A system for recovering valuable components from high-copper-iron complex gold extraction carbon calcination slag

Abstract

The utility model relates to a system of valuable component recovery from high copper iron complex gold extraction carbon calcination slag, including ball mill, the discharge outlet of ball mill is connected with the feed inlet of hydrocyclone through the ore pulp pump, the sand trap of hydrocyclone is connected with the feed inlet of ball mill, the overflow of hydrocyclone is connected with the feed inlet of flotation system, the concentrate of flotation system is connected with calcination ash system, the tailing of flotation system and the slag outlet of calcination ash system are connected with copper leaching tank, and copper leaching tank is connected with copper recovery system and 1# cyanide leaching tank respectively through 1# filter, and 1# cyanide leaching tank outlet is connected with 2# filter, 2# cyanide leaching tank and 3# filter in proper order. The utility model is cleverly combined with the equipment such as grinding classification closed circuit system, flotation system, copper leaching tank, two stage cyanide leaching and copper recovery system, and the efficient comprehensive recovery of gold, silver and copper in high copper iron complex gold extraction carbon calcination slag is realized.

Description

Technical Field

[0001] This utility model belongs to the field of secondary recycling technology of precious metal materials, specifically relating to a system for recovering valuable components from complex gold extraction charcoal roasting slag with high copper and iron content. Background Technology

[0002] In gold ore recovery, the carbon-in-pulp (CIP) process is widely used due to its highly efficient gold and silver adsorption capacity. However, during long-term operation, the activated carbon in the CIP continuously wears down, producing carbon fragments that are enriched with large amounts of precious metals such as gold and silver. Currently, companies typically collect these carbon fragments, roast and ashed them, and then return them to the original process for secondary gold and silver recovery. However, during the roasting and ashing process, on the one hand, some activated carbon is difficult to burn completely; on the other hand, gold ore resources often contain high levels of harmful elements such as copper and iron, which are enriched in the carbon fragments, making the return of the roasted and ashed material to the original process technically challenging. Currently, most gold-bearing materials are mainly stored, failing to recover valuable components in a timely and effective manner, leading to inventory backlog and capital tied up, seriously affecting the economic benefits of enterprises.

[0003] In the secondary recovery of gold and silver from scrap materials, there are currently two main technical routes: pyrometallurgy and hydrometallurgy. While pyrometallurgical smelting has advantages such as mature processes, fast reaction speeds, and high gold and silver recovery efficiency, and is widely used in the processing of high-grade gold concentrates, gold-bearing materials, and enriched intermediate products, it faces several technical challenges when processing high-grade gold and silver materials containing high levels of impurities such as copper and iron. Copper forms low-melting-point alloys with gold and silver, interfering with the separation of precious metals and increasing flux usage; iron increases slag viscosity, making the molten system unstable and increasing the loss rate of gold and silver inclusions, severely impacting recovery efficiency. Furthermore, the pyrometallurgical process has strict requirements for raw material particle size, reducing agent ratios, and smelting atmosphere, resulting in poor adaptability. Especially for materials with high silver content, silver is easily lost in the form of volatiles or dust, leading to low recovery rates and significant resource waste. Simultaneously, pollutants such as sulfur dioxide, heavy metal dust, and nitrogen oxides generated during the smelting process require costly environmental protection facilities, increasing the operational burden and hindering the achievement of green metallurgy and carbon reduction goals.

[0004] While existing conventional wet gold and silver recovery processes are simple to operate and have low energy consumption, they suffer from low gold and silver recovery rates and poor adaptability when processing complex gold extraction slag from high-copper and high-iron charcoal roasting and ashing. On the one hand, residual powdered carbon in the ashing slag can re-adsorb leached gold and silver; on the other hand, high copper content during cyanide leaching not only increases cyanide consumption but also generates cuprous cyanide precipitate, which covers the gold and silver surfaces and hinders leaching. Furthermore, activated carbon has a relatively weak adsorption capacity for silver, and directly using carbon leaching in high-gold and silver materials can easily lead to significant silver loss.

[0005] Therefore, there is an urgent need to develop a simple and adaptable recycling system to recover valuable components from the complex gold extraction charcoal roasting and ashing slag of high copper and iron, in order to reduce production costs, improve the overall recovery rate, promote the effective comprehensive utilization of resources, alleviate the inventory pressure of enterprises, and increase the technical and economic benefits of enterprises. Utility Model Content

[0006] This invention provides a system for recovering valuable components from complex gold-extraction charcoal roasting slag with high copper and iron content. Through reasonable equipment matching and connection, it achieves efficient and comprehensive recovery of valuable components such as gold, silver and copper.

[0007] The specific technical solution is as follows:

[0008] A system for recovering valuable components from complex high-copper-iron gold-extraction charcoal roasting slag includes a ball mill. The outlet of the ball mill is connected to the inlet of a hydrocyclone via a slurry pump. The sedimentation port of the hydrocyclone is connected to the inlet of the ball mill. The overflow port of the hydrocyclone is connected to the inlet of a flotation system. The concentrate port of the flotation system is connected to a roasting and ashing system. The tailings port of the flotation system and the slag outlet of the roasting and ashing system are both connected to a copper leaching tank. The copper leaching tank is connected to a copper recovery system and a cyanide leaching tank via a No. 1 filter. The outlet of the No. 1 cyanide leaching tank is sequentially connected to a No. 2 filter, a No. 2 cyanide leaching tank, and a No. 3 filter.

[0009] Furthermore, preferably, the filtrate outlet of the No. 1 filter is connected to the copper recovery system, and the filter residue outlet is connected to the No. 1 cyanide leaching tank.

[0010] Furthermore, preferably, the filter residue inlet of the No. 2 filter is connected to the No. 2 cyanide leaching tank.

[0011] Furthermore, preferably, the distillate from the copper recovery system is returned to the copper leaching tank via a pipeline.

[0012] The beneficial effects of this invention are as follows: This invention achieves efficient and comprehensive recovery of gold, silver, and copper from complex gold-extraction charcoal roasting slag containing high copper and iron content through a clever combination of equipment such as a grinding and classification closed-circuit system, a flotation system, a copper leaching tank, a two-stage cyanide leaching system, and a copper recovery system. The system is simple in equipment, has a short process flow, low energy consumption, is environmentally friendly, and highly adaptable. It is not only suitable for processing complex gold-extraction charcoal roasting slag containing high copper and iron content, but can also be applied to the processing of other gold-containing materials with high gold and silver grades and impurities. This solves the problem of capital tied up in inventory for enterprises, improving their economic and social benefits. Specific beneficial effects are as follows:

[0013] (1) This utility model can not only significantly improve the recovery rate of gold and silver, but also take into account the efficient recovery of copper. The test results show that the gold recovery rate can reach about 95%, the silver recovery rate can reach about 84%, and the copper recovery rate can reach about 95%. Compared with the traditional direct cyanide leaching process, the gold recovery rate is increased by about 55% and the silver recovery rate is increased by about 38%.

[0014] (2) This invention sets up a flotation system before the roasting and ashing system, which can pre-flot the activated carbon that has not been fully ashed, and then perform secondary roasting on it, effectively avoiding the problem of secondary sintering caused by the direct roasting of all the crushed carbon slag in the traditional process. In addition, the fine activated carbon particles can also be pre-flotted at the same time, which can prevent them from being directly mixed into the cyanidation process and reverse adsorbing gold and silver in the solution, resulting in a significant decrease in the gold and silver recovery rate.

[0015] (4) This utility model uses a two-stage cyanide leaching system and appropriate concentrations of cyanide and oxidant to quickly leach exposed free gold and some easily leached silver under low cyanide concentration conditions. Then, with the addition of cyanide and oxidant, it can deeply dissolve gold and silver with more complex structures or tighter encapsulation, solving the problem of low silver recovery rate, effectively improving the overall gold and silver recovery rate, and reducing the interference of residual impurities by changing the solution, avoiding waste of cyanide and changes in the gold and silver complexation balance.

[0016] (5) This utility model reduces equipment investment and energy consumption by optimizing the process system, while improving resource recovery rate and reducing production costs. In addition, the recycling of ammonia water through the distillate circulation design further reduces the consumption of chemical reagents in the production process. Attached Figure Description

[0017] Figure 1 This is a diagram illustrating the equipment for recovering valuable components from complex high-copper-iron gold-extraction charcoal roasting slag according to this utility model.

[0018] In the diagram: 1-Ball mill; 2-Slurry pump; 3-Hydrocyclone; 4-Flotation system; 5-Roasting and ashing system; 6-Copper leaching tank; 7-Filter #1; 8-Copper recovery system; 9-Cyanide leaching tank #1; 10-Filter #2; 11-Cyanide leaching tank #2; 12-Filter #3. Detailed Implementation

[0019] To make the technical problems and solutions solved by this utility model clearer, the present utility model will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely for explaining the present utility model and are not intended to limit the present utility model.

[0020] In the description of this utility model, it should be understood that the terms "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this utility model and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this utility model.

[0021] In the description of this utility model, it should also be noted that, unless otherwise explicitly specified and limited, the terms "set," "install," and "connect" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0022] like Figure 1 As shown, this embodiment provides a system for recovering valuable components from complex gold-extraction crushed carbon roasting slag with high copper and iron content. The system includes a ball mill 1, the outlet of which is connected to the inlet of a hydrocyclone 3 via a slurry pump 2, and the underflow outlet of the hydrocyclone 3 is connected to the inlet of the ball mill 1. This part constitutes a closed-loop grinding and classification system.

[0023] The overflow port of hydrocyclone 3 is connected to the feed port of flotation system 4. The concentrate port of flotation system 4 is connected to roasting and ashing system 5. The tailings port of flotation system 4 and the slag outlet of roasting and ashing system 5 are both connected to copper leaching tank 6. Copper leaching tank 6 is connected to copper recovery system 8 and cyanide leaching tank 9 via filter #1 7. The filtrate port of filter #1 7 is connected to copper recovery system 8, and the filter residue port is connected to cyanide leaching tank 9. The outlet of cyanide leaching tank 9 is sequentially connected to filter #2 10, cyanide leaching tank 11, and filter #3 12. The filter residue port of filter #2 10 is connected to cyanide leaching tank 11.

[0024] In a preferred embodiment, the distillate from the copper recovery system 8 is returned to the copper leaching tank 6 via a pipeline for recycling.

[0025] It should be noted that the above-mentioned equipment are all existing equipment, and this application only relates to the application of these existing equipment, and does not involve any improvement of their structure.

[0026] The specific working principle of the above system for recovering low-grade complex oxidized lead-zinc-gold-silver ores is as follows:

[0027] (1) Grinding and classification: The material to be processed is fed to ball mill 1 for fine grinding. After fine grinding until the material has a particle size of -0.074mm of 70% to 80%, it is fed to hydrocyclone 3 for classification by slurry pump 2.

[0028] (2) Flotation decarbonization: The material classified in step (1) is transported to the flotation system 4, starch is added and stirred evenly, and then kerosene or light diesel oil is added for roughing to obtain carbon-containing concentrate and tailings. The carbon-containing concentrate is returned to the roasting and ashing system 5 for roasting again to obtain concentrate roasting residue.

[0029] (3) Selective leaching of copper: The tailings and concentrate roasting residue from step (2) are sent into the copper leaching tank 6, and ammonia-chlorine solution is added for pre-leaching. After the leaching operation is completed, copper-containing leaching solution and leaching residue are obtained by filtration through filter #1 7. The copper-containing leaching solution enters the copper recovery system 8, and the leaching residue enters the cyanide leaching tank #1 9.

[0030] (4) First-stage preferential leaching: After the leaching residue from step (3) enters the 1# cyanide leaching tank 9, sodium cyanide is added for first-stage preferential leaching. After the leaching operation is completed, it is filtered by the 2# filter machine 10 to obtain gold and silver precious liquid and first-stage leaching residue. The first-stage leaching residue is then transferred to the 2# cyanide leaching tank 11.

[0031] (5) Second-stage enhanced leaching: After the first-stage leaching residue from step (4) enters the No. 2 cyanide leaching tank 11, sodium cyanide is added for second-stage enhanced leaching. After the leaching operation is completed, the gold and silver precious liquid and the second-stage leaching residue are obtained by filtration through the No. 3 filter machine 12.

[0032] (6) Recovery of elemental copper: The copper-containing leaching solution from step (3) is distilled after entering the copper recovery system 8. The copper in the leaching solution is precipitated as copper hydroxide, and the ammonia water produced by distillation is returned to the copper leaching tank 6 for recycling through pipeline.

[0033] Application Example 1

[0034] Raw material 1#: A complex gold-extracting crushed carbon roasting slag with high copper and iron content, the main elements and contents are as follows: gold 410.1g / t, silver 2900.5g / t, copper 5.1% (of which 70.5% is bound copper), carbon 7.3%, iron 10.1%, and calcium 30.2%.

[0035] like Figure 1 As shown, the specific steps for recovering raw ore #1 using the system described in this utility model are as follows:

[0036] (1) Grinding and classification: Raw material #1 is fed to ball mill 1 for fine grinding. After grinding, the proportion of -0.074mm particles in the material is 70% to 80%. Then, it is pumped by slurry pump 2 to hydrocyclone 3 for classification. During this process, the grinding concentration is controlled at 75% to 85%, the classification concentration is 50% to 55%, and the concentration of the classified slurry is 20% to 25%.

[0037] (2) Flotation decarbonization: The material classified in step (1) is transported to flotation system 4, 50 g / t starch is added and stirred evenly, and then 800 g / t kerosene or light diesel oil is added for roughing to obtain carbon-containing concentrate and tailings. The carbon-containing concentrate is returned to roasting and ashing system 5 for re-roasting to obtain concentrate roasting slag. 80 g / t frother 2# oil is added during roughing, and the roughing time is 6-10 min.

[0038] (3) Selective leaching of copper: The tailings and concentrate roasting residue from step (2) are fed into copper leaching tank 6, and ammonia-chlorine solution is added for pre-leaching. After the leaching operation is completed, the copper-containing leaching solution and leaching residue are obtained by filtration through filter #1 7. The copper-containing leaching solution enters the copper recovery system 8, and the leaching residue enters cyanide leaching tank #1 9. During this process, the ammonia concentration (ammonia water added) in the solution is 1.5-2 mol / L, and the chloride concentration is 1.5-2 mol / L. - The concentration (with added sodium chloride) is 1-1.5 mol / L, the pre-soaking time is 6 hours, the solution pH is controlled at 9-10, and the temperature is controlled at 40-50℃;

[0039] (4) First-stage preferential leaching: After the leaching residue from step (3) enters the No. 1 cyanide leaching tank 9, sodium cyanide is added for first-stage preferential leaching. After the leaching operation is completed, it is filtered by the No. 2 filter 10 to obtain the gold and silver precious solution and the first-stage leaching residue. The first-stage leaching residue is then transferred to the No. 2 cyanide leaching tank 11. During this process, the sodium cyanide concentration is 0.05% to 0.1%, the liquid-solid ratio is 2:1 to 4:1, the pH value is 10.5 to 11.5, and the leaching time is 12 hours.

[0040] (5) Second-stage enhanced leaching: After the first-stage leaching residue from step (4) enters the No. 2 cyanide leaching tank 11, sodium cyanide is added for second-stage enhanced leaching. After the leaching operation is completed, the residue is filtered by the No. 3 filter 12 to obtain the gold and silver precious solution and the second-stage leaching residue. During this process, the sodium cyanide concentration is 0.2% to 0.3%, the pH value is 10.5 to 11.5, the hydrogen peroxide concentration is 0.5% to 1%, the liquid-solid ratio is 3:1 to 5:1, and the leaching time is 30 hours.

[0041] (6) Recovery of elemental copper: The copper-containing leaching solution from step (3) is distilled after entering the copper recovery system 8. The copper in the leaching solution is precipitated as copper hydroxide, and the ammonia water produced by distillation is returned to the copper leaching tank 6 for recycling through pipelines. During this process, the distillation temperature is 70-90℃ and the pH is controlled at 9-10.

[0042] The experimental results obtained were as follows: gold recovery rate reached 94.5%, silver recovery rate reached 85.4%, and copper recovery rate reached 96.3%. Compared with direct cyanide leaching, the gold recovery rate increased by about 55%, the silver recovery rate increased by about 40%, and copper recovery was also taken into account.

[0043] Application Example 2

[0044] Raw material 2#: A complex gold-extracting crushed carbon roasting slag with high copper and iron content, the main elements and contents are as follows: gold 380.56g / t, silver 2500.34g / t, copper 5.6% (of which 80.1% is bound copper), carbon 6.8%, iron 9.8%, and calcium 29.5%.

[0045] The method described in this utility model is applied to raw material #2, and the specific steps are as follows:

[0046] (1) Grinding and classification: Raw material 2# is fed to ball mill 1 for fine grinding. After grinding, the proportion of -0.074mm particles is 70% to 80%. Then, it is pumped by slurry pump 2 to hydrocyclone 3 for classification. During this process, the grinding concentration is controlled at 75% to 85%, the classification concentration is 50% to 55%, and the concentration of the classified slurry is 20% to 25%.

[0047] (2) Flotation decarbonization: The material classified in step (1) is transported to flotation system 4, 100 g / t starch is added and stirred evenly, and then 300 g / t kerosene or light diesel oil is added for roughing to obtain carbon-containing concentrate and tailings. The carbon-containing concentrate is returned to roasting and ashing system 5 for re-roasting to obtain concentrate roasting slag. 100 g / t frother 2# oil is added during roughing, and the roughing time is 6-10 min.

[0048] (3) Selective leaching of copper: The tailings and concentrate roasting residue from step (2) are fed into copper leaching tank 6, and ammonia-chlorine solution is added for pre-leaching. After the leaching operation is completed, the copper-containing leaching solution and leaching residue are obtained by filtration through filter #1 7. The copper-containing leaching solution enters the copper recovery system 8, and the leaching residue enters cyanide leaching tank #1 9. During this process, the ammonia concentration (ammonia water added) in the solution is 1.5-2 mol / L, and the chloride concentration is 1.5-2 mol / L. - The concentration (with added sodium chloride) is 1-1.5 mol / L, the pre-soaking time is 5 hours, the solution pH is controlled at 9-10, and the temperature is controlled at 40-50℃;

[0049] (4) First-stage preferential leaching: After the leaching residue from step (3) enters the No. 1 cyanide leaching tank 9, sodium cyanide is added for first-stage preferential leaching. After the leaching operation is completed, it is filtered by the No. 2 filter 10 to obtain the gold and silver precious solution and the first-stage leaching residue. The first-stage leaching residue is then transferred to the No. 2 cyanide leaching tank 11. During this process, the sodium cyanide concentration is 0.05% to 0.1%, the liquid-solid ratio is 2:1 to 4:1, the pH value is 10.5 to 11.5, and the leaching time is 10 hours.

[0050] (5) Second-stage enhanced leaching: After the first-stage leaching residue from step (4) enters the No. 2 cyanide leaching tank 11, sodium cyanide is added for second-stage enhanced leaching. After the leaching operation is completed, the residue is filtered by the No. 3 filter 12 to obtain the gold and silver precious solution and the second-stage leaching residue. During this process, the sodium cyanide concentration is 0.2% to 0.3%, the pH value is 10.5 to 11.5, the hydrogen peroxide concentration is 0.5% to 1%, the liquid-solid ratio is 3:1 to 5:1, and the leaching time is 24 hours.

[0051] (6) Recovery of elemental copper: The copper-containing leaching solution from step (3) is distilled after entering the copper recovery system 8. The copper in the leaching solution is precipitated as copper hydroxide, and the ammonia water produced by distillation is returned to the copper leaching tank 6 for recycling through pipelines. During this process, the distillation temperature is 70-90℃ and the pH is controlled at 9-10.

[0052] The experimental results obtained were as follows: gold recovery rate reached 95.1%, silver recovery rate reached 84.2%, and copper recovery rate reached 95.4%. Compared with direct cyanide leaching, the gold recovery rate increased by about 54%, the silver recovery rate increased by about 39%, and copper recovery was also taken into account.

[0053] Application Example 3

[0054] Raw material #3: A complex gold-extracting charcoal roasting slag with high copper and iron content, its main elements and contents are as follows: gold 350.67g / t, silver 2789.4g / t, copper 6.7% (of which 75.1% is bound copper), carbon 8.2%, iron 9.5%, and calcium 35%.

[0055] The following are the specific steps for implementing this invention on the complex gold extraction charcoal roasting slag with high copper and iron content:

[0056] (1) Grinding and classification: Raw material #3 is fed to ball mill 1 for fine grinding. After grinding, the proportion of -0.074mm particles in the material is 70% to 80%. Then, it is pumped by slurry pump 2 to hydrocyclone 3 for classification. During this process, the grinding concentration is controlled at 75% to 85%, the classification concentration is 50% to 55%, and the concentration of the classified slurry is 20% to 25%.

[0057] (2) Flotation decarbonization: The material classified in step (1) is transported to flotation system 4, 200 g / t starch is added and stirred evenly, and then 300 g / t kerosene or light diesel oil is added for roughing to obtain carbon-containing concentrate and tailings. The carbon-containing concentrate is returned to roasting and ashing system 5 for re-roasting to obtain concentrate roasting slag. 40 g / t frother 2# oil is added during roughing, and the roughing time is 6-10 min.

[0058] (3) Selective leaching of copper: The tailings and concentrate roasting residue from step (2) are fed into copper leaching tank 6, and ammonia-chlorine solution is added for pre-leaching. After the leaching operation is completed, the copper-containing leaching solution and leaching residue are obtained by filtration through filter #1 7. The copper-containing leaching solution enters the copper recovery system 8, and the leaching residue enters cyanide leaching tank #1 9. During this process, the ammonia concentration (ammonia water added) in the solution is 1.5-2 mol / L, and the chloride concentration is 1.5-2 mol / L. - The concentration (with added sodium chloride) is 1-1.5 mol / L, the pre-soaking time is 4 hours, the solution pH is controlled at 9-10, and the temperature is controlled at 40-50℃;

[0059] (4) First-stage preferential leaching: After the leaching residue from step (3) enters the No. 1 cyanide leaching tank 9, sodium cyanide is added for first-stage preferential leaching. After the leaching operation is completed, it is filtered by the No. 2 filter 10 to obtain the gold and silver precious solution and the first-stage leaching residue. The first-stage leaching residue is then transferred to the No. 2 cyanide leaching tank 11. During this process, the sodium cyanide concentration is 0.05% to 0.1%, the liquid-solid ratio is 2:1 to 4:1, the pH value is 10.5 to 11.5, and the leaching time is 8 hours.

[0060] (5) Second-stage enhanced leaching: After the first-stage leaching residue from step (4) enters the No. 2 cyanide leaching tank 11, sodium cyanide is added for second-stage enhanced leaching. After the leaching operation is completed, the residue is filtered by the No. 3 filter 12 to obtain the gold and silver precious solution and the second-stage leaching residue. During this process, the sodium cyanide concentration is 0.2% to 0.3%, the pH value is 10.5 to 11.5, the hydrogen peroxide concentration is 0.5% to 1%, the liquid-solid ratio is 3:1 to 5:1, and the leaching time is 28 hours.

[0061] (6) Recovery of elemental copper: The copper-containing leaching solution from step (3) is distilled after entering the copper recovery system 8. The copper in the leaching solution is precipitated as copper hydroxide, and the ammonia water produced by distillation is returned to the copper leaching tank 6 for recycling through pipelines. During this process, the distillation temperature is 70-90℃ and the pH is controlled at 9-10.

[0062] The experimental results obtained were as follows: gold recovery rate reached 95.4%, silver recovery rate reached 84.6%, and copper recovery rate reached 95.6%. Compared with direct cyanide leaching, the gold recovery rate increased by about 55%, the silver recovery rate increased by about 38%, and copper recovery was also taken into account.

[0063] In summary, applying this invention to the complex gold extraction charcoal roasting slag of high-copper and iron content achieves good recovery rates of approximately 95% for gold, 84% for silver, and 95% for copper. Compared to direct leaching using a cyanide system, the gold recovery rate is increased by approximately 55%, the silver recovery rate by approximately 38%, and copper recovery is also considered, effectively solving the comprehensive recovery problem of valuable components in complex gold extraction charcoal roasting slag of high-copper and iron content. This system features simple equipment, a short process, low energy consumption, environmental friendliness, and strong adaptability. It effectively improves gold and silver recovery rates while also considering copper recovery, reducing production costs, alleviating inventory pressure for enterprises, and enhancing their technical, economic, and social benefits.

[0064] The present invention has been described in detail above through specific and preferred embodiments. However, those skilled in the art should understand that the present invention is not limited to the embodiments described above. Any modifications or equivalent substitutions made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A system for recovering valuable components from complex gold-extraction charcoal roasting slag with high copper and iron content, characterized in that: The system includes a ball mill (1), the outlet of which is connected to the inlet of a hydrocyclone (3) via a slurry pump (2), the sand outlet of which is connected to the inlet of the ball mill (1), the overflow outlet of which is connected to the inlet of a flotation system (4), the concentrate outlet of which is connected to a roasting and ashing system (5), the tailings outlet of which is connected to the slag outlet of which is connected to a copper leaching tank (6), the copper leaching tank (6) is connected to a copper recovery system (8) and a cyanide leaching tank (9) via a No. 1 filter (7), and the outlet of the No. 1 cyanide leaching tank (9) is connected in sequence to a No. 2 filter (10), a No. 2 cyanide leaching tank (11) and a No. 3 filter (12).

2. The system for recovering valuable components from complex high-copper-iron gold-extraction charcoal roasting slag according to claim 1, characterized in that: The filtrate port of the No. 1 filter (7) is connected to the copper recovery system (8), and the filter residue port is connected to the No. 1 cyanide leaching tank (9).

3. The system for recovering valuable components from complex gold-extraction charcoal roasting slag with high copper and iron content according to claim 1, characterized in that: The filter residue port of the No. 2 filter (10) is connected to the No. 2 cyanide leaching tank (11).

4. The system for recovering valuable components from complex gold-extraction charcoal roasting slag with high copper and iron content according to any one of claims 1-3, characterized in that: The distillate from the copper recovery system (8) is returned to the copper leaching tank (6) via a pipeline.

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