A method for recovering valuable elements in electrolytic manganese leaching residue

Abstract

This disclosure relates to a method for recovering valuable elements from electrolytic manganese leaching residue. The method includes: feeding electrolytic manganese leaching residue slurry into a leaching tank and mixing it with sodium cyanide solution for leaching treatment to obtain a leaching slurry; introducing the leaching slurry and sodium cyanide solution into an adsorption unit and mixing it with activated carbon for adsorption treatment to obtain mixed tailings and mixed gold-loaded carbon; the adsorption unit includes multiple adsorption tanks arranged in series; introducing the leaching slurry from a first-stage adsorption tank into the adsorption unit, obtaining mixed tailings from the last-stage adsorption tank; introducing activated carbon from the last-stage adsorption tank into the adsorption unit, obtaining mixed gold-loaded carbon from the first-stage adsorption tank; subjecting the mixed gold-loaded carbon to a first screening to obtain gold-loaded carbon and first gold-loaded powdered carbon; and subjecting the mixed tailings to a second screening to obtain second gold-loaded powdered carbon and leaching tailings. Using the method of this disclosure can reduce operational difficulty, improve the recovery rate of valuable elements, and increase the adsorption rate of valuable elements by activated carbon.

Description

Technical Field

[0001] The present disclosure relates to the technical field of valuable element recovery, and in particular, to a method for recovering valuable elements in electrolytic manganese leaching residue. Background Art

[0002] The main components that can be recovered from the polymetallic primary manganese carbonate ore are manganese, gold and silver, which can all be used as objects for comprehensive utilization. Among them, the ore contains 21.16% manganese, 1.84g / t gold, 192g / t silver, 0.59% lead and 0.78% zinc. The leaching residue produced by the electrolytic process to prepare metallic manganese contains a variety of valuable elements such as gold and silver. These valuable elements have great utilization value. If comprehensive recovery can be achieved, it will bring good economic benefits, not only reduce resource waste, but also avoid damage to the ecological environment after these materials are discarded, causing heavy metal pollution.

[0003] In the existing related technologies, this part of leaching residue is difficult to handle, the cost of recovering valuable elements in the leaching residue is high, the process is relatively complicated, and the recovery rate of valuable elements such as gold and silver is low. Summary of the invention

[0004] The purpose of the present invention is to provide a method for recovering valuable elements in electrolytic manganese leaching residue, which is used to solve the problems of high recovery cost, complicated process and low recovery rate of valuable elements such as gold and silver in the prior art.

[0005] In order to achieve the above-mentioned object, the present disclosure provides a method for recovering valuable elements in electrolytic manganese leaching residue, which method comprises: mixing electrolytic manganese leaching residue slurry with sodium cyanide solution in a leaching tank for leaching treatment to obtain leaching slurry; allowing the leaching slurry and sodium cyanide solution to enter a leaching unit and mix with activated carbon for leaching treatment to obtain mixed tailings and mixed gold-loaded carbon; the leaching unit comprises a plurality of leaching tanks arranged in series; allowing the leaching slurry to enter the leaching unit from a first-stage leaching tank, and obtaining the mixed tailings from a last-stage leaching tank; the activated carbon enters the leaching unit from the last-stage leaching tank, and obtaining the mixed gold-loaded carbon from the first-stage leaching tank; subjecting the mixed gold-loaded carbon to a first screening to obtain gold-loaded carbon and a first gold-loaded powdered carbon, and subjecting the mixed tailings to a second screening to obtain a second gold-loaded powdered carbon and leaching tailings.

[0006] Optionally, the solid content of the electrolytic manganese leaching slurry is 35-45% by weight.

[0007] Optionally, the method further comprises: subjecting the electrolytic manganese leaching residue to ball milling to obtain fine slurry powder; subjecting the fine slurry powder to sequential classification treatment to obtain slurry to be treated and graded sand settling; subjecting the slurry to be treated to chip removal treatment and thickening treatment to obtain the electrolytic manganese leaching residue slurry.

[0008] Optionally, the grinding fineness of the electrolytic manganese leaching slag is 90.30-93.80 weight % of particles with a particle size below 0.074 mm; the gold content in the electrolytic manganese leaching slag is 2.5-3 g / t, and the silver content is 300-350 g / t; in terms of mass percentage, the manganese content is 6.25-8.12 weight %.

[0009] Optionally, the leaching treatment includes: adjusting the pH value of the electrolytic manganese leaching slurry to 10-11; and adding the sodium cyanide solution to the obtained mixed ore pulp for the leaching treatment for 12-72 hours; the concentration of the sodium cyanide solution is 28-30 weight %.

[0010] Optionally, the leaching treatment conditions include: a temperature of 15 to 35° C., a stirring speed of 25 to 35 r / min, and a weight ratio of the electrolytic manganese leaching residue slurry to the sodium cyanide solution of 1:(2 to 5).

[0011] Optionally, the conditions of the leaching treatment include: a temperature of 15 to 40°C, a time of 15 to 35 hours, a stirring speed of 25 to 35 r / min, a weight ratio of the leaching slurry to the sodium cyanide solution of 1:(1 to 5); a weight ratio of the leaching slurry to the activated carbon of 1:(15 to 25).

[0012] Optionally, a carbon box is provided at the carbon outlet of each of the impregnation and absorption tanks, and a carbon feeding port is provided on the last-stage impregnation and absorption tank; the method further comprises allowing the activated carbon to continuously enter the last-stage impregnation and absorption tank from the carbon feeding port; under the action of compressed air, the activated carbon enters the impregnation and absorption tank of the previous stage through the carbon box; the pressure of the compressed air is 3 to 5 barg, and the gas velocity is 10 to 12 m / s.

[0013] Optionally, the method includes returning the first gold-loaded powdered carbon to the first-stage leaching tank for the leaching treatment.

[0014] Optionally, the gold content in the gold-loaded carbon is 1000-1500 g / t, the silver content is 2000-2800 g / t; and the manganese content is 6.25-8.12 weight % by mass.

[0015] Through the above technical scheme, the electrolytic manganese leaching residue slurry is treated by cyanide leaching method, which can effectively separate and recover valuable elements such as gold and silver in the electrolytic manganese leaching residue, and then activated carbon is used to adsorb the leached valuable elements such as gold and silver; the method disclosed in the present invention can reduce the difficulty of operation, improve the recovery rate of valuable elements and the adsorption rate of activated carbon for gold and silver.

[0016] Other features and advantages of the present disclosure will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] The accompanying drawings are used to provide a further understanding of the present disclosure and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present disclosure but do not constitute a limitation of the present disclosure. In the accompanying drawings:

[0018] Figure 1 It is a process flow chart of a method for recovering valuable elements in electrolytic manganese leaching slag provided by the present invention.

[0019] Description of Reference Numerals

[0020] 1. Ball mill; 2. Hydrocyclone; 3. Thickener; 4. Leaching tank; 5. Immersion absorption tank; 501. First immersion absorption tank; 502. Second immersion absorption tank; 503. Third immersion absorption tank; 504. Fourth immersion absorption tank; 505. Fifth immersion absorption tank; 6. Air compressor; 7. Separation screen; 8. Gold-loaded carbon storage tank; 9. Safety screen; 10. Conveyor; 11. First pump tank; 12. First slurry pump; 13. De-chip screen; 14. Second pump tank; 15. Second slurry pump. DETAILED DESCRIPTION

[0021] The specific implementation of the present disclosure is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described herein is only used to illustrate and explain the present disclosure, and is not used to limit the present disclosure.

[0022] It should be noted that all actions of acquiring signals, information or data in this application are carried out in compliance with the relevant data protection laws and policies of the country where they are located, and with the authorization given by the owner of the corresponding device.

[0023] In the present disclosure, unless otherwise stated, the directional words used, such as "upper" and "lower", generally refer to the upper and lower parts of the device in normal use. In addition, the terms "first" and "second" are used for descriptive purposes only and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, the features defined as "first" and "second" may explicitly or implicitly include one or more of the features. In the description of the present disclosure, the meaning of "plurality" is two or more, unless otherwise clearly and specifically defined.

[0024] like Figure 1As shown, the first aspect of the present disclosure provides a method for recovering valuable elements in electrolytic manganese leaching residue, the method comprising: feeding the electrolytic manganese leaching residue slurry into a leaching tank 4 and mixing it with a sodium cyanide solution for leaching treatment to obtain a leaching slurry; allowing the leaching slurry and the sodium cyanide solution to enter a leaching unit and mix them with activated carbon for leaching treatment to obtain mixed tailings and mixed gold-loaded carbon; the leaching unit comprises a plurality of leaching tanks 5 arranged in series; allowing the leaching slurry to enter the leaching unit from a first-stage leaching tank, and obtaining the mixed tailings from a last-stage leaching tank; the activated carbon enters the leaching unit from the last-stage leaching tank, and obtaining the mixed gold-loaded carbon from the first-stage leaching tank; subjecting the mixed gold-loaded carbon to a first screening to obtain gold-loaded carbon and a first gold-loaded powdered carbon, and subjecting the mixed tailings to a second screening to obtain a second gold-loaded powdered carbon and leaching tailings; wherein the valuable elements include gold and silver.

[0025] Through the above technical solution, the electrolytic manganese leaching residue slurry enters the leaching tank 4 for leaching operation, which can effectively separate and recover valuable elements such as gold and silver in the electrolytic manganese leaching residue; the slurry after leaching operation flows into multiple leaching and absorption tanks 5 in turn, and the tailings produced are sent to the safety screen 9 for second separation to obtain the second gold-loaded powdered carbon and leached tailings; the activated carbon in the leaching and absorption tank 5 absorbs the valuable elements such as gold and silver in the slurry of the leaching operation and passes through the separation screen 7 to obtain the gold-loaded carbon and the first gold-loaded powdered carbon. The method disclosed in the present invention can reduce the difficulty of operation, improve the recovery rate of valuable elements and the adsorption rate of activated carbon to gold and silver.

[0026] In one embodiment, the concentration of the sodium cyanide solution used in the present disclosure is 28 to 30 weight %.

[0027] In one embodiment, the gold content in the electrolytic manganese leaching slag is 2.5-3 g / t, and the silver content is 300-350 g / t; in terms of mass percentage, the manganese content is 6.25-8.12 weight %, the lead content is 0.5-1 weight %, the zinc content is 0.8-2 weight %, and the sulfur content is 7.5-9 weight %.

[0028] In one embodiment, the method further comprises: subjecting the electrolytic manganese leaching residue to ball milling to obtain a fine slurry powder; subjecting the fine slurry powder to sequential classification treatment to obtain a slurry to be treated and a graded sand settling; subjecting the slurry to be treated to a chip removal treatment and a thickening treatment to obtain the electrolytic manganese leaching residue slurry.

[0029] The ball milling process disclosed in the present invention is carried out in a ball mill 1, wherein the ball mill 1 is a conventional choice in the art and has no special requirements in this application. A conveyor 10 for transporting electrolytic manganese leaching residue can be provided at the inlet of the ball mill 1, and the conveyor 10 can be a belt conveyor, and the electrolytic manganese leaching residue is transported to the ball mill 1 for grinding via the belt conveyor.

[0030] In this embodiment, the grinding fineness of the electrolytic manganese leaching slag that has not been ball-milled is -200 mesh, that is, the grinding fineness of the electrolytic manganese leaching slag is 66.05% by weight of the particle size below 0.074 mm; after the electrolytic manganese leaching slag is ball-milled, the particle size of the electrolytic manganese leaching slag can be reduced, for example, the grinding fineness of the electrolytic manganese leaching slag is 90.30-93.80% by weight of the particle size below 0.074 mm. In one embodiment of the present disclosure, the grinding fineness of the electrolytic manganese leaching slag can be 90.30% by weight of the particle size below 0.074 mm, 93.80% by weight of the particle size below 0.074 mm, or 90.30% by weight of the particle size below 0.045 mm. Through ball milling treatment, the leaching rate of valuable elements increases with the increase of grinding fineness, especially the leaching rate of gold and silver increases significantly; considering that the fine grinding index has not been significantly improved, and too fine grinding will greatly increase the grinding cost and make subsequent solid-liquid separation operations difficult, the appropriate grinding fineness is determined to be 93.80% with a particle size below 0.074 mm.

[0031] The classification process of the present disclosure is carried out in the hydrocyclone 2, the chip removal process is carried out in the chip removal screen 13, and the thickening process is carried out in the thickener 3. Among them, a first pump pool 11 can be provided between the ball mill 1 and the hydrocyclone 2, and a first slurry pump 12 can be provided between the first pump pool 11 and the hydrocyclone 2. The slurry flowing out of the ball mill 1 enters the first pump pool 11, and then the milled slurry is pumped into the hydrocyclone 2 for classification by the first slurry pump 12. A chip removal screen 13 for removing impurities from the slurry can be provided between the hydrocyclone 2 and the thickener 3. The slurry overflowing after classification by the hydrocyclone 2 is firstly removed by the chip removal screen 13, and then enters the high-efficiency thickener 3 for concentration. In addition, a second pump pool 14 is provided at the slurry outlet of the thickener 3, and a second slurry pump 15 can be provided at the outlet of the second pump pool 14. The slurry concentrated by the thickener 3 enters the second pump pool 14, and then the concentrated slurry is pumped into the leaching tank 4 by the second slurry pump 15 for leaching operation.

[0032] In one embodiment, the solid content of the electrolytic manganese leaching residue slurry obtained after the concentration treatment is 35-45% by weight. In this embodiment, by concentrating the electrolytic manganese leaching residue slurry, the effects of the subsequent leaching treatment and the leaching absorption treatment can be improved.

[0033] In one embodiment, the leaching treatment includes: allowing the electrolytic manganese leaching residue slurry to enter the leaching tank 4 and mix with lime for 2 to 4 hours, preferably 2 to 3 hours; adjusting the pH value of the electrolytic manganese leaching residue slurry to 10 to 11; and adding the sodium cyanide solution to the obtained mixed ore pulp for leaching treatment for 12 to 72 hours, preferably 20 to 48 hours; the conditions of the leaching treatment include: a temperature of 15 to 35°C, preferably 20 to 30°C; a stirring speed of 25 to 35 r / min, preferably 27.2 to 31 r / min; a weight ratio of the electrolytic manganese leaching residue slurry to the lime is 1: (2 to 5), preferably 1: (2 to 4); a weight ratio of the electrolytic manganese leaching residue slurry to the sodium cyanide solution is 1: (2 to 5), preferably 1: (2 to 4).

[0034] The leaching unit described in the present disclosure includes a plurality of leaching tanks 5 connected in sequence to the downstream of the leaching tank 4. For example, in a specific embodiment of the present disclosure, the number of the leaching tanks 5 can be five, including a first leaching tank 501, a second leaching tank 502, a third leaching tank 503, a fourth leaching tank 504 and a fifth leaching tank 505 connected in sequence to the downstream of the leaching tank 4.

[0035] In a further embodiment, the leaching tank 4, the first leaching and absorption tank 501, the second leaching and absorption tank 502, and the third leaching and absorption tank 503 may respectively have a drug inlet for adding sodium cyanide solution, and the sodium cyanide solution is selected as the leaching agent to extract minerals such as gold and silver from the electrolytic manganese leaching residue. In the embodiment of the present disclosure, it is only necessary to add the sodium cyanide solution to the leaching tank 4 and the first three leaching and absorption tanks 5, and the number of leaching and absorption tanks 5 to which the drug needs to be added can be adjusted according to the actual dosage. It should be noted that the number of leaching and absorption tanks 5 is not limited here.

[0036] Each immersion and absorption tank 5 of the present disclosure can be provided with a carbon adding port to add activated carbon for immersion and absorption. The preferred arrangement is to further provide a carbon adding port on the last stage of the immersion and absorption tank 5, and further provide a carbon string box at the carbon outlet of each immersion and absorption tank 5.

[0037] In one embodiment, the method further includes allowing the activated carbon to continuously enter the last-stage immersion and absorption tank from the carbon feeding port; under the action of compressed air, the activated carbon enters the previous-stage immersion and absorption tank through the carbon string box.

[0038] In one embodiment, compressed air is sent into the leaching tank 4 and the plurality of leaching and absorption tanks 5 through an air compressor 6; the leaching and absorption tank 5 is also provided with an air inlet for connecting to the air compressor 6, so that high-pressure wind can blow the activated carbon from the last stage leaching and absorption tank to the first stage leaching and absorption tank. In this way, the activated carbon can be in countercurrent contact with the leached slurry, thereby further enhancing the effect of the leaching and absorption treatment. The pressure of the compressed air is 3 to 5 barg, and the air velocity is 10 to 12 m / s.

[0039] The air compressor 6 used in the present disclosure is a conventional choice in the art, and this application does not make any special requirements. For example, the air compressor 6 can be a screw air compressor.

[0040] In one embodiment, the conditions of the leaching treatment include: a temperature of 15 to 40°C, preferably 15 to 30°C; a time of 15 to 35 hours, preferably 15 to 25 hours; a stirring speed of 25 to 35 r / min, preferably 27.2 to 31 r / min; a weight ratio of the leaching slurry to the sodium cyanide solution of 1:(1 to 5), preferably 1:(1 to 4); a weight ratio of the leaching slurry to the activated carbon of 1:(15 to 25), preferably 1:(16 to 20).

[0041] In the above-mentioned embodiment, by limiting the method and conditions of the leaching treatment, the activated carbon can better adsorb valuable elements such as gold and silver, thereby further improving the recovery rate of the valuable elements and the adsorption rate of the activated carbon for the valuable elements.

[0042] In one embodiment, after the slurry is separated by the separation screen 7, the water screened out from the under-screen outlet and the first gold-loaded powdered carbon are returned to the leaching tank 5 for the leaching treatment, and the upstream leaching tank 5 close to the leaching tank 4 is preferentially selected to continue the operation, and the gold-loaded carbon screened out from the upper-screen outlet enters the gold-loaded carbon storage tank 8 for desorption electrolysis (path a) to generate finished gold.

[0043] In one embodiment, the gold-loaded powdered carbon produced in each operation link is concentrated through a safety screen 9, and then effectively recovered and sold directly separately (path c), so as to prevent the gold-loaded powdered carbon from flowing away with the tailings and causing metal loss, and the remaining screened tailings are discharged into the tailings pond (path b).

[0044] In one embodiment, the gold content in the gold-loaded carbon is 1000-1500 g / t, preferably 1200-1500 g / t; the silver content is 2000-2800 g / t, preferably 2500-2800 g / t; and the manganese content is 6.25-8.12 wt % by mass.

[0045] In one embodiment, if Figure 1As shown, the method for recovering valuable elements in electrolytic manganese leaching residue includes:

[0046] The electrolytic manganese leaching residue is sent to a ball mill 1 for ball milling, the ball-milled powder is graded by a hydrocyclone 2, and the obtained slurry is sent to a thickener 3 for thickening to obtain the electrolytic manganese leaching residue slurry with a solid content of 35-45% by weight.

[0047] The electrolytic manganese leaching residue slurry is put into the leaching tank 4 and mixed with lime, and the pH value of the electrolytic manganese leaching residue slurry is adjusted to 10-11; sodium cyanide solution is added to the mixed ore pulp for leaching treatment to obtain leaching slurry; the leaching treatment conditions include: temperature of 20-30°C and stirring speed of 27.2-31r / min.

[0048] The leached slurry and the sodium cyanide solution are introduced into the leaching unit to be mixed with the activated carbon for leaching treatment, so as to obtain mixed tailings and mixed gold-loaded carbon; the leaching unit comprises a plurality of leaching tanks 5 arranged in series; the leached slurry is introduced into the leaching unit from the first-stage leaching tank, and the mixed tailings are obtained from the last-stage leaching tank; the activated carbon is introduced into the leaching unit from the last-stage leaching tank, and the mixed gold-loaded carbon is obtained from the first-stage leaching tank;

[0049] The mixed gold-loaded carbon is subjected to a first screening through a separation screen 7 to obtain gold-loaded carbon and a first gold-loaded powdered carbon, and the mixed tailings are subjected to a second screening through a safety screen 9 to obtain a second gold-loaded powdered carbon and leached tailings.

[0050] The present disclosure is further illustrated by examples below, but the present disclosure is not limited thereto. The reagents, instruments and equipment involved in the following examples of the present disclosure can be purchased from the market unless otherwise specified, wherein the concentration of the sodium cyanide solution is 30% by weight. In the examples of the present disclosure, the gold content of the electrolytic manganese leaching residue involved is 2.97 g / t, the silver content is 316 g / t, the manganese content is 6.58% by mass, the lead content is 0.85%, the zinc content is 1.23%, and the sulfur content is 8.13%.

[0051] Example 1

[0052] The electrolytic manganese leaching residue is sent to a ball mill 1 for ball milling treatment, the ball-milled powder is graded by a hydrocyclone 2, and the obtained slurry is sent to a thickener 3 for thickening treatment to obtain the electrolytic manganese leaching residue slurry with a solid content of 40 weight%, wherein the grinding fineness of the electrolytic manganese leaching residue is less than 0.074 mm and the content is 93.80 weight%.

[0053] 1 t of electrolytic manganese leaching residue slurry is put into the leaching tank 4 and mixed with 9 kg / t of lime for 2.06 hours, and the pH value of the slurry is adjusted to 10.5; 3 kg / t of sodium cyanide solution is added to the mixed slurry for leaching treatment for 48 hours to obtain a leached slurry; the leaching treatment conditions include: a temperature of 20-30°C and a stirring speed of 30 r / min.

[0054] 2.5t of leached slurry and 3kg / t of sodium cyanide solution are sequentially passed through the first absorption tank 501, the second absorption tank 502, the third absorption tank 503, the fourth absorption tank 504 and the fifth absorption tank 505, and mixed with 18kg / t of activated carbon which sequentially passes through the fifth absorption tank 505, the fourth absorption tank 504, the third absorption tank 503, the second absorption tank 502 and the first absorption tank 501 to obtain mixed tailings mixed gold-loaded carbon and mixed gold-loaded carbon mixed tailings; the conditions of the leaching treatment include: temperature of 20°C, time of 22h, and stirring speed of 28.5r / min.

[0055] The mixed gold-loaded carbon is subjected to a first screening through a separation screen 7 to obtain the gold-loaded carbon and the first gold-loaded powdered carbon, and the mixed tailings are subjected to a second screening through a safety screen 9 to obtain the second gold-loaded powdered carbon and the leached tailings;

[0056] The properties of the leaching slurry obtained after treatment by the method disclosed in the present invention are shown in Table 1, and the properties of the remaining tail liquid and the gold-loaded carbon are shown in Table 1.

[0057] Example 2

[0058] The method for recovering valuable elements in electrolytic manganese leaching residue is the same as that in Example 1, except that the grinding fineness of the electrolytic manganese leaching residue is less than 0.074 mm and the content is 66.05% by weight. The properties of the leached slurry obtained after treatment by the method disclosed in the present invention are shown in Table 1, and the properties of the remaining tail liquid and the gold-loaded carbon are shown in Table 2.

[0059] Example 3

[0060] The method for recovering valuable elements in electrolytic manganese leaching residue is the same as in Example 1, except that 2 kg / t of sodium cyanide solution is added to the mixed slurry for leaching treatment for 48 hours to obtain a leaching slurry. The properties of the leaching slurry obtained after treatment by the method disclosed in the present invention are shown in Table 1, and the properties of the remaining tailings and gold-loaded carbon are shown in Table 2.

[0061] Example 4

[0062] The method for recovering valuable elements in electrolytic manganese leaching residue is the same as in Example 1, except that 3 kg / t of sodium cyanide solution is added to the mixed slurry for leaching treatment for 12 hours to obtain a leaching slurry. The properties of the leaching slurry obtained after treatment by the method disclosed in the present invention are shown in Table 1, and the properties of the remaining tailings and gold-loaded carbon are shown in Table 2.

[0063] Comparative Example 1

[0064] The method for recovering valuable elements in electrolytic manganese leaching residue is the same as that in Example 1, except that the activated carbon is sequentially mixed and leached in the first leaching tank 501, the second leaching tank 502, the third leaching tank 503, the fourth leaching tank 504 and the fifth leaching tank 505. The properties of the leached slurry obtained after treatment by the method disclosed in the present invention are shown in Table 1, and the properties of the remaining tail liquid and the gold-loaded carbon are shown in Table 2.

[0065] Table 1 Properties and leaching rates of leaching products

[0066]

[0067]

[0068] Table 2 Residual tail liquid, adsorption rate of leaching treatment and properties of gold-loaded carbon

[0069]

[0070] Among them, the gold grade and silver grade are obtained by analysis using a PerkinElmer AAnalyst400 atomic absorption spectrometer. The calculation methods for the leaching rate of the leaching slurry in Table 1 and the recovery rate of the valuable elements of the gold-bearing carbon in Table 1 are as follows:

[0071]

[0072]

[0073] According to Table 1, by comparing the data in Examples 1 to 4 with Comparative Example 1, it can be seen that the recovery method disclosed in the present invention can reduce the difficulty of operation and improve the recovery rate of valuable elements. By comparing the data in Example 1 and Comparative Example 1, it can be seen that the countercurrent contact between the leaching slurry and the activated carbon can improve the adsorption rate of the activated carbon to the valuable elements. By comparing the data in Example 1 and Example 2, it can be seen that the grinding fineness of the electrolytic manganese leaching slag is 90.30-93.80% by weight of the particle size below 0.074 mm, which can improve the recovery rate of valuable elements. By comparing the data in Example 1 and Example 3, it can be seen that when the weight ratio of the electrolytic manganese leaching slag slurry to the sodium cyanide solution is 1: (2-4), the recovery rate of valuable elements can be further improved. By comparing the data in Example 1 and Example 4, it can be seen that when the leaching time is 20-48h, the recovery rate of valuable elements can be further improved.

[0074] The preferred embodiments of the present disclosure are described in detail above in conjunction with the accompanying drawings; however, the present disclosure is not limited to the specific details in the above embodiments. Within the technical concept of the present disclosure, a variety of simple modifications can be made to the technical solution of the present disclosure, and these simple modifications all fall within the protection scope of the present disclosure.

[0075] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present disclosure will not further describe various possible combinations.

[0076] In addition, various embodiments of the present disclosure may be arbitrarily combined, and as long as they do not violate the concept of the present disclosure, they should also be regarded as the contents disclosed by the present disclosure.

Claims

1. A method for recovering valuable elements in electrolytic manganese leaching residue, characterized in that: The method includes: The electrolytic manganese leaching residue slurry is sent into a leaching tank and mixed with a sodium cyanide solution for leaching treatment to obtain a leaching slurry; The leached slurry and the sodium cyanide solution are introduced into the leaching unit to be mixed with the activated carbon for leaching treatment, so as to obtain mixed tailings and mixed gold-loaded carbon; the leaching unit comprises a plurality of leaching tanks arranged in series; the leached slurry is introduced into the leaching unit from the first-stage leaching tank, and the mixed tailings are obtained from the last-stage leaching tank; the activated carbon is introduced into the leaching unit from the last-stage leaching tank, and the mixed gold-loaded carbon is obtained from the first-stage leaching tank; The mixed gold-loaded carbon is subjected to a first screening to obtain the gold-loaded carbon and the first gold-loaded powdered carbon, and the mixed tailings are subjected to a second screening to obtain the second gold-loaded powdered carbon and the leached tailings; Each of the immersion and absorption tanks is also provided with a charcoal box at the charcoal outlet, and the last level of the immersion and absorption tank is also provided with a charcoal adding port; The method further includes allowing the activated carbon to continuously enter the last-stage immersion and absorption tank from the carbon feeding port; under the action of compressed air, the activated carbon enters the upper-stage immersion and absorption tank through the carbon string box; The method further comprises ball milling the electrolytic manganese leaching residue to obtain slurry fine powder; The slurry fine powder is subjected to classification treatment in sequence to obtain slurry to be treated and graded sand settling; The slurry to be treated is subjected to a chip removal treatment and a thickening treatment to obtain the electrolytic manganese leaching slag slurry; The grinding fineness of the electrolytic manganese leaching slag is 90.30-93.80% by weight of the particle size below 0.074 mm; the gold content in the electrolytic manganese leaching slag is 2.5-3 g / t, and the silver content is 300-350 g / t; in terms of mass percentage, the manganese content is 6.25-8.12% by weight; The solid content of the electrolytic manganese leaching slurry is 35-45% by weight; The concentration of the sodium cyanide solution is 28-30% by weight; The leaching treatment conditions include: a temperature of 15-35°C, a stirring speed of 25-35 r / min, and a weight ratio of the electrolytic manganese leaching residue slurry to the sodium cyanide solution of 1:(2-5); The conditions of the leaching treatment include: a temperature of 15-40°C, a time of 15-35h, a stirring speed of 25-35r / min, a weight ratio of the leaching slurry to the sodium cyanide solution of 1:(1-5); a weight ratio of the leaching slurry to the activated carbon of 1:(15-25).

2. The recycling method according to claim 1, characterized in that: The leaching treatment includes: adjusting the pH value of the electrolytic manganese leaching residue slurry to 10-11, and adding the sodium cyanide solution to the obtained mixed ore pulp to carry out the leaching treatment for 12-72 hours.

3. The recycling method according to claim 1, characterized in that: The pressure of the compressed air is 3-5 barg, and the air velocity is 10-12 m / s.

4. The recycling method according to claim 1, characterized in that: The method comprises returning the first gold-loaded powdered carbon to the first-stage leaching tank for the leaching treatment.

5. The recycling method according to claim 1, characterized in that: The gold content of the gold-loaded carbon is 1000-1500 g / t, the silver content is 2000-2800 g / t; and the manganese content is 6.25-8.12 weight % by mass.

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