阅读说明：本技术 一种含碳砷金精矿梯级分离综合回收的方法 (Method for step separation and comprehensive recovery of carbon-containing arsenic gold concentrate ) 是由 郭建东 朱德兵 于 2021-09-10 设计创作，主要内容包括：本发明属于黄金选冶技术领域,涉及一种含碳砷金精矿梯级分离综合回收的方法。将浮选工艺与冶炼工艺进行了有效的结合,对含碳砷金精矿进行预先浮选,获得碳精矿,碳精矿单独氰化提金、银、铜,使碳精矿中的金、银、铜得到综合回收,破解碳矿物对焙烧及后续氰化过程对金的回收影响,碳精矿浸出渣通过有色冶炼生产工艺得到无废化、综合处理；将选碳尾矿低温脱砷、酸浸处理、高温脱硫的有效结合,通过制粒、低温还原焙烧、烧渣细磨、酸浸工艺处理,破解了常规两段焙烧过程中砷矿物焙烧不完全、金属氧化物、硫化物对金的包裹,实现了金的最大限度的裸露,显著提高了氰化过程金、银的浸出率、经济效益显著。(The invention belongs to the technical field of gold dressing and metallurgy, and relates to a method for step separation and comprehensive recovery of carbon and arsenic-containing gold concentrate. The flotation process and the smelting process are effectively combined, the gold concentrate containing carbon and arsenic is subjected to pre-flotation to obtain carbon concentrate, the carbon concentrate is subjected to cyaniding to extract gold, silver and copper independently, so that the gold, silver and copper in the carbon concentrate are comprehensively recovered, the influence of the carbon mineral on the recovery of gold in the roasting and subsequent cyaniding processes is broken, and leaching residues of the carbon concentrate are subjected to non-waste and comprehensive treatment through a non-ferrous smelting production process; the method effectively combines low-temperature dearsenification, acid leaching treatment and high-temperature desulfurization of the carbon-selecting tailings, and solves the problems of incomplete roasting of arsenic minerals, and gold wrapping by metal oxides and sulfides in the conventional two-stage roasting process through granulation, low-temperature reduction roasting, fine grinding of roasted slag and acid leaching treatment, so that the maximum bare of gold is realized, the leaching rate of gold and silver in the cyanidation process is obviously improved, and the economic benefit is obvious.)

1. A method for step separation and comprehensive recovery of carbon and arsenic-containing gold concentrate is characterized by comprising the following steps:

1) first-stage pre-flotation decarburization: mixing carbon-containing arsenic gold concentrate and two-stage roasting cyanidation tailings, adjusting the concentration of ore pulp, adjusting the pH to be alkaline, adding sodium sulfite and kerosene, adding No. 2 oil, stirring, and scraping foam to obtain carbon concentrate by adopting a flotation process of primary roughing, secondary scavenging and tertiary concentration, wherein the product in a tank is carbon-concentration tailings;

2) and (3) high-concentration cyaniding leaching of the carbon concentrate to extract gold and silver: putting the carbon concentrate obtained in the step 1) into a cyaniding leaching device, controlling the concentration of ore pulp and the concentration of sodium cyanide, adjusting the cyaniding temperature and the cyaniding leaching time, recovering gold and silver from a leaching solution by adopting a zinc powder displacement process, recovering copper from a solution after recovering gold and silver by adopting an acidification precipitation process, and producing copper concentrate containing 10-50% of copper; the leached slag is used as fuel by a non-ferrous smelting production process, and metals such as gold, silver, lead and the like are comprehensively recovered by high-temperature smelting;

3) and (3) low-temperature dearsenifying of the carbon-selected tailings: adding water into the carbon-selecting tailings obtained in the step 2), granulating, controlling the temperature of a kiln head, the temperature of a kiln inside and the temperature of a kiln tail in a rotary kiln, controlling roasting time, and sending tail gas into a smelting flue gas acid-making production system to produce sulfuric acid after the flue gas is subjected to arsenic collection treatment by a cloth bag in the roasting process to obtain primary roasted sand;

4) primary calcine acid leaching treatment: grinding the primary calcine obtained in the step 3), adding lead nitrate in the grinding process, controlling the concentration of ore pulp and the acidity of initial sulfuric acid, adjusting the acid leaching temperature and the acid leaching time, performing filter pressing and dehydration after the acid leaching to obtain acid leaching residue, recovering and producing cathode copper products by using an extraction electrodeposition process for acid leaching liquid, and recycling the liquid after copper extraction after the copper extraction is treated by using a neutralization method;

5) high-temperature desulfurization of acid leaching residue in a rotary kiln: adding water into the acid leaching residues in the step 4), granulating, controlling the temperature of a kiln head, the temperature of a kiln inside and the temperature of a kiln tail in a rotary kiln, controlling roasting time, and sending smoke in the roasting process into a smelting smoke acid production system to produce sulfuric acid to obtain secondary roasted sand;

6) cyaniding and leaching gold and silver by secondary calcine: grinding the secondary calcine obtained in the step 5), adding sodium hexametaphosphate in the grinding process, controlling the concentration of the ore pulp in the leaching process, adjusting the pH, adding sodium cyanide, and recovering gold and silver from cyanide solution through a zinc powder replacement process; after cyanide leaching slag is treated by an acidification method and a sulfur dioxide method, the cyanide slag after harmless treatment meets the requirement of tailings pond treatment standard.

2. The method for step separation and comprehensive recovery of the carbon and arsenic-containing gold concentrate according to claim 1, wherein the mass ratio of the carbon and arsenic-containing gold concentrate to the two-stage roasting and cyaniding tailings in the step 1) is 1: 0.1-1: 0.5, mixing, wherein the concentration of the ore pulp is 10-19%, adjusting the PH value to 9-11 by lime, the using amount of sodium sulfite is 500-2000 g/t, the using amount of kerosene is 50-300 g/t, stirring for 10-30 minutes, then adding 50-200 g/t of No. 2 oil, and stirring for 3-5 minutes.

3. The method for step separation and comprehensive recovery of the carbon-arsenic-containing gold concentrate according to claim 1, wherein the flotation time in the step 1) is 10-40 minutes, and the main components of the carbon concentrate are 10-40% of carbon, 50-200 g/t of gold, 300-600 g/t of silver, 3-8% of sulfur, 5-8% of lead, 3-5% of copper and 0.30-1.00% of arsenic; the carbon-selecting tailings contain 0.2-0.4% of carbon, 20-50 g/t of gold, 10-30 g/t of silver, 0.1-0.4% of lead, 0.1-0.3% of copper, 20-40% of sulfur and 3-15% of arsenic.

4. The method for step separation and comprehensive recovery of the carbon-arsenic-containing gold concentrate according to claim 1, wherein in the step 2), the concentration of the ore pulp is 10-20%, the concentration of the sodium cyanide is 2-10%, the cyaniding temperature is 50-70 ℃, the cyaniding leaching time is 5-15 hours, and the leaching residue contains 10-40% of carbon, 5-20 g/t of gold, 30-60 g/t of silver, 3-8% of sulfur, 5-8% of lead, 0.2-0.5% of copper and 0.30-1.00% of arsenic.

5. The method for step separation and comprehensive recovery of the carbon-arsenic-containing gold concentrate according to claim 1, wherein the water is added in the step 3) in an amount of 5-10 wt%, the granulation granularity is 5-10 mm, the temperature of the kiln head is 400-450 ℃, the temperature in the kiln is 450-500 ℃, the temperature of the kiln tail is 500-550 ℃, the roasting time is 2-6 h, and the primary roasted product contains 0.05-0.1% of carbon, 30-80 g/t of gold, 20-60 g/t of silver, 0.2-0.8% of lead, 0.2-0.6% of copper, 15-28% of sulfur and 0.20-0.50% of arsenic.

6. The method for step separation and comprehensive recovery of the carbon-containing arsenic-containing gold concentrate according to claim 1, wherein the amount of lead nitrate used in the step 4) is 500-1500 g/t, the fineness of grinding is controlled to 90-95% by a-400 mesh, the concentration of ore pulp is 20-40%, the acidity of the initial sulfuric acid is 10-30%, the acid leaching temperature is 70-80 ℃, and the acid leaching time is 4-8 h.

7. The method for step separation and comprehensive recovery of the carbon-arsenic-containing gold concentrate according to claim 1, wherein the water is added in the step 5) in an amount of 5-10 wt%, the grain size of the granules is 5-10 mm, the temperature of the kiln head is 550-600 ℃, the temperature in the kiln is 600-650 ℃, the temperature of the kiln tail is 650-680 ℃, the roasting time is 2-6 h, the secondary calcine contains 0.05-0.1% of carbon, 50-120 g/t of gold, 40-100 g/t of silver, 0.4-1.6% of lead, 0.02-0.06% of copper, 0.2-0.5% of sulfur and 0.08-0.20% of arsenic.

8. The method for step separation and comprehensive recovery of the carbon-containing arsenic-containing gold concentrate according to claim 1, wherein the addition amount of the sodium hexametaphosphate in the step 6) is 500-1500 g/t, the fineness of the ground ore is controlled to 90-95 meshes, the concentration of the ore pulp is 20-50%, the pH value is adjusted to 7-8 by using soda ash, the addition rate of sodium cyanide is 0.3-0.5 kg/t per hour in the first 8 hours, the addition amount of the sodium cyanide is 0.2-0.4 kg/t per hour in the later period, and the cyaniding leaching time is 12-24 hours; the cyanide leaching residue contains 0.6-1.2 g/t of gold and 5-10 g/t of silver.

Technical Field

The invention belongs to the technical field of gold dressing and metallurgy, and particularly relates to a method for step separation and comprehensive recovery of carbon and arsenic-containing gold concentrate.

Background

Along with the large-scale exploitation of the world mineral resources, the treatment of the easily-treated gold mine resources is continuously reduced, the difficultly-treated gold mine becomes an important raw material for extracting gold in all countries in the world, and the proportion of the difficultly-treated gold mine in the crust accounts for 60 percent of the total amount of gold. Therefore, the research on the process technology for extracting gold from refractory gold ores has attracted attention from all countries in the world, and the research on the reasonable and efficient development and utilization technology of refractory gold ores has been the hot point of the research of all gold producing countries in the world.

The prospect reserves of the gold mine which is difficult to treat in China are considerable. The refractory metallurgical ore has complex properties, is difficult to treat, has various components, has different process requirements and even conflicts among different types of refractory metallurgical concentrate oxidizing and roasting processes, and has the problems of low utilization rate of valuable elements, low automation degree, high cost, serious environmental pollution and the like in the process of dressing and smelting.

The carbon-arsenic-containing gold concentrate belongs to a complex gold concentrate difficult to smelt, and the gold concentrate is characterized by containing elements such as carbon, arsenic and the like, the gold and silver are mainly wrapped by arsenopyrite, the recovery rate of gold and silver by adopting a conventional process is extremely low, when the carbon-arsenic-containing gold concentrate is treated by a two-section roasting system, although the temperature in a furnace meets the carbon combustion condition, because the carbon mineral is light in weight and is influenced by blast from the bottom of the furnace and negative pressure of the system, the carbon mineral is too short in retention time in the furnace and is easy to blow out of the furnace along with smoke dust, the decarburization rate of the two-section roasting system is not ideal, because unburned carbon has adsorbability, a large amount of adsorption can be formed on gold after entering a cyaniding system during cyaniding gold extraction, the recovery rate of gold in the cyaniding process is influenced, and a large amount of cyaniding tailings and arsenic-containing gypsum slag hazardous waste are produced in the production process, so that the current national environmental protection policy is not met; if a pyrometallurgical copper smelting process is adopted, the recovery rate of gold and silver is high, but a large amount of copper-containing materials are needed for ore blending, the arsenic content after ore blending has strict requirements, the quality of copper products is seriously affected once the arsenic exceeds the standard, a large amount of arsenic-containing hazardous waste is generated, and the treatment difficulty is high. At present, the conventional method for treating the carbon-containing arsenic gold concentrate can only enter a pyrometallurgical copper smelting system through a two-stage roasting and cyaniding process or a small amount of mixing, so that the cost is high, the time period is long, the working procedures are complicated, and the labor intensity is high. Therefore, a new process technology for comprehensively recovering valuable elements from carbon and arsenic-containing refractory gold concentrate is developed on the basis of technical integration and innovation, and a series of key technical problems of low comprehensive utilization rate of the valuable elements in the carbon and arsenic-containing gold concentrate are urgently solved.

Disclosure of Invention

According to the defects of the prior art, the invention aims to provide a method for step separation and comprehensive recovery of carbon and arsenic-containing gold concentrate, which overcomes the defects of poor decarburization and dearsenification boiling effects, re-wrapping of gold particles in the roasting process and low gold leaching rate in the process of treating the carbon and arsenic-containing gold concentrate by a two-section fluidized bed roaster.

In order to realize the purposes, the adopted specific technical scheme is as follows:

a method for step separation and comprehensive recovery of carbon-containing arsenic gold concentrate comprises the following steps:

1) first-stage pre-flotation decarburization: mixing carbon-containing arsenic gold concentrate and two-stage roasting cyanidation tailings, adjusting the concentration of ore pulp, adjusting the pH to be alkaline, adding sodium sulfite and kerosene, adding No. 2 oil, stirring, and scraping foam to obtain carbon concentrate by adopting a flotation process of primary roughing, secondary scavenging and tertiary concentration, wherein the product in a tank is carbon-concentration tailings;

2) and (3) high-concentration cyaniding leaching of the carbon concentrate to extract gold and silver: putting the carbon concentrate obtained in the step 1) into a cyaniding leaching device, controlling the concentration of ore pulp and the concentration of sodium cyanide, adjusting the cyaniding temperature and the cyaniding leaching time, recovering gold and silver from a leaching solution by adopting a zinc powder displacement process, recovering copper from a solution after recovering gold and silver by adopting an acidification precipitation process, and producing copper concentrate containing 10-50% of copper; the leached slag is used as fuel by a non-ferrous smelting production process, and metals such as gold, silver, lead and the like are comprehensively recovered by high-temperature smelting;

3) and (3) low-temperature dearsenifying of the carbon-selected tailings: adding water into the carbon-selecting tailings obtained in the step 2), granulating, controlling the temperature of a kiln head, the temperature of a kiln inside and the temperature of a kiln tail in a rotary kiln, controlling roasting time, and sending tail gas into a smelting flue gas acid-making production system to produce sulfuric acid after the flue gas is subjected to arsenic collection treatment by a cloth bag in the roasting process to obtain primary roasted sand;

4) primary calcine acid leaching treatment: grinding the primary calcine obtained in the step 3), adding lead nitrate in the grinding process, controlling the concentration of ore pulp and the acidity of initial sulfuric acid, adjusting the acid leaching temperature and the acid leaching time, performing filter pressing and dehydration after the acid leaching to obtain acid leaching residue, recovering and producing cathode copper products by using an extraction electrodeposition process for acid leaching liquid, and recycling the liquid after copper extraction after the copper extraction is treated by using a neutralization method;

5) high-temperature desulfurization of acid leaching residue in a rotary kiln: adding water into the acid leaching residues in the step 4), granulating, controlling the temperature of a kiln head, the temperature of a kiln inside and the temperature of a kiln tail in a rotary kiln, controlling roasting time, and sending smoke in the roasting process into a smelting smoke acid production system to produce sulfuric acid to obtain secondary roasted sand;

6) cyaniding and leaching gold and silver by secondary calcine: grinding the secondary calcine obtained in the step 5), adding sodium hexametaphosphate in the grinding process, controlling the concentration of the ore pulp in the leaching process, adjusting the pH, adding sodium cyanide, and recovering gold and silver from cyanide solution through a zinc powder replacement process; after cyanide leaching slag is treated by an acidification method and a sulfur dioxide method, the cyanide slag after harmless treatment meets the requirement of tailings pond treatment standard.

Further, the mass ratio of the carbon-containing arsenic gold concentrate to the two-stage roasting cyanidation tailings in the step 1) is 1: 0.1-1: 0.5, mixing, wherein the concentration of the ore pulp is 10-19%, adjusting the PH value to 9-11 by lime, the using amount of sodium sulfite is 500-2000 g/t, the using amount of kerosene is 50-300 g/t, stirring for 10-30 minutes, then adding 50-200 g/t of No. 2 oil, and stirring for 3-5 minutes.

Further, the flotation time in the step 1) is 10-40 minutes, and the main components of the carbon concentrate are 10% -40% of carbon, 50-200 g/t of gold, 300-600 g/t of silver, 3-8% of sulfur, 5-8% of lead, 3-5% of copper and 0.30-1.00% of arsenic; the carbon-selecting tailings contain 0.2-0.4% of carbon, 20-50 g/t of gold, 10-30 g/t of silver, 0.1-0.4% of lead, 0.1-0.3% of copper, 20-40% of sulfur and 3-15% of arsenic.

Further, in the step 2), the concentration of the ore pulp is 10-20%, the concentration of sodium cyanide is 2-10%, the cyaniding temperature is 50-70 ℃, the cyaniding leaching time is 5-15 hours, and the leached slag contains 10-40% of carbon, 5-20 g/t of gold, 30-60 g/t of silver, 3-8% of sulfur, 5-8% of lead, 0.2-0.5% of copper and 0.30-1.00% of arsenic.

Further, in the step 3), the addition amount of water is 5-10 wt%, the particle size of the granules is 5-10 mm, the temperature of the kiln head is 400-450 ℃, the temperature of the kiln is 450-500 ℃, the temperature of the kiln tail is 500-550 ℃, the roasting time is 2-6 h, the primary calcine contains 0.05-0.1% of carbon, 30-80 g/t of gold, 20-60 g/t of silver, 0.2-0.8% of lead, 0.2-0.6% of copper, 15-28% of sulfur and 0.20-0.50% of arsenic.

Further, in the step 4), the using amount of the lead nitrate is 500-1500 g/t, the fineness of ground ore is controlled to be 90-95% in a 400-mesh mode, the concentration of ore pulp is 20-40%, the acidity of the initial sulfuric acid is 10-30%, the acid leaching temperature is 70-80 ℃, and the acid leaching time is 4-8 hours.

Further, in the step 5), the addition amount of water is 5-10 wt%, the particle size of the granules is 5-10 mm, the temperature of the kiln head is 550-600 ℃, the temperature of the kiln is 600-650 ℃, the temperature of the kiln tail is 650-680 ℃, the roasting time is 2-6 h, the secondary calcine contains 0.05-0.1% of carbon, 50-120 g/t of gold, 40-100 g/t of silver, 0.4-1.6% of lead, 0.02-0.06% of copper, 0.2-0.5% of sulfur and 0.08-0.20% of arsenic.

Further, the addition amount of the sodium hexametaphosphate in the step 6) is 500-1500 g/t, the fineness-400 meshes of the ground ore is controlled to be 90-95%, the concentration of the ore pulp is 20-50%, the PH value is adjusted to be 7-8 by adopting soda ash, the addition rate of sodium cyanide is in the first 8 hours, the addition amount per hour is 0.3-0.5 kg/t, the addition amount per hour is 0.2-0.4 kg/t in the later period, and the cyaniding leaching time is 12-24 hours; the cyanide leaching residue contains 0.6-1.2 g/t of gold and 5-10 g/t of silver.

Compared with the prior art, the invention has the beneficial effects that:

(1) the flotation process and the smelting process are effectively combined, the carbon-arsenic-containing gold concentrate is subjected to pre-flotation to obtain carbon concentrate, the carbon concentrate is subjected to cyaniding to extract gold, silver and copper independently, so that the gold, silver and copper in the carbon concentrate are comprehensively recovered, the influence of the carbon mineral on the recovery of gold in the roasting and subsequent cyaniding processes is broken, and leaching residues of the carbon concentrate are subjected to non-waste and comprehensive treatment through a non-ferrous smelting production process.

(2) The method effectively combines low-temperature dearsenification, acid leaching treatment and high-temperature desulfurization of the carbon-selecting tailings, and solves the problems of incomplete roasting of arsenic minerals, and gold wrapping by metal oxides and sulfides in the conventional two-stage roasting process through granulation, low-temperature reduction roasting, fine grinding of roasted slag and acid leaching treatment, so that the maximum bare of gold is realized, the leaching rate of gold and silver in the cyanidation process is obviously improved, and the economic benefit is obvious.

(3) The method has the advantages of simple technical conditions, convenient operation and environment-friendly operation, realizes the step comprehensive recovery of carbon, gold, silver, copper, arsenic and sulfur in the carbon-arsenic-containing gold concentrate, belongs to clean production in the whole process, does not generate waste gas and waste water, and has good environmental protection benefit.

Detailed Description

The present invention is described below with reference to examples, which are provided for illustration only and are not intended to limit the scope of the present invention.

Example 1

1) First-stage pre-flotation decarburization: mixing carbon-containing arsenical gold concentrate and two-stage roasting cyanidation tailings in a mass ratio of 1:0.1, adjusting the concentration of ore pulp to 10%, adjusting the pH value to 9 by using lime, adjusting the using amount of sodium sulfite to 500g/t and adjusting the using amount of kerosene to 50g/t, stirring for 10 minutes, adding 50g/t of 2# oil, stirring for 3 minutes, carrying out flotation for 10 minutes, adopting a primary roughing, secondary scavenging and tertiary concentration flotation flow to scrape out foam to obtain carbon concentrate, wherein the main components of the carbon concentrate comprise 10% of carbon, 50g/t of gold, 300g/t of silver, 3% of sulfur, 5% of lead, 3% of copper and 0.30% of arsenic; the product in the tank is carbon-selecting tailings containing 0.2% of carbon, 20g/t of gold, 10g/t of silver, 0.1% of lead, 0.1% of copper, 20% of sulfur and 3% of arsenic;

2) and (3) high-concentration cyaniding leaching of the carbon concentrate to extract gold and silver: putting the carbon concentrate obtained in the step 1) into a cyanidation leaching device, controlling the concentration of ore pulp to be 10%, the concentration of sodium cyanide to be 2%, the cyanidation temperature to be 50 ℃ and the cyanidation leaching time to be 5 hours, recovering gold and silver from a leaching solution by adopting a zinc powder replacement process, recovering copper from a solution after recovering the gold and silver by adopting an acidification precipitation process, and producing copper concentrate containing 10% of copper; the leached slag contains 10% of carbon, 5g/t of gold, 30g/t of silver, 3% of sulfur, 5% of lead, 0.2% of copper and 0.30% of arsenic, the leached slag is used as fuel by a nonferrous smelting production process, and metals such as gold, silver, lead and the like are comprehensively recovered by high-temperature smelting;

3) and (3) low-temperature dearsenifying of the carbon-selected tailings: adding 5% of water into the carbon-selecting tailings obtained in the step 1), granulating by using a disc granulator to obtain granules with the granularity of 5mm, controlling the temperature of a kiln head to be 400 ℃, the temperature in the kiln to be 450 ℃, the temperature of a kiln tail to be 500 ℃ and roasting time to be 2h in an external heating rotary kiln, wherein flue gas in the roasting process is subjected to arsenic collection treatment by a cloth bag in advance, and then the tail gas is sent into a smelting flue gas acid production system to produce sulfuric acid, wherein primary roasted sand contains 0.05% of carbon, 30g/t of gold, 20g/t of silver, 0.2% of lead, 0.2% of copper, 15% of sulfur and 0.20% of arsenic;

4) primary calcine acid leaching treatment: grinding the primary calcine obtained in the step 3) by using a ceramsite grinding machine, adding 500g/t of lead nitrate in the grinding process, controlling the grinding fineness to be 90 percent with-400 meshes, controlling the ore pulp concentration to be 20 percent, controlling the initial acidity of sulfuric acid to be 10 percent, controlling the acid leaching temperature to be 70 ℃, and carrying out acid leaching for 4 hours, after the acid leaching is finished, carrying out filter pressing and dehydration by using an anticorrosive filter press to obtain acid leaching residue, recovering and producing a cathode copper product by using an extraction electrodeposition process for the acid leaching solution, and recycling the copper-extracted solution after treatment by using a neutralization method;

5) high-temperature desulfurization of acid leaching residue in a rotary kiln: adding 5% of proper amount of water into the acid leaching residue obtained in the step 4), granulating by adopting a disc granulator to obtain granules with the granularity of 5mm, controlling the temperature of a kiln head to be 550 ℃, the temperature of the kiln to be 600 ℃, the temperature of a kiln tail to be 650 ℃ and roasting time to be 2h in an external heating type rotary kiln, sending flue gas generated in the roasting process into a smelting flue gas acid production system to produce sulfuric acid, wherein secondary calcine contains 0.05% of carbon, 50g/t of gold, 40g/t of silver, 0.4% of lead, 0.02% of copper, 0.2% of sulfur and 0.08% of arsenic;

6) cyaniding and leaching gold and silver by secondary calcine: grinding the secondary calcine obtained in the step 5) by using a ceramsite grinding machine, adding 500g/t of sodium hexametaphosphate in the grinding process, controlling the grinding fineness to be 90 percent by a 400-mesh sieve, controlling the ore pulp concentration to be 20 percent in the leaching process, adjusting the pH to be 7 by using soda ash, controlling the adding speed of sodium cyanide to be 8h at the early stage, adding the sodium cyanide to be 0.3kg/t per hour, adding the sodium cyanide to be 0.2kg/t per hour at the later stage, and carrying out cyaniding leaching for 12 h; recovering gold and silver from cyanide solution by zinc powder replacement process; the cyanide leaching residue contains 0.6g/t of gold and 5g/t of silver, and after the cyanide leaching residue is treated by an acidification method and a sulfur dioxide method, the cyanide residue after harmless treatment meets the requirements of tailings pond disposal standard of HJ 943-2018 & lt & gt gold industry cyanide residue pollution control technical Specification & gt.

Example 2

1) First-stage pre-flotation decarburization: mixing carbon-containing arsenical gold concentrate and two-stage roasting cyanidation tailings in a mass ratio of 1:0.3, adjusting the concentration of ore pulp to 15%, adjusting the pH value to 10 by using lime, adjusting the using amount of sodium sulfite to 1250g/t and the using amount of kerosene to 175g/t, stirring for 20 minutes, adding No. 2 oil to 125g/t, stirring for 4 minutes, carrying out flotation for 25 minutes, adopting a primary roughing, secondary scavenging and tertiary concentration flotation process, scraping out foam to obtain carbon concentrate, wherein the main components of the carbon concentrate comprise 25% of carbon, 125g/t of gold, 450g/t of silver, 5.5% of sulfur, 6.5% of lead, 4% of copper and 0.65% of arsenic; the product in the tank is carbon-dressing tailings containing 0.3% of carbon, 35g/t of gold, 20g/t of silver, 0.25% of lead, 0.2% of copper, 30% of sulfur and 9% of arsenic;

2) and (3) high-concentration cyaniding leaching of the carbon concentrate to extract gold and silver: putting the carbon concentrate obtained in the step 1) into a cyanidation leaching device, controlling the concentration of ore pulp to be 15%, the concentration of sodium cyanide to be 6%, the cyanidation temperature to be 60 ℃, the cyanidation leaching time to be 10 hours, recovering gold and silver from a leaching solution by adopting a zinc powder replacement process, recovering copper from a solution after recovering the gold and silver by adopting an acidification precipitation process, and producing copper concentrate containing 30% of copper; the leached slag contains 25% of carbon, 12.5g/t of gold, 45g/t of silver, 5.5% of sulfur, 6.5% of lead, 0.35% of copper and 0.65% of arsenic, the leached slag is used as fuel by a non-ferrous smelting production process, and metals such as gold, silver, lead and the like are comprehensively recovered by high-temperature smelting;

3) and (3) low-temperature dearsenifying of the carbon-selected tailings: adding 7.5% of a proper amount of water into the carbon-selecting tailings obtained in the step 1), granulating by using a disc granulator to obtain granules with the granularity of 7.5mm, controlling the temperature of a kiln head to be 425 ℃, the temperature of a kiln to be 475 ℃, the temperature of a kiln tail to be 525 ℃ and the roasting time to be 4 hours in an external heating type rotary kiln, wherein flue gas is subjected to arsenic collection treatment by a cloth bag in advance in the roasting process, tail gas is sent into a flue gas smelting acid production system to produce sulfuric acid, and primary roasted sand contains 0.08% of carbon, 55g/t of gold, 40g/t of silver, 0.5% of lead, 0.4% of copper, 21.5% of sulfur and 0.35% of arsenic;

4) primary calcine acid leaching treatment: grinding the primary calcine obtained in the step 3) by using a ceramsite grinding machine, adding 1000g/t of lead nitrate in the grinding process, controlling the grinding fineness to be 400 meshes, controlling the ore pulp concentration to be 30%, controlling the initial sulfuric acid acidity to be 20%, carrying out acid leaching at the temperature of 75 ℃, and carrying out acid leaching for 6 hours, after the acid leaching is finished, carrying out filter pressing and dehydration by using an anticorrosive filter press to obtain acid leaching residue, recovering and producing a cathode copper product by using an extraction electrodeposition process for acid leaching solution, and recycling the copper-extracted solution after treatment by using a neutralization method;

5) high-temperature desulfurization of acid leaching residue in a rotary kiln: adding 7.5% of proper amount of water into the acid leaching residue obtained in the step 4), granulating by adopting a disc granulator to obtain granules with the granularity of 7.5mm, controlling the temperature of a kiln head in an external heating type rotary kiln at 575 ℃, controlling the temperature in the kiln at 625 ℃, controlling the temperature of a kiln tail at 665 ℃ and roasting for 4 hours, sending flue gas generated in the roasting process into a smelting flue gas acid production system to produce sulfuric acid, wherein secondary roasted sand contains 0.08% of carbon, 85g/t of gold, 70g/t of silver, 1.0% of lead, 0.04% of copper, 0.35% of sulfur and 0.14% of arsenic;

6) cyaniding and leaching gold and silver by secondary calcine: grinding the secondary calcine obtained in the step 5) by using a ceramsite grinding machine, adding 1000g/t of sodium hexametaphosphate in the grinding process, controlling the grinding fineness to be 400 meshes to be 92.5%, controlling the ore pulp concentration in the leaching process to be 35%, adjusting the pH to be 7.5 by using soda ash, adjusting the adding speed of sodium cyanide to be 8h at the early stage, adding the amount of sodium cyanide to be 0.4kg/t per hour, adding the amount of sodium cyanide to be 0.3kg/t per hour at the later stage, and carrying out cyaniding leaching for 18 h; recovering gold and silver from cyanide solution by zinc powder replacement process; the cyanide leaching residue contains 0.9g/t of gold and 7.5g/t of silver, and after the cyanide leaching residue is treated by an acidification method and a sulfur dioxide method, the cyanide residue after harmless treatment meets the requirements of tailings pond treatment standard of HJ 943-2018 & lt gold industry & gt technical Specification for pollution control of cyanide residue.

Example 3

1) First-stage pre-flotation decarburization: mixing carbon-containing arsenic gold concentrate and two-stage roasting cyanidation tailings in a mass ratio of 1: 0.5, adjusting the concentration of the ore pulp to 19%, adjusting the pH value to 11 by lime, adjusting the dosage of sodium sulfite to 2000g/t and the dosage of kerosene to 300g/t, stirring for 30 minutes, adding 200g/t of 2# oil, stirring for 5 minutes, performing flotation for 40 minutes, performing primary roughing, secondary scavenging and tertiary concentration flotation, scraping out foam to obtain a carbon concentrate, wherein the main components of the carbon concentrate comprise 40% of carbon, 200g/t of gold, 600g/t of silver, 8% of sulfur, 8% of lead, 5% of copper and 1.00% of arsenic, and performing next treatment; the product in the tank is carbon-dressing tailings containing 0.4% of carbon, 50g/t of gold, 30g/t of silver, 0.4% of lead, 0.3% of copper, 40% of sulfur and 15% of arsenic.

2) And (3) high-concentration cyaniding leaching of the carbon concentrate to extract gold and silver: putting the carbon concentrate obtained in the step 1) into a cyanidation leaching device, controlling the concentration of ore pulp to be 20%, the concentration of sodium cyanide to be 10%, the cyanidation temperature to be 70 ℃, the cyanidation leaching time to be 15h, recovering gold and silver from a leaching solution by adopting a zinc powder replacement process, recovering copper from a solution after recovering the gold and silver by adopting an acidification precipitation process, and producing copper concentrate containing 50% of copper; the leached slag contains 40% of carbon, 20g/t of gold, 60g/t of silver, 8% of sulfur, 8% of lead, 0.5% of copper and 1.00% of arsenic, the leached slag is used as fuel by a nonferrous smelting production process, and metals such as gold, silver, lead and the like are comprehensively recovered by high-temperature smelting;

3) and (3) low-temperature dearsenifying of the carbon-selected tailings: adding 10% of appropriate amount of water into the carbon-selecting tailings obtained in the step 1), granulating by using a disc granulator to obtain granules with the granularity of 10mm, controlling the temperature of a kiln head to be 450 ℃, the temperature of the kiln to be 500 ℃, the temperature of a kiln tail to be 550 ℃ and the roasting time to be 6h in an external heating type rotary kiln, wherein flue gas in the roasting process is subjected to arsenic collection treatment by a cloth bag in advance, and then the tail gas is sent into a smelting flue gas acid production system to produce sulfuric acid, wherein primary roasted sand contains 0.1% of carbon, 80g/t of gold, 60g/t of silver, 0.8% of lead, 0.6% of copper, 28% of sulfur and 0.50% of arsenic;

4) primary calcine acid leaching treatment: grinding the primary calcine obtained in the step 3) by using a ceramsite grinding machine, adding 1500g/t of lead nitrate in the grinding process, controlling the grinding fineness to be 95 percent with-400 meshes, controlling the concentration of ore pulp to be 40 percent, controlling the initial acidity of sulfuric acid to be 30 percent, controlling the acid leaching temperature to be 80 ℃, and carrying out acid leaching for 8 hours;

5) high-temperature desulfurization of acid leaching residue in a rotary kiln: adding 10% of proper amount of water into the acid leaching residue obtained in the step 4), granulating by adopting a disc granulator to obtain granules with the granularity of 10mm, controlling the temperature of a kiln head to be 600 ℃, the temperature of a kiln to be 650 ℃, the temperature of a kiln tail to be 680 ℃ and roasting time to be 6h in an external heating type rotary kiln, sending flue gas generated in the roasting process into a smelting flue gas acid production system to produce sulfuric acid, wherein secondary calcine contains 0.1% of carbon, 120g/t of gold, 100g/t of silver, 1.6% of lead, 0.06% of copper, 0.5% of sulfur and 0.20% of arsenic;

6) cyaniding and leaching gold and silver by secondary calcine: grinding the secondary calcine obtained in the step 5) by using a ceramsite grinding machine, adding 1500g/t of sodium hexametaphosphate in the grinding process, controlling the grinding fineness to be 95 percent by 400 meshes, controlling the ore pulp concentration to be 50 percent in the leaching process, adjusting the pH value to be 8 by using soda ash, wherein the adding speed of sodium cyanide is in the previous 8h, the adding amount of the sodium cyanide is 0.5kg/t per hour, the adding amount of the sodium cyanide is 0.4kg/t per hour in the later stage, and the cyaniding leaching time is 24 h; recovering gold and silver from cyanide solution by zinc powder replacement process; cyanide leaching residue contains 1.2g/t of gold and 10g/t of silver, and after the cyanide leaching residue is treated by an acidification method and a sulfur dioxide method, the cyanide residue after harmless treatment meets the requirements of tailings pond disposal standard of HJ 943-2018 & lt & gt gold industry cyanide residue pollution control technical Specification & gt.

The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, but rather as the subject matter of the invention is to be construed in all aspects and as broadly as possible, and all changes, equivalents and modifications that fall within the true spirit and scope of the invention are therefore intended to be embraced therein.