A method for improving the recovery rate of silver and copper by utilizing wet leaching of antimony high-salt wastewater

Abstract

The present invention relates to the field of metallurgy technology and relates to a method for improving the recovery rate of silver and copper by utilizing high-salt wastewater from wet antimony leaching, comprising the following steps: (1) first-stage silver-copper-gold concentrate blending; (2) second-stage high-salt wastewater output; (3) third-stage wet slurry mixing; (4) fourth-stage sulfuric acid roasting; (5) fifth-stage acid leaching of copper; and (6) sixth-stage cyanide leaching of gold and silver. The present invention achieves comprehensive recovery of silver-copper-gold concentrate and high-value utilization of high-salt wastewater by mixing silver-copper-gold concentrate with high-salt wastewater from wet antimony leaching at high temperature and sulfuric acid roasting, without generating wastewater or hazardous solid waste, thus meeting environmental protection requirements. The equipment of the present invention has a simple structure, stable operation, and strong adaptability, effectively solving the impact of circulating high-salt wastewater on the system during wet antimony leaching, and providing convenience for subsequent production. The process has low production costs and requires fewer personnel, effectively reducing costs.

Description

Technical Field

[0001] The invention belongs to the technical field of metallurgy, and in particular relates to a method for improving the recovery rate of silver and copper by utilizing wet-process antimony leaching high-salt waste liquid. Background Art

[0002] The alkaline wet antimony leaching process typically uses sodium sulfide and sodium hydroxide as the leaching medium. As the liquid circulates, the content of sodium sulfide and other salts in the liquid increases continuously. The presence of these salts can significantly impact the electrowinning process. Currently, the electrowinning wastewater contains approximately 90g / L of sodium sulfide, 20-30g / L of sodium hydroxide, 80-90g / L of sodium sulfate, 20-30g / L of sodium sulfite, and 20-30g / L of sodium thiosulfate. Due to long-term recycling, some of the sodium sulfide is continuously oxidized to form sodium sulfate, sodium sulfite, and sodium thiosulfate. During the electrowinning process, a layer of sodium salts forms above the electrowinning tank, severely interfering with production and determining drug quantity, and significantly affecting the purity of the cathode antimony product. The remaining lean liquid after electrowinning further impacts leaching, reducing leaching efficiency and directly impacting production costs. Conventional evaporation crystallization and cooling crystallization processes are difficult to effectively separate sodium sulfide from other miscellaneous salts. Therefore, there is an urgent need for a high-value comprehensive utilization method for antimony leaching high-salt wastewater to enable efficient utilization of antimony leaching high-salt wastewater.

[0003] Currently, the roasting and cyaniding process for producing silver-copper-gold concentrate remains an important process used worldwide. While the process is stable and the recovery rates of elements such as gold and sulfur have reached high levels, the silver recovery rate is relatively low, at only around 35%. Furthermore, while the copper recovery rate is relatively high, the copper content of the leached residue is still only 0.40-0.50%. Therefore, there is an urgent need for a method to increase the recovery rates of silver and copper in gold concentrate and improve the comprehensive utilization of gold concentrate resources.

[0004] Therefore, a method is needed to achieve high-value comprehensive utilization of high-salt waste liquid from antimony leaching, while achieving efficient recovery of silver and copper in silver-copper-gold concentrates and improving the level of comprehensive resource utilization. Summary of the Invention

[0005] In order to address the deficiencies of the above-mentioned prior art, the present invention provides a method for improving the recovery rate of silver and copper by utilizing high-salt waste liquid from wet antimony leaching to achieve high-value comprehensive utilization of high-salt waste liquid, and simultaneously achieve efficient recovery of silver and copper from silver-copper-gold concentrate, thereby improving the level of comprehensive resource utilization. The specific technical solution is as follows:

[0006] A method for improving the recovery rate of silver and copper by utilizing wet leaching of antimony high-salt waste liquid comprises the following steps:

[0007] (1) Blending of first-level silver-copper-gold concentrate: blending of silver-copper-gold concentrate, the content of each element after blending is: gold 30-50g / t, silver 200-500g / t, copper 2-4w%, sulfur 23-28w%, lead 0.3-0.5w%, arsenic 0.30-0.50w%;

[0008] (2) Secondary high-salt waste liquid production: The antimony-containing ore is slurried with water to a concentration of 40-50w%, and then stirred and leached with sodium hydroxide and sodium sulfide to obtain an antimony-containing liquid. The antimony-containing liquid is subjected to high-temperature oxidation treatment to obtain an antimony-containing precipitate and high-salt waste liquid. The antimony-containing precipitate is washed and dried to produce sodium pyroantimonate;

[0009] (3) Three-stage wet slurry mixing: adding high-salt waste liquid to the silver-copper-gold concentrate after ore blending in step (1), and then adding water to adjust the slurry concentration to 68-72w%;

[0010] (4) Four-stage sulphate roasting: the adjusted slurry is transported to a fluidized bed roaster for roasting to obtain roasting flue gas and roasted sand;

[0011] (5) Five-stage acid leaching of copper: the calcined sand obtained in step (4) is acid-leached using sulfuric acid, potassium permanganate and hydrogen peroxide to obtain acid leaching residue and acid leaching solution;

[0012] (6) Sixth-stage cyanide leaching of gold and silver: water is added to the acid leaching residue obtained in step (5) to adjust the pulp concentration to 30-40%, sodium hydroxide is added for alkaline leaching, and then filtered to obtain a filter cake, cyanide leaching solution is added to the filter cake to adjust the pulp concentration to 33-43w%, and ammonium bicarbonate and sodium cyanide are added for leaching to obtain leaching residue and leachate.

[0013] The high-salt waste liquid obtained in step (2) of the method for improving the silver and copper recovery rate by wet-leaching antimony high-salt waste liquid of the present invention mainly contains 20-40 g / L of sodium sulfide, 12-15 g / L of sodium hydroxide, 100-150 g / L of sodium sulfate, 20-30 g / L of sodium sulfite, and 20-30 g / L of sodium thiosulfate; the acid leaching residue obtained in step (5) contains 40-70 g / t of gold, 300-700 g / t of silver, 0.20-0.50 w% of sulfur, 0.10-0.20 w% of copper, and the copper leaching rate reaches 96-98%; and the leaching residue obtained in the final step (6) contains 0.5-1.5 g / t of gold, 20-50 g / t of silver, and the silver leaching rate reaches 90-96%.

[0014] The method of the present invention utilizes high-salt waste liquid from wet antimony leaching to improve the silver and copper recovery rate, so that the salts in the high-salt waste liquid from wet antimony leaching are utilized in a high-value manner, which has great economic benefits and plays an important role in the roasting process, effectively improving the conversion degree of silver compounds and copper compounds in the silver-copper-gold concentrate, so that silver and copper resources are efficiently recovered; the silver-copper-gold concentrate is effectively treated and utilized in a high-value manner by mixing the silver-copper-gold concentrate with the high-salt waste liquid from wet antimony leaching and subjecting the concentrate to high-temperature sulfuric acid roasting, thereby solving the technical problem that high-salt wastewater cannot be effectively treated, and at the same time achieving the ideal effect of improving the silver and copper recovery rate of the silver-copper-gold concentrate.

[0015] Furthermore, in the step (2), the antimony-containing mineral contains 2 to 20w% antimony and has a fineness of -0.037mm accounting for 88 to 90%.

[0016] Furthermore, in the step (2), the amount of sodium hydroxide used is 20-40 kg / t, the amount of sodium sulfide used is 20-140 kg / t, the leaching temperature is 50-70° C., the stirring speed is 50-150 r / min, and the leaching time is 60-180 min.

[0017] Furthermore, in the step (2), the temperature of the high temperature oxidation treatment is 70-90°C, the oxidation is carried out with pure oxygen, and the oxygen flow rate is 10-30m 3 / h.

[0018] Furthermore, in the step (3), the mass ratio of the silver-copper-gold concentrate after blending to the high-salt waste liquid is 1:0.10-0.20.

[0019] Furthermore, in the step (4), the bottom pressure of the fluidized bed roasting furnace is 11000-14000 Pa, the roasting temperature is 600-650° C., and the roasting time is 20-30 min.

[0020] Furthermore, in the step (4), the temperature of the fluidized bed roasting furnace is controlled by adding high-salt wastewater to the fluidized bed roasting furnace, and the amount of high-salt wastewater added is 0.1 to 0.3 m 3 / t.

[0021] Furthermore, in the step (4), the sulfur dioxide concentration of the roasting flue gas is controlled at 4-6% by volume, and the roasting flue gas is used to produce industrial sulfuric acid.

[0022] Furthermore, in the step (5), during the acid leaching process, the acid leaching ore concentration is controlled to be 35-50w%, the acid leaching temperature is 80-90°C, the sulfuric acid concentration is 2-5w%, the amount of potassium permanganate added is 1-3kg / t, the amount of hydrogen peroxide added is 1-3kg / t, and the acid leaching time is 120-240min.

[0023] Furthermore, in step (6), the amount of sodium hydroxide added is 10 to 20 kg / t, and the alkali leaching time is 2 to 6 hours.

[0024] Furthermore, in step (6), the concentration of sodium cyanide in the cyanide leaching solution is 0.20-0.50w%, and the pH value is 9-11.

[0025] Furthermore, in step (6), the amount of ammonium bicarbonate added is 0.5-1.5 kg / t, the concentration of sodium cyanide is 0.50-1.0 w%, and the leaching time is 48-96 h.

[0026] The beneficial effects of the present invention are:

[0027] The present invention achieves comprehensive recovery of silver-copper-gold concentrate and high-value utilization of high-salt wastewater by mixing silver-copper-gold concentrate with high-salt wastewater from wet antimony leaching and subjecting it to high-temperature sulfuric acid roasting, without generating wastewater or hazardous solid waste, thus meeting environmental protection requirements. The equipment of the present invention has a simple structure, stable operation, and strong adaptability, effectively solves the impact of circulating wet antimony leaching with high-salt wastewater on the system, and provides convenience for subsequent production. The process has low production cost, requires fewer people, and effectively reduces costs. DETAILED DESCRIPTION

[0028] The principles and features of the present invention are described below in conjunction with embodiments. The examples given are only used to explain the present invention and are not used to limit the scope of the present invention.

[0029] Example 1:

[0030] A method for improving the recovery rate of silver and copper by utilizing wet leaching of antimony high-salt waste liquid comprises the following steps:

[0031] (1) Blending of the first-level silver-copper-gold concentrate: The gold concentrate is blended to meet the autothermal roasting temperature conditions during the roasting process. The content of each element after blending in this embodiment is as follows: 30g / t gold, 200g / t silver, 2w% copper, 23w% sulfur, 0.3w% lead, and 0.30w% arsenic;

[0032] (2) Secondary high-salt waste liquid output: The mineral containing 2w% antimony and 88% fineness of -0.037mm is slurried with water to a mineral concentration of 40w%, the amount of sodium hydroxide is 20kg / t, the amount of sodium sulfide is 20kg / t, the temperature is controlled at 50℃, the stirring speed is 50r / min, the leaching time is 60min, and the temperature of the antimony-containing liquid after leaching is 80℃, the oxygen flow rate is 20m 3 / h high-temperature oxidation treatment, the obtained antimony-containing precipitate is washed, dried, and sodium pyroantimonate is produced. At the same time, the high-salt waste liquid obtained mainly contains 20g / L of sodium sulfide, 12g / L of sodium hydroxide, 100g / L of sodium sulfate, 20g / L of sodium sulfite, and 20g / L of sodium thiosulfate;

[0033] (3) three-stage wet slurry mixing: adding the silver-copper-gold concentrate after ore blending in step (1) into a slurry mixing tank, and adding high-salt waste liquid to the ore blended silver-copper-gold concentrate and high-salt waste liquid at a mass ratio of 1:0.10, and adding water at the same time, finally controlling the slurry concentration to 68w%, and the total sodium content in the slurry to 20g / l;

[0034] (4) Four-stage sulfation roasting: The slurry after slurry adjustment is transported to the boiling roasting furnace through high-pressure air. The furnace bottom pressure is controlled at 11000Pa, the roasting temperature is 600℃, and the roasting time is 20min. The furnace temperature is controlled by adding high-salt wastewater to the boiling furnace. The amount of high-salt wastewater added is 0.1m 3 / t, the roasting flue gas is used to produce industrial sulfuric acid, and the sulfur dioxide concentration of the roasting flue gas is controlled to 4v%, and the calcine enters the next acid leaching process;

[0035] (5) Five-stage acid leaching of copper: the roasted sand obtained in step (4) is transferred to three consecutive acid leaching tanks. During the process, the acid leaching ore concentration is controlled to be 35w%, the temperature is 80°C, the sulfuric acid concentration is 2w%, the amount of potassium permanganate added is 1kg / t, the amount of hydrogen peroxide added is 1kg / t, and the acid leaching time is 120min to obtain the acid leaching residue. The acid leaching residue contains 40g / t of gold, 300g / t of silver, 0.20w% of sulfur, and 0.10w% of copper. The copper leaching rate reaches 96%. The acid leaching residue enters the next step of cyanide leaching of gold and silver;

[0036] (6) Sixth-stage cyanide leaching of gold and silver: water is added to the acid leaching residue of step (5) to adjust the pulp to 30w%, and 10kg / t of sodium hydroxide is added. The alkaline leaching time is 2h. The filter cake is filtered through a filter press to obtain a filter cake. The filter cake is added with a cyanide leaching solution with a concentration of 0.35w% and a pH of 10 to adjust the pulp concentration to 33w%. Then, 0.5kg / t of ammonium bicarbonate is added, and the sodium cyanide concentration is controlled to 0.50w%. The leaching time is 48h. The leached residue contains 0.5g / t of gold and 20g / t of silver, and the silver leaching rate reaches 90%.

[0037] Example 2:

[0038] A method for improving the recovery rate of silver and copper by wet leaching of antimony high-salt waste liquid comprises the following steps:

[0039] (1) Blending of the first-level silver-copper-gold concentrate: The gold concentrate is blended to meet the autothermal roasting temperature conditions during the roasting process. The content of each element after blending in this embodiment is as follows: 40g / t gold, 350g / t silver, 3w% copper, 25.5w% sulfur, 0.4w% lead, and 0.40w% arsenic;

[0040] (2) Output of secondary high-salt waste liquid: a mineral containing 11w% antimony and 89% fineness of -0.037mm is slurried with water to a mineral concentration of 45w%, a sodium hydroxide dosage of 30kg / t, a sodium sulfide dosage of 80kg / t, a temperature control of 60°C, a stirring speed of 100r / min, a leaching time of 120min, and the antimony-containing liquid after leaching is subjected to a high-temperature oxidation treatment at a temperature of 80°C and an oxygen flow rate of 20m3 / h. The obtained antimony-containing precipitate is washed, dried, and sodium antimonate is produced. At the same time, the obtained high-salt waste liquid mainly contains 30g / L of sodium sulfide, 13.5g / L of sodium hydroxide, 125g / L of sodium sulfate, 25g / L of sodium sulfite, and 25g / L of sodium thiosulfate;

[0041] (3) three-stage wet slurry mixing: adding the silver-copper-gold concentrate after ore blending in step (1) into a slurry mixing tank, and adding high-salt waste liquid to the ore blended silver-copper-gold concentrate and high-salt waste liquid at a mass ratio of 1:0.15, and adding water at the same time, finally controlling the slurry concentration to 70w%, and the total sodium content in the slurry to 25g / l;

[0042] (4) Four-stage sulfation roasting: The slurry after slurry adjustment is transported to the boiling roasting furnace through high-pressure air. The furnace bottom pressure is controlled at 12500Pa, the roasting temperature is 625℃, and the roasting time is 25min. The furnace temperature is controlled by adding high-salt wastewater to the boiling furnace. The amount of high-salt wastewater added is 0.2m 3 / t, the roasting flue gas is used to produce industrial sulfuric acid, and the sulfur dioxide concentration of the roasting flue gas is controlled to 5v%, and the calcine enters the next acid leaching process;

[0043] (5) Five-stage acid leaching of copper: The roasted sand obtained in step (4) is transferred to three consecutive acid leaching tanks. During the process, the acid leaching ore concentration is controlled to be 40w%, the temperature is 85°C, the sulfuric acid concentration is 3.5w%, the amount of potassium permanganate added is 2kg / t, the amount of hydrogen peroxide added is 2kg / t, and the acid leaching time is 180min to obtain the acid leaching residue. The acid leaching residue contains 55g / t of gold, 500g / t of silver, 0.35w% of sulfur, and 0.15w% of copper. The copper leaching rate reaches 97%. The acid leaching residue enters the next step of cyanide leaching of gold and silver;

[0044] (6) Sixth-stage cyanide leaching of gold and silver: water was added to the acid leaching residue of step (5) to adjust the pulp to 35w%, and 15kg / t of sodium hydroxide was added. The alkaline leaching time was 4h. The filter cake was filtered through a filter press to obtain a filter cake. The filter cake was added with a cyanide leaching solution with a concentration of 0.35w% of sodium cyanide and a pH of 10 to adjust the pulp concentration to 38w%. Then, 1.0kg / t of ammonium bicarbonate was added, and the sodium cyanide concentration was controlled to 0.75w%. The leaching time was 72h. The leached residue contained 1.0g / t of gold and 35g / t of silver, and the silver leaching rate reached 93%.

[0045] Example 3:

[0046] A method for improving the recovery rate of silver and copper by wet leaching of antimony high-salt waste liquid comprises the following steps:

[0047] (1) Control of the blending of the first-level silver-copper-gold concentrate: the gold concentrate is blended to meet the autothermal roasting temperature conditions during the roasting process. The content of each element after blending in this embodiment is: 50g / t gold, 500g / t silver, 4w% copper, 28w% sulfur, 0.5w% lead, and 0.50w% arsenic;

[0048] (2) Secondary high-salt waste liquid output: a mineral containing 20w% antimony and 90% fineness of -0.037mm is slurried with water to a mineral concentration of 50w%, a sodium hydroxide dosage of 40kg / t, a sodium sulfide dosage of 140kg / t, a temperature control of 70°C, a stirring speed of 150r / min, a leaching time of 180min, and the antimony-containing liquid after leaching is subjected to a high-temperature oxidation treatment at a temperature of 80°C and an oxygen flow rate of 20m3 / h. The obtained antimony-containing precipitate is washed, dried, and sodium pyroantimonate is produced. At the same time, the obtained high-salt waste liquid mainly contains the required sodium sulfide content of 40g / L, and the sodium hydroxide content is 15g / L, 150g / L of sodium sulfate, 30g / L of sodium sulfite, and 30g / L of sodium thiosulfate;

[0049] (3) three-stage wet slurry mixing: adding the silver-copper-gold concentrate after ore blending in step (1) into a slurry mixing tank, and adding high-salt waste liquid to the ore blended silver-copper-gold concentrate and high-salt waste liquid at a mass ratio of 1:0.20, and adding water at the same time, finally controlling the slurry concentration to 72w%, and the total sodium content in the slurry to 30g / l;

[0050] (4) Four-stage sulfation roasting: The slurry after slurry adjustment is transported to the boiling roasting furnace through high-pressure air. The furnace bottom pressure is controlled at 14000Pa, the roasting temperature is 650℃, and the roasting time is 30min. The furnace temperature is controlled by adding high-salt wastewater to the boiling furnace. The amount of high-salt wastewater added is 0.3m 3 / t, the roasting flue gas is used to produce industrial sulfuric acid, and the sulfur dioxide concentration of the roasting flue gas is controlled to 6v%, and the calcine enters the next acid leaching process;

[0051] (5) Five-stage acid leaching of copper: the roasted sand obtained in step (4) is transferred to three consecutive acid leaching tanks. During the process, the acid leaching ore concentration is controlled to be 50w%, the temperature is 90°C, the sulfuric acid concentration is 5w%, the amount of potassium permanganate added is 3kg / t, the amount of hydrogen peroxide added is 3kg / t, and the acid leaching time is 240min to obtain the acid leaching residue. The acid leaching residue contains 70g / t of gold, 700g / t of silver, 0.50w% of sulfur, and 0.20w% of copper. The copper leaching rate reaches 98%. The acid leaching residue enters the next step of cyanide leaching of gold and silver;

[0052] (6) Sixth-stage cyanide leaching of gold and silver: water was added to the acid leaching residue of step (5) to adjust the pulp to 40w%, 20kg / t of sodium hydroxide was added, and the alkaline leaching time was 6h. The filter cake was filtered through a filter press to obtain a filter cake. The filter cake was added with a cyanide leaching solution with a concentration of 0.35w% of sodium cyanide and a pH of 10 to adjust the pulp concentration to 43w%. Then, 1.5kg / t of ammonium bicarbonate was added, and the sodium cyanide concentration was controlled to 1.0w%. The leaching time was 96h. The leached residue contained 1.5g / t of gold and 50g / t of silver, and the silver leaching rate reached 96%.

[0053] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, 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 improving the recovery rate of silver and copper by wet leaching of antimony high-salt waste liquid, characterized in that: The steps include: (1) Blending of first-level silver-copper-gold concentrate: blending of silver-copper-gold concentrate, the content of each element after blending is: gold 30-50g / t, silver 200-500g / t, copper 2-4w%, sulfur 23-28w%, lead 0.3-0.5w%, arsenic 0.30-0.50w%; (2) Secondary high-salt waste liquid production: The antimony-containing ore is slurried with water to a concentration of 40-50w%, and then stirred and leached with sodium hydroxide and sodium sulfide to obtain an antimony-containing liquid. The antimony-containing liquid is subjected to high-temperature oxidation treatment to obtain an antimony-containing precipitate and high-salt waste liquid. The antimony-containing precipitate is washed and dried to produce sodium pyroantimonate; (3) Three-stage wet slurry mixing: adding high-salt waste liquid to the silver-copper-gold concentrate after ore blending in step (1), and then adding water to adjust the slurry concentration to 68-72w%; (4) Four-stage sulfuric acid roasting: the slurry after slurry adjustment is transported to a boiling roasting furnace for roasting to obtain roasting flue gas and roasted sand; (5) Five-stage acid leaching of copper: the calcined sand obtained in step (4) is acid-leached using sulfuric acid, potassium permanganate and hydrogen peroxide to obtain acid leaching residue and acid leaching solution; (6) Sixth-stage cyanide leaching of gold and silver: water is added to the acid leaching residue obtained in step (5) to prepare a slurry, sodium hydroxide is added for alkaline leaching, and then the filter cake is filtered to obtain a filter cake, cyanide leaching solution is added to the filter cake to adjust the pulp concentration to 33-43w%, and ammonium bicarbonate and sodium cyanide are added for leaching to obtain leaching residue and leaching solution.

2. The method for improving the silver and copper recovery rate by utilizing wet antimony leaching high-salt waste liquid according to claim 1, characterized in that: In the step (2), the antimony-containing mineral contains 2-20w% antimony and has a fineness of -0.037mm accounting for 88-90%.

3. The method for improving the silver and copper recovery rate by utilizing wet antimony leaching high-salt waste liquid according to claim 2, characterized in that: In the step (2), the amount of sodium hydroxide used is 20-40 kg / t, the amount of sodium sulfide used is 20-140 kg / t, the leaching temperature is 50-70° C., the stirring speed is 50-150 r / min, and the leaching time is 60-180 min.

4. The method for improving the silver and copper recovery rate by utilizing wet antimony leaching high-salt waste liquid according to claim 1, characterized in that: In the step (3), the mass ratio of the silver-copper-gold concentrate after blending to the high-salt waste liquid is 1:0.10-0.

20.

5. The method for improving the silver and copper recovery rate by utilizing wet antimony leaching high-salt waste liquid according to claim 4, characterized in that: In the step (4), the bottom pressure of the fluidized bed roasting furnace is 11000-14000 Pa, the roasting temperature is 600-650° C., and the roasting time is 20-30 min.

6. The method for improving the silver and copper recovery rate by utilizing wet antimony leaching high-salt waste liquid according to claim 5, characterized in that: In the step (4), the temperature of the fluidized bed roasting furnace is controlled by adding high-salt wastewater into the fluidized bed roasting furnace, and the amount of high-salt wastewater added is 0.1 to 0.3 m 3 / t.

7. The method for improving the recovery rate of silver and copper by utilizing wet antimony leaching high-salt waste liquid according to claim 6, characterized in that: In the step (4), the sulfur dioxide concentration of the roasting flue gas is controlled at 4-6% by volume, and the roasting flue gas is used to produce industrial sulfuric acid.

8. The method for improving the silver and copper recovery rate by utilizing wet antimony leaching high-salt waste liquid according to claim 1, characterized in that: In the step (5), during the acid leaching process, the acid leaching ore concentration is controlled to be 35-50w%, the acid leaching temperature is 80-90°C, the sulfuric acid concentration is 2-5w%, the amount of potassium permanganate added is 1-3kg / t, the amount of hydrogen peroxide added is 1-3kg / t, and the acid leaching time is 120-240min.

9. The method for improving the silver and copper recovery rate by utilizing wet antimony leaching high-salt waste liquid according to claim 1, characterized in that: In the step (6), the amount of sodium hydroxide added is 10 to 20 kg / t, and the alkali leaching time is 2 to 6 hours.

10. The method for improving the silver and copper recovery rate by utilizing wet antimony leaching high-salt waste liquid according to claim 9, characterized in that: In the step (6), the amount of ammonium bicarbonate added is 0.5-1.5 kg / t, the concentration of sodium cyanide is 0.50-1.0 w%, and the leaching time is 48-96 h.