CN113737012A - Method for co-roasting treatment of neutralized waste residues and lead-containing gold concentrate - Google Patents
Method for co-roasting treatment of neutralized waste residues and lead-containing gold concentrate Download PDFInfo
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Abstract
The invention relates to a method for co-roasting treatment of neutralized waste residues and lead-containing gold concentrate, which comprises the following steps: 1) neutralizing and outputting waste residues; 2) mixing the lead-containing gold concentrate and the neutralized waste residues, and grinding; 3) neutralizing waste residues and mixing slurry; 4) boiling and roasting to prepare acid; 5) acid leaching and leaching the calcine; 6) leaching the gold and silver. Wherein, the pickle liquor of the step 5) is processed to obtain copper and zinc concentrate; flue gas generated by roasting in the step 4) is used for producing sulfuric acid, and is recycled in the step 1). The sulfuric acid in the acid making process is used for decyanation treatment of cyanidation tailings, and the neutralization waste residue containing multiple metals and the lead-containing gold concentrate produced in the process are roasted cooperatively, so that the fluidized roasting effect is adjusted and optimized to the maximum extent, the fluidized roasting requirement is met, the production stability is improved, sintering, ore particle bonding and gold and silver wrapping in the roasting process of the lead-containing gold concentrate are eliminated, the roasting quality of the gold concentrate is improved, the recovery rate of the gold and silver is improved, and the cooperative roasting treatment and safe treatment of the neutralization waste residue and the lead-containing gold concentrate are realized.
Description
Technical Field
The invention relates to a method for treating pollutants and lead-containing gold concentrate in the technical field of environmental protection, in particular to a method for co-roasting treatment of neutralized waste residues and lead-containing gold concentrate.
Background
Cyaniding gold extraction technology is often adopted in the production process of gold mines. The cyaniding gold extraction process comprises a direct cyaniding gold extraction process and a roasting cyaniding gold extraction process, and both processes generate a large amount of cyaniding tailings after gold extraction, and the cyaniding tailings contain a large amount of pollutants such as sulfur, copper, arsenic, mercury and extremely toxic cyanides.
The cyanidation tailings are listed as HW33 hazardous wastes in the national records of hazardous wastes, have obvious pollution characteristics and serious pollution, and the environmental protection pressure of the country and enterprises is increased sharply, so that a feasible control technology is urgently needed to eliminate the harm of the hazardous wastes to the environment.
At present, the technology for treating cyanidation tailings mainly adopts a flotation method and is supplemented with an evaporation pressure method, a chlorination roasting method, a molten salt roasting method, a reduction roasting method, an oxidation method, a solidification method, silicate cement preparation and the like. The flotation method is mostly carried out under an acidic condition, sulfuric acid is used as a main acidifying agent, and waste water after acidification is treated by a lime neutralization method to generate neutralized waste residues containing a large amount of calcium sulfate, wherein the waste residues also contain elements such as copper, iron, lead, zinc, arsenic and the like. The neutralized waste residues are not processed effectively, and can be disposed only by stacking or direct landfill. Therefore, a large amount of land resources are occupied, surface water, underground water, soil and the like can be polluted, and great potential safety hazards and potential environmental protection hazards are generated to the surrounding environment. Therefore, the harmless treatment of the neutralization waste slag is an important technical challenge problem to be solved urgently by gold smelting enterprises and non-ferrous smelting enterprises.
Meanwhile, a boiling roasting process is mostly adopted in gold smelting enterprises to treat multi-metal complex gold concentrate, but when gold concentrate with lead content of about 2 wt% is treated, sintering and ore particle bonding phenomena occur in the boiling roasting process, so that the boiling state effect is poor, the roasting quality of the gold concentrate is poor, the leaching rate of gold and silver is low, the production stability fluctuates, and even furnace burden accumulation and difficult discharge occur in the roasting process, so that the serious consequence of furnace quenching is caused. When the lead content of the gold concentrate is more than 5 wt%, the gold concentrate is difficult to directly treat by a roasting and cyaniding process. Therefore, the method is a technical problem to be solved for improving the boiling roasting efficient treatment and the production index stability of the lead-containing gold concentrate.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a method for the synergistic roasting treatment of the neutralized waste residues and the lead-containing gold concentrate, so that valuable elements in the neutralized waste residues are effectively utilized, the production operation stability of the roasting treatment of the lead-containing gold concentrate is improved, and the leaching rate of gold and silver in subsequent cyanidation production is improved.
The invention provides a method for co-roasting treatment of neutralized waste residues and lead-containing gold concentrate, which comprises the following steps:
1) and (3) output of neutralization waste residues: mixing and stirring sulfuric acid and cyanidation tailings in a stirring tank according to a certain proportion, performing concentration treatment after stirring reaction to obtain decyanation tailings and acidic wastewater, treating the acidic wastewater by adopting a lime neutralization method, and producing neutralized waste residues through filter pressing;
2) mixing and grinding lead-containing gold concentrate and neutralized waste residues: mixing lead-containing gold concentrate and neutralized waste residues in proportion, adding water for size mixing, and grinding after size mixing to obtain ore pulp;
3) neutralizing waste residues and mixing slurry: adding water into the neutralized waste residues for size mixing treatment to obtain slurry;
4) boiling roasting to prepare acid: conveying the ore pulp obtained in the step 2) to a fluidized bed roaster for roasting, conveying the slurry obtained in the step 3) to the roaster during roasting, adjusting and stabilizing the temperature during roasting and the boiling state of materials in the roaster, and roasting to obtain roasted sand;
5) acid leaching of calcine: adding dilute sulfuric acid and hydrogen peroxide into the calcine to carry out acid leaching treatment, controlling the pH value to be 1-2 at the end point of the reaction, and carrying out liquid-solid separation after the reaction is finished to obtain solid acid leaching residue and acid leaching liquid;
6) leaching gold and silver: adjusting the pH value of the solid acid leaching residue obtained in the step 5) to 7-9, grinding, leaching with cyanide to obtain a leaching solution, and purifying and replacing the leaching solution with pregnant solution, and smelting gold and silver to obtain gold and silver products.
The mechanism and thought of the method for the synergistic roasting treatment of the neutralized waste residues and the lead-containing gold concentrate are as follows:
the waste sulfuric acid in the acid making process is firstly used for decyanation treatment of cyanidation tailings, and the lead-containing gold concentrate and the neutralized residues produced in the process are proportionally mixed, so that ore grinding meets the requirements of fluidized roasting.
In the boiling roasting process, the single input of the neutralized waste residue slurry is innovatively implemented, the boiling roasting effect is maximally adjusted and optimized, and the roasted product is subjected to acid leaching, gold and silver leaching and smelting. Meanwhile, the neutralized waste residues are used as a roasting stabilizing additive for roasting the lead-containing gold concentrate, so that the production stability is improved, sintering in the roasting process of the lead-containing gold concentrate and coating of gold and silver are eliminated, and the recovery rate of the gold and silver is improved, so that the synergistic roasting treatment and safe treatment of the neutralized waste residues and the lead-containing gold concentrate are realized.
The method for the synergistic roasting treatment of the neutralized waste residues and the lead-containing gold concentrate has the beneficial effects that:
sulfuric acid in the acid making process is used for decyanation treatment of cyanidation tailings, and neutralization waste residues containing multiple metals and lead-containing gold concentrate produced in the process are roasted in a synergistic manner, so that the boiling roasting effect is adjusted and optimized to the maximum extent, the boiling roasting requirement is met, the production stability is improved, sintering, bonding ore grains and gold and silver wrapping in the roasting process of the lead-containing gold concentrate are eliminated, the roasting quality of the gold concentrate is improved, the recovery rate of the gold and silver is improved, and the synergistic roasting treatment and safety treatment of the neutralization waste residues and the lead-containing gold concentrate are realized.
Further, the pickle liquor obtained in the step 5) is processed by an extraction electrodeposition process and a vulcanization process to respectively obtain 1# cathode copper and zinc concentrate.
The further technical characteristics have the following technical effects: and recovering copper and zinc in the neutralized waste residue.
Further, the flue gas generated in the roasting process in the step 4 is subjected to sulfuric acid production, and is recycled in the step 1) and the waste residue output process.
The further technical characteristics have the following technical effects: the roasted sulfuric acid is synchronously produced and comprehensively utilized circularly.
Further, the concentration of the sulfuric acid in the step 1) is 10-30 wt%, and the mixing ratio of the sulfuric acid to the cyanidation tailings is (1-5): 1;
the further technical characteristics have the following technical effects: in the acid making process after roasting, waste sulfuric acid with the sulfuric acid concentration of 10-30 wt% is produced in the wet flue gas purification process and is matched with the waste sulfuric acid, and the redundant acid concentration adjustment process is not required; the proper mixing proportion of the sulfuric acid and the cyaniding tailings is beneficial to the decyanation treatment of the cyaniding tailings.
Further, in the step 1), the temperature is 50-80 ℃, the stirring speed is 50-200r/min, and the aeration quantity is 50-150m3Stirring for 4-6 h;
further, the concentration treatment in the step 1) is carried out by a concentrator, the underflow is dehydrated by a filter press to obtain decyanation tailings, and the overflow is acidic wastewater;
the further technical characteristics have the following technical effects: is more beneficial to the decyanation treatment of the cyanidation tailings.
Further, the lead content of the gold concentrate in the step 2) is 5-10 wt%, the adding proportion of the neutralized waste residues is 1-5 wt% of the mass of the lead-containing gold concentrate, and the pulp mixing concentration is 65-75 wt%;
the further technical characteristics have the following technical effects: the lead-containing gold concentrate and the neutralized waste slag are proportionally mixed and subjected to size mixing concentration, so that ore grinding meets the requirements of fluidized roasting.
Further, grinding the ore by adopting a ball mill in the step 2), wherein the grinding time is 20-40 minutes;
the further technical characteristics have the following technical effects: the ball mill is more beneficial to grinding the mixture of the lead-containing gold concentrate and the neutralized waste residue, so that the ground ore meets the requirements of fluidized roasting.
Further, the concentration of the slurry in the step 3) is 30-50 wt%, and the stirring time is 4-6 h;
the further technical characteristics have the following technical effects: the method is more beneficial to the independent input of the neutralization waste residue slurry in the boiling roasting process, and the boiling roasting effect is maximally adjusted and optimized.
Further, in the step 4), the roasting temperature is 560-620 ℃, and the air volume is controlled to 8000-3The roasting time is 3-5 h;
the further technical characteristics have the following technical effects: the proper roasting temperature, air quantity and roasting time are favorable for preventing the phenomena of sintering and ore particle bonding in the boiling roasting process, improving the boiling state effect, improving the roasting quality of gold concentrate, the leaching rate of gold and silver, stable production and the like.
Further, the slurry conveying amount in the step 4) is 0.5-3 t/h;
the further technical characteristics have the following technical effects: the proper slurry conveying amount is beneficial to exerting the effect of neutralizing waste residues as a roasting stabilizing additive for roasting the lead-containing gold concentrate, the production stability is improved, sintering and coating of gold and silver in the roasting process of the lead-containing gold concentrate are eliminated, and the recovery rate of the gold and the silver is improved.
Further, dilute sulfuric acid and hydrogen peroxide are adopted in the step 5) for calcine acid leaching;
further, in the step 5), the concentration of the initial sulfuric acid is 50-100 g/L, the addition amount of hydrogen peroxide is 5-10 kg per ton of the calcine, the liquid-solid mass ratio is (2-5): 1, the stirring speed is 20-40 r/min, and the reaction time is controlled to be 4-6 hours;
the further technical characteristics have the following technical effects: is favorable for improving the leaching rate of the gold and silver in the calcine.
Further, adjusting the pH value of the solid acid leaching residue in the step 6) by adopting ammonia water;
further, a wet ball mill is adopted during ore grinding in the step 6), sodium hexametaphosphate is used as a grinding aid, and the using amount is 3-5 kg/t;
further, the fineness of the ground ore in the step 6), namely 400 meshes, accounts for 90-95 wt%;
further, in the step 6), the concentration of cyanide is 0.20-0.50 wt%, and the air volume is 60-80m3And/h, the leaching time is 36-72 h.
The further technical characteristics have the following technical effects: is beneficial to the extraction of gold and silver products.
Detailed Description
The principles and features of this invention are described below in conjunction with examples, which are set forth to illustrate, but are not to be construed to limit the scope of the invention.
Specific example 1:
1) mixing waste sulfuric acid with the sulfuric acid concentration of 10 wt% generated in the roasting acid making process and cyanidation tailings in a stirring tank according to the liquid-solid mass ratio of 1:1, wherein the temperature is 50 ℃, the stirring speed is 50r/min, and the aeration quantity is 50m3The stirring time is 4 hours, the mixture enters a thickener after the stirring reaction, the underflow is dehydrated by a filter press to obtain decyanation tailings, the overflow is acid wastewater, the acid wastewater is treated by a lime neutralization method, and neutralized waste residues containing 0.5 wt% of copper, 0.1 wt% of lead, 0.3 wt% of zinc, 5 wt% of iron and 0.5 wt% of arsenic are obtained after the filter pressing;
2) preparing gold concentrate containing 5 wt% of lead, adding neutralization waste residues, wherein the adding proportion of the neutralization waste residues is 1 wt%, mixing, feeding into a stirring tank, adding water for size mixing, the size mixing concentration is 65 wt%, feeding into a ball mill for ore grinding for 20 minutes, and feeding into an ore pulp storage tank after ore grinding;
3) independently mixing the neutralized waste residues, adding water into the neutralized waste residues in a mixing and stirring tank, adjusting the concentration of slurry to be 30 wt%, and stirring for 4 hours;
4) conveying the ore pulp obtained by adding the neutralization waste residues in the step 2) to a fluidized bed roaster through a conveying pump, wherein the roasting temperature is 560 ℃, and the air volume is controlled to be 8000m3The roasting time is 3 hours, in the roasting process, the slurry obtained by independently pulping the neutralized waste residues in the step 3) is conveyed to a roasting furnace through a conveying pump, the conveying capacity of the slurry is 0.5t/h, the temperature in the roasting process and the boiling state of materials in the furnace are adjusted and stabilized, and the roasted sand obtained after roasting is subjected to next treatment;
wherein, the flue gas generated by roasting enters sulfuric acid production, wherein waste sulfuric acid with the sulfuric acid concentration of 10 wt% is generated in the wet purification process of the flue gas and is recycled in the step 1) and waste residue generation process;
5) conveying the roasted product obtained after roasting to an acid leaching stirring tank by a scraper conveyor, adding dilute sulfuric acid and hydrogen peroxide, wherein the initial sulfuric acid concentration is 50g/L, the hydrogen peroxide addition amount is 5kg/t, the liquid-solid mass ratio in the acid leaching process is 2:1, the stirring speed is 20r/min, the reaction time is controlled for 4 hours, the pH value is controlled to be 1 at the reaction end point, liquid-solid separation is carried out after the reaction is finished, the solid residue is acid leaching residue containing gold and silver, and the liquid is acid leaching solution containing copper and zinc;
respectively obtaining 1# cathode copper and zinc concentrate with zinc grade of 58 wt% by using the copper-containing and zinc acid leaching solution through an extraction electrodeposition process and a vulcanization process;
6) adjusting the pH value of the gold-silver-containing acid leaching residue obtained in the step 5) to 7 by adopting ammonia water, grinding the gold-silver-containing acid leaching residue in a wet ball mill by using 3kg/t of sodium hexametaphosphate as a grinding aid, controlling the concentration of sodium cyanide to be 0.20 wt% and the air flow to be 60m, wherein the grinding fineness is-400 meshes and accounts for 90 wt%, and the ground gold-silver-containing acid leaching residue enters a leaching stirring tank after grinding3And/h, leaching for 36h, and performing pregnant solution purification, zinc powder replacement and gold and silver smelting on the leachate to obtain gold and silver products.
Specific example 2:
1) mixing waste sulfuric acid with the sulfuric acid concentration of 20 wt% generated in the roasting acid making process and cyanidation tailings in a stirring tank according to the liquid-solid mass ratio of 3:1, wherein the temperature is 65 ℃, the stirring speed is 120r/min, and the aeration quantity is 100m3The stirring time is 5 hours, the mixture enters a thickener after the stirring reaction, the underflow is dehydrated by a filter press to obtain decyanation tailings, the overflow is acid wastewater, the acid wastewater is treated by a lime neutralization method, and neutralized waste residues containing 1.0 wt% of copper, 0.3 wt% of lead, 0.5 wt% of zinc, 7.5 wt% of iron and 1.0 wt% of arsenic are obtained after the filter pressing;
2) preparing mixed neutralization waste residues from gold concentrate containing 7 wt% of lead, wherein the adding proportion of the neutralization waste residues is 3 wt%, mixing, feeding into a stirring tank, adding water for size mixing, the size mixing concentration is 70 wt%, feeding into a ball mill for ore grinding for 30 minutes, and feeding into an ore pulp storage tank after ore grinding;
3) independently mixing the neutralized waste residues, adding a proper amount of water into the neutralized waste residues in a mixing and stirring tank, adjusting the concentration of slurry to 40 wt%, and stirring for 5 h;
4) conveying the ore pulp obtained by adding the neutralized waste residues in the step 2) to a fluidized bed roaster through a conveying pump, wherein the roasting temperature is 590 ℃, and the air volume is controlled to be 9000m3The roasting time is 4 hours, in the roasting process, the slurry of the neutralized waste residues in the step 3) is conveyed to a roasting furnace through a conveying pump, the conveying capacity of the slurry is 1.8t/h, the temperature in the roasting process and the boiling state of materials in the furnace are adjusted and stabilized, and the roasted sand is treated next step;
wherein, the flue gas generated by roasting enters sulfuric acid production, wherein, waste sulfuric acid with the sulfuric acid concentration of 20 wt% is generated in the wet purification process of the flue gas and is recycled in the step 1) and the waste residue generation process;
5) conveying the roasted product obtained after roasting to an acid leaching stirring tank by a scraper conveyor, adding dilute sulfuric acid and hydrogen peroxide, wherein the initial sulfuric acid concentration is 75g/L, the addition amount of the hydrogen peroxide is 7.5kg/t, the liquid-solid mass ratio in the acid leaching process is 3:1, the stirring speed is 30r/min, the reaction time is controlled for 5 hours, the pH value is controlled to be 1.5 at the end point of the reaction, liquid-solid separation is carried out after the reaction is finished, solid residues are acid leaching residues containing gold and silver, and liquid is acid leaching solution containing copper and zinc;
respectively obtaining 1# cathode copper and zinc concentrate with zinc grade of 60 wt% by using the copper-containing and zinc acid immersion liquid through an extraction electrodeposition process and a vulcanization process;
6) adjusting the pH value of the gold-silver-containing acid leaching residue obtained in the step 5) to 8 by adopting ammonia water, grinding the gold-silver-containing acid leaching residue in a wet ball mill by using 5kg/t of sodium hexametaphosphate as a grinding aid, controlling the concentration of sodium cyanide to be 0.35 wt% and the air flow to be 70m, wherein the grinding fineness is-400 meshes and accounts for 92.5 wt%, and the ground gold-silver-containing acid leaching residue enters a leaching stirring tank after grinding3And/h, leaching time is 54h, and gold and silver products are obtained by the leaching solution through the processes of pregnant solution purification, zinc powder replacement and gold and silver smelting.
Specific example 3:
1) mixing waste sulfuric acid with the sulfuric acid concentration of 30 wt% generated in the roasting acid making process and cyanidation tailings in a stirring tank according to the liquid-solid mass ratio of 5:1, wherein the temperature is 80 ℃, the stirring speed is 200r/min, and the aeration quantity is 150m3Stirring for 6h, reacting while stirring, concentrating, and filtering with filter pressDewatering to obtain decyanation tailings, treating the overflow to obtain acidic wastewater by adopting a lime neutralization method, and performing filter pressing to obtain neutralized waste residues containing 1.5 wt% of copper, 0.5 wt% of lead, 0.7 wt% of zinc, 10 wt% of iron and 1.5 wt% of arsenic;
2) preparing mixed neutralization waste residues from gold concentrate containing 10% of lead, wherein the adding proportion of the neutralization waste residues is 5 wt%, mixing, feeding into a stirring tank, adding water for size mixing, the size mixing concentration is 75 wt%, feeding into a ball mill for ore grinding for 40 minutes, and feeding into an ore pulp storage tank after ore grinding;
3) independently mixing the neutralized waste residues, adding a proper amount of water into the neutralized waste residues in a mixing and stirring tank, adjusting the concentration of slurry to 50 wt%, and stirring for 6 h;
4) conveying the ore pulp obtained by adding the neutralized waste residues in the step 2) to a fluidized bed roaster through a conveying pump, wherein the roasting temperature is 620 ℃, and the air volume is controlled to be 10000m3The roasting time is 5 hours, in the roasting process, the slurry obtained by independently pulping the neutralized waste residues in the step 3) is conveyed to a roasting furnace through a conveying pump, the conveying capacity of the slurry is 3t/h, the temperature in the roasting process and the boiling state of materials in the furnace are adjusted and stabilized, and the roasted sand is subjected to next treatment;
wherein, the flue gas generated by roasting enters sulfuric acid production, wherein waste sulfuric acid with the sulfuric acid concentration of 30 wt% is generated in the wet purification process of the flue gas and is recycled in the step 1) and the waste residue generation process;
5) conveying the roasted product obtained after roasting to an acid leaching stirring tank by a scraper conveyor, adding dilute sulfuric acid and hydrogen peroxide, wherein the initial sulfuric acid concentration is 100g/L, the hydrogen peroxide addition amount is 10kg/t, the liquid-solid mass ratio in the acid leaching process is 5:1, the stirring speed is 40r/min, the reaction time is controlled for 6 hours, the pH value is controlled to be 2 at the reaction end point, liquid-solid separation is carried out after the reaction is finished, the solid residue is acid leaching residue containing gold and silver, and the liquid is acid leaching solution containing copper and zinc;
respectively obtaining 1# cathode copper and zinc concentrate with zinc grade of 62 wt% by using the copper-containing and zinc acid leaching solution through an extraction electrodeposition process and a vulcanization process;
6) adjusting the pH value of the gold and silver-containing acid leaching residue obtained in the step 5) to 9 by adopting ammonia water, taking sodium hexametaphosphate as a grinding aid with the dosage of 5kg/t, and placing the mixture in a wet ballGrinding in a mill until the grinding fineness is 95 wt% with 400 meshes, feeding into a leaching and stirring tank, controlling the sodium cyanide concentration to be 0.50 wt% and the air volume to be 80m3And h, leaching for 72h, and performing pregnant solution purification, zinc powder replacement and gold and silver smelting on the leachate to obtain gold and silver products.
It is to be understood that the present invention has been described with reference to certain embodiments, and that various changes in the features and embodiments, or equivalent substitutions may be made therein by those skilled in the art without departing from the spirit and scope of the invention. In addition, many modifications may be made to adapt a particular situation or material to the teachings of the invention without departing from the essential scope thereof. Therefore, it is intended that the invention not be limited to the particular embodiment disclosed, but that the invention will include all embodiments falling within the scope of the appended claims.
Claims (10)
1. A method for the synergistic roasting treatment of neutralized waste residues and lead-containing gold concentrate is characterized by comprising the following steps:
1) and (3) output of neutralization waste residues: mixing and stirring sulfuric acid and cyanidation tailings, performing concentration treatment after stirring reaction to obtain decyanation tailings and acidic wastewater, treating the acidic wastewater by adopting a lime neutralization method, and performing filter pressing to produce neutralized waste residues;
2) mixing and grinding lead-containing gold concentrate and neutralized waste residues: mixing lead-containing gold concentrate with the neutralized waste residues, adding water for size mixing, and grinding after size mixing to obtain ore pulp;
3) neutralizing waste residues and mixing slurry: adding water into the neutralized waste residues for size mixing treatment to obtain slurry;
4) boiling roasting to prepare acid: conveying the ore pulp obtained in the step 2) to a fluidized bed roaster for roasting, conveying the slurry obtained in the step 3) to the roaster during roasting, adjusting and stabilizing the temperature during roasting and the boiling state of materials in the roaster, and roasting to obtain roasted sand;
5) acid leaching of calcine: adding dilute sulfuric acid and hydrogen peroxide into the calcine to carry out acid leaching treatment, controlling the pH value to be 1-2 at the end point of the reaction, and carrying out liquid-solid separation after the reaction is finished to obtain solid acid leaching residue and acid leaching liquid;
6) leaching gold and silver: adjusting the pH value of the solid acid leaching residue obtained in the step 5) to 7-9, grinding, leaching by using cyanide to obtain a leaching solution, and purifying and replacing the leaching solution with pregnant solution, and smelting gold and silver to obtain gold and silver products.
2. The method for the co-roasting treatment of the neutralized waste residue and the lead-containing gold concentrate according to claim 1, characterized in that,
in the step 4), the roasting temperature is 560-3The roasting time is 3-5 h;
the slurry conveying amount in the step 4) is 0.5-3 t/h.
3. The method for the synergic roasting treatment of the neutralized waste residues and the lead-containing gold concentrates according to the claim 1, characterized in that the acid leaching solution obtained in the step 5) is subjected to an extraction electrodeposition process and a sulfidization process to obtain copper and zinc concentrates respectively.
4. The method for the synergic roasting treatment of the neutralized waste residues and the lead-containing gold concentrates according to claim 1, characterized in that the flue gas generated in the roasting process in the step 4) is subjected to sulfuric acid production and recycled for the neutralized waste residue output process in the step 1).
5. The method for the co-roasting treatment of the neutralized waste residue and the lead-containing gold concentrate according to claim 1, characterized in that in the step 1): the concentration of the sulfuric acid is 10-30 wt%, and the mixing mass ratio of the sulfuric acid to the cyanidation tailings is (1-5): 1.
6. the method for the co-roasting treatment of the neutralized waste residue and the lead-containing gold concentrate according to claim 1, characterized in that in the step 1):
the mixing and stirring temperature is 50-80 ℃, the stirring speed is 50-200r/min, and the aeration quantity is 50-150m3And h, stirring for 4-6 h.
7. The method for the co-roasting treatment of the neutralized waste residue and the lead-containing gold concentrate according to claim 1, wherein in the step 2):
the lead content of the gold concentrate is 5-10 wt%, the adding proportion of the neutralized waste residues is 1-5 wt% of the mass of the lead-containing gold concentrate, and the slurry mixing concentration is 65-75 wt%.
8. The method for the collaborative roasting treatment of the neutralized waste residues and the lead-containing gold concentrate according to claim 1, wherein the slurry concentration in the step 3) is 30-50 wt%, and the stirring time is 4-6 h.
9. The method for the co-roasting treatment of the neutralized waste residue and the lead-containing gold concentrate according to claim 1, characterized in that in the step 5):
the concentration of the initial sulfuric acid is 50-100 g/L, the addition amount of hydrogen peroxide is 5-10 kg per ton of calcine, the liquid-solid mass ratio is (2-5): 1, the stirring speed is 20-40 r/min, and the reaction time is controlled to be 4-6 hours.
10. The method for the co-roasting treatment of the neutralized waste residue and the lead-containing gold concentrate according to claim 1, characterized in that in the step 6):
cyanide concentration of 0.20-0.50 wt%, and air volume of 60-80m3And/h, the leaching time is 36-72 h.
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