Method for comprehensively recovering valuable elements by resource utilization of roasting cyanidation tailings

Abstract

The invention relates to the technical field of comprehensive recovery and resource utilization of gold dressing and smelting, in particular to a method for comprehensively recovering valuable elements by resource utilization of roasting cyanidation tailings. Comprising the following steps: S1, acidifying and curing the roasted cyanidation tailings; s2, carrying out high-acid leaching on the acidified and cured filter cake; s3, recovering gold, copper and iron; s4, roasting the high-acid acid leaching residues and the copper-zinc-silver oxide ore; s5, recovering copper and zinc from the roasted ore; and S6, gold and silver are extracted from the copper-zinc acid leaching residues. Valuable elements in the roasting cyanidation tailings are efficiently recycled and utilized, high-value utilization and clean production of resources of the roasting cyanidation tailings are achieved, the technical problem that the valuable elements in the roasting cyanidation tailings are difficult to effectively recycle is solved, the technological process is smooth, operability is high, the environment is good, and the method is suitable for industrial production. The method has remarkable economic benefits, social benefits and environmental benefits.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of gold ore dressing comprehensive recovery and resource utilization, and particularly relates to a method for resource utilization of roasting cyanidation tailings and comprehensive recovery of valuable elements. BACKGROUND

[0002] The main associated metal minerals of gold and silver are pyrite, arsenopyrite, etc., followed by galena, sphalerite, pyrrhotite, arsenic, etc., and the non-metallic minerals are quartz, feldspar and carbonate minerals, etc. At present, three kinds of pre-treatment process methods are mainly used for gold concentrate: one is roasting process technology; two is hot-pressing process technology; three is biological oxidation process technology. Among them, the roasting process is the main method for treating gold concentrate at present, and gold is extracted by combining the cyanidation process after pre-treatment by roasting. The roasting cyanidation tailings are solid waste produced after roasting acid and cyanidation gold extraction of gold concentrate. Since the cyanide tailings contain a large amount of cyanide and heavy metals such as arsenic and lead, the cyanide tailings will bring great risk to the ecological environment.

[0003] With the continuous utilization of mineral resources and the need for environmental protection, the recovery of valuable metals from cyanide tailings has received more and more attention. Developing and utilizing cyanide tailings as secondary resources can reduce the harm to the environment and is of great significance to the development of economy and society. The main component of roasting cyanidation tailings produced by roasting cyanidation process is Fe2O3, containing 20-60% of iron, and also containing precious metals such as gold and silver, with gold grade of 1.5-3.0 g / t and silver grade of 50-100 g / t. When treating complex arsenic-containing gold concentrate, the gold grade of roasting cyanidation tailings can sometimes reach 5-10 g / t. Gold and iron have great recycling value.

[0004] At present, the main methods for extracting iron from roasting cyanidation tailings are magnetic separation, magnetization roasting-magnetic separation, acid dissolution, reduction / activation roasting-acid dissolution and direct activation-acid dissolution. Among them, the magnetic separation method is limited by the form of iron in the roasted slag, the magnetization roasting not only consumes energy but also causes environmental pollution, and the direct acid dissolution method has low leaching efficiency. Therefore, the existing roasting cyanidation tailings iron extraction process has certain defects in applicability, energy consumption, cost, secondary pollution, etc., and the gold and silver in the roasting cyanidation tailings have not been effectively recovered and utilized. It is of great significance to develop and utilize roasting cyanidation tailings and reduce the harm of roasting cyanidation tailings to the environment.

[0005] How to develop a new process with high efficiency, environmental protection and energy saving to cope with the resource utilization of roasting cyanidation tailings has become the focus of the industry, and is also an important direction for enterprises to realize economic growth and sustainable development, and is an inevitable requirement to improve resource conservation and comprehensive utilization efficiency. SUMMARY

[0006] In order to solve the above technical problems in the prior art, the present application provides a method for comprehensively recovering valuable elements by resource utilization of roasting cyanidation tailings.

[0007] The technical scheme for solving the above technical problems is as follows: The first aspect of the present application is to provide a method for comprehensively recovering valuable elements by resource utilization of roasting cyanidation tailings, comprising the following steps: S1, roasting cyanidation tailings acidification and maturation: roasting cyanidation tailings are subjected to acidification and maturation treatment to obtain acidification and maturation filter cake and acidification and maturation liquid, the acidification and maturation filter cake enters step S2, and the acidification and maturation liquid enters step S3; S2, high-acid leaching of acidification and maturation filter cake: the acidification and maturation filter cake is subjected to acid leaching to obtain copper, iron and acid leaching liquid, the acid leaching liquid is subjected to pressure filtration treatment to obtain high-acid leaching liquid and high-acid leaching residue, the high-acid leaching liquid is returned to step S1, and the high-acid leaching residue enters step S4; S3, recovery of gold, copper and iron: the acidification and maturation liquid sequentially passes through an adsorption device, an iron powder replacement device and a neutralization and precipitation device, the acidification and maturation liquid is subjected to recovery of gold elements in the adsorption device, recovery of copper elements in the iron powder replacement device, and recovery of iron elements in the neutralization and precipitation device; S4, high-acid acid leaching residue and copper-zinc-silver oxide ore roasting: the high-acid leaching residue is mixed with copper-zinc-silver oxide ore with a mass percentage of copper of 1-3%, a mass percentage of zinc of 2-5% and a silver content of 500-2000g / t, pellets are prepared, and then the pellets are subjected to roasting to obtain roasted ore; S5, recovery of copper and zinc from roasted ore: the roasted ore is subjected to acid leaching treatment, and then subjected to pressure filtration to obtain acid leaching liquid, the acid leaching liquid sequentially passes through the iron powder replacement device and the zinc recovery device to obtain copper-zinc acid leaching residue, copper elements are obtained after passing through the iron powder replacement device, and zinc elements are obtained after passing through the zinc recovery device; S6, extraction of gold and silver from copper-zinc acid leaching residue.

[0008] The method for comprehensively recovering valuable elements by resource utilization of roasting cyanidation tailings provided by the present application, wherein, through step S1 of roasting cyanidation tailings acidification and maturation, iron elements in the roasting cyanidation tailings generate iron sulfate, and copper elements are converted into copper sulfate; through step S3, an adsorption device is used for recovery of gold elements, and an iron powder replacement device is used for recovery of copper elements, specifically, iron powder is used to replace copper, so that copper sulfate in the solution is converted into elemental copper, and iron is converted into iron sulfate or ferrous sulfate; through step S4, ore blending is performed, that is, the high-acid leaching residue is mixed with copper-zinc-silver oxide ore to ensure uniformity of the gold, silver and copper content of the raw ore.

[0009] On the basis of the above technical scheme, the present application can also be improved as follows: Further, in step S1, the mass percentage of the fineness of 0.074 mm in the roasted cyanide tailings is 70-90%, the mass percentage of iron is 20-60%, and the content of gold is 1.50-10 g / t.

[0010] Further, in step S1, the acidification and curing process is as follows: the roasted cyanide tailings are stirred and uniformly mixed with sulfuric acid with a concentration of 70-90% in an acidification and curing tank, the acidification and curing temperature is controlled at 260-350°C, the sulfuric acid dosage is 0.6-1.5 t, the acidification and curing time is 3-8 h, and after the curing is completed, the acidification and curing filter cake and the acidification and curing liquid are obtained by entering the stirring and washing device and the blowing and washing pressure filtration device.

[0011] Further, the moisture content in the acidification and curing filter cake is 20-25%, the gold content is 3.0-20.0 g / t, and the iron content is 5-10%; the gold content in the acidification and curing liquid is 0.20-1.0 g / m 3、 , the copper content is 1-3 g / l, and the iron content is 100-200 g / l.

[0012] Further, in step S2, the process specifically includes the following: the acidification and curing filter cake enters a high-acid acid leaching device, the slurry concentration in the acid leaching process is controlled at 20-40%, the sulfuric acid concentration is 20-50%, the acid leaching temperature is 80-90°C, the acid leaching time is 2-4 h, copper and iron are leached with the acid leaching liquid, and the acid leaching liquid is subjected to blowing and washing pressure filtration to obtain the high-acid leaching liquid and the high-acid leaching residue; the gold content in the high-acid leaching residue is 3.2-20.5 g / t, the silver content is 100-200 g / t, and the iron content is 2-4%.

[0013] Further, in step S3, the process specifically includes the following: the acidification and curing liquid is countercurrently passed through a three-stage carbon adsorption device at a speed of 2-5 m 3 / h, the gold content in the adsorbed liquid is 0.01-0.06 g / m 3 ; the adsorbed liquid is subjected to iron powder replacement, the stirring speed is controlled at 30-50 r / min, the iron powder dosage is 1-3 kg / m 3 , the reaction time is 0.5-1.5 h, and the copper content in the replaced liquid is 0.02-0.10 g / l; the replaced liquid is subjected to neutralization and precipitation, sodium hydroxide and sodium carbonate are used as the precipitants, the precipitation pH is controlled at 3-5, the iron is precipitated in the form of iron hydroxide or iron carbonate for the production of iron products, and the sodium content in the iron-precipitated liquid is 100-200 g / l.

[0014] The three-stage carbon adsorption device comprises a first-stage carbon adsorption tank, a second-stage carbon adsorption tank and a third-stage carbon adsorption tank, the first-stage carbon adsorption tank, the second-stage carbon adsorption tank and the third-stage carbon adsorption tank are sequentially connected in series, and the acidification and maturation liquid sequentially flows through the first-stage carbon adsorption tank, the second-stage carbon adsorption tank and the third-stage carbon adsorption tank.

[0015] Further, in step S4, the mixing ratio of the high-acid leaching residue and the copper-zinc-silver oxide ore is 1:3, and a mineral preparation liquid is obtained.

[0016] Further, in step S4, the following process is specifically included: the water content of the mineral preparation liquid is adjusted to 20-25% by using the post-iron precipitation liquid, then the balling is prepared with a particle size of 5-8 mm, the balling is placed in a rotary roasting furnace for roasting, and a roasted ore is obtained; the roasting includes a feeding section, a roasting section and a discharging end, the temperature of the feeding section is 200-400 DEG C, the time of the feeding section is 60-80 min, after passing through the feeding section, the water content of the balling is dried to 5-8%, the temperature of the roasting section is 550-650 DEG C, the time of the roasting section is 120-150 min, the temperature of the discharging end is 300-350 DEG C, and the time of the discharging end is 30-50 min; the roasted ore has a gold content of 2-5.0 g / t, a silver content of 150-550 g / t, a copper content of 0.30-0.75%, and a zinc content of 0.5-1.0%.

[0017] Further, in step S5, the following process is specifically included: after the roasted ore is ground in a wet-type grinding mill, the mass percentage of the fineness of 0.074 mm is 85-95%, the acid leaching process is pumped into an acid leaching tank, the pulp concentration is 30-50%, the sulfuric acid concentration is 1.0-3.0%, the acid leaching temperature is 80-90 DEG C, the acid leaching time is 2-4 h, after the leaching is completed, the air blowing, pressing, washing and filtering device is used, the acid leaching liquid containing copper of 3-10 g / l and zinc of 5-15 g / l is produced, the iron powder replacement device is used, the stirring speed is controlled to be 30-50 r / min, the iron powder dosage is 1-3 kg / m 3 , the reaction time is 0.5-1.5 h, the copper content of the post-replacement liquid is 0.02-0.10 g / l; the post-replacement liquid is introduced into the zinc sulfidation recovery device, the stirring speed is controlled to be 20-40 r / min, the sodium hydrosulfide dosage is 5-10 kg / m 3 , the reaction time is 20-40 min, the post-zinc precipitation liquid contains zinc of 0.02-0.05 g / l; the copper-zinc acid leaching residue contains gold of 3.0-8.0 g / t, silver of 220-800 g / t, copper of 0.05-0.07% and zinc of 0.05-0.07%.

[0018] Further, step S6 specifically includes the following process: the copper-zinc acid leaching residue is sent to a grinding machine, the grinding concentration is controlled to be 40-50%, the grinding fineness is 95% of 0.037mm, the concentration of the ore slurry after grinding is adjusted to be 30-35%, the ore slurry is pumped to a gold and silver leaching device, the pH value is adjusted to 8-9 by sodium carbonate, an environment-friendly gold extraction agent is added, the addition amount of the environment-friendly gold extraction agent is 3-5kg / t, the leaching temperature is 30-40 DEG C, the leaching time is 24-36h, after leaching, liquid-solid separation is carried out, and the gold and silver containing liquid is recovered by zinc powder replacement process, and the gold and silver leaching rates are 90-92% and 92-94% respectively.

[0019] Compared with the prior art, the present application has the following technical effects: The present application efficiently processes the sulfuric acid residue and the gold-containing mineral through a six-stage processing process, the first stage is roasting cyanidation tail residue maturation and acidification, obtaining acidified maturation filter cake and acidified maturation liquid; the second stage is high-acid leaching of the acidified maturation filter cake, further leaching copper and iron; the third stage is recovery of gold, copper and iron from the acidified maturation liquid; the fourth stage is roasting of high-acid acid leaching residue and oxidized copper-zinc silver ore; the fifth stage is acid leaching of the roasted ore to leach copper and zinc, and gradient recovery of copper and zinc from the copper-zinc acid leaching liquid; and the sixth stage is environment-friendly extraction of gold and silver from the copper-zinc acid leaching residue. Valuable elements in the roasted cyanidation tail residue are efficiently recovered and utilized, realizing high-value utilization and clean production of the roasted cyanidation tail residue, solving the technical problem of difficult efficient recovery of valuable elements in the roasted cyanidation tail residue, and the process flow is smooth, the operability is strong, the environment is excellent, and the present application has significant economic, social and environmental benefits. DETAILED DESCRIPTION

[0020] The following describes the embodiments of the present application by specific examples, and those skilled in the art can easily understand other advantages and effects of the present application from the disclosure. Although the description of the present application will be introduced in combination with the preferred embodiments, this does not mean that the features of the present application are limited to the embodiments. On the contrary, the purpose of introducing the present application in combination with the embodiments is to cover other options or modifications that can be extended based on the claims of the present application. In order to provide a deep understanding of the present application, many specific details will be included in the following description. The present application can also be implemented without using these details. In addition, in order to avoid confusion or obscure the focus of the present application, some specific details will be omitted in the description. It should be noted that the embodiments in the present application and the features in the embodiments can be combined with each other without conflict.

[0021] Example 1 S1, primary roasting cyanidation tailings curing acidification: roasting cyanidation tailings fineness of -0.074 mm accounts for 70%, containing iron 20%, containing gold 1.50 g / t, using 70% concentration sulfuric acid and roasting cyanidation tailings in acid curing tank, stirring and mixing uniformly, controlling acid curing temperature 260℃, acid curing sulfuric acid dosage 0.6t, acid curing time 3h, curing into stirring washing device, blowing pressing washing and filter pressing device, obtaining acid curing filter cake and acid curing liquid, entering next step process; S2, secondary acid curing filter cake high acid leaching: acid curing residue containing moisture 20%, containing gold 3.0 g / t, containing iron 5% into high acid leaching device, acid leaching process slurry concentration 20%, sulfuric acid concentration 20%, acid leaching temperature 80℃, acid leaching time 2h, further leaching copper and iron, through blowing pressing washing and filter pressing device, outputting high acid leaching liquid returning to step (1), configuring suitable concentration of sulfuric acid to be used, obtaining high acid leaching residue containing gold 3.2 g / t, containing silver 100 g / t, containing iron 2% into next step process; S3, third stage acid curing liquid recovering gold, copper and iron: acid curing liquid containing gold 0.20 g / m 3 , containing copper 1 g / l, containing iron 100 g / l countercurrently passing through 3-stage carbon adsorption device at a speed of 2 m 3 / h, adsorbed liquid containing gold 0.01 g / m 3 ; adsorbed liquid passing through iron powder displacement device, stirring speed 30 r / min, iron powder dosage 1 kg / m 3 , reaction time 0.5h, displacement liquid containing copper 0.02 g / l; displacement liquid passing through neutralization and precipitation device, using sodium hydroxide and sodium carbonate as precipitants, precipitation pH control 3, making iron precipitate as iron hydroxide or iron carbonate for producing iron products; main components of iron precipitation liquid containing sodium 100 g / l into next step process; S4, fourth stage high acid leaching residue and oxidized copper zinc silver ore roasting: high acid leaching residue and oxidized copper zinc silver ore containing copper 1%, containing zinc 2%, containing silver 500 g / t are mixed according to 1:3 ratio, using iron precipitation liquid to adjust moisture content to 20%, and preparing 5 mm diameter pellets into rotary roasting furnace, feeding port temperature 200℃, moisture drying to 5%, drying time 60 min, roasting section temperature 550℃, roasting time 120 min, discharging section temperature 300℃, time 30 min; roasting ore containing gold 2.0 g / t, containing silver 150 g / t, containing copper 0.30%, containing zinc 0.5% into next step process; S5, after five-stage roasting ore acid leaching leaching copper zinc, copper zinc acid leaching liquid stage recovery copper, zinc: after roasting ore into wet grinding mill grinding, fineness -0.074mm 85%, pump into acid leaching tank, acid leaching process ore pulp concentration 30%, sulfuric acid concentration 1.0%, acid leaching temperature 80℃, acid leaching time 2h, after leaching by blowing press washing washing filter device, output containing copper 3g / l, containing zinc 5g / l acid leaching liquid, through iron powder replacement device, stirring speed 30r / min, iron powder dosage 1kg / m 3 , reaction time 0.5h, after replacement liquid containing copper 0.02g / l; replacement liquid into sulfidation recovery zinc device, stirring speed 20r / min, sodium hydrosulfide dosage 5kg / m 3 , reaction time 20min, after zinc precipitation liquid containing zinc 0.02g / l; containing gold 3.0g / t, containing silver 220g / t, containing copper 0.05%, containing zinc 0.05% copper zinc acid leaching residue into the next step process.

[0022] S6, six-stage copper zinc acid leaching residue environmental protection extraction of gold and silver: copper zinc acid leaching residue through ALC-1500L grinding mill, control grinding concentration 40%, grinding fineness -0.037mm 95%, after grinding ore pulp concentration is adjusted to 30%, pump to gold and silver leaching device, sodium carbonate adjust PH value to 8, environmental protection gold extraction agent addition 3kg / t, leaching temperature 30℃, leaching time 24h, after leaching through liquid-solid separation, gold and silver containing liquid is recovered by zinc powder replacement process, gold and silver leaching rate reaches 90%, 92% respectively.

[0023] Example 2 S1, first-stage roasting cyanidation tailings curing acidification: roasting cyanidation tailings fineness -0.074mm 80%, containing iron 40%, containing gold 5.50g / t, using concentration 80% sulfuric acid and roasting cyanidation tailings in acid curing tank stirring, control acid curing temperature 300℃, acid curing sulfuric acid dosage 1.1t, acid curing time 5.5h, after curing into stirring washing device, blowing press washing washing filter device, get acid curing filter cake and acid curing liquid, into the next step process; S2, second-stage acid curing filter cake high acid leaching: acid curing residue containing moisture 22.5%, containing gold 11.5g / t, containing iron 7.5% into high acid acid leaching device, acid leaching process ore pulp concentration 30%, sulfuric acid concentration 35%, acid leaching temperature 85℃, acid leaching time 3h, further leaching copper, iron, through blowing press washing washing filter device, output high acid leaching liquid return to step (1), configuration suitable concentration of sulfuric acid to be used, get containing gold 11.3g / t, containing silver 150g / t, containing iron 3% high acid leaching residue into the next step process; S3, third-stage acid curing liquid recovery of gold, copper, iron: gold 0.6g / m 3, the acidified matured solution containing copper 2 g / l and iron 150 g / l flows countercurrently through the 3-stage carbon adsorption device at a speed of 3.5 m 3 / h, the adsorbed solution containing gold 0.35 g / m 3 ; the adsorbed solution passes through the iron powder replacement device, the stirring speed is 40 r / min, the iron powder dosage is 2 kg / m 3 , the reaction time is 1.0 h, the replaced solution contains copper 0.06 g / l; the replaced solution passes through the neutralization and precipitation device, sodium hydroxide and sodium carbonate are used as the precipitants, the precipitation pH is controlled at 4, so that the iron is precipitated in the form of iron hydroxide or iron carbonate for producing iron products; the iron-precipitated solution mainly contains sodium 150 g / l and enters the next process; S4, high-acid acid leaching residue and oxidized copper-zinc-silver ore roasting: the high-acid acid leaching residue is mixed with the oxidized copper-zinc-silver ore containing copper 2%, zinc 3.5% and silver 1250 g / t at a ratio of 1:3, the iron-precipitated solution is adjusted to a moisture content of 22.55% and prepared into pellets with a particle size of 6 mm, which enters the rotary roasting furnace through the belt conveyor, the feeding port temperature is 300℃, the moisture is dried to 6.5%, the drying time is 70 min, the roasting section temperature is 600℃, the roasting time is 135 min, the discharging section temperature is 325℃, and the time is 40 min; the roasted ore containing gold 3.5 g / t, silver 350 g / t, copper 0.55% and zinc 0.75% enters the next process; S5, fifth-stage roasted ore acid leaching and copper-zinc leaching, copper-zinc acid leaching solution gradient recovery of copper and zinc: after the roasted ore is ground in the wet grinding machine, the fineness of-0.074 mm is 90%, the pump enters the acid leaching tank, the acid leaching process has a pulp concentration of 40%, a sulfuric acid concentration of 2.0%, an acid leaching temperature of 85℃, and an acid leaching time of 3 h, after the leaching is completed, it passes through the air blowing, pressing, washing and pressure filtration device, the acid leaching solution containing copper 6.5 g / l and zinc 10 g / l is produced, which enters the iron powder replacement device, the stirring speed is 40 r / min, the iron powder dosage is 2 kg / m 3 , the reaction time is 1.0 h, the replaced solution contains copper 0.06 g / l; the replaced solution enters the zinc sulfidation recovery device, the stirring speed is 30 r / min, the sodium hydrosulfide dosage is 7.5 kg / m 3 , the reaction time is 30 min, the zinc-precipitated solution contains zinc 0.35 g / l; the copper-zinc acid leaching residue containing gold 5.5 g / t, silver 510 g / t, copper 0.06% and zinc 0.06% enters the next process.

[0024] S6. Environmentally friendly extraction of gold and silver from grade 6 copper-zinc acid leaching residue: The copper-zinc acid leaching residue is processed by an ALC-1500L mill, with the grinding concentration controlled at 45% and the grinding fineness at -0.037mm accounting for 95%. After grinding, the slurry concentration is adjusted to 32.5% and pumped to the gold and silver leaching unit. Sodium carbonate is used to adjust the pH value to 8.5, and 4 kg / t of environmentally friendly gold extraction agent is added. The leaching temperature is 35℃ and the leaching time is 30 hours. After leaching, liquid-solid separation is performed, and the gold and silver-containing precious solution is treated with a zinc powder replacement process to recover gold and silver. The gold and silver leaching rates reach 91% and 93%, respectively.

[0025] Example 3 S1. Primary roasting cyanide tailings ripening and acidification: The roasting cyanide tailings have a fineness of -0.074mm (90%), contain 60% iron and 10g / t of gold. They are mixed with 90% sulfuric acid in an acidification and ripening tank. The acidification and ripening temperature is controlled at 350℃, the amount of sulfuric acid used is 1.5t, and the acidification and ripening time is 8h. After ripening, the residue enters a stirring and washing device, a blowing and pressing washing and filtration device, and the resulting acidified and ripened filter cake and acidified and ripened liquid are obtained for the next step. S2, Secondary acidification and aging filter cake high acid leaching: Acidification and aging residue with 25% moisture, 20.0g / t gold, and 10% iron is fed into the high acid leaching device. The slurry concentration is 40%, the sulfuric acid concentration is 50%, the leaching temperature is 90℃, and the leaching time is 4h. Copper and iron are further leached. After blowing, pressing, washing, and filtering, the high acid leaching liquid is returned to step (1). Sulfuric acid of appropriate concentration is prepared and used. The resulting high acid leaching residue with 20.5g / t gold, 200g / t silver, and 4% iron is fed into the next process. S3, Three-stage acidification and aging solution for gold, copper, and iron recovery: gold content 1.0 g / m³ 3 An acidification and aging solution containing 3 g / L copper and 200 g / L iron was prepared at 5 m 3 The solution flows countercurrently through a three-stage carbon adsorption unit at a flow rate of / h, and the gold content in the post-adsorption solution is 0.06 g / m³. 3 The adsorbed liquid is then passed through an iron powder replacement device, with a stirring speed of 50 r / min and an iron powder dosage of 3 kg / m³. 3 The reaction time is 1.5 hours, and the solution after displacement contains 0.10 g / L of copper. The solution after displacement passes through a neutralization and precipitation device, using sodium hydroxide and sodium carbonate as precipitants. The pH of the precipitation is controlled at 5, so that iron is precipitated in the form of ferric hydroxide or ferric carbonate for the production of iron products. The main component of the solution after iron precipitation is sodium with a content of 200 g / L, which is then used in the next process. S4, four high acid leaching residue and copper zinc silver oxide roasting: high acid leaching residue and copper 3%, zinc 5%, silver 2000g / t of copper zinc silver oxide according to 1:3 ratio mixed, after iron precipitation liquid adjustment to moisture content 25% and preparation of particle size 8mm ball into the belt conveyor into the rotary roasting furnace kiln, the temperature of the inlet 400℃, moisture drying to 8%, drying time 80min, roasting section temperature 650℃, roasting time 150min, discharge section temperature 350℃, time 50min; gold 5.0g / t, silver 550g / t, copper 0.75%, zinc 1.0% of the roasted ore into the next step process; S5, five stage roasting after ore acid leaching copper zinc, copper zinc acid leaching liquid step recovery copper, zinc: after roasting ore into wet grinding mill grinding, fineness-0.074mm 95%, pump into acid leaching tank, acid leaching process slurry concentration 50%, sulfuric acid concentration 3.0%, acid leaching temperature 90℃, acid leaching time 4h, after leaching by blowing washing and washing filter device, copper 10g / l, zinc 15g / l of acid leaching liquid, through iron powder replacement device, stirring speed 50r / min, iron powder 3kg / m 3 , reaction time 1.5h, replacement liquid copper 0.10g / l; replacement liquid into the sulfidation recovery zinc device, stirring speed 40r / min, sodium hydrosulfide dosage 10kg / m 3 , reaction time 40min, zinc after the liquid containing zinc 0.05g / l; gold 8.0g / t, silver 800g / t, copper 0.07%, zinc 0.07% of copper zinc acid leaching residue into the next step process.

[0026] S6, six stage copper zinc acid leaching residue environmental protection extraction of gold and silver: copper zinc acid leaching residue through ALC-1500L grinding mill, control grinding concentration 50%, grinding fineness-0.037mm 95%, after grinding slurry concentration adjustment for 35%, pump to gold and silver leaching device, sodium carbonate adjust PH value to 9, environmental protection gold extraction agent 5kg / t, leaching temperature 40℃, leaching time 36h, after leaching through liquid solid separation, gold and silver containing liquid using zinc powder replacement process to recover gold and silver, gold and silver leaching rate reached 92%, 94% respectively.

[0027] The above only for the preferred embodiments of the present application, and not to limit the present application, any modification, equivalent replacement, improvement, etc. made within the spirit and principles of the present application, should be included in the protection scope of the present application.

Claims

1. A method for comprehensive recovery of valuable elements from roasting cyanidation tailings for resource utilization, characterized in that, It comprises the following steps: S1, roasting cyanide tailings acidification curing: the roasting cyanide tailings are acidified and cured to obtain acidification curing filter cake and acidification curing liquid, the acidification curing filter cake enters step S2, and the acidification curing liquid enters step S3; S2, high-acid leaching of acidification curing filter cake: the acidification curing filter cake is subjected to acid leaching to obtain copper, iron and acid leaching liquid, the acid leaching liquid is subjected to pressure filtration treatment to obtain high-acid leaching liquid and high-acid leaching residue, the high-acid leaching liquid returns to step S1, and the high-acid leaching residue enters step S4; S3, recovery of gold, copper and iron: the acidification curing liquid sequentially passes through an adsorption device, an iron powder displacement device and a neutralization precipitation device, the acidification curing liquid is subjected to recovery of gold elements in the adsorption device, recovery of copper elements in the iron powder displacement device and recovery of iron elements in the neutralization precipitation device; S4, high-acid acid leaching residue and roasted copper-zinc-silver oxide ore: the high-acid leaching residue is mixed with a roasted copper-zinc-silver oxide ore with a mass percentage of copper of 1-3%, a mass percentage of zinc of 2-5% and a silver content of 500-2000 g / t, pellets are prepared, and then the pellets are roasted to obtain roasted ore; S5, recovery of copper and zinc from roasted ore: the roasted ore is subjected to acid leaching treatment, and then pressure filtration to obtain acid leaching liquid, the acid leaching liquid sequentially passes through an iron powder displacement device and a zinc recovery device to obtain copper-zinc acid leaching residue, copper elements are obtained after passing through the iron powder displacement device, and zinc elements are obtained after passing through the zinc recovery device; S6, extraction of gold and silver from copper-zinc acid leaching residue.

2. The method according to claim 1, characterized in that, In step S1, the mass percentage of 0.074 mm fine particles in the roasting cyanide tailings is 70-90%, the mass percentage of iron is 20-60%, and the gold content is 1.50-10 g / t.

3. The method according to claim 1 or 2, c h a r a c t e r i z e d in that, In step S1, the acidification curing process is as follows: sulfuric acid with a concentration of 70-90% is stirred and uniformly mixed with the roasting cyanide tailings in an acidification curing tank, the acidification curing temperature is controlled to be 260-350℃, the sulfuric acid dosage is 0.6-1.5 t, and the acidification curing time is 3-8 h; after curing, the mixture enters a stirring and washing device and a blowing and pressing washing and pressure filtration device to obtain acidification curing filter cake and acidification curing liquid.

4. The method according to claim 3, characterized in that, The moisture content of the acidification and maturation filter cake is 20-25%, the gold content is 3.0-20.0 g / t, and the iron content is 5-10%; the gold content of the acidification and maturation liquid is 0.20-1.0 g / m 3、 The copper content is 1-3 g / l, and the iron content is 100-200 g / l.

5. The method according to claim 1 or 2 or 4, c h a r a c t e r i z e d in that, In step S2, the acidification curing filter cake enters a high-acid acid leaching device, the slurry concentration during acid leaching is controlled to be 20-40%, the sulfuric acid concentration is 20-50%, the acid leaching temperature is 80-90℃, the acid leaching time is 2-4 h, copper and iron are leached, and acid leaching liquid is obtained; the acid leaching liquid is subjected to blowing and pressing washing and pressure filtration to obtain high-acid leaching liquid and high-acid leaching residue; the high-acid leaching residue has a gold content of 3.2-20.5 g / t, a silver content of 100-200 g / t and an iron content of 2-4%.

6. The method according to claim 1 or 2 or 4, c h a r a c t e r i z e d in that, In step S3, the process specifically includes the following: The acidified matured liquid flows countercurrently through the three-stage carbon adsorption device at a speed of 2-5 m 3 / h, and the liquid gold content after adsorption is 0.01-0.06 g / m 3 ; the liquid after adsorption flows through the iron powder replacement device, the stirring speed is controlled to be 30-50 r / min, the iron powder dosage is 1-3 kg / m 3 , the reaction time is 0.5-1.5 h, and the copper content of the liquid after replacement is 0.02-0.10 g / l; the liquid after replacement flows through the neutralization and precipitation device, sodium hydroxide and sodium carbonate are used as the precipitants, the precipitation pH is controlled to be 3-5, the iron is precipitated in the form of iron hydroxide or iron carbonate for producing iron products; and the sodium content of the liquid after iron precipitation is 100-200 g / l.

7. The method according to claim 6, characterized in that, In step S4, the mixing ratio of the high-acid leaching residue to the copper-zinc-silver oxide ore is 1:3 to obtain ore preparation liquid.

8. The method according to claim 7, c h a r a c t e r i z e d in that, In step S4, the process specifically includes the following steps: adjusting the water content of the ore preparation liquid to 20-25% by using the iron precipitation liquid, then preparing pellets with a particle size of 5-8 mm, and placing the pellets in a rotary roasting furnace for roasting to obtain roasted ore; the roasting includes a feeding section, a roasting section and a discharge end, the temperature of the feeding section is 200-400°C, the time of the feeding section is 60-80 min, after passing through the feeding section, the water content of the pellets is dried to 5-8%; the temperature of the roasting section is 550-650°C, the time of the roasting section is 120-150 min; the temperature of the discharge end is 300-350°C, the time of the discharge end is 30-50 min; the roasted ore has a gold content of 2-5.0 g / t, a silver content of 150-550 g / t, a copper content of 0.30-0.75%, and a zinc content of 0.5-1.0%.

9. The method according to claim 1 or 2, c h a r a c t e r i z e d in that, The step S5 specifically comprises the following processes: after the roasting ore is ground in a wet grinder, the mass percentage of the 0.074 mm fine ore is 85-95%, the ore slurry is pumped into an acid leaching tank, the ore slurry concentration in the acid leaching process is 30-50%, the sulfuric acid concentration is 1.0-3.0%, the acid leaching temperature is 80-90℃, the acid leaching time is 2-4h, after the leaching is completed, the leaching liquid is produced by a blowing, pressing, washing and filtering device, the acid leaching liquid contains 3-10g / l of copper and 5-15g / l of zinc, the leaching liquid is controlled to pass through an iron powder replacement device, the stirring speed is 30-50r / min, the iron powder dosage is 1-3kg / m 3 , the reaction time is 0.5-1.5h, the copper content in the replacement liquid is 0.02-0.10g / l; the replacement liquid enters a zinc sulfuration recovery device, the stirring speed is controlled to be 20-40r / min, the sodium hydrosulfide dosage is 5-10kg / m 3 , the reaction time is 20-40min, the zinc content in the zinc precipitation liquid is 0.02-0.05g / l; the gold content in the copper-zinc acid leaching residue is 3.0-8.0g / t, the silver content is 220-800g / t, the copper content is 0.05-0.07%, and the zinc content is 0.05-0.07%.

10. The method according to claim 1 or 2, c h a r a c t e r i z e d in that, In step S6, the process specifically includes the following steps: the copper-zinc acid leaching residue passes through a grinding machine, the grinding concentration is controlled to be 40-50%, the grinding fineness is 0.037 mm, the mass percentage of the grinding fineness is 95%, the concentration of the ground ore slurry is adjusted to 30-35%, and the slurry is pumped to a gold and silver leaching device by a pump, sodium carbonate is used to adjust the pH value to 8-9, an environmentally-friendly gold extraction agent is added, the addition amount of the environmentally-friendly gold extraction agent is 3-5 kg / t, the leaching temperature is 30-40°C, the leaching time is 24-36 h, after leaching, liquid-solid separation is performed, zinc powder is used to replace gold and silver in the gold and silver-containing liquid, and the gold and silver leaching rates are 90-92% and 92-94%, respectively.