A method for comprehensive utilization of tailings from roasting and gold extraction of high-copper gold ore

Abstract

This invention relates to the field of comprehensive resource utilization technology, and in particular to a method for the comprehensive utilization of high-copper gold ore roasting tailings. The method includes adding a loosening agent, a first oxidant, and a co-solvent to the tailings, mixing them evenly, and then conducting a roasting reaction to obtain a roasted product. The roasted product is then ground, washed with water, mixed with hydrochloric acid, and subjected to a first leaching reaction. After the reaction, the mixture is cooled, and solid-liquid separation is performed to obtain a first solid phase and a first liquid phase. Ammonium bromide, a second oxidant, sulfuric acid, and water are added to the first solid phase, and a second leaching reaction is performed under stirring at room temperature. Solid-liquid separation is then performed to obtain iron-silicon slag and a second liquid phase. Finally, the second liquid phase is subjected to multi-stage treatment using resin adsorption. This invention, through the addition of a combined loosening agent in the roasting pretreatment, effectively breaks down the encapsulation of valuable components such as gold, silver, and copper by iron minerals and quartz. It then uses bromination to efficiently leach gold, silver, and copper, and employs resin adsorption for separate adsorption, thus solving the technological challenges of comprehensive utilization of high-copper roasting tailings.

Description

Technical Field

[0001] This invention relates to the field of comprehensive resource utilization technology, and in particular to a method for comprehensive utilization of tailings from the roasting and gold extraction of high-copper gold ore. Background Technology

[0002] For example, after roasting and leaching gold concentrate to extract gold and silver, the tailings of a certain gold smelter still contain 3.0-8.0 grams of gold per ton, 30.0-200.0 grams of silver per ton, and 1.5%-3.0% copper, which has high economic value. The quantity exceeds 20 million tons, equivalent to 60-160 tons of gold, 600-4000 tons of silver, and 300,000-600,000 tons of copper. This is equivalent to a super-large deposit, and there are many similar resources in China.

[0003] Gold roasting tailings undergo significant changes in their original mineral structure, composition, and occurrence state due to high-temperature treatment. Furthermore, after leaching to extract gold and silver, the remaining gold is almost entirely encapsulated in fine-grained form by iron and quartz minerals, while silver minerals exist in difficult-to-extract forms such as silver ferrite and silver silicate. Copper is mostly present in the form of chrysocolla, making direct leaching difficult, thus it is considered a tough nut to crack. The overall utilization rate of this type of resource is low, especially the roasting tailings from high-copper gold mines containing >0.5% copper, which severely hinders the extraction and reuse of gold and silver. Therefore, researching the efficient and economical development and utilization of this type of encapsulated gold resource has significant social, ecological, and economic benefits.

[0004] In recent years, scholars at home and abroad have conducted a lot of research on the recovery of gold from cyanide tailings and have achieved phased results.

[0005] For example, Chinese patent CN110819820A discloses a method for gold extraction from roasted cyanide tailings by chlorination and volatilization. This method utilizes the characteristics of metal chlorides, such as their generally low boiling points, easy volatility, and high-temperature decomposition, to recover gold from the tailings. However, the high-temperature chlorination and volatilization method suffers from drawbacks such as high energy consumption, permanent copper loss, low silver utilization, complex production system, large investment, and excessively high costs.

[0006] Chinese patent CN103014319A discloses a method for enhancing gold extraction from roasted sulfur-containing arsenic gold concentrate. This method addresses the problem of iron oxide encapsulation of gold in roasted gold ore by proposing a "metallization reduction roasting-acid leaching-gold leaching" approach. First, the iron oxides are reduced, and then acid leaching is used to break the encapsulation of gold by the iron oxides. However, this method generates a large amount of iron-containing waste acid, which is difficult to treat, and the process is cumbersome and costly, making it unsuitable for industrialization.

[0007] Chinese patent CN112111647A discloses a method for pre-treating gold leaching from roasted gold ore or roasted cyanide tailings. This method first treats the roasted gold ore or roasted cyanide tailings with carbonates, converting hematite and quartz into insoluble iron silicates and soluble silicates. Then, through an alkaline decomposition reaction, the iron silicates are further converted into loose, porous amorphous iron oxide and soluble silicates. This phase transformation eliminates the encapsulation of gold by hematite and silicon-containing compounds in the roasted gold ore or roasted cyanide tailings, significantly improving the gold leaching rate. However, this method is energy-intensive and cannot comprehensively recover and utilize silver, copper, and iron from the tailings.

[0008] In view of this, the present invention is proposed. Summary of the Invention

[0009] The purpose of this invention is to provide a method for the comprehensive utilization of tailings from the roasting and gold extraction of high-copper gold ore. This method significantly improves the extraction rates of gold, silver, and copper from the tailings, avoids the discharge of large amounts of wastewater, and has good ecological benefits. The main components of the leaching tailings are iron and silicon, which can be further processed and utilized.

[0010] This invention provides a method for the comprehensive utilization of tailings from the roasting and gold extraction of high-copper gold ore, comprising the following steps:

[0011] S1. Add a loosening agent, a first oxidizing agent and a co-solvent to the tailings, mix them evenly, and carry out a calcination reaction. After the reaction is completed, cool to obtain the calcined product.

[0012] S2. After grinding and washing with water, the calcined product is mixed with hydrochloric acid and subjected to the first leaching reaction. After the reaction is completed, the product is cooled and the solid and liquid phases are separated to obtain the first solid phase and the first liquid phase.

[0013] S3. Add ammonium bromide and a second oxidant to the first solid phase, and adjust the pH to 0.5-2 with sulfuric acid solution. Stir at room temperature to carry out the second leaching reaction, and separate the solid and liquid phases to obtain iron-silicon slag and a second liquid phase.

[0014] S4. The second liquid phase is adsorbed by a cation exchange resin and then eluted to obtain a silver and copper-loaded cation exchange resin and a third liquid phase.

[0015] S5. The third liquid phase is adsorbed by an anion exchange resin and eluted to obtain a gold-loaded anion exchange resin and a fourth liquid phase. The silver-loaded and copper-loaded cation exchange resins are eluted to obtain a cation exchange resin and a fifth liquid phase.

[0016] S6. Elute the gold-loaded anion exchange resin to obtain anion exchange resin and a sixth liquid phase. The sixth liquid phase is reduced and separated into solid and liquid phases to obtain gold.

[0017] S7. The fifth liquid phase is subjected to first-stage reduction and second-stage reduction in sequence to obtain silver and copper, respectively;

[0018] There is no order restriction between steps 6 and S7.

[0019] This invention first pre-treats the tailings by adding a combination of loosening agents. The use of the combination loosening agents can effectively break the encapsulation of valuable components such as gold, silver and copper by iron minerals and quartz. Then, the gold, silver and copper are leached efficiently using the bromination method. Finally, the gold, silver and copper in the tailings are efficiently recovered by using cationic resin and anionic resin for adsorption and elution, respectively.

[0020] Therefore, this invention not only solves the problems of high energy consumption in high-temperature chlorination volatilization, permanent loss of copper, low silver utilization, complex production system, large investment, and abnormally high cost, but also solves the problem that cyanide and thiourea methods cannot effectively extract gold, silver, and copper. At the same time, the bromide in the leachate can be recycled, avoiding a large amount of wastewater discharge and achieving good ecological benefits. The main components of the leaching tailings are iron and silicon, which can be further processed and utilized.

[0021] As a preferred embodiment of this technical solution, in step S1, the loosening agent is K2S2O7, the first oxidizing agent is Na2O2, the fluxing agent is NaOH, and the amount of loosening agent is 5-10% of the tailings mass, the amount of the first oxidizing agent is 2-5% of the tailings mass, and the amount of fluxing agent is 2-5% of the tailings mass.

[0022] This invention uses a combination of loosening agents K2S2O7 and Na2O2 to pretreat the tailings, followed by roasting. This effectively breaks down the encapsulation of valuable components such as gold, silver, and copper by iron minerals and quartz, and thoroughly oxidizes and removes residual organic matter, thereby facilitating the leaching of gold, silver, and copper from the tailings.

[0023] As a preferred embodiment of this technical solution, in step S1, the roasting temperature is controlled at 600-700℃ and the processing time is 60-120min, wherein the processing time is preferably 90min.

[0024] In a preferred embodiment of this technical solution, in step S2, during the first leaching reaction, the mass ratio of the calcined product to the hydrochloric acid leachate is 1:(1-2), preferably 1:1, and the leaching reaction temperature is 90-95℃, the time is 1-3h, preferably 2h.

[0025] In a preferred embodiment of this technical solution, in step S3, the second oxidant is NaBrO3, and the amount of ammonium bromide is 10-20% of the mass of the first solid phase, preferably 15%, and the amount of the second oxidant is 15-25% of the mass of the first solid phase, preferably 20%. Specifically, ammonium bromide and NaBrO3 can be added to the first solid phase first, followed by sulfuric acid and water, and the pH of the leaching system can be adjusted to 0.5-2.0. Meanwhile, during the second leaching reaction, this invention does not strictly limit the solid-liquid ratio and leaching time. Specifically, the mass ratio of the first solid phase to the leaching solution can be controlled to be 1:(2-3), and the leaching reaction time can be 1-3 hours.

[0026] As a preferred embodiment of this technical solution, in step S4, the cation exchange resin is KP-300GR to adsorb and extract silver and copper in the second liquid phase. After adsorption, elution is performed using 2-4 MHCl to obtain a third liquid phase containing gold ions and a silver and copper-loaded cation exchange resin. The preferred elution solution here is 3 M HCl.

[0027] In a preferred embodiment of this technical solution, in step S5, the anion exchange resin is CH-90, used to adsorb and extract gold from the third liquid phase. After adsorption, elution is performed using 1-3M NaOH to obtain a fourth liquid phase containing other impurities and a gold-loaded anion exchange resin. The bromide in the leachate obtained after regeneration of the fourth liquid phase can continue to be used as the leachate for the first solid phase. The gold-loaded anion exchange resin is eluted with 1-3M NaOH to obtain a sixth liquid phase containing sodium chloroaurate and anion exchange resin. The sixth liquid phase containing sodium chloroaurate is further reduced with a reducing agent to obtain elemental gold.

[0028] The present invention does not strictly limit the type of reducing agent for reducing sodium chloroaurate, including but not limited to any one of sodium bisulfite, hydrogen and metallic iron.

[0029] The silver and copper-loaded cation exchange resin is eluted with 2-4M HCl to obtain a fifth liquid phase and a cation exchange resin containing silver and copper ions. The cation exchange resin can be reused. The fifth liquid phase is subjected to primary reduction and secondary reduction to obtain silver and copper respectively. This invention does not strictly limit the types of reducing agents used in the primary and secondary reductions. Specifically, in the primary reduction, the reducing agent used is limited to copper; in the secondary reduction, the reducing agent used includes, but is not limited to, any one of Zn and Fe.

[0030] The method for comprehensive utilization of tailings from high-copper gold ore roasting and gold extraction of the present invention has at least the following beneficial effects:

[0031] This invention first pre-treats the leaching tailings by adding a combination of loosening agents. The use of these agents effectively breaks down the encapsulation of valuable components like gold, silver, and copper by iron minerals and quartz, thoroughly oxidizing the organic matter. Further, a bromination method is used to efficiently leach gold, silver, and copper. Finally, cationic and anionic resins are used for adsorption and elution, respectively, to efficiently recover gold, silver, and copper from the tailings. Therefore, this invention effectively solves the technological challenges of comprehensive utilization of high-copper roasting tailings, avoiding the drawbacks of high energy consumption from high-temperature chlorination volatilization, permanent copper loss, low silver utilization, complex production systems, high investment, and exorbitant costs. It also solves the problem that cyanide and thiourea methods cannot effectively extract gold, silver, and copper. Simultaneously, the bromide in the leachate can be recycled, avoiding large amounts of wastewater discharge and resulting in good ecological benefits. The main components of the leaching tailings are iron and silicon, which can be further processed and utilized. Suitable products include ferric polysulfate, iron oxide red, and silica. Attached Figure Description

[0032] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0033] Figure 1 This is a flowchart of the method for comprehensive utilization of tailings from the roasting and gold extraction of high-copper gold ore according to the present invention. Detailed Implementation

[0034] It should be noted that the following detailed descriptions are illustrative and intended to provide further explanation of this application. Unless otherwise specified, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application pertains.

[0035] It should be noted that the terminology used herein is for the purpose of describing particular implementations only and is not intended to limit the exemplary implementations according to this application. As used herein, the singular form includes the plural form unless the context clearly indicates otherwise. Furthermore, it should be understood that when the terms "comprising" and / or "including" are used in this description, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0036] The technical solution of the present invention will be clearly and completely described below with reference to the embodiments. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0037] Example 1

[0038] S11. Add 100g K2S2O7, 20g Na2O2 and 80g NaOH to 1kg tailings (40-100 mesh), mix well, and calcine at 600℃ for 120min. After the reaction is completed, cool to obtain the calcined product.

[0039] S12. Grind the calcined product to a particle size of less than 350 mesh (more than 50% of the particles are below 350 mesh), wash with water to pH 7-8, add hydrochloric acid to the calcined product at a solid-liquid ratio of 1:1, mix evenly, and treat at 90-95℃ for 120 min to carry out the first leaching reaction. After the reaction is completed, cool and separate the solid and liquid phases to obtain the first solid phase and the first liquid phase.

[0040] S13. Add 200g NH4Br, 250g NaBrO3, 60mL H2SO4 and 1940mL water to the first solid phase, adjust the pH to 0.5-2, stir at room temperature for 2h to carry out the second leaching reaction, separate the solid and liquid phases to obtain iron-silicon slag and the second liquid phase. The main components of the iron-silicon slag are iron and silicon, which can be further processed and utilized.

[0041] S14. The second liquid phase is subjected to cation resin adsorption using a KP-300GR adsorption column. After adsorption, it is eluted with 3MHCL to obtain silver and copper loaded cation resin and the third liquid phase.

[0042] S15. The third liquid phase is subjected to anion exchange resin adsorption using a CH-90 adsorption column. After adsorption, it is eluted with 2M NaOH to obtain gold-loaded anion exchange resin and the fourth liquid phase. The silver and copper-loaded cation exchange resin is eluted with 3MHCL to obtain cation exchange resin and the fifth liquid phase. The obtained cation exchange resin can be reused for adsorption in the second liquid phase.

[0043] S16. The gold-loaded anion exchange resin is eluted with 2M NaOH to obtain anion exchange resin and a sixth liquid phase. Sodium bisulfite is added to the sixth liquid phase and solid-liquid separation is performed to obtain gold. The obtained anion exchange resin can be reused for adsorption in the third liquid phase.

[0044] S17. Add Cu to the fifth liquid phase for primary reduction, and then separate the solid and liquid phases to obtain silver. Add Zn to the obtained liquid phase for secondary reduction, and then separate the solid and liquid phases to obtain copper.

[0045] Example 2

[0046] S21. Add 75g K2S2O7, 30g Na2O2 and 50g NaOH to 1kg tailings (40-100 mesh), mix well, and calcine at 650℃ for 120min. After the reaction is completed, cool to obtain the calcined product.

[0047] S22. Grind the calcined product to a particle size of less than 350 mesh (more than 50% of the particles are below 350 mesh), wash with water to pH 7-8, add hydrochloric acid to the calcined product at a solid-liquid ratio of 1:1, mix evenly, and treat at 90-95℃ for 120 min to carry out the first leaching reaction. After the reaction is completed, cool and separate the solid and liquid phases to obtain the first solid phase and the first liquid phase.

[0048] S23. Add 150g NH4Br, 200g NaBrO3, 60mL H2SO4 and 1940mL water to the first solid phase, adjust the pH to 0.5-2, stir at room temperature for 2h to carry out the second leaching reaction, separate the solid and liquid phases to obtain iron-silicon slag and the second liquid phase. The main components of the iron-silicon slag are iron and silicon, which can be further processed and utilized.

[0049] S24. The second liquid phase is subjected to cation resin adsorption using a KP-300GR adsorption column. After adsorption, it is eluted with 3MHCl to obtain silver and copper loaded cation resin and the third liquid phase.

[0050] S25. The third liquid phase is subjected to anion exchange resin adsorption using a CH-90 adsorption column. After adsorption, it is eluted with 2M NaOH to obtain gold-loaded anion exchange resin and the fourth liquid phase. The silver and copper-loaded cation exchange resin is eluted with 3M HCl to obtain cation exchange resin and the fifth liquid phase. The obtained cation exchange resin can be reused for adsorption in the second liquid phase.

[0051] S26. The gold-loaded anion exchange resin is eluted with 2M NaOH to obtain anion exchange resin and a sixth liquid phase. Sodium bisulfite is added to the sixth liquid phase and solid-liquid separation is performed to obtain gold. The obtained anion exchange resin can be reused for adsorption in the third liquid phase.

[0052] S27. Add Cu to the fifth liquid phase for primary reduction, and then separate the solid and liquid phases to obtain silver. Add Zn to the obtained liquid phase for secondary reduction, and then separate the solid and liquid phases to obtain copper.

[0053] Example 3

[0054] S31. Add 50g K2S2O7, 50g Na2O2 and 30g NaOH to 1kg tailings (40-100 mesh), mix well, and calcine at 700℃ for 90min. After the reaction is completed, cool to obtain the calcined product.

[0055] S32. Grind the calcined product to a particle size of less than 350 mesh (more than 50% of the particles are below 350 mesh), wash with water to pH 7-8, add hydrochloric acid to the calcined product at a solid-liquid ratio of 1:1, mix evenly, and treat at 90-95℃ for 120 min to carry out the first leaching reaction. After the reaction is completed, cool and separate the solid and liquid phases to obtain the first solid phase and the first liquid phase.

[0056] S33. Add 100g NH4Br, 150g NaBrO3, 60mL H2SO4 and 1940mL water to the first solid phase, adjust the pH to 0.5-2, stir at room temperature for 2h to carry out the second leaching reaction, separate the solid and liquid phases to obtain iron-silicon slag and the second liquid phase. The main components of the iron-silicon slag are iron and silicon, which can be further processed and utilized.

[0057] S34. The second liquid phase is subjected to cation resin adsorption using a KP-300GR adsorption column. After adsorption, it is eluted with 3MHCl to obtain silver and copper loaded cation resin and the third liquid phase.

[0058] S35. The third liquid phase is subjected to anion exchange resin adsorption using a CH-90 adsorption column. After adsorption, it is eluted with 2M NaOH to obtain gold-loaded anion exchange resin and the fourth liquid phase. The silver and copper-loaded cation exchange resin is eluted with 3M HCl to obtain cation exchange resin and the fifth liquid phase. The obtained cation exchange resin can be reused for adsorption in the second liquid phase.

[0059] S36. The gold-loaded anion exchange resin is eluted with 2M NaOH to obtain anion exchange resin and a sixth liquid phase. Sodium bisulfite is added to the sixth liquid phase and solid-liquid separation is performed to obtain gold. The obtained anion exchange resin can be reused for adsorption in the third liquid phase.

[0060] S37. Add Cu to the fifth liquid phase for primary reduction, and then separate the solid and liquid phases to obtain silver. Add Fe to the obtained liquid phase for secondary reduction, and then separate the solid and liquid phases to obtain copper.

[0061] Example 4

[0062] S41. Add 100g K2S2O7, 30g Na2O2 and 50g NaOH to 1kg tailings (40-100 mesh), mix well, and calcine at 700℃ for 90min. After the reaction is completed, cool to obtain the calcined product.

[0063] S42. Grind the calcined product to a particle size of less than 350 mesh (more than 50% of the particles are below 350 mesh), wash with water to pH 7-8, add hydrochloric acid to the calcined product at a solid-liquid ratio of 1:1, mix evenly, and treat at 90-95℃ for 120 min to carry out the first leaching reaction. After the reaction is completed, cool and separate the solid and liquid phases to obtain the first solid phase and the first liquid phase.

[0064] S43. Add 150g NH4Br, 200g NaBrO3, 60mL H2SO4 and 1940mL water to the first solid phase, adjust the pH to 0.5-2, stir at room temperature for 2h to carry out the second leaching reaction, separate the solid and liquid phases to obtain iron-silicon slag and the second liquid phase. The main components of the iron-silicon slag are iron and silicon, which can be further processed and utilized.

[0065] S44. The second liquid phase is subjected to cation adsorption using a KP-300GR adsorption column. After adsorption, it is eluted with 3MHCl to obtain silver and copper loaded cation resin and the third liquid phase.

[0066] S45. The third liquid phase is subjected to anion exchange resin adsorption using a CH-90 adsorption column. After adsorption, it is eluted with 2M NaOH to obtain gold-loaded anion exchange resin and the fourth liquid phase. The silver and copper-loaded cation exchange resin is eluted with 3M HCl to obtain cation exchange resin and the fifth liquid phase. The obtained cation exchange resin can be reused for adsorption in the second liquid phase.

[0067] S46. The gold-loaded anion exchange resin is eluted with 2M NaOH to obtain anion exchange resin and a sixth liquid phase. Sodium bisulfite is added to the sixth liquid phase, and solid-liquid separation is performed to obtain gold. The obtained anion exchange resin can be reused for adsorption in the third liquid phase.

[0068] S47. Add Cu to the fifth liquid phase for primary reduction, and then separate the solid and liquid phases to obtain silver. Add Fe to the obtained liquid phase for secondary reduction, and then separate the solid and liquid phases to obtain copper.

[0069] To investigate the leaching effect of the ammonium bromide stirring leaching method of the present invention on tailings, the contents of gold, silver and copper in the iron-silicon slag obtained in Examples 1-4 were tested, and the test results are shown in Table 1.

[0070] Table 1 Test Results of Examples 1-4

[0071]

[0072] Compare with Example 1

[0073] 1 kg of tailings was treated using a conventional cyanidation method (7.5 g ammonium cyanide), with a solid-liquid ratio of 1:(2-5), a leaching time of 24 h, and a pH of 10-11.

[0074] The resin adsorption process and parameters after the leaching reaction are basically the same as those in Example 1.

[0075] The treatment results compared to Example 1 are shown in Table 2:

[0076] Table 2 shows the test results compared to Example 1.

[0077]

[0078]

[0079] As shown in Table 2, the cyanidation method cannot effectively leach gold and silver, and the leaching tailings are hazardous solid waste, posing a high risk to production safety.

[0080] Compare with Example 2

[0081] The conventional thiourea method was used (sulfuric acid 125-175 mL, Fe...). 3+ 30-75g) was used to treat 1kg of tailings, wherein the solid-liquid ratio of leaching was 1:3, the leaching time was 5h, and the pH was 0.5-2.0;

[0082] The resin adsorption process and parameters after the leaching reaction are basically the same as those in Example 1.

[0083] The treatment results compared to Example 2 are shown in Table 3:

[0084] Table 3 shows the test results compared to Example 2.

[0085]

[0086] As shown in Table 3, the thiourea method is also ineffective in leaching gold and silver from the tailings.

[0087] Compare with Example 3

[0088] 1 kg of tailings was treated using the conventional thiourea method (80-129 g ammonium thiosulfate, 3-5 g / L copper ammonia), with a solid-liquid ratio of 1:2, a leaching time of 5 h, and a temperature of 40-55 ℃.

[0089] The resin adsorption process and parameters after the leaching reaction are basically the same as those in Example 1.

[0090] The treatment results compared to Example 3 are shown in Table 4:

[0091] Table 4. Test results compared to Example 2

[0092]

[0093] As shown in Table 4, the thiosulfate process is also ineffective in leaching gold and silver from the tailings.

[0094] In summary, this invention effectively solves the technological challenges of comprehensive utilization of high-copper roasting tailings, avoids the drawbacks of high energy consumption from high-temperature chlorination volatilization, permanent copper loss, low silver utilization, complex production systems, large investments, and exorbitant costs. It also solves the problem that cyanide and thiourea methods cannot effectively extract gold, silver, and copper. At the same time, the bromide in the leachate can be recycled, avoiding large amounts of wastewater discharge and resulting in good ecological benefits. Furthermore, the main components of the leaching tailings are iron and silicon, which can be further processed and utilized.

[0095] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A comprehensive utilization method of high-copper gold ore roasting gold extraction tailings, characterized in that, The method comprises the following steps: S1, adding a loose agent, a first oxidizing agent and a fluxing agent into tailings, mixing uniformly, and then performing a roasting reaction, and obtaining a roasting product after cooling; S2, performing a first leaching reaction on the roasting product after ball milling and washing to near neutral, mixing uniformly with hydrochloric acid, and then cooling, solid-liquid separation, and obtaining a first solid phase and a first liquid phase; S3, adding ammonium bromide and a second oxidizing agent into the first solid phase, adjusting the pH to 0.5-2 using a sulfuric acid solution, and then performing a second leaching reaction at room temperature, and obtaining iron-silicon slag and a second liquid phase after solid-liquid separation; S4, performing cation resin adsorption on the second liquid phase, eluting, and obtaining silver and copper cation resin and a third liquid phase; S5, performing anion resin adsorption on the third liquid phase, eluting, and obtaining gold anion resin and a fourth liquid phase, and eluting the silver and copper cation resin, and obtaining cation resin and a fifth liquid phase; S6, eluting the gold anion resin, and obtaining anion resin and a sixth liquid phase, and obtaining gold after reduction and solid-liquid separation of the sixth liquid phase; S7, sequentially performing a first reduction and a second reduction on the fifth liquid phase, and obtaining silver and copper, respectively; The steps S6 and S7 have no order limitation; In step S1, the loose agent is K2S2O7, the first oxidizing agent is Na2O2, and the fluxing agent is NaOH, and the amount of the loose agent is 5-10% of the mass of the tailings, the amount of the first oxidizing agent is 2-5% of the mass of the tailings, and the amount of the fluxing agent is 2-5% of the mass of the tailings; In step S2, the second oxidizing agent is NaBrO3.

2. The comprehensive utilization method of high-copper gold ore roasting gold extraction tailings according to claim 1, characterized in that, In step S1, the temperature is controlled to be 600-700 DEG C during the roasting, and the time is 60-120 min.

3. The high-copper gold ore roasting gold extraction tailings comprehensive utilization method according to claim 1, characterized in that, In step S2, the mass ratio of the roasting product to the hydrochloric acid leaching solution is 1:(1-2) during the first leaching reaction, and the temperature of the leaching reaction is 90-95 DEG C, and the time is 1-3 h.

4. The comprehensive utilization method of high-copper gold ore roasting gold extraction tailings according to claim 1, characterized in that, In step S3, the amount of ammonium bromide is 10-20% of the mass of the first solid phase, and the amount of the second oxidizing agent is 15-25% of the mass of the first solid phase.

5. The high-copper gold ore roasting gold extraction tailings comprehensive utilization method according to claim 1, characterized in that, In step S3, the mass ratio of the first solid phase to the leaching solution is 1:(2-3) during the second leaching reaction, and the time of the leaching reaction is 1-3 h.

6. The high-copper gold ore roasting gold extraction tailings comprehensive utilization method according to claim 1, characterized in that, In step S4, the cation resin is KP-300GR, and the eluent is 2-4M HCl.

7. The high-copper gold ore roasting gold extraction tailings comprehensive utilization method according to claim 1, characterized in that, In step S5, the anion resin is CH-90, and the eluent is 1-3M NaOH; When the silver and copper cation resin is eluted, the eluent is 2-4M HCl; In step S6, when the gold anion resin is eluted, the eluent is 1-3M NaOH.

8. The high-copper gold ore roasting gold extraction tailings comprehensive utilization method according to claim 1, characterized in that, In step S6, the reducing agent used during the reduction includes any one of sodium bisulfite, hydrogen and metal iron.

9. The high-copper gold ore roasting gold extraction tailings comprehensive utilization method according to claim 1, characterized in that, In step S7, the reducing agent used during the first reduction includes metal copper; The reducing agent used during the second reduction includes any one of Zn and Fe.

Images