Method for improving silver and copper recovery rate by using wet antimony leaching high-salt waste liquid

Abstract

The invention belongs to the technical field of metallurgy, and relates to a method for improving the recovery rate of silver and copper by using wet antimony leaching high-salt waste liquid, which comprises the following steps: (1) first-grade silver-copper-containing gold concentrate ore blending; (2) secondary high-salt waste liquid output; (3) carrying out third-stage wet-process size mixing; (4) four-stage sulfating roasting; (5) five-stage acid leaching copper leaching; and (6) gold and silver are leached through six-stage cyanidation. According to the method, comprehensive recovery of the silver-copper-containing gold concentrate and high-value utilization of the high-salinity wastewater are achieved in the mode that the silver-copper-containing gold concentrate and the wet-process antimony leaching high-salinity waste liquid are mixed and subjected to high-temperature sulfating roasting, no wastewater or dangerous solid waste is generated, and the environment-friendly requirement is met; the equipment is simple in structure, stable in operation and high in adaptability, the influence of circulating wet antimony immersion of the high-salinity wastewater on the system is effectively solved, and convenience is provided for subsequent production; and the process production cost is low, the number of users is small, and the cost is effectively reduced.

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 high-salt waste liquid. Background Art

[0002] The alkaline wet antimony leaching process usually uses sodium sulfide and sodium hydroxide as the leaching medium for antimony. With the continuous circulation of the liquid, the content of sodium sulfide and miscellaneous salts in the liquid will continue to increase. The presence of miscellaneous salts will have a great impact on the electrolytic process. At present, the electrolytic waste liquid contains about 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, part of the sodium sulfide will be continuously oxidized to form sodium sulfate, sodium sulfite and sodium thiosulfate. During the electrolytic process, a layer of sodium salt will be formed above the electrolytic tank, which will seriously interfere with the production and the judgment of the amount of drugs, and will also have a serious impact on the purity of the cathode antimony product. The electrolytic lean liquid after electrolytic deposition will continue to affect the leaching, reduce the leaching effect, and directly affect the production cost. Conventional evaporation crystallization process and cooling crystallization process are difficult to effectively separate sodium sulfide from other impurities. Therefore, there is an urgent need for a high-value comprehensive utilization method for antimony leaching high-salt waste liquid so that the antimony leaching high-salt waste liquid can be efficiently utilized.

[0003] At present, the roasting and cyaniding production process of silver-copper-gold concentrate is still an important process used in the world today. The process flow is stable, and the recovery rate of gold, sulfur and other elements has reached a high level, but the recovery rate of silver is low, only about 35%. At the same time, although the recovery rate of copper is 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 improve the recovery rate of silver and copper in gold concentrate and improve the comprehensive utilization level of gold concentrate resources.

[0004] Therefore, there is a need for a method that can 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 view of the shortcomings of the above-mentioned prior art, the high-value comprehensive utilization of high-salt waste liquid from antimony leaching is realized, and at the same time, the efficient recovery of silver and copper in silver-copper-gold concentrate is realized, and the level of comprehensive resource utilization is improved. 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. The specific technical scheme 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 mineral is slurried with water to a mineral 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 pulping: adding high-salt waste liquid to the silver-copper-gold concentrate after ore preparation in step (1), and then adding water to adjust the pulp 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 fume and roasted sand;

[0011] (5) Five-stage acid leaching of copper: the roasted sand obtained in step (4) is acid-leached with 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 to 30-40%, sodium hydroxide is added for alkaline leaching, and then filtered to obtain a filter cake, and 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.

[0013] The high-salt waste liquid obtained in step (2) of the method for improving the recovery rate of silver and copper by wet leaching of 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%; 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 the high-salt waste liquid of wet antimony leaching to improve the silver-copper recovery rate, so that the salts in the high-salt waste liquid of wet antimony leaching are utilized in a high-value manner, which has great economic benefits, plays an important role in the roasting process, effectively improves the conversion degree of the silver compound and the copper compound of the silver-copper-gold concentrate, and enables the silver and copper resources to be efficiently recovered; the silver-copper-gold concentrate is effectively disposed and utilized in a high-value manner by mixing the silver-copper-gold concentrate with the high-salt waste liquid of wet antimony leaching and high-temperature sulfuric acid roasting, thereby solving the technical problem that high-salt wastewater cannot be effectively disposed, and at the same time improving the ideal effect of the silver-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 step (2), the temperature of the high temperature oxidation treatment is 70 to 90°C, the oxidation is carried out with pure oxygen, and the oxygen flow rate is 10 to 30 m 3 / h.

[0018] Furthermore, in the step (3), the mass ratio of the silver-copper-gold concentrate to the high-salt waste liquid after blending 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 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 potassium permanganate addition amount is 1-3kg / t, the hydrogen peroxide addition amount is 1-3kg / t, and the acid leaching time is 120-240min.

[0023] Furthermore, 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.

[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 invention realizes the comprehensive recovery of silver-copper-gold concentrate and the high-value utilization of high-salt wastewater by mixing silver-copper-gold concentrate with high-salt wastewater from wet antimony leaching and high-temperature sulfuric acid roasting, without generating wastewater and hazardous solid waste, thus meeting environmental protection requirements; the equipment of the invention has a simple structure, stable operation and strong adaptability, effectively solves the influence of circulating wet antimony leaching of high-salt wastewater on the system, and provides convenience for subsequent production; the process production cost is low, fewer people are used, and the cost is effectively reduced. 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] Embodiment 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 first-level silver-copper-gold concentrate: blending the gold concentrate to meet the self-heating roasting temperature conditions during the roasting process. The content of each element after blending in this embodiment is as follows: 30 g / t of gold, 200 g / t of silver, 2w% of copper, 23w% of sulfur, 0.3w% of lead, and 0.30w% of 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%, with a sodium hydroxide dosage of 20kg / t and a sodium sulfide dosage of 20kg / t. The temperature is controlled at 50°C, the stirring speed is 50r / min, the leaching time is 60min, and the temperature of the antimony-containing liquid after leaching is 80°C, and 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, and the high-salt waste liquid obtained at the same time mainly contains 20g / L sodium sulfide, 12g / L sodium hydroxide, 100g / L sodium sulfate, 20g / L sodium sulfite, and 20g / L sodium thiosulfate;

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

[0034] (4) Four-stage sulphate 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 be 4v%, and the roasted sand 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 was added to the acid leaching residue of step (5) to adjust the slurry to 30w%, and 10kg / t of sodium hydroxide was added. The alkali leaching time was 2h. 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% and a pH of 10 to adjust the pulp concentration to 33w%. Then, 0.5kg / t of ammonium bicarbonate was added, and the sodium cyanide concentration was controlled to 0.50w%. The leaching time was 48h. The leached residue contained 0.5g / t of gold and 20g / t of silver, and the silver leaching rate reached 90%.

[0037] Embodiment 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 primary silver-copper-gold concentrate: Blending of gold concentrate to meet the self-heating roasting temperature condition in the roasting process. The content of each element after blending in this embodiment is as follows: 40 g / t of gold, 350 g / t of silver, 3 w% of copper, 25.5 w% of sulfur, 0.4 w% of lead, and 0.40 w% of arsenic;

[0040] (2) Secondary high-salt waste liquid output: 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 antimony-containing precipitate obtained is washed, dried, and sodium pyroantimonate is produced. At the same time, the high-salt waste liquid obtained 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 preparation: adding the silver-copper-gold concentrate after ore preparation in step (1) into a slurry preparation tank, and adding high-salt waste liquid to the silver-copper-gold concentrate after ore preparation at a mass ratio of 1:0.15, and adding water, and finally controlling the slurry concentration to 70w%, and the total sodium content in the slurry to 25g / l;

[0042] (4) Four-stage sulphation 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 be 5v%, and the roasted sand 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 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 slurry to 35w%, and 15kg / t of sodium hydroxide was added. The alkali 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% 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] Embodiment 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: blending the gold concentrate to meet the self-heating roasting temperature conditions during the roasting process. The content of each element after blending in this embodiment is as follows: 50 g / t of gold, 500 g / t of silver, 4 w % of copper, 28 w % of sulfur, 0.5 w % of lead, and 0.50 w % of 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 antimony-containing precipitate obtained is washed, dried, and sodium pyroantimonate is produced. At the same time, the high-salt waste liquid obtained mainly contains the required sodium sulfide content of 40g / L, and the sodium hydroxide content is 15g / L, sodium sulfate is 150g / L, sodium sulfite is 30g / L, and sodium thiosulfate is 30g / L;

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

[0050] (4) Four-stage sulphation 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 be 6v%, and the roasted sand 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 potassium permanganate addition amount is 3kg / t, the hydrogen peroxide addition amount 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 slurry to 40w%, and 20kg / t of sodium hydroxide was added. The alkali 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% 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 principle of the present invention should be included in the protection scope 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 mineral is slurried with water to a mineral 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 pulping: adding high-salt waste liquid to the silver-copper-gold concentrate after ore blending in step (1), and then adding water to adjust the pulp concentration to 68-72w%; (4) Four-stage sulphate roasting: the slurry after slurry adjustment is transported to a fluidized bed roaster for roasting to obtain roasting fume and roasted sand; (5) Five-stage acid leaching of copper: the roasted sand obtained in step (4) is acid-leached with 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 the slurry, sodium hydroxide is added for alkaline leaching, and then filtered to obtain a filter cake, and cyanide leaching solution is added to the filter cake to adjust the ore 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 recovery rate of silver and copper by wet leaching of antimony 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 recovery rate of silver and copper by wet leaching of antimony 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 recovery rate of silver and copper by wet leaching of antimony high-salt waste liquid according to claim 1, characterized in that: In the step (3), the mass ratio of the silver-copper-gold concentrate to the high-salt waste liquid after blending is 1:0.10-0.

20.

5. The method for improving the recovery rate of silver and copper by wet leaching of antimony 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 recovery rate of silver and copper by wet leaching of antimony high-salt waste liquid according to claim 5, characterized in that: In the step (4), the furnace 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 wet leaching of antimony 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 recovery rate of silver and copper by wet leaching of antimony 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 potassium permanganate addition amount is 1-3kg / t, the hydrogen peroxide addition amount is 1-3kg / t, and the acid leaching time is 120-240min.

9. The method for improving the recovery rate of silver and copper by wet leaching of antimony 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 recovery rate of silver and copper by utilizing wet leaching of antimony 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.