feed pipe according to the pH detected by the first pH detection component. Through the coordinated use of the first pH detection component and the fourth regulating valve, the pH in the first reaction tank can be kept within a preset range, thereby ensuring a smooth reaction in the first reaction tank and achieving a better iron removal effect.

[0020] As a further improvement of the above technical solution, the feed assembly further includes a second steam pipe and a second neutralizer feed pipe, and the leaching liquid iron removal device further includes:

[0021] A second reaction tank is provided between the first reaction tank and the thickener, the outlet end of the first reaction tank is communicated with the second reaction tank, the outlet ends of the second steam pipe and the second neutralizer feed pipe are respectively communicated with the second reaction tank, and the outlet end of the first reaction tank, the outlet end of the second steam pipe and the outlet end of the second neutralizer feed pipe are all located at the upper part of the second reaction tank;

[0022] A second feeding pipe, the inlet end of which extends into the bottom of the second reaction tank, a second discharge pipe is provided on the upper part of the second feeding pipe, the second discharge pipe extends out of the second reaction tank and is connected to the inlet end of the thickener.

[0023] Providing a second reaction tank can allow the leaching solution to react further, making the reaction between the leaching solution and hydrogen peroxide more complete, thereby improving the iron removal effect of the leaching solution.

[0024] As a further improvement of the above technical solution, the leaching solution iron removal device further includes:

[0025] a third reaction tank, which is disposed between the second reaction tank and the thickener, wherein the outlet end of the second discharge pipe is connected to the third reaction tank, the outlet end of the second discharge pipe is located at the upper part of the third reaction tank, and a first liquid level gauge is disposed at the upper end of the third reaction tank, and the first liquid level gauge is used to detect the liquid level in the third reaction tank;

[0026] A discharge conveying pump, wherein the inlet end of the discharge conveying pump is connected to the bottom of the third reaction tank, the outlet end of the discharge conveying pump is connected to the thickener, and a fifth regulating valve is provided between the outlet end of the discharge conveying pump and the thickener, and the fifth regulating valve is configured to control the flow rate entering the thickener according to the detected liquid level of the first liquid level meter.

[0027] The third reaction tank is provided to further make the iron removal reaction more complete. The fifth regulating valve is used in conjunction with the first liquid level meter to intelligently adjust the opening size of the fifth regulating valve to keep the liquid level in the third reaction tank at a preset height level.

[0028] As a further improvement of the above technical solution, the leaching solution iron removal device also includes a seed pipe, the bottom of the thickener is provided with a slurry outlet, the slurry outlet is connected to the inlet end of the seed pipe, and the outlet end of the seed pipe is connected to the first reaction tank of the leaching solution iron removal device. Since the slurry concentrated by the thickener is returned to the first reaction tank as a seed, the iron slag grains after the reaction can grow larger, the precipitation efficiency of iron ions can be improved, the iron slag filtering performance can be improved, the problem of difficulty in iron slag filtering can be solved, and the leaching solution can be more thoroughly iron-removed.

[0029] As a further improvement of the above technical solution, a supernatant outlet is provided at the top of the thickener, and the leaching solution iron removal device further comprises a supernatant storage tank, wherein the supernatant outlet is connected to the inlet end of the supernatant storage tank. The supernatant storage tank can collect and store the supernatant for subsequent processing. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] In order to more clearly illustrate the technical solutions in the embodiments of the present utility model, the following is a brief description of the drawings required for the description of the embodiments. Obviously, the drawings described are only part of the embodiments of the present utility model, not all of the embodiments, and those skilled in the art can also obtain other design solutions and drawings based on these drawings without creative work.

[0031] Figure 1 This is a schematic diagram of the overall structure of the leaching solution iron removal device of the utility model embodiment;

[0032] Figure 2 It is a structural schematic diagram of a pipeline mixer according to an embodiment of the utility model;

[0033] Figure 3 is a top view of a pipeline mixer according to an embodiment of the utility model;

[0034] Figure 4 It is a schematic structural diagram of the first reaction tank of an embodiment of the utility model;

[0035] Figure 5 It is a structural schematic diagram of the second reaction tank of an embodiment of the utility model;

[0036] Figure 6 It is a schematic structural diagram of the third reaction tank of the embodiment of the utility model;

[0037] Figure 7 It is a structural schematic diagram of a thickener of an embodiment of the utility model;

[0038] Figure 8 It is a schematic structural diagram of the supernatant liquid storage tank of an embodiment of the utility model.

[0039] Reference numerals: 100, feed assembly; 110, leachate feed pipe; 111, first regulating valve; 112, first flowmeter; 120, hydrogen peroxide feed pipe; 121, second regulating valve; 122, second flowmeter; 130, first steam pipe; 131, third regulating valve; 132, third flowmeter; 140, first neutralizer feed pipe; 141, fourth regulating valve; 142, fourth flowmeter; 150, seed pipe; 151, eighth regulating valve; 152, eighth flowmeter; 160, second steam pipe; 161, sixth regulating valve; 162, sixth flowmeter; 170, second neutralizer feed pipe; 171, seventh regulating valve; 172, seventh flowmeter;

[0040] 200, pipeline mixer; 210, first inlet; 220, second inlet; 230, mixing outlet; 240, flange;

[0041] 300, first reaction tank; 310, first material extraction pipe; 320, first material discharge pipe; 330, first pH detection component; 340, first thermometer;

[0042] 400, thickener; 410, supernatant outlet; 420, slurry outlet; 430, slurry delivery pump; 440, second sampling port;

[0043] 500, second reaction tank; 510, second material extraction pipe; 520, second material discharge pipe; 530, second pH detection component; 540, second thermometer;

[0044] 600, third reaction tank; 610, discharging delivery pump; 611, fifth regulating valve; 612, fifth flow meter; 613, first sampling port; 620, first liquid level meter; 630, third thermometer;

[0045] 700, supernatant liquid storage tank; 710, supernatant liquid delivery pump; 720, second liquid level meter; 730, third sampling port;

[0046] 800, filter press;

[0047] 900. Fine filtration device. DETAILED DESCRIPTION

[0048] Embodiments of the present invention are described in detail below, examples of which are shown in the accompanying drawings, wherein the same or similar reference numerals throughout represent the same or similar elements or elements having the same or similar functions. The embodiments described below with reference to the accompanying drawings are exemplary and are only used to explain the present invention, and should not be construed as limiting the present invention.

[0049] In the description of the present invention, descriptions of orientations, such as up, down, front, back, left, right, etc., and orientations or positional relationships indicated are based on the orientations or positional relationships shown in the drawings and are only for the convenience of describing the present invention and simplifying the description. They 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 should not be understood as a limitation on the present invention.

[0050] In the description of the present utility model, "several" means one or more, "more" means more than two, "greater than", "less than", "exceed" etc. are understood to exclude the number itself, and "above", "below", "within" etc. are understood to include the number itself. If there is a description of "first" or "second", it is only used for the purpose of distinguishing the technical features, and cannot be understood as indicating or implying the relative importance or implicitly indicating the number of the indicated technical features or implicitly indicating the order of the indicated technical features.

[0051] In the description of the present invention, unless otherwise clearly defined, terms such as setting, installing, connecting, etc. should be understood in a broad sense, and technicians in the relevant technical field can reasonably determine the specific meanings of the above terms in the present invention based on the specific content of the technical solution.

[0052] Obviously, the described embodiments are only part of the embodiments of the utility model, not all of them. Based on the embodiments of the utility model, other embodiments obtained by technicians in this field without creative work are all within the scope of protection of the utility model. The various technical features in the utility model can be combined interchangeably without conflicting with each other.

[0053] Reference Figures 1 to 8 The embodiment of the utility model proposes a device for removing iron from a leachate, including a feed assembly 100, a pipeline mixer 200, a first reaction tank 300 and a thickener 400. The device can use hydrogen peroxide to remove iron from the leachate after copper removal. No new substances will be generated during the iron removal process, and no other metal particles will be introduced. Moreover, the problem of low utilization rate of hydrogen peroxide in the prior art can be solved. The direction of the arrow in the figure indicates the direction of material flow.

[0054] Among them, the feeding assembly 100 includes a leachate feed pipe 110, a hydrogen peroxide feed pipe 120, a first steam pipe 130 and a first neutralizer feed pipe 140. The leachate feed pipe 110 is used to provide the leachate after copper removal to the leachate iron removal device, the hydrogen peroxide feed pipe 120 is used to provide hydrogen peroxide to the leachate iron removal device, the first steam pipe 130 is used to provide steam to the leachate, and the first neutralizer feed pipe 140 is used to provide a neutralizer for adjusting the pH to the leachate iron removal device.

[0055] The pipeline mixer 200 is used to pre-mix the leachate and hydrogen peroxide. A first inlet 210, a second inlet 220 and a mixing outlet 230 are provided in the pipeline mixer 200. The pipeline mixer 200 is arranged in a vertical direction. The first inlet 210 is arranged on the side wall surface of the pipeline mixer 200 and is located at the upper part of the pipeline mixer 200. The second inlet 220 is arranged at the upper end of the pipeline mixer 200, and the mixing outlet 230 is arranged at the lower end of the pipeline mixer 200. Among them, the first inlet 210 is connected to the leachate feed pipe 110, the second inlet 220 is connected to the hydrogen peroxide feed pipe 120, and the mixing outlet 230 is connected to the first reaction tank 300.

[0056] The leachate after copper removal enters the pipeline mixer 200 from the first inlet 210 along the leachate feed pipe 110, and the hydrogen peroxide enters the pipeline mixer 200 from the second inlet 220 along the hydrogen peroxide feed pipe 120. The leachate and the hydrogen peroxide are mixed in the pipeline mixer 200, and the mixed mixture flows into the first reaction tank 300 from the mixing outlet 230 of the pipeline mixer 200.

[0057] It can be understood that since the first inlet 210 and the second inlet 220 are both arranged at the upper part of the pipeline mixer 200, and the mixing outlet 230 is arranged at the lower end of the pipeline mixer 200, the hydrogen peroxide and the leachate can be fully mixed while flowing from top to bottom along the pipeline mixer 200, and then flow into the first reaction tank 300.

[0058] In addition, the outlet ends of the first steam pipe 130 and the first neutralizer feed pipe 140 are respectively connected to the first reaction tank 300. The first steam pipe 130 provides high-temperature steam to the first reaction tank 300, and the first neutralizer feed pipe 140 provides a neutralizer for adjusting the pH value to the first reaction tank 300. After the hydrogen peroxide and the leachate mixed in the pipeline mixer 200 enter the first reaction tank 300, a goethite precipitation reaction can be carried out, and the iron ions in the leachate react to form a precipitate.

[0059] The thickener 400 is used for solid-liquid separation. The inlet end of the thickener 400 is connected to the outlet end of the first reaction tank 300. The leachate after the reaction can achieve the effect of removing iron from the leachate after solid-liquid separation in the thickener 400.

[0060] In this embodiment, the chemical reaction equation using hydrogen peroxide as an oxidant to react with the leaching solution is as follows:

[0061] 2H + +2Fe 2+ +H2O2→2Fe 3+ +2H2O

[0062] Fe 3+ +2H2O→FeOOH+3H +

[0063] The pH of the reaction is in the range of 2.5 to 4.0, which is adjusted by the amount of neutralizer used, and the temperature is kept between 65℃-100℃, which is adjusted by the steam flow rate. In order to ensure the smooth precipitation of goethite, the Fe content in the leaching solution must also be controlled. 3+ concentration, so that the precipitation process Fe 3+ The concentration of H is always maintained at about 1 g / L. During the reaction process of goethite formation, H +This will cause the pH value of the solution to gradually decrease. At this time, a neutralizer needs to be added to control the pH value of the solution in the iron removal reaction tank to remain between 2.5-4.0.

[0064] The neutralizing agent can be one of soda ash, liquid caustic soda, lime, limestone, and nickel carbonate.

[0065] According to the above-mentioned reaction mechanism of iron removal, the leaching solution oxidation iron removal process includes the oxidation of low-valent iron and the hydrolysis of high-valent iron. During the entire reaction process, no new substances are produced and no other metal particles are introduced. This is very friendly to the battery material industry, which has very strict control over impurity ions.

[0066] The leachate and hydrogen peroxide are pre-mixed before entering the first reaction tank 300, which can prevent the hydrogen peroxide from escaping with the steam without being evenly mixed with the leachate in the first reaction tank 300. In the pipeline mixer 200, the mixing temperature of the leachate and hydrogen peroxide is low, which can prevent the problem of hydrogen peroxide overflowing and escaping, reduce the amount of hydrogen peroxide used, and improve the utilization rate of hydrogen peroxide. Moreover, since the pipeline mixer 200 is provided, the hydrogen peroxide storage tank at the front end can be protected. Even if the hydrogen peroxide feeding pump at the front end fails, the mixture in the first reaction tank 300 will not be siphoned into the hydrogen peroxide storage tank, thereby improving the safety of production.

[0067] Reference Figure 2 and Figure 3 In some embodiments, the outlet end of the leachate feed pipe 110 is arranged along the tangent direction of the side wall surface of the pipeline mixer 200. In this arrangement, the leachate can flow along the extension direction of the leachate feed pipe 110 and enter the pipeline mixer 200 along the tangent direction of the side wall surface of the pipeline mixer 200, while the hydrogen peroxide is vertically fed from the top of the pipeline mixer 200, and the two materials form a vortex in the pipeline mixer 200, further improving the degree of mixing of the hydrogen peroxide and the leachate.

[0068] In this embodiment, the diameter of the pipeline mixer 200 is designed to be 2.5 times that of the leachate feed pipe 110, and the height-to-diameter ratio of the pipeline mixer 200 is greater than 5, which can ensure the proportion of the leachate entering the pipeline mixer 200, and can ensure that the leachate and hydrogen peroxide are fully mixed in the pipeline mixer 200 and then flow out to the first reaction tank 300.

[0069] In this embodiment, the bottom of the pipeline mixer 200 is a conical structure, the mixing outlet 230 is located at the lower end of the conical structure, the diameter of the conical structure gradually decreases from top to bottom, and the diameter of the mixing outlet 230 is half the diameter of the middle part of the pipeline mixer 200. The conical structure can guide the mixed material in the pipeline mixer 200 to move to the mixing outlet 230 and further fully mix them.

[0070] In some embodiments, the outlet end of the first steam pipe 130, the outlet end of the first neutralizer feed pipe 140, and the mixing outlet 230 of the pipeline mixer 200 are all arranged at the upper part of the first reaction tank 300, and the steam, neutralizer and leachate mixed with hydrogen peroxide enter the first reaction tank 300 from the upper end of the first reaction tank 300 to react.

[0071] In this embodiment, a top cover is provided on the top of the first reaction tank 300, and mounting holes for mounting the pipeline mixer 200, the first steam pipe 130, and the first neutralizer feed pipe 140 are provided on the top cover, so that the materials can enter the first reaction tank 300 for reaction. A flange 240 is provided on the outer side of the pipeline mixer 200 for mounting the pipeline mixer 200 on the corresponding mounting hole on the first reaction tank 300, and the pipeline mixer 200 can be kept vertically arranged.

[0072] Reference Figure 4 In some embodiments, the leaching solution iron removal device also includes a first feeding pipe 310, which is extended in the vertical direction, and its inlet end extends into the bottom of the first reaction tank 300. A first discharge pipe 320 is arranged on the upper part of the first feeding pipe 310, and the outlet end of the first discharge pipe 320 extends out of the first reaction tank 300. The outlet end of the first discharge pipe 320 is connected to the inlet end of the thickener 400.

[0073] Such arrangement allows the leachate to flow out after the leachate has reacted completely in the first reaction tank 300, thereby preventing the leachate from leaving the first reaction tank 300 directly after entering the first reaction tank 300, thereby improving the iron removal effect of the first reaction tank 300 on the leachate.

[0074] In some embodiments, a first regulating valve 111 is provided on the leachate feed pipe 110, and the first regulating valve 111 is used to control the flow rate of the leachate in the leachate feed pipe 110, thereby controlling the flow rate of the leachate entering the pipeline mixer 200. A second regulating valve 121 is provided on the hydrogen peroxide feed pipe 120, and the second regulating valve 121 is used to control the flow rate of hydrogen peroxide in the hydrogen peroxide feed pipe 120, thereby controlling the flow rate of hydrogen peroxide entering the pipeline mixer 200. Through the joint action of the first regulating valve 111 and the second regulating valve 121, the ratio of hydrogen peroxide and leachate entering the pipeline mixer 200 can be adjusted, thereby ensuring that the hydrogen peroxide and leachate react fully in the subsequent chemical reaction, and further improving the utilization rate of hydrogen peroxide.

[0075] In some embodiments, a first flowmeter 112 is further provided on the leachate feed pipe 110, and a second flowmeter 122 is provided on the hydrogen peroxide feed pipe 120. The first flowmeter 112 is used to detect the flow rate of the leachate in the leachate feed pipe 110, and is used in conjunction with the first regulating valve 111, so that the operator can more accurately control the amount of leachate entering the pipeline mixer 200. The second flowmeter 122 is used to detect the flow rate of hydrogen peroxide in the hydrogen peroxide feed pipe 120, and is used in conjunction with the second regulating valve 121, so that the operator can accurately control the amount of hydrogen peroxide entering the pipeline mixer 200 according to the flow value detected by the second flowmeter 122, thereby avoiding the waste caused by excessive hydrogen peroxide or insufficient leachate reaction caused by insufficient hydrogen peroxide.

[0076] It is understandable that the first regulating valve 111 and the second regulating valve 121 may be manual valves or solenoid valves, etc., which are not specifically limited herein.

[0077] In some embodiments, the first reaction tank 300 is provided with a first thermometer 340, and the first thermometer 340 is used to obtain the temperature of the mixed liquid in the first reaction tank 300. The first steam pipe 130 is provided with a third regulating valve 131, and the third regulating valve 131 is used to control the flow of the first steam pipe 130, and the first thermometer 340 is electrically connected to the third regulating valve 131. When the temperature in the first reaction tank 300 is too low, the first thermometer 340 measures the temperature and transmits the temperature signal to the control module of the third regulating valve 131. The control module determines that the temperature in the first reaction tank 300 is too low, and controls the opening of the third regulating valve 131 to increase, increase the flow of steam, and thus increase the temperature in the first reaction tank 300. When the temperature in the first reaction tank 300 is too high, the first thermometer 340 measures the temperature and transmits the temperature signal to the control module of the third regulating valve 131. The control module controls the opening of the third regulating valve 131 to decrease, reduce the flow of steam, and thus reduce the temperature in the first reaction tank 300.

[0078] It is understandable that the control module of the third regulating valve 131 may be a single chip microcomputer, a PLC controller, etc., which can simply realize the function of controlling the opening size of the third regulating valve 131 according to the first thermometer 340 .

[0079] It is understandable that if the temperature in the first reaction tank 300 is too low or too high, the oxidation reaction of the leachate will be affected. The temperature of the first reaction tank 300 can be regulated by intelligently controlling the steam flow added to the first reaction tank 300 through the first thermometer 340 and the third regulating valve 131. In this embodiment, the temperature in the first reaction tank 300 needs to be controlled within the range of 65°C-95°C to ensure the smooth progress of the reaction.

[0080] In some embodiments, a third flow meter 132 is also provided on the first steam pipe 130. The third flow meter 132 is used to obtain the flow value of the first steam pipe 130. When used in conjunction with the third control valve, the operator can be informed of the flow value on the first steam pipe 130 and control the third control valve more accurately.

[0081] In some embodiments, a first pH detection component 330 is provided on the first discharge pipe 320, a fourth regulating valve 141 is provided on the first neutralizer feed pipe 140, and the first pH detection component 330 is electrically connected to the fourth regulating valve 141. The first pH detection component 330 is used to detect the pH of the liquid on the first discharge pipe 320, so as to obtain the pH in the first reaction tank 300. It is understandable that the pH in the first reaction tank 300 should be maintained within a predetermined range. In this embodiment, the pH value needs to be controlled within the range of 2.5-4.0. During the reaction process, hydrogen ions are generated to reduce the pH value in the first reaction tank 300. When the pH value is detected to be too low, an alkaline neutralizer needs to be added to adjust the pH value of the reaction to ensure the smooth progress of the reaction.

[0082] In this embodiment, the first pH detection component 330 transmits the pH information on the first discharge pipe 320 to the control module of the fourth regulating valve 141. The control module of the fourth regulating valve 141 determines whether the detected pH is within a preset pH range. If the pH is detected to be too low, the opening of the fourth regulating valve 141 is controlled to increase, so that the flow rate of the neutralizer is increased, thereby increasing the pH value in the first reaction tank 300. If the pH is too high, the opening of the fourth regulating valve 141 is controlled to decrease, so that the flow rate of the neutralizer entering the first reaction tank 300 is reduced to ensure that the pH value in the first reaction tank 300 is within the preset range.

[0083] It is understandable that the control module of the fourth regulating valve 141 can be a single chip microcomputer, a PLC controller, etc., which can simply control the opening size of the fourth regulating valve 141 according to the first pH detection component 330. In this embodiment, the first pH detection component 330 is a pH-potential detector.

[0084] In some embodiments, a fourth flow meter 142 is also provided on the first neutralizer feed pipe 140. The fourth flow meter 142 is used to obtain the flow value of the first neutralizer feed pipe 140. When used in conjunction with the fourth control valve, the operator can be informed of the flow value on the first neutralizer feed pipe 140, and the opening control of the fourth control valve can be more accurate.

[0085] Reference Figure 1 and Figure 5In some embodiments, the leaching solution iron removal device further includes a second reaction tank 500, which is disposed between the first reaction tank 300 and the thickener 400, and the feed assembly 100 further includes a second steam pipe 160 and a second neutralizer feed pipe 170. The outlet ends of the second steam pipe 160 and the second neutralizer feed pipe 170 are respectively connected to the second reaction tank 500, and the outlet end of the first reaction tank 300 is connected to the second reaction tank 500. The second steam pipe 160 is used to provide steam to the second reaction tank 500, and the second neutralizer feed pipe 170 is used to provide a neutralizer to the second reaction tank 500. The reacted material in the first reaction tank 300 enters the second reaction tank 500 and is mixed with the steam entering the second reaction tank 500 from the second steam pipe 160 and the neutralizer entering the second reaction tank 500 from the second neutralizer feed pipe 170. The second reaction tank 500 is used to further react the material that has not been completely reacted in the first reaction tank 300, so as to improve the iron removal effect of the leaching solution.

[0086] In some embodiments, the outlet end of the second steam pipe 160, the outlet end of the second neutralizer, and the outlet end of the first reaction tank 300 are all located at the upper part of the second reaction tank 500, and the leaching liquid iron removal device also includes a second feed pipe 510, which is extended in the vertical direction, and its inlet end extends to the bottom of the second reaction tank 500. A second discharge pipe 520 is arranged at the upper part of the second feed pipe 510, and the second discharge pipe 520 extends out of the second reaction tank 500 and is connected to the inlet end of the thickener 400.

[0087] Such an arrangement allows the leachate and the neutralizer to flow to the bottom of the second reaction tank 500 first, and then flow out after the reaction is complete in the second reaction tank 500, thereby preventing the leachate that has just entered the second reaction tank 500 from directly leaving the second reaction tank 500, thereby improving the iron removal reaction effect of the leachate in the second reaction tank 500.

[0088] In this embodiment, the outlet of the first discharge pipe 320 is the outlet end of the first reaction tank 300, and the outlet of the first discharge pipe 320 is connected to the second reaction tank 500. In this embodiment, the first reaction tank 300 and the second reaction tank 500 have the same height, and the first discharge pipe 320 is horizontally arranged.

[0089] It can be understood that the number of the second reaction tanks 500 can be one or more, the number of the second feed pipes 510 is consistent with the number of the second reaction tanks 500, the second feed pipes 510 are arranged one-to-one with the second reaction tanks 500, and each second reaction tank 500 is matched with at least one second steam pipe 160 and at least one second neutralizer feed pipe 170. When multiple second reaction tanks 500 are provided, two adjacent second reaction tanks 500 are connected through the second discharge pipe 520 of the previous second reaction tank 500, and the material flows from the first reaction tank 300 to the first second reaction tank 500, and then flows through multiple second reaction tanks 500 in sequence, and flows out through the second feed pipe 510 of the second reaction tank 500 at the end.

[0090] It is understandable that providing a plurality of second reaction tanks 500 can further ensure that the reaction is carried out completely, thereby improving the iron removal effect of the leaching solution.

[0091] In some embodiments, the second reaction tank 500 is provided with a second thermometer 540, and the second thermometer 540 is used to obtain the temperature of the mixed liquid in the second reaction tank 500. The second steam pipe 160 is provided with a sixth regulating valve 161, and the sixth regulating valve 161 is used to control the flow of the second steam pipe 160, and the second thermometer 540 is electrically connected to the sixth regulating valve 161. When the temperature in the second reaction tank 500 is too low, the second thermometer 540 measures the temperature and transmits the temperature signal to the control module of the sixth regulating valve 161. The control module of the sixth regulating valve 161 determines that the temperature in the second reaction tank 500 is too low, and controls the opening of the sixth regulating valve 161 to increase, thereby increasing the steam flow entering the second reaction tank 500, so that the temperature of the second reaction tank 500 increases. When the temperature in the second reaction tank 500 is too high, the second thermometer 540 measures the temperature and transmits the temperature signal to the control module of the sixth regulating valve 161. The control module of the sixth regulating valve 161 controls the opening of the sixth regulating valve 161 to decrease, thereby reducing the steam flow entering the second reaction tank 500 and lowering the temperature in the second reaction tank 500.

[0092] It is understandable that the control module of the sixth regulating valve 161 can be a single chip microcomputer, a PLC controller, etc., which can simply realize the function of controlling the opening size of the sixth regulating valve 161 according to the second thermometer 540.

[0093] In some embodiments, a sixth flow meter 162 is further provided on the second steam pipe 160. The sixth flow meter 162 is used to obtain the flow value of the second steam pipe 160. When used in conjunction with the sixth control valve, the operator can be informed of the flow value on the second steam pipe 160 and the opening control of the sixth control valve can be more accurate.

[0094] In this embodiment, the temperature in the second reaction tank 500 needs to be controlled within the range of 65° C.-95° C. to ensure the smooth progress of the reaction.

[0095] In some embodiments, a second pH detection component 530 is provided on the second discharge pipe 520, a seventh regulating valve 171 is provided on the second neutralizer feed pipe 170, and the second pH detection component 530 is electrically connected to the seventh regulating valve 171. The second pH detection component 530 is used to detect the pH of the liquid on the second discharge pipe 520, so as to obtain the pH in the second reaction tank 500. It is understandable that the pH in the second reaction tank 500 should be maintained within a predetermined range. In this embodiment, the pH value needs to be controlled within the range of 2.5-4.0. During the reaction process, hydrogen ions are generated to reduce the pH value in the second reaction tank 500. When the pH value is detected to be too low, an alkaline neutralizer needs to be added to adjust the pH value of the reaction to ensure the smooth progress of the reaction.

[0096] In this embodiment, the second pH detection component 530 transmits the pH information on the second discharge pipe 520 to the control module of the seventh regulating valve 171. The control module of the seventh regulating valve 171 determines whether the detected pH is within the preset pH range. If the pH is detected to be too low, the opening of the seventh regulating valve 171 is controlled to increase, so that the flow rate of the neutralizer is increased, thereby increasing the pH value in the second reaction tank 500. If the pH is too high, the opening of the seventh regulating valve 171 is controlled to decrease, so that the flow rate of the neutralizer entering the second reaction tank 500 is reduced to ensure that the pH value in the second reaction tank 500 is within the preset range.

[0097] It is understandable that the control module of the seventh regulating valve 171 can be a single chip microcomputer, a PLC controller, etc., which can simply realize the function of controlling the opening size of the seventh regulating valve 171 according to the second pH detection component 530. In this embodiment, the second pH detection component 530 is a pH-potential detector.

[0098] In some embodiments, a seventh flow meter 172 is further provided on the second neutralizer feed pipe 170. The seventh flow meter 172 is used to obtain the flow value of the second neutralizer feed pipe 170. When used together with the seventh control valve, the operator can be informed of the flow value on the second neutralizer feed pipe 170, and the opening control of the seventh control valve can be more accurate.

[0099] In this embodiment, the inlet ends of the first neutralizer feed pipe 140 and the second neutralizer feed pipe 170 are connected to the storage tank for storing the neutralizer through the same pipeline, and the inlet ends of the first steam pipe 130 and the second steam pipe 160 are connected to the steam generator through the same pipeline.

[0100] Reference Figure 1 and Figure 6 In some embodiments, the device for removing iron from the leachate further includes a third reaction tank 600 and a discharge conveying pump 610. The third reaction tank 600 is disposed between the second reaction tank 500 and the thickener 400. The outlet end of the third discharge pipe is connected to the third reaction tank 600. The outlet end of the second discharge pipe 520 is located at the upper part of the third reaction tank 600. The inlet end of the discharge conveying pump 610 is connected to the bottom of the third reaction tank 600. The outlet of the discharge conveying pump 610 is connected to the inlet of the thickener 400. The leachate after the reaction from the second reaction tank 500 enters the third reaction tank 600 through the second discharge pipe 520 for further reaction. The leachate after the complete reaction flows out from the bottom of the third reaction tank 600 to the thickener 400 for solid-liquid separation under the action of the discharge conveying pump 610, which can further improve the iron removal effect of the leachate.

[0101] In some embodiments, a first liquid level gauge 620 is provided at the upper end of the third reaction tank 600, and the first liquid level gauge 620 is used to detect the liquid level in the third reaction tank 600. A fifth regulating valve 611 is provided at the outlet end of the discharge delivery pump 610, and the fifth regulating valve 611 is electrically connected to the first liquid level gauge 620. When the first liquid level gauge 620 detects that the liquid level in the third reaction tank 600 exceeds a preset height, the first liquid level gauge 620 transmits a liquid level signal to the control module of the fifth regulating valve 611, and the control module of the fifth regulating valve 611 controls the opening of the fifth regulating valve 611 to increase so as to increase the discharge flow rate of the material. When the first liquid level gauge 620 detects that the liquid level in the third reaction tank 600 is lower than a preset height, the opening of the fifth regulating valve 611 is reduced to keep the liquid level in the third reaction tank 600 at a preset height level.

[0102] In some embodiments, a fifth flow meter 612 is also provided at the outlet end of the discharge conveying pump 610. The fifth flow meter 612 is used in conjunction with the fifth regulating valve 611 and can detect the flow rate between the outlet end of the discharge conveying pump 610 and the inlet end of the thickener 400, so that the operator can adjust the fifth regulating valve 611 and promptly detect abnormalities such as blockages in the pipeline.

[0103] It is understandable that the control module of the fifth regulating valve 611 may be a single chip microcomputer, a PLC controller, etc., which can simply realize the function of controlling the opening size of the fifth regulating valve 611 according to the first liquid level meter 620 .

[0104] In some embodiments, the third reaction tank 600 is provided with a third thermometer 630, which is used to detect the temperature inside the third reaction tank 600. When the third thermometer 630 detects that the temperature inside the third reaction tank 600 is too high or too low, the operator can increase or decrease the temperature of the third reaction tank 600 according to the temperature value.

[0105] It is understood that the thickener 400 can separate the solid and liquid of the reacted leachate. Figure 1 and Figure 7 The thickener 400 is provided with a slurry outlet 420 and a supernatant outlet 410, wherein the supernatant outlet 410 is located at the upper portion of the thickener 400 and the slurry outlet 420 is located at the bottom of the thickener 400. The hydrated iron oxide (FeOOH) formed after the leachate reacts is precipitated to the bottom of the thickener 400 and discharged from the slurry outlet 420, while the supernatant from which the iron has been removed is discharged through the supernatant outlet 410.

[0106] In some embodiments, the leachate iron removal device further includes a seed pipe 150, the slurry outlet 420 of the thickener 400 is connected to the inlet end of the seed pipe 150, and the outlet end of the seed pipe 150 is connected to the first reaction tank 300 of the leachate iron removal device. In this way, the underflow slurry concentrated by the thickener 400 can be returned to the first reaction tank 300 as a seed, so that the iron slag grains in the first reaction tank 300 grow larger, which can improve the precipitation efficiency of iron ions, improve the iron slag filtering performance, and solve the problem of difficult iron slag filtering to a certain extent.

[0107] In some embodiments, an eighth flowmeter 152 and an eighth regulating valve 151 are provided on the seed pipe 150. The eighth regulating valve 151 is used to adjust the flow in the seed pipe 150. By adjusting the opening size of the eighth regulating valve 151, the seed flow entering the first reaction tank 300 can be adjusted. The eighth flowmeter 152 is used to detect the flow in the seed pipe 150 to facilitate the operator to adjust the flow.

[0108] In some embodiments, reference Figure 1 and Figure 8 The leachate iron removal device further includes a supernatant storage tank 700 , the supernatant outlet 410 is connected to the inlet end of the supernatant storage tank 700 , and the supernatant storage tank 700 can collect and store the supernatant.

[0109] In some embodiments, a first sampling port 613 is provided at the inlet end of the thickener 400 , and a second sampling port 440 is provided at the slurry outlet 420 . Operators can sample and test the material entering the thickener 400 and the material after being concentrated in the thickener 400 through the first sampling port 613 and the second sampling port 440 .

[0110] In some embodiments, a slurry delivery pump 430 is provided at the slurry outlet 420 of the thickener 400 , and the slurry flowing out of the slurry outlet 420 of the thickener 400 is sent to the filter press 800 for further solid-liquid separation under the action of the slurry delivery pump 430 to improve the utilization rate of the leachate.

[0111] In some embodiments, a supernatant delivery pump 710 is provided at the outlet end of the supernatant storage tank 700. After the supernatant is collected, the supernatant is delivered to the fine filtration device 900 for fine filtration under the action of the supernatant delivery pump 710 to improve the quality of the supernatant.

[0112] In some embodiments, the supernatant storage tank 700 is provided with a second liquid level meter 720, which is used to detect the liquid level of the supernatant storage tank 700. When the liquid level in the supernatant storage tank 700 is too high, the operator can use the material in the supernatant storage tank 700 in time to ensure that the supernatant in the thickener 400 can smoothly enter the supernatant storage tank 700.

[0113] In some embodiments, a third sampling port 730 is provided at the outlet end of the supernatant storage tank 700 to facilitate sampling and testing of the supernatant entering the fine filtration device 900 .

[0114] In this embodiment, stirring components are provided in the first reaction tank 300 , the second reaction tank 500 and the third reaction tank 600 , which can stir the materials during the reaction process to improve the reaction efficiency.

[0115] In this embodiment, the entire device adopts a continuous reaction production mode. The first liquid level meter 620, the second liquid level meter 720, the first flow meter 112, the second flow meter 122, the third flow meter 132, the fourth flow meter 142, the fifth flow meter 612, the sixth flow meter 162, the seventh flow meter 172, the eighth flow meter 152, the first regulating valve 111, the second regulating valve 121, the third regulating valve 131, the fourth regulating valve 141, the fifth regulating valve 611, the sixth regulating valve 161, the seventh regulating valve 171, the eighth regulating valve 151, the first thermometer 340, the second thermometer 540, the third thermometer 630, the first pH detection component 330, the second pH detection component 530, the discharge conveying pump 610, the slurry conveying pump 430, the supernatant conveying pump 710 and other electrical components are precisely controlled by a distributed control system (DCS) to ensure that the entire device operates fully automatically and stably, reduce human intervention, and save operating costs.

[0116] The working process of the leaching liquid iron removal device of the utility model is as follows:

[0117] The leachate enters the pipeline mixer 200 through the leachate feed pipe 110, and the hydrogen peroxide enters the pipeline mixer 200 through the hydrogen peroxide feed pipe 120. After the leachate and the hydrogen peroxide are evenly mixed in the pipeline mixer 200, they enter the first reaction tank 300 and react in the first reaction tank 300.

[0118] During the reaction in the first reaction tank 300, the first steam pipe 130 provides steam to the first reaction tank 300 to adjust the temperature in the first reaction tank 300, and the first neutralizer feed pipe 140 provides a neutralizer to the first reaction tank 300 to adjust the pH in the first reaction tank 300. The material after the reaction in the first reaction tank 300 enters the second reaction tank 500 for further reaction, the second steam pipe 160 provides steam to the second reaction tank 500 to adjust the temperature in the second reaction tank 500, and the second intermediate feed pipe provides a neutralizer to the second reaction tank 500 to adjust the pH in the second reaction tank 500. The material after the reaction in the second reaction tank 500 enters the third reaction tank 600 for further reaction, and the material is transported to the thickener 400 under the action of the discharge delivery pump 610.

[0119] The material is concentrated in the thickener 400 and separated into a supernatant and a slurry with iron slag crystals. The supernatant flows from the supernatant outlet 410 of the thickener 400 to the supernatant storage tank 700 for collection, and is transported to the fine filtration device 900 for fine filtration under the action of the supernatant delivery pump 710 for subsequent use. The slurry is discharged from the slurry outlet 420 of the thickener 400, and part of the slurry is sent to the filter press 800 for further solid-liquid separation under the action of the slurry delivery pump 430, and the other part of the slurry returns to the first reaction tank 300 along the seed crystal pipeline 150 for use as a seed crystal.

[0120] Since the leachate iron removal device of the present embodiment is provided with the pipeline mixer 200, the leachate and hydrogen peroxide are mixed in the pipeline mixer 200, and the leachate is oxidized in the pipeline mixer 200. At this time, the temperature of the leachate is not high, and it is fully mixed with the hydrogen peroxide, which can maximize the utilization rate of the hydrogen peroxide and prevent the hydrogen peroxide from volatilizing and escaping excessively, thereby reducing the amount of hydrogen peroxide used and improving production efficiency, and there is no safety risk of hydrogen peroxide siphoning backflow.

[0121] In addition, since the slurry concentrated by the thickener 400 is returned to the first reaction tank 300 for use as a seed crystal, the iron slag grains after the reaction can grow larger, the sedimentation efficiency of iron ions can be increased, the iron slag filtering performance can be improved, the problem of difficulty in iron slag filtering can be solved, and the leaching liquid can be more thoroughly deironed.

[0122] The preferred implementation modes of the present invention are specifically described above, but the present invention is not limited to the described embodiments. Those skilled in the art may make various equivalent modifications or substitutions without violating the spirit of the present invention, and these equivalent modifications or substitutions are all included in the scope defined by the claims of this application.

Claims

1. A leachate iron removal device, characterized in that: include: A feed assembly (100) comprises a leachate feed pipe (110), a hydrogen peroxide feed pipe (120), a first steam pipe (130) and a first neutralizer feed pipe (140); A pipeline mixer (200) is provided with a first inlet (210), a second inlet (220) and a mixing outlet (230), the pipeline mixer (200) being arranged in a vertical direction, the first inlet (210) being arranged on a side wall surface of the pipeline mixer (200) and being located at an upper portion of the pipeline mixer (200), the second inlet (220) being arranged at an upper end of the pipeline mixer (200), the mixing outlet (230) being arranged at a lower end of the pipeline mixer (200), the first inlet (210) being connected to the leachate feed pipe (110), and the second inlet (220) being connected to the hydrogen peroxide feed pipe (120); A first reaction tank (300), wherein the first steam pipe (130), the first neutralizer feed pipe (140) and the mixing outlet (230) are respectively connected to the first reaction tank (300); The thickener (400) is used for solid-liquid separation, and the outlet end of the first reaction tank (300) is connected to the inlet end of the thickener (400).

2. The device for removing iron from the leaching solution according to claim 1, characterized in that: The outlet end of the leachate feed pipe (110) is arranged along the tangent direction of the side wall surface of the pipeline mixer (200).

3. The device for removing iron from the leaching solution according to claim 1, characterized in that: The outlet end of the first steam pipe (130), the outlet end of the first neutralizer feed pipe (140) and the mixed outlet (230) are all located at the upper part of the first reaction tank (300). The leaching liquid iron removal device also includes a first feed pipe (310), the inlet end of the first feed pipe (310) extends to the bottom of the first reaction tank (300), and a first discharge pipe (320) is provided at the upper part of the first feed pipe (310). The outlet end of the first discharge pipe (320) extends out of the first reaction tank (300) and is connected to the inlet end of the thickener (400).

4. The device for removing iron from leaching solution according to claim 1, characterized in that: The leachate feed pipe (110) is provided with a first regulating valve (111), and the first regulating valve (111) is used to control the flow rate of the leachate entering the pipeline mixer (200). The hydrogen peroxide feed pipe (120) is provided with a second regulating valve (121), and the second regulating valve (121) is used to control the flow rate of the hydrogen peroxide entering the pipeline mixer (200).

5. The device for removing iron from leachate according to claim 1, characterized in that: The first reaction tank (300) is provided with a first thermometer (340), and the first thermometer (340) is used to obtain the temperature of the mixed liquid in the first reaction tank (300). The first steam pipe (130) is provided with a third regulating valve (131), and the third regulating valve (131) is configured to control the flow of the first steam pipe (130) according to the detected temperature of the first thermometer (340).

6. The device for removing iron from the leaching solution according to claim 3, characterized in that: The first discharge pipe (320) is provided with a first pH detection component (330), and the first neutralizer feed pipe (140) is provided with a fourth regulating valve (141), and the fourth regulating valve (141) is configured to control the flow of the first neutralizer feed pipe (140) according to the pH detected by the first pH detection component (330).

7. The device for removing iron from leachate according to claim 1, characterized in that: The feed assembly (100) further comprises a second steam pipe (160) and a second neutralizer feed pipe (170), and the leaching solution iron removal device further comprises: a second reaction tank (500) disposed between the first reaction tank (300) and the thickener (400); an outlet end of the first reaction tank (300) is connected to the second reaction tank (500); outlet ends of the second steam pipe (160) and the second neutralizer feed pipe (170) are respectively connected to the second reaction tank (500); and the outlet end of the first reaction tank (300), the outlet end of the second steam pipe (160) and the outlet end of the second neutralizer feed pipe (170) are all located at an upper portion of the second reaction tank (500); A second feeding pipe (510), the inlet end of the second feeding pipe (510) extends into the bottom of the second reaction tank (500), and a second discharge pipe (520) is provided on the upper part of the second feeding pipe (510), and the second discharge pipe (520) extends out of the second reaction tank (500) and is connected to the inlet end of the thickener (400).

8. The device for removing iron from leachate according to claim 7, characterized in that: The leaching solution iron removal device also includes: a third reaction tank (600) disposed between the second reaction tank (500) and the thickener (400); an outlet end of the second discharge pipe (520) is communicated with the third reaction tank (600); the outlet end of the second discharge pipe (520) is located at the upper part of the third reaction tank (600); a first liquid level meter (620) is disposed at the upper end of the third reaction tank (600); the first liquid level meter (620) is used to detect the liquid level in the third reaction tank (600); A discharge conveying pump (610), wherein the inlet end of the discharge conveying pump (610) is connected to the bottom of the third reaction tank (600), and the outlet end of the discharge conveying pump (610) is connected to the thickener (400). A fifth regulating valve (611) is provided between the outlet end of the discharge conveying pump (610) and the thickener (400), and the fifth regulating valve (611) is configured to control the flow rate entering the thickener (400) according to the detected liquid level of the first liquid level meter (620).

9. The device for removing iron from leachate according to claim 1, characterized in that: The leachate iron removal device also includes a seed crystal pipeline (150), and a slurry outlet (420) is provided at the bottom of the thickener (400), and the slurry outlet (420) is connected to the inlet end of the seed crystal pipeline (150), and the outlet end of the seed crystal pipeline (150) is connected to the first reaction tank (300) of the leachate iron removal device.

10. The device for removing iron from leachate according to claim 1, characterized in that: A supernatant liquid outlet (410) is provided at the upper portion of the thickener (400), and the leaching liquid iron removal device further comprises a supernatant liquid storage tank (700), and the supernatant liquid outlet (410) is connected to an inlet end of the supernatant liquid storage tank (700).

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