Method for recovering valuable components from high-copper-iron complex gold extraction broken carbon roasting slag

Abstract

The invention relates to a method for recovering valuable components from high-copper and high-iron complex gold extraction broken carbon roasting slag. The method comprises the following steps: grinding and grading: grinding and grading a material to be treated into a fine material with the particle size of-0.074 mm accounting for 70%-80%; flotation decarburization is conducted, specifically, primary roughing is conducted on the fine material slurry, carbon-containing concentrate and tailings are obtained, and the carbon-containing concentrate is returned to an original roasting ashing system to be roasted again to obtain concentrate roasting slag; selective leaching of copper: feeding the tailings and the concentrate roasting slag into an ammonia-chlorine solution for pre-leaching to obtain copper-containing leaching liquid and leaching slag; first-stage preferential leaching is conducted, specifically, the leaching residues are fed into a cyaniding system to be subjected to first-stage preferential leaching, and a gold and silver pregnant solution and first-stage leaching residues are obtained; second-stage intensified leaching is conducted, specifically, the first-stage leaching residues are subjected to second-stage intensified leaching, and gold and silver pregnant solution and second-stage leaching residues are obtained; and recovery of element copper: conveying the copper-containing immersion liquid to a copper recovery system for distillation to obtain ammonia water and a copper hydroxide precipitate. According to the method, efficient comprehensive recovery of gold, silver and copper in the high-copper-iron complex gold extraction broken carbon roasting slag is achieved.

Description

Technical Field

[0001] The invention belongs to the technical field of secondary recovery of precious metal materials, and particularly relates to a method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag. Background Art

[0002] In the gold resource recovery process, the carbon-in-slurry process is widely used due to its efficient gold and silver adsorption capacity. However, over long-term operation, the activated carbon in the carbon slurry will continuously wear out, producing carbon fragments that are enriched with precious metals such as gold and silver. Currently, companies typically collect the carbon fragments, roast them, and then return them to the original process for secondary recovery of gold and silver. However, during the roasting and ashing process, some activated carbon cannot be fully burned. Furthermore, gold resources often contain high levels of harmful elements such as copper and iron, which are concentrated in the carbon fragments. This creates technical challenges when returning the roasted and ashed materials to the original process. Currently, gold-containing materials are primarily stored, and the valuable components are not recovered in a timely and effective manner. This leads to inventory backlogs and capital tie-up, seriously impacting the economic benefits of companies.

[0003] For the secondary recovery of gold and silver from scrap materials, there are currently two main technical routes: pyrometallurgy and hydrometallurgy. While pyrometallurgical smelting offers advantages such as mature processes, fast reaction speeds, and high gold and silver recovery efficiency, it is widely used to process high-grade gold concentrates, gold-bearing materials, and enriched intermediates. However, when processing high-grade gold and silver materials containing high levels of impurities such as copper and iron, numerous technical challenges exist. Copper forms low-melting-point alloys with gold and silver, interfering with precious metal separation and increasing flux requirements. Iron increases slag viscosity, destabilizing the melt system and increasing the loss rate of gold and silver inclusions, severely impacting recovery efficiency. Furthermore, pyrometallurgical processes have stringent requirements for raw material particle size, reducing agent ratio, and smelting atmosphere, resulting in poor adaptability. Especially for materials with high silver content, silver is easily lost in the form of volatilization or smoke, resulting in low recovery rates and significant resource waste. Furthermore, pollutants such as sulfur dioxide, heavy metal dust, and nitrogen oxides generated during the smelting process require costly environmental protection facilities, increasing operational burdens and hindering the achievement of green metallurgy and carbon emission reduction goals.

[0004] While existing conventional wet-process gold and silver recovery methods are simple to operate and offer low energy consumption, they suffer from low gold and silver recovery rates and poor adaptability when processing the ash slag from the complex gold extraction process involving crushed carbon roasting, which is high in copper and iron. For one thing, the residual powdered carbon in the ash slag can re-adsorb the leached gold and silver. Furthermore, the high copper content in the cyanide leaching process not only increases cyanide consumption but also forms cuprous cyanide precipitates, which coat the gold and silver surfaces and hinder leaching. Furthermore, activated carbon has a relatively weak adsorption capacity for silver, making direct carbon leaching of high-gold and silver materials prone to significant silver losses.

[0005] Therefore, it is urgent to develop a recycling technology with simple process and strong adaptability to recover valuable components in the ash slag of high-copper and iron complex gold extraction crushed charcoal roasting, so as to reduce production costs, improve the comprehensive recovery rate, promote the effective comprehensive utilization of resources, alleviate the inventory pressure of enterprises, and increase the technical and economic benefits of enterprises. Summary of the Invention

[0006] The present invention provides a method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag. The method realizes efficient and comprehensive recovery of valuable components such as gold, silver and copper through a series of innovative process steps.

[0007] The specific technical solution is: a method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag, comprising the following steps: (1) Grinding and classification: The material to be processed is transported to the ball mill and hydrocyclone classification system for grinding and classification to obtain fine materials with a particle size of -0.074 mm accounting for 70% to 80%; (2) Flotation decarbonization: The fine material slurry from step (1) is transported to the flotation system, starch is added and stirred evenly, and then kerosene or light diesel is added to perform a roughing process to obtain carbon-containing concentrate and tailings. The carbon-containing concentrate is returned to the original roasting and ashing system and roasted again to obtain concentrate roasting slag; This step cleverly utilizes a flotation system to pre-float partially ash-treated activated carbon, which is then returned to the original calcination and ashing system for secondary calcination. This effectively avoids the secondary sintering problem caused by direct calcination of all the charcoal residue in traditional processes, while also reducing the processing volume and energy consumption of the calcination process. Furthermore, the fine-grained activated carbon is also pre-floated simultaneously, preventing it from directly entering the cyanidation process and adsorbing gold and silver in the solution, which would significantly reduce the recovery rate.

[0008] (3) Selective leaching of copper: the tailings and concentrate roasting residue from step (2) are sent to an ammonia-chlorine solution for pre-leaching to obtain a copper-containing leaching solution (which enters a copper recovery system) and leaching residue; This step cleverly utilizes NH3 and CI - The synergistic effect and selective complexing ability of the copper leaching agent dissolve the free copper and the bound copper, which are stably present in the solution in the form of copper-ammine complexes, creating favorable conditions for subsequent cyanide leaching and solving the problem of low copper leaching rate in conventional methods.

[0009] (4) One-stage preferential leaching: the leaching residue from step (3) is fed into the cyanidation system for one-stage preferential leaching to obtain a gold and silver precious liquid and a one-stage leaching residue; This step quickly dissolves exposed free gold and some easily leached silver at low cyanide concentrations, achieving low-cost and rapid enrichment, providing favorable conditions for subsequent enhanced leaching.

[0010] (5) Second stage enhanced leaching: the first stage leaching residue of step (4) is subjected to second stage enhanced leaching to obtain gold and silver precious liquid and second stage leaching residue; This step increases the cyanide concentration and adds an oxidant to enhance the leaching power, deeply leaching the gold and silver with more complex structures or tighter packaging in the slag, and can significantly improve the overall leaching rate of gold and silver.

[0011] (6) Recovery of elemental copper: The copper-containing leaching solution from step (3) is transported to a copper recovery system for distillation to obtain ammonia water and copper hydroxide precipitate.

[0012] This step cleverly volatilizes NH3 through distillation, hydrolyzing copper ions into copper hydroxide precipitates, and returning NH3 for reuse, achieving efficient copper recovery and recycling of ammonia.

[0013] Furthermore, the concentration of the fine material in step (1) is 20% to 25%.

[0014] Furthermore, in step (1), the grinding concentration is controlled to be 75% to 85%, and the classification concentration is controlled to be 50% to 55%.

[0015] Furthermore, in step (2), the amount of starch added is 50-200 g / t, and the amount of kerosene or light diesel added is 300-800 g / t.

[0016] Furthermore, in step (2), 40 to 100 g / t of 2# oil as a foaming agent is added during the roughing process, and the roughing time is 6 to 10 minutes.

[0017] Furthermore, the ammonia concentration in the ammonia-chlorine solution in step (3) (adding ammonia water) is 1.5-2 mol / L, CI - The concentration (with sodium chloride added) is 1-1.5 mol / L, the pre-immersion time is 4-6 hours, the solution pH is controlled at 9-10, and the temperature is controlled at 40-50°C.

[0018] Furthermore, in step (4), the concentration of sodium cyanide 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 to 12 hours.

[0019] Furthermore, in step (5), 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 to 30 hours.

[0020] Furthermore, in step (6), the distillation temperature is 70-90° C., and the pH is controlled at 9-10.

[0021] Furthermore, the ammonia water obtained in step (6) is returned to step (3) for recycling.

[0022] Beneficial effects of the present invention: The present invention achieves efficient and comprehensive recovery of gold, silver and copper from high-copper and iron complex gold extraction crushed charcoal roasting slag through a clever combination of technical means such as grinding classification, flotation decarbonization, selective leaching of copper, first-stage preferential leaching, second-stage enhanced leaching, and distillation recovery of elemental copper. The process is short, the equipment is simple, the energy consumption is low, it is environmentally friendly and has strong adaptability. It is not only suitable for the treatment of high-copper and iron complex gold extraction crushed charcoal roasting slag, but can also be applied to the treatment of other gold-containing materials with high gold and silver grades and containing impurities, solving the problem of capital occupation caused by inventory backlogs for enterprises and improving the economic and social benefits of enterprises. The specific beneficial effects are as follows: (1) The present invention not only significantly improves the recovery rates of gold and silver, but also takes into account the efficient recovery of copper. 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%.

[0023] (2) The present invention innovatively introduces flotation decarbonization technology before the roasting and ashing process, which allows the activated carbon that has not been fully ashed to be floated out in advance and then subjected to secondary roasting. This effectively avoids the problem of secondary sintering caused by the direct roasting of all the broken carbon slag in the traditional process. In addition, the fine particles of activated carbon are also pre-floated, which can prevent them from being directly mixed into the cyanidation process and adsorbing gold and silver in the solution, resulting in a significant decrease in the gold and silver recovery rate.

[0024] (3) The present invention cleverly utilizes the synergistic effect and selective complexing ability of the strong complexing agent NH3 and the weak complexing agent CI⁻ to dissolve free copper and most of the difficult-to-leach bound copper, stably presenting it in the solution as a copper-ammine complex, and then efficiently recovering it. This innovation solves the problem of low copper leaching rate in conventional methods and creates favorable conditions for subsequent cyanide leaching.

[0025] (4) The present invention adopts a two-stage leaching process: the first stage rapidly leaches exposed free gold and some easily leached silver under low cyanide concentration conditions; the second stage specifically adds cyaniding agents and oxidants to enhance leaching kinetics and deeply dissolve gold and silver with more complex structures or tighter packing. This design solves the problem of low silver recovery, effectively improves the overall recovery rate of gold and silver, and reduces interference from residual impurities by changing the solution, avoiding waste of cyaniding agents and changes in the gold-silver complex equilibrium.

[0026] (5) By optimizing the process flow, the present invention reduces equipment investment and energy consumption, while improving resource recovery and reducing production costs. In addition, by distilling and recycling ammonia water for reuse, the consumption of chemical reagents in the production process is further reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1This is a flow chart of a method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag of the present invention. DETAILED DESCRIPTION

[0028] In order to make the technical problems and technical solutions solved by the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention. Example 1

[0029] Raw material 1#: A high-copper and iron complex gold extraction crushed carbon roasting slag, whose main elements and contents are: 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%.

[0030] The method of the present invention is implemented on raw material 1#, and the specific steps are as follows: (1) Grinding and Classification: Raw material 1# is conveyed to the ball mill and hydrocyclone classification system for grinding and classification, obtaining a slurry with a concentration of 20% to 25%, of which the -0.074mm particle size accounts for 70% to 80%. During this process, the grinding concentration is controlled at 75% to 85%, and the classification concentration is 50% to 55%.

[0031] (2) Flotation decarbonization: The slurry from step (1) is transferred to a flotation system, 50 g / t starch is added and stirred evenly, and then 800 g / t kerosene or light diesel is added for a roughing process to obtain a carbon concentrate and tailings. The carbon concentrate is returned to the original roasting and ashing system for further roasting to obtain a concentrate roasting slag. 80 g / t of frother 2# oil is added during the roughing process, and the roughing time is 6 to 10 minutes.

[0032] (3) Selective leaching of copper: The tailings and concentrate roasting residue from step (2) are sent to an ammonia-chlorine solution for pre-leaching to obtain a copper-containing leaching solution (entering the copper recovery system) and leaching residue. In this process, the ammonia concentration in the solution (adding ammonia water) is 1.5-2 mol / L, and the CI - The concentration (with sodium chloride added) is 1-1.5 mol / L, the pre-immersion time is 6 hours, the solution pH is controlled at 9-10, and the temperature is controlled at 40-50°C; (4) First-stage preferential leaching: The leaching residue from step (3) is fed into a cyanidation system for first-stage preferential leaching to obtain a precious gold and silver solution and a first-stage leaching residue. 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; (5) Second-stage enhanced leaching: The first-stage leaching residue of step (4) is subjected to second-stage enhanced leaching to obtain precious gold and silver solution and second-stage leaching residue. In 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; (6) Recovery of elemental copper: The copper-containing leaching solution from step (3) is transported to a copper recovery system for distillation to obtain ammonia water and copper hydroxide precipitate, wherein the ammonia water is returned to step (3) for recycling. During this process, the distillation temperature is 70-90°C and the pH is controlled at 9-10.

[0033] The test results achieved gold recovery rates of 94.5%, silver recovery rates of 85.4%, and copper recovery rates of 96.3%. Compared with direct cyanide leaching, the gold recovery rate increased by approximately 55%, the silver recovery rate increased by approximately 40%, and the copper recovery rate was also taken into account. Example 2

[0034] Raw material 2#: A high-copper and iron complex gold extraction crushed carbon roasting slag, whose main elements and contents are: gold 380.56g / t, silver 2500.34g / t, copper 5.6% (80.1% of which is bound copper), carbon 6.8%, iron 9.8%, and calcium 29.5%.

[0035] The method of the present invention is implemented on raw material 2#, and the specific steps are as follows: (1) Grinding and Classification: Raw material 2 is conveyed to the ball mill and hydrocyclone classification system for grinding and classification, obtaining a slurry with a concentration of 20% to 25%, of which the -0.074mm particle size accounts for 70% to 80%. During this process, the grinding concentration is controlled at 75% to 85%, and the classification concentration is 50% to 55%.

[0036] (2) Flotation decarbonization: The slurry from step (1) is transferred to a flotation system, 100 g / t starch is added and stirred evenly, and then 300 g / t kerosene or light diesel is added for a roughing process to obtain a carbon concentrate and tailings. The carbon concentrate is returned to the original roasting and ashing system for further roasting to obtain a concentrate roasting slag. 100 g / t of frother 2# oil is added during the roughing process, and the roughing time is 6 to 10 minutes.

[0037] (3) Selective leaching of copper: The tailings and concentrate roasting residue from step (2) are sent to an ammonia-chlorine solution for pre-leaching to obtain a copper-containing leaching solution (entering the copper recovery system) and leaching residue. In this process, the ammonia concentration in the solution (adding ammonia water) is 1.5-2 mol / L, and the CI - The concentration (with sodium chloride added) is 1-1.5 mol / L, the pre-immersion time is 5 hours, the solution pH is controlled at 9-10, and the temperature is controlled at 40-50°C; (4) First-stage preferential leaching: The leaching residue from step (3) is fed into a cyanidation system for first-stage preferential leaching to obtain a precious gold and silver solution and a first-stage leaching residue. 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; (5) Second-stage enhanced leaching: The first-stage leaching residue of step (4) is subjected to second-stage enhanced leaching to obtain precious gold and silver solution and second-stage leaching residue. In 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; (6) Recovery of elemental copper: The copper-containing leaching solution from step (3) is transported to a copper recovery system for distillation to obtain ammonia water and copper hydroxide precipitate, wherein the ammonia water is returned to step (3) for recycling. During this process, the distillation temperature is 70-90°C and the pH is controlled at 9-10.

[0038] The test results achieved gold recovery rates of 95.1%, silver recovery rates of 84.2%, and copper recovery rates of 95.4%. Compared with direct cyanide leaching, the gold recovery rate increased by approximately 54%, the silver recovery rate increased by approximately 39%, and the copper recovery rate was also taken into account. Example 3

[0039] Raw material 3#: A high-copper and iron complex gold extraction crushed carbon roasting slag, whose main elements and contents are: 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%.

[0040] The present invention is used to carry out the complex gold extraction of high-copper and iron crushed carbon roasted slag, and the specific steps are as follows: (1) Grinding and Classification: Raw material 3 is conveyed to the ball mill and hydrocyclone classification system for grinding and classification, obtaining a slurry with a concentration of 20% to 25%, of which the -0.074mm particle size accounts for 70% to 80%. During this process, the grinding concentration is controlled at 75% to 85%, and the classification concentration is 50% to 55%.

[0041] (2) Flotation decarbonization: The slurry from step (1) is transferred to a flotation system, 200 g / t starch is added and stirred evenly, and then 300 g / t kerosene or light diesel is added for a roughing process to obtain a carbon concentrate and tailings. The carbon concentrate is returned to the original roasting and ashing system for further roasting to obtain a concentrate roasting slag. 40 g / t of frother 2# oil is added during the roughing process, and the roughing time is 6 to 10 minutes.

[0042] (3) Selective leaching of copper: The tailings and concentrate roasting residue from step (2) are sent to an ammonia-chlorine solution for pre-leaching to obtain a copper-containing leaching solution (entering the copper recovery system) and leaching residue. In this process, the ammonia concentration in the solution (adding ammonia water) is 1.5-2 mol / L, and the CI - The concentration (with sodium chloride) is 1-1.5 mol / L, the pre-immersion time is 4 hours, the solution pH is controlled at 9-10, and the temperature is controlled at 40-50°C; (4) First-stage preferential leaching: The leaching residue from step (3) is fed into a cyanidation system for first-stage preferential leaching to obtain a precious gold and silver solution and a first-stage leaching residue. 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; (5) Second-stage enhanced leaching: The first-stage leaching residue of step (4) is subjected to second-stage enhanced leaching to obtain precious gold and silver solution and second-stage leaching residue. In 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; (6) Recovery of elemental copper: The copper-containing leaching solution from step (3) is transported to a copper recovery system for distillation to obtain ammonia water and copper hydroxide precipitate, wherein the ammonia water is returned to step (3) for recycling. During this process, the distillation temperature is 70-90°C and the pH is controlled at 9-10.

[0043] The test results achieved gold recovery rates of 95.4%, silver recovery rates of 84.6%, and copper recovery rates of 95.6%. Compared with direct cyanide leaching, the gold recovery rate increased by approximately 55%, the silver recovery rate increased by approximately 38%, and the copper recovery rate was also taken into account.

[0044] In summary, the present invention can be applied to this type of high-copper and iron complex gold extraction crushed charcoal roasted slag, achieving good recovery indicators of approximately 95% gold recovery, approximately 84% silver recovery, and approximately 95% copper recovery. Compared with direct cyanide leaching, the gold recovery rate is increased by approximately 55%, the silver recovery rate is increased by approximately 38%, and copper recovery is also taken into account, effectively solving the problem of comprehensive recovery of valuable components in high-copper and iron complex gold extraction crushed charcoal roasted slag. The process is short, the equipment is simple, the energy consumption is low, and it is environmentally friendly and highly adaptable. It effectively improves the gold and silver recovery rate while taking into account the recovery of copper, reduces production costs, alleviates the inventory pressure of the enterprise, and enhances the technical, economic and social benefits of the enterprise.

[0045] The present invention has been described in detail above through specific and preferred embodiments, but those skilled in the art should understand that the present invention is not limited to the embodiments described above. Any modifications, equivalent substitutions, etc. made within the spirit and principles of the present invention should be included in the scope of protection of the present invention.

Claims

1. A method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag, characterized in that: The steps include: (1) Grinding and classification: The material to be processed is transported to the ball mill and hydrocyclone classification system for grinding and classification to obtain fine materials with a particle size of -0.074 mm accounting for 70% to 80%; (2) Flotation decarbonization: The fine material slurry from step (1) is transported to the flotation system, starch is added and stirred evenly, and then kerosene or light diesel is added to perform a roughing process to obtain carbon-containing concentrate and tailings. The carbon-containing concentrate is returned to the original roasting and ashing system and roasted again to obtain concentrate roasting slag; (3) Selective leaching of copper: the tailings and concentrate roasting residue from step (2) are fed into an ammonia-chlorine solution for pre-leaching to obtain a copper-containing leaching solution and leaching residue; (4) One-stage preferential leaching: the leaching residue from step (3) is fed into the cyanidation system for one-stage preferential leaching to obtain a gold and silver precious liquid and a one-stage leaching residue; (5) Second stage enhanced leaching: the first stage leaching residue of step (4) is subjected to second stage enhanced leaching to obtain gold and silver precious liquid and second stage leaching residue; (6) Recovery of elemental copper: The copper-containing leaching solution from step (3) is transported to a copper recovery system for distillation to obtain ammonia water and copper hydroxide precipitate.

2. The method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag according to claim 1, characterized in that: The concentration of fine material in step (1) is 20% to 25%.

3. A method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag according to claim 1 or 2, characterized in that: In step (1), the grinding concentration is controlled at 75% to 85%, and the classification concentration is controlled at 50% to 55%.

4. A method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag according to claim 1 or 2, characterized in that: In step (2), the amount of starch added is 50-200 g / t, and the amount of kerosene or light diesel added is 300-800 g / t.

5. The method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag according to claim 4, characterized in that: In step (2), 40-100 g / t of 2# oil, a foaming agent, is added during the roughing process, and the roughing time is 6-10 min.

6. A method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag according to claim 1 or 5, characterized in that: The ammonia concentration in the ammonia-chlorine solution in step (3) (adding ammonia water) is 1.5-2 mol / L, and the Cl - The concentration (with sodium chloride added) is 1-1.5 mol / L, the pre-immersion time is 4-6 hours, the solution pH is controlled at 9-10, and the temperature is controlled at 40-50°C.

7. The method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag according to claim 6, characterized in that: In step (4), the concentration of sodium cyanide 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 to 12 hours.

8. The method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag according to claim 7, characterized in that: In step (5), 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 to 30 hours.

9. The method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag according to claim 6, characterized in that: In step (6), the distillation temperature is 70-90° C. and the pH is controlled at 9-10.

10. The method for recovering valuable components from high-copper and iron complex gold extraction crushed carbon roasting slag according to claim 1, characterized in that: The ammonia water obtained in step (6) is returned to step (3) for recycling.

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