A method for reusing lead-zinc ore beneficiation wastewater

Abstract

This invention provides a method for reusing lead-zinc ore beneficiation wastewater. Wastewater generated from different flotation steps during the beneficiation process can be reused in the corresponding flotation operations without treatment or after only simple treatment. This eliminates the need for specialized water treatment processes, ensures the wastewater does not affect beneficiation indicators, and helps reduce collector usage, thereby improving lead-zinc beneficiation performance. The process described above can beneficiate lead-zinc ore at the natural pH of the ore pulp without adding lime or sulfuric acid, achieving the goals of reducing beneficiation reagents, improving beneficiation indicators, and eliminating wastewater discharge—all in a highly efficient lead-zinc beneficiation process. This process features simple water treatment, with no strong acids or alkalis added throughout the entire process, significantly reducing water treatment and beneficiation reagent costs, resulting in substantial social and economic benefits.

Description

Technical Field

[0001] This invention relates to a method for reusing wastewater in the field of mineral processing, and more particularly to a method for reusing mineral processing wastewater in lead-zinc ore beneficiation, applicable to various lead-zinc ore beneficiation applications. Background Technology

[0002] Lead and zinc are important non-ferrous metal ores in my country, with a wide range of applications. Lead is widely used in the electrical, machinery, and military industries, and especially with the current development of new energy sources and the large-scale use of lead-acid batteries, a large amount of lead metal is needed. Zinc, due to its excellent properties such as good rollability, wear resistance, and corrosion resistance, can be alloyed with various metals to form alloys with even better physical and chemical properties, making it an important non-ferrous metal ore.

[0003] Lead-zinc mines require significant amounts of water during both mining and beneficiation processes, with beneficiation water accounting for the largest proportion of water used in mine production. Lead-zinc ore beneficiation typically employs flotation, which usually requires 4–7 ml of water to process one ton of ore. 3 Lead-zinc mines typically involve the recovery of a large number of metals. To better separate these metals, various mineral processing reagents are added during the flotation process. This results in mineral processing wastewater often containing significant amounts of residual reagents, heavy metal ions, and suspended solids, making it a major factor impacting the mine environment. Because untreated or poorly treated wastewater inevitably affects mineral processing production to varying degrees, severe cases can even halt normal plant operations. Therefore, in traditional mineral processing, a large portion of the wastewater, containing substantial amounts of toxic and harmful substances, is directly discharged, causing serious harm to the natural environment and even threatening the survival of humans and other organisms.

[0004] Currently, mineral processing plants both domestically and internationally primarily rely on natural sedimentation, coagulation sedimentation, and neutralization methods for wastewater treatment. These methods are ineffective at removing organic flotation reagents from the wastewater, resulting in treated water that still fails to meet flotation requirements. While research has explored advanced oxidation methods such as photocatalysis and microbial degradation to treat organic matter in wastewater, these methods are difficult to implement in mines due to high costs or stringent environmental requirements. Therefore, simple, effective, and low-cost wastewater treatment remains a crucial and urgent issue in mineral processing production. Efficient recycling of mineral processing wastewater not only solves the environmental pollution problem caused by mine wastewater discharge but also conserves water resources, yielding significant economic and social benefits.

[0005] Background Example 1: Invention Patent: A process and equipment for treating and reusing lead-zinc ore beneficiation wastewater, publication number: CN109502900B. This patent discloses a process for treating and reusing lead-zinc ore beneficiation wastewater, enabling complete reuse. The process involves: collecting wastewater through pipelines, adjusting the flow rate, and initial sedimentation to reduce suspended particulate matter; then, two-stage ozone targeted catalytic oxidation to remove foaming substances; the ozone oxidation effluent is mechanically aerated and then subjected to anaerobic and aerated biological filters for biochemical treatment; the biochemical effluent undergoes secondary sedimentation and is then filtered through sand to obtain the final effluent, which is reused in the mineral processing flotation process. This process requires two stages of ozone targeted catalytic oxidation to remove foaming substances, followed by mechanical aeration and then anaerobic and aerated biological filters for biochemical treatment. The process is complex and costly, making it unaffordable for most beneficiation plants.

[0006] Background Example 2, Invention Patent: A Method for Reusing Wastewater from Lead-Zinc Ore Beneficiation, Publication No.: CN111495581B. This patent discloses a method primarily addressing the problem of reusing wastewater from lead-zinc ore beneficiation. Specifically targeting the treatment and resource utilization of lead-zinc ore beneficiation wastewater in high-altitude and cold regions, it involves treating the wastewater to varying degrees before returning it to the corresponding lead-zinc flotation operation. This fully utilizes residual reagents and heavy metal ions in the wastewater, requiring only a small portion of the water for advanced treatment to achieve good separation indicators. However, since this method primarily targets the treatment and resource utilization of lead-zinc ore beneficiation wastewater in high-altitude and cold regions, further advanced treatment is still necessary.

[0007] Background Example 3: Invention Patent: A Four-Step Method for Treating and Recycling Tin Ore Beneficiation Wastewater, Publication No.: CN102030445B, discloses a four-step method for treating and recycling tin ore beneficiation wastewater, including four steps: new beneficiation technology, chemical treatment, physical treatment, and biological treatment. The process is complex and difficult for general beneficiation plants to implement.

[0008] Background Example 4, Invention Patent: A Method for Recycling Wastewater from Sulfide Lead-Zinc Ore Beneficiation, Publication No.: CN105084490A. This patent discloses a method for recycling wastewater from sulfide lead-zinc ore beneficiation. The wastewater first enters a purification tank for natural purification, then undergoes coagulation treatment with coagulant in a coagulation tank, and finally is reused in beneficiation operations. This technology is a conventional wastewater treatment process and is unlikely to meet the actual water needs of beneficiation plants. Summary of the Invention

[0009] The purpose of this invention is to adopt a highly efficient, environmentally friendly, and low-cost mineral processing wastewater treatment process to reduce the cost of mineral processing wastewater treatment and enable its efficient and comprehensive utilization.

[0010] The principle of this invention is as follows:

[0011] Generally, the main factor affecting mineral processing production through wastewater reuse is the residual collector in the wastewater. In this process, the residual reagent in wastewater 1 is mainly P1, which has no adverse effect on lead beneficiation and can even reduce the amount of collector P1 used. The residual reagent in wastewater 2 is mainly LY, which has no adverse effect on zinc processing and can even reduce the amount of collector LY used. The main impact of wastewater 3 and wastewater 4 in the elevated water tank is the residual xanthate; after treatment with Ts3 when returned to the grinding and classification process, it will have virtually no adverse effect on lead and zinc processing. Ts3 is a compound reagent composed of sodium carbonate, sodium sulfide, and high-polymer aluminum sulfate. The sodium carbonate in the combined reagent can be hydrolyzed in the slurry to obtain OH-. - HCO 3- CO3 2- Plasma can eliminate unavoidable Ca ions in water. 2+ Mg 2+ The harmful effects of sodium carbonate and residual zinc sulfate are eliminated. Sodium carbonate reacts with residual zinc sulfate to deposit both hydrophilic Zn(OH)₂ and hydrophilic Zn(CO₃)(OH)₆ colloidal particles on the surface of sphalerite and pyrite. These particles cover the surface of sphalerite and pyrite, enhancing their hydrophilicity and thus inhibiting their activity. Sodium sulfide combined with high-polymer aluminum sulfate undergoes micro-flocculation, masking residual collectors in the water and eliminating suspended solids (SS). Therefore, the modifier Ts₃ can eliminate the impact on production when wastewater 3+ wastewater 4 is returned to the grinding and classification process. All collectors in this process do not affect the flotation of sulfur; therefore, returning wastewater 3+ wastewater 4 from the high-level pool to the sulfur processing has no adverse effects, requires no water treatment, and reduces the amount of xanthate collector used in the process. The above principles illustrate that the mineral processing and water treatment method provided by this invention can achieve simple treatment of mineral processing wastewater, enabling its efficient resource utilization. Furthermore, the mineral processing indicators for lead, zinc, and sulfur after reuse are all higher than those of conventional processes, resulting in high-quality lead and zinc concentrates. The costs of mineral processing wastewater treatment and mineral processing reagents are also significantly reduced.

[0012] This invention is achieved through the following technical solution:

[0013] A method for reusing wastewater from lead-zinc ore beneficiation includes grinding the raw ore to obtain a raw ore slurry, then performing lead flotation on the raw ore slurry, performing zinc flotation on the lead flotation tailings, and performing sulfur flotation on the zinc flotation tailings; the wastewater 1 obtained after thickening and dewatering the lead concentrate obtained from lead flotation is returned to the lead flotation operation, the wastewater 2 obtained after thickening and dewatering the zinc concentrate obtained from zinc flotation is returned to the zinc flotation operation, and the wastewater 3 obtained after thickening and dewatering the sulfur concentrate obtained from sulfur flotation and the wastewater 4 obtained after thickening and dewatering the tailings obtained from sulfur flotation are recycled to a high-level water tank;

[0014] Then, based on the water consumption and requirements of grinding, lead flotation, zinc flotation and sulfur flotation, the wastewater recovered from the high-level water tank is adjusted and returned to the grinding, lead flotation, zinc flotation and sulfur flotation operations respectively.

[0015] Preferably, the wastewater 1 is clarified in the collection tank 1 before being returned to the lead flotation operation.

[0016] Preferably, the wastewater 2 is clarified in the collection tank 2 before being returned to the zinc flotation operation.

[0017] Preferably, a modifier Ts3 is added to the wastewater returned from the high-level water tank to the grinding operation; the modifier Ts3, by weight percentage, comprises: 70%–80% sodium carbonate, 5%–20% sodium sulfide, and 5%–20% high polyaluminum sulfate.

[0018] Preferably, the lead flotation steps include: adding inhibitors to the raw ore slurry, stirring, adding lead collectors, and performing lead roughing to obtain lead roughing concentrate and lead roughing tailings; repeatedly adding inhibitors to the lead roughing concentrate for multiple lead cleaning operations, and repeatedly adding lead collectors to the lead roughing tailings for multiple lead scavenging operations to finally obtain lead concentrate and lead tailings; thickening and dewatering the lead concentrate to obtain wastewater 1, which is then returned to the lead cleaning operation for use; the lead tailings enter the zinc flotation operation; and the wastewater from the high-level water tank is returned to the lead roughing scavenging operation for use.

[0019] Preferably, the zinc flotation steps include: adding copper sulfate to the lead tailings obtained after lead flotation, stirring, adding zinc collector, and then performing zinc roughing to obtain zinc roughing concentrate and zinc roughing tailings; performing multiple zinc cleaning operations on the zinc roughing concentrate, and adding zinc collector to the zinc roughing tailings multiple times to perform multiple zinc scavenging operations to finally obtain zinc concentrate and zinc tailings; thickening and dewatering the zinc concentrate to obtain wastewater 2, and returning wastewater 2 to the zinc cleaning and zinc roughing operations for use; and the zinc tailings entering the sulfur flotation operation.

[0020] Preferably, the sulfur flotation steps include: adding sulfur collectors and frothers to the zinc tailings obtained after zinc flotation for sulfur roughing to obtain sulfur roughing concentrate and sulfur roughing tailings; performing multiple sulfur cleaning operations on the sulfur roughing concentrate and multiple sulfur scavenging operations on the sulfur roughing tailings by adding sulfur collectors multiple times to finally obtain sulfur concentrate and tailings; obtaining wastewater 3 after thickening and dewatering the sulfur concentrate and obtaining wastewater 4 after thickening and dewatering the tailings; recycling wastewater 3 and wastewater 4 to a high-level water tank; and returning the wastewater from the high-level water tank to the sulfur cleaning and sulfur flotation operations for use.

[0021] Preferredly, the raw ore is ground to obtain a raw ore slurry with a particle size of -0.074 mm accounting for 60% to 85%.

[0022] Compared with existing technologies, the beneficial effects of this invention are as follows: By adopting a wastewater branching and reuse method, the wastewater generated from different flotation steps in the mineral processing can be reused in the corresponding flotation operations without treatment or after simple treatment. This not only eliminates the need for specialized water treatment processes, but also ensures that the mineral processing wastewater does not affect the mineral processing indicators, and helps reduce the amount of collector used, thereby improving lead-zinc mineral processing indicators. The above process can carry out lead-zinc mineral processing at the natural pH of the slurry, achieving the goal of reducing mineral processing reagents, improving mineral processing indicators, and achieving highly efficient lead-zinc mineral processing with no wastewater discharge. This process has a simple water treatment method, with no addition of strong acids or alkalis throughout the entire process, greatly reducing the cost of water treatment and mineral processing reagents, resulting in significant social and economic benefits. Attached Figure Description

[0023] To more clearly illustrate the technical solutions in the embodiments of the present invention, the present invention will be further described below with reference to the accompanying drawings.

[0024] Figure 1 This is a flow chart of the wastewater treatment and mineral processing technology used in this invention;

[0025] Figure 2 This is a flow chart of existing lead-zinc mine wastewater treatment and mineral processing technology. Detailed Implementation

[0026] This invention relates to wastewater treatment in mineral processing and corresponding mineral processing methods. Wastewater from mineral processing plants mainly originates from four parts: lead concentrate, zinc concentrate, sulfur concentrate, and tailings. Calculations of the water volume for each part show that the proportion of wastewater generated from lead concentrate, zinc concentrate, sulfur concentrate, and tailings is approximately 8:16:16:60. Water usage in mineral processing plants is primarily for grinding and classification, lead flotation, zinc flotation, and sulfur-lead flotation. Process analysis shows that the proportion of water used in grinding and classification, lead flotation, zinc flotation, and sulfur flotation is approximately 50:20:16:14. This invention employs highly efficient and environmentally friendly lead and zinc collectors, utilizing their high selectivity for sequential preferential flotation of lead, zinc, and sulfur. The component with the greatest impact on wastewater reuse in the involved mineral processing process is the residual sulfur collector xanthate in the wastewater. Returning wastewater from lead, zinc, and sulfur processes to their respective corresponding operations would be beneficial to the process flow. However, the analysis of wastewater sources and production water usage shows that the wastewater and water usage generated by each operation are not perfectly matched. Through detailed analysis, a refined reuse approach was adopted to minimize the amount of water requiring treatment. The specific operations are as follows: wastewater from lead concentrate is returned to the lead beneficiation operation after clarification; wastewater from zinc concentrate is returned to the zinc flotation operation after clarification; and wastewater from sulfur concentrate and tailings is collected and then dispersed back to the grinding and classification, lead roughing, and sulfur flotation operations. However, the wastewater returned to the grinding and classification operation requires simple treatment by adding the modifier Ts3. Ts3 masks calcium and magnesium ions and excess xanthate molecules to eliminate the wastewater's impact on subsequent beneficiation processes. Since all reagents have no adverse effect on the sulfur flotation operation, the wastewater returned to the sulfur flotation operation requires no further treatment.

[0027] The above wastewater reuse mineral processing technology employs highly efficient and environmentally friendly lead and zinc collectors, carrying out sequential preferential flotation of lead, zinc, and sulfur at the natural pH of the slurry. Lead flotation utilizes a novel depressant, Ts2, and a novel lead collector, P1; zinc flotation uses CuSO4 as an activator and LY as the zinc collector; and sulfur flotation uses butyl xanthate as the collector. # Oil is used as a foaming agent. The entire mineral processing and water treatment process does not add lime or strong acids and alkalis, which is beneficial to environmental protection. Furthermore, after wastewater is recycled, the amount of reagents used in each operation is reduced, and the lead and zinc levels are higher than those of conventional processes.

[0028] The above-mentioned modifier Ts3, calculated by weight percentage, includes: 70%–80% sodium carbonate, 5%–20% sodium sulfide, and 5%–20% aluminum polysulfate.

[0029] The following are some examples of modifier Ts3 for further illustration.

[0030] Modifier Ts3 in Example 1: 70% sodium carbonate, 10% sodium sulfide, and 20% aluminum polysulfate.

[0031] In Example 2, the modifier Ts3 contains 75% sodium carbonate, 20% sodium sulfide, and 5% aluminum polysulfate.

[0032] In Example 3, the modifier Ts3 contained 78% sodium carbonate, 9% sodium sulfide, and 13% aluminum polysulfate.

[0033] In Example 4, the modifier Ts3 contains 80% sodium carbonate, 5% sodium sulfide, and 15% aluminum polysulfate.

[0034] The inhibitor Ts2, by weight percentage, includes: sodium carbonate 20%–30%, humate 1%–5%, lignin sulfonate 1%–5%, bleaching powder 1%–5%, sodium sulfite 10%–20%, and zinc sulfate 50%–60%.

[0035] Some examples of modifier Ts2 are given below for further illustration.

[0036] Example 1 of the inhibitor Ts2: 30% sodium carbonate, 4% humate, 1% lignin sulfonate, 5% bleaching powder, 10% sodium sulfite, and 50% zinc sulfate.

[0037] Example 2 of the inhibitor Ts2: Sodium carbonate 20%, humate 1%, lignin sulfonate 5%, bleaching powder 4%, sodium sulfite 10%, zinc sulfate 60%.

[0038] Example 3 of the inhibitor Ts2: Sodium carbonate 21%, humate 5%, lignin sulfonate 2%, bleaching powder 1%, sodium sulfite 20%, zinc sulfate 51%.

[0039] Example 4 of the inhibitor Ts2: Sodium carbonate 23%, humate 3%, lignin sulfonate 3%, bleaching powder 2%, sodium sulfite 12%, zinc sulfate 57%.

[0040] Lead collector P1, by weight percentage, comprises: 5% sodium hydroxide, 70%–80% dipropyl dithiophosphate, 5%–15% imidazole thiol, and 5%–15% trithiocarbonate. Its preparation steps are as follows: Prepare a 10% aqueous solution of sodium hydroxide; mix dipropyl dithiophosphate and imidazole thiol thoroughly and add them to the sodium hydroxide solution; heat to 50°C and react for 0.5 hours to obtain solution 1. Then add trithiocarbonate to solution 1, maintain the temperature at 50°C, and react for another 0.5 hours. After the reaction is complete, a brown to dark brown solution is obtained, which is the lead collector P1.

[0041] Some examples of lead collector P1 are given below for further illustration.

[0042] Lead collector P1 Example 1: Sodium hydroxide 5%, dipropyl dithiophosphate 80%, imidazole thiol 5%, trithiocarbonate 10%.

[0043] Lead collector P1 Example 2: 5% sodium hydroxide, 70% dipropyl dithiophosphate, 10% imidazole thiol, and 15% trithiocarbonate.

[0044] Lead collector P1 Example 3: Sodium hydroxide 5%, dipropyl dithiophosphate 75%, imidazole thiol 15%, trithiocarbonate 5%.

[0045] Lead collector P1 Example 4: Sodium hydroxide 5%, dipropyl dithiophosphate 73%, imidazole thiol 11%, trithiocarbonate 11%.

[0046] The zinc collector LY, by weight percentage, comprises: 70-80% N,N-dialkyldithiocarbamate, 10-20% alkyl dithiophosphate thioether ester, 3-5% octanol, and 5-10% nonpolar oil. Its preparation involves uniformly mixing N,N-dialkyldithiocarbamate and alkyl dithiophosphate thioether ester, then adding octanol and 0... # Diesel fuel, stirred at 300 r / min for 0.5 h, yields zinc collector LY.

[0047] The following are some examples of zinc collector LY for further illustration.

[0048] Zinc collector LY Example 1: 70% N,N-dialkyl dithiocarbamate, 20% alkyl dithiophosphate thioether ester, 3% octanol, 0 # Diesel fuel 7%.

[0049] Zinc collector LY Example 2, N,N-dialkyl dithiocarbamate 72%, alkyl dithiophosphate thioether ester 13%, octanol 5%, 0 # Diesel fuel 10%.

[0050] Zinc collector LY Example 3: 80% N,N-dialkyl dithiocarbamate, 10% alkyl dithiophosphate thioether ester, 5% octanol, 0 # Diesel fuel 5%.

[0051] Zinc collector LY Example 4, N,N-dialkyl dithiocarbamate 78%, alkyl dithiophosphate thioether ester 12%, octanol 4%, 0 # Diesel fuel 6%.

[0052] The technical solution of the present invention will be described in detail below through specific embodiments, but this does not limit the scope of the present invention. The embodiments described below are only some embodiments of the present invention, not all embodiments. All other similar embodiments made by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0053] In the following embodiments, unless otherwise specified, all reagents used are commercially available products. Specific experimental procedures or conditions were performed in accordance with the conventional experimental procedures and conditions described in the literature in this field.

[0054] The process flow of the example is shown below. Figure 1 Lead, zinc, and sulfur were preferentially floated in the order described above. The properties of the raw ore in the comparative example were consistent with those in the embodiment. The process flow and reagent types are as follows. Figure 2 The results are shown in Table 2.

[0055] Example 1: An experimental study was conducted on the mineral processing wastewater treatment process and mineral processing technology of a lead-zinc mine in Yunnan.

[0056] A lead-zinc mine in Yunnan Province has Pb, Zn, and S contents of 5.33%, 15.60%, and 28.86%, respectively. The main useful minerals are galena, sphalerite, and pyrite, while the gangue minerals are primarily dolomite and calcite. It is a high-sulfur lead-zinc mine. The wastewater from the new beneficiation process (lead concentrate wastewater) has a pH of 8.15, a COD content of 58 mg / L, and a Ca content of... 2+ The content is 86 mg / L, Pb 2+ The content is 10.5 mg / L, Zn 2+ The content is 3.5 mg / L, Cu 2+ The concentration of the first wastewater was 0.8 mg / L, and the suspended solids (SS) concentration was 48 mg / L; the pH of wastewater 2 (zinc concentrate wastewater) was 8.26, the COD concentration was 65 mg / L, and the Ca concentration was... 2+ The content is 78 mg / L, Pb 2+ The content is 5.3 mg / L, Zn 2+ The content is 8.5 mg / L, Cu 2+ The concentration was 0.4 mg / L, and the suspended solids (SS) concentration was 57 mg / L; the pH value of wastewater 3 + wastewater 4 (sulfur concentrate wastewater + tailings wastewater) was 8.09, the COD concentration was 126 mg / L, and the Ca concentration was... 2+ The content is 77 mg / L, Pb 2+ The content is 4.6 mg / L, Zn 2+ The content is 4.9 mg / L, Cu 2+ The concentration was 0.3 mg / L, and the suspended solids (SS) concentration was 55 mg / L. The treatment, resource utilization, and lead-zinc recovery methods for lead-zinc ore beneficiation wastewater are carried out according to the following steps:

[0057] (1) In the process, the lead concentrate thick water is pumped into the collection tank 1 and does not need to be treated as supplementary water for lead beneficiation. In the process, the zinc concentrate thick water is pumped into the collection tank 2 and does not need to be treated as supplementary water for zinc flotation operations. In the process, the sulfur concentrate and tailings water are pumped into the high-level water tank and used as supplementary water for grinding and classification operations, lead rough scavenging operations and sulfur flotation operations.

[0058] (2) Add the raw ore and water from the collection pool to the mill in a certain proportion, add 600g / t of modifier Ts3 and grind to obtain a slurry with a grinding fineness of -0.074mm particle size accounting for 75%.

[0059] (3) The slurry obtained in step (2) was added to a flotation machine for lead-preferred flotation. The lead-preferred flotation consisted of one roughing, three scavenging, and three cleaning processes to obtain lead concentrate and lead scavenging tailings. The slurry obtained in step (2) was added to 1000 g / t inhibitor Ts2 and 100 g / t collector P1 for lead roughing to obtain lead roughing concentrate and lead roughing tailings.

[0060] (4) Add 30g / t collector P1 to the lead roughing tailings obtained in step (3) for lead scavenging 1 to obtain lead scavenging 1 concentrate and lead scavenging 1 tailings; add 15g / t collector P1 to the lead scavenging 1 tailings for lead scavenging 2 to obtain lead scavenging 2 concentrate and lead scavenging 2 tailings; add 10g / t collector P1 to the lead scavenging 2 tailings for lead scavenging 3 to obtain lead scavenging 3 concentrate and lead scavenging 3 tailings, which is the final lead scavenging tailings; the lead scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0061] (5) Add 200g / t inhibitor Ts2 to the lead roughing concentrate obtained in step (3) for lead beneficiation 1 to obtain lead beneficiation 1 concentrate and lead beneficiation 1 tailings; add 100g / t inhibitor Ts2 to the lead beneficiation 1 concentrate for lead beneficiation 2 to obtain lead beneficiation 2 concentrate and lead beneficiation 2 tailings; add 50g / t inhibitor Ts2 to the lead beneficiation 2 concentrate for lead beneficiation 3 to obtain lead beneficiation 3 concentrate and lead beneficiation 3 tailings. The lead beneficiation 3 concentrate is the final lead concentrate; the lead beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0062] (6) The lead scavenging tailings obtained in step (4) are subjected to zinc preferential flotation. The zinc preferential flotation consists of one roughing, three scavenging, and two cleaning processes to obtain zinc concentrate and zinc scavenging tailings. The lead scavenging tailings obtained in step (4) are then subjected to zinc roughing by adding 500 g / t activator CuSO4 and 80 g / t collector LY to obtain zinc roughing concentrate and zinc roughing tailings.

[0063] (7) Add 30g / t collector LY to the zinc roughing tailings obtained in step (6) for zinc scavenging 1 to obtain zinc scavenging 1 concentrate and zinc scavenging 1 tailings; add 20g / t collector LY to the zinc scavenging 1 tailings for zinc scavenging 2 to obtain zinc scavenging 2 concentrate and zinc scavenging 2 tailings; add 10g / t collector LY to the zinc scavenging 2 tailings for zinc scavenging 3 to obtain zinc scavenging 3 concentrate and zinc scavenging 3 tailings, and the zinc scavenging 3 tailings are the final zinc scavenging tailings; each zinc scavenging concentrate is returned to the previous stage as middlings in sequence.

[0064] (8) The zinc roughing concentrate obtained in step (6) is subjected to zinc beneficiation 1 without adding reagents to obtain zinc beneficiation 1 concentrate and zinc beneficiation 1 tailings; the zinc beneficiation 1 concentrate is subjected to zinc beneficiation 2 without adding reagents to obtain zinc beneficiation 2 concentrate and zinc beneficiation 2 tailings. The zinc beneficiation 2 concentrate is the final zinc concentrate; the zinc beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0065] (9) The zinc scavenging tailings obtained in step (7) were subjected to sulfur flotation. The sulfur flotation consisted of one roughing, two scavenging, and one cleaning stage to obtain sulfur concentrate and tailings. 150 g / t of collector butyl xanthate and 20 g / t of frother were added to the zinc scavenging tailings obtained in step (7). # The oil undergoes sulfur roughing to obtain sulfur roughing concentrate and sulfur roughing tailings.

[0066] (10) Add 50g / t of collector butyl xanthate to the sulfur roughing tailings obtained in step (9) for sulfur scavenging 1 to obtain sulfur scavenging 1 concentrate and sulfur scavenging 1 tailings; add 20g / t of collector butyl xanthate to the sulfur scavenging 1 tailings for sulfur scavenging 2 to obtain sulfur scavenging 2 concentrate and sulfur scavenging 2 tailings, and sulfur scavenging 2 tailings are the final tailings; the sulfur scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0067] (11) The sulfur roughing concentrate obtained in step (9) is subjected to sulfur refining without adding reagents to obtain sulfur refined concentrate and sulfur refined tailings. The sulfur refined concentrate is the final sulfur concentrate, and the sulfur refined tailings are returned to the sulfur roughing operation as middlings.

[0068] Comparative Example 1: The raw ore was the same as in Example 1.

[0069] Comparative Example 1 Figure 1 The process flow includes water treatment and mineral processing. The resulting total wastewater from mineral processing (wastewater 1 + wastewater 2 + wastewater 3 + wastewater 4) has a pH of 12.5, a COD content of 386 mg / L, and a Ca content of... 2+ The content is 658 mg / L, Pb 2+ The content is 8.6 mg / L, Zn 2+ The content is 5.7 mg / L, Cu 2+ The concentration was 0.5 mg / L, and the suspended solids (SS) concentration was 256 mg / L. The treatment, resource utilization, and lead-zinc recovery methods for lead-zinc ore beneficiation wastewater are carried out according to the following steps:

[0070] (1) In the process, lead concentrate, zinc concentrate, sulfur concentrate, and tailings are concentrated and dewatered to obtain mineral processing wastewater. The wastewater is pumped into a collection tank and then flows into a regulating tank. In the regulating tank, 3000 g / t sodium carbonate is added for calcium removal. The water after calcium removal enters a coagulation reaction tank, where 1500 g / t sulfuric acid is added to adjust the pH value. Then, 100 g / t PAM and 50 g / t PAC are added for three-stage flocculation and sedimentation. The clarified water obtained after sedimentation enters an aeration tank, where ozone is introduced for aeration. After that, it enters an adsorption tank, where 100 g / t activated carbon is added for adsorption and impurity removal. The water after the above water treatment process is pumped into a high-level water tank for use in various parts of the mineral processing production.

[0071] (2) The raw ore and water from the high-level water tank are added to the mill in a certain proportion for grinding to obtain a slurry with a grinding fineness of -0.074mm particle size accounting for 75%.

[0072] (3) The slurry obtained in step (2) was added to a flotation machine for lead-preferred flotation. The lead-preferred flotation consisted of one roughing, three scavenging, and three cleaning processes to obtain lead concentrate and lead scavenging tailings. The slurry obtained in step (2) was then mixed with 1500 g / t lime, 800 g / t zinc sulfate, 120 g / t collector SN-9, and 50 g / t frother 2. # The oil is subjected to lead roughing to obtain lead roughing concentrate and lead roughing tailings.

[0073] (4) Add 50g / t collector SN-9 to the lead roughing tailings obtained in step (3) for lead scavenging 1 to obtain lead scavenging 1 concentrate and lead scavenging 1 tailings; add 25g / t collector SN-9 to the lead scavenging 1 tailings for lead scavenging 2 to obtain lead scavenging 2 concentrate and lead scavenging 2 tailings; add 15g / t collector SN-9 to the lead scavenging 2 tailings for lead scavenging 3 to obtain lead scavenging 3 concentrate and lead scavenging 3 tailings, which is the final lead scavenging tailings; the lead scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0074] (5) Add 300g / t lime and 150g / t zinc sulfate to the lead roughing concentrate obtained in step (3) for lead beneficiation 1 to obtain lead beneficiation 1 concentrate and lead beneficiation 1 tailings; add 150g / t lime and 50g / t zinc sulfate to the lead beneficiation 1 concentrate for lead beneficiation 2 to obtain lead beneficiation 2 concentrate and lead beneficiation 2 tailings; add 100g / t lime and 30g / t zinc sulfate to the lead beneficiation 2 concentrate for lead beneficiation 3 to obtain lead beneficiation 3 concentrate and lead beneficiation 3 tailings. The lead beneficiation 3 concentrate is the final lead concentrate; the lead beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0075] (6) The lead scavenging tailings obtained in step (4) were subjected to zinc preferential flotation. The zinc preferential flotation consisted of one roughing, three scavenging, and two cleaning processes to obtain zinc concentrate and zinc scavenging tailings. 2000 g / t lime, 600 g / t activator CuSO4, 100 g / t collector butyl xanthate, and 30 g / t frother 2 were added to the lead scavenging tailings obtained in step (4). # The oil is subjected to zinc roughing to obtain zinc roughing concentrate and zinc roughing tailings.

[0076] (7) Add 35g / t of collector butyl xanthate to the zinc roughing tailings obtained in step (6) for zinc scavenging 1 to obtain zinc scavenging 1 concentrate and zinc scavenging 1 tailings; add 20g / t of collector butyl xanthate to the zinc scavenging 1 tailings for zinc scavenging 2 to obtain zinc scavenging 2 concentrate and zinc scavenging 2 tailings; add 10g / t of collector butyl xanthate to the zinc scavenging 2 tailings for zinc scavenging 3 to obtain zinc scavenging 3 concentrate and zinc scavenging 3 tailings, which is the final zinc scavenging tailings; each zinc scavenging concentrate is returned to the previous stage as middlings in sequence.

[0077] (8) The zinc roughing concentrate obtained in step (6) is subjected to zinc beneficiation 1 without adding reagents to obtain zinc beneficiation 1 concentrate and zinc beneficiation 1 tailings; the zinc beneficiation 1 concentrate is subjected to zinc beneficiation 2 without adding reagents to obtain zinc beneficiation 2 concentrate and zinc beneficiation 2 tailings. The zinc beneficiation 2 concentrate is the final zinc concentrate; the zinc beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0078] (9) The zinc scavenging tailings obtained in step (7) were subjected to sulfur flotation. The sulfur flotation consisted of one roughing, two scavenging, and one cleaning stage to obtain sulfur concentrate and tailings. 500 g / t of activator sulfuric acid, 180 g / t of collector butyl xanthate, and 20 g / t of frother were added to the zinc scavenging tailings obtained in step (7). # The oil undergoes sulfur roughing to obtain sulfur roughing concentrate and sulfur roughing tailings.

[0079] (10) Add 50g / t of collector butyl xanthate to the sulfur roughing tailings obtained in step (9) for sulfur scavenging 1 to obtain sulfur scavenging 1 concentrate and sulfur scavenging 1 tailings; add 30g / t of collector butyl xanthate to the sulfur scavenging 1 tailings for sulfur scavenging 2 to obtain sulfur scavenging 2 concentrate and sulfur scavenging 2 tailings, and sulfur scavenging 2 tailings are the final tailings; the sulfur scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0080] (11) The sulfur roughing concentrate obtained in step (9) is subjected to sulfur refining without adding reagents to obtain sulfur refined concentrate and sulfur refined tailings. The sulfur refined concentrate is the final sulfur concentrate, and the sulfur refined tailings are returned to the sulfur roughing operation as middlings.

[0081] Example 2: An experimental study was conducted on the mineral processing wastewater treatment process and mineral processing technology of a lead-zinc mine in Yunnan.

[0082] A lead-zinc mine in Yunnan Province has Pb, Zn, and S contents of 6.58%, 19.26%, and 27.56%, respectively. The main useful minerals are galena, sphalerite, and pyrite, while the gangue minerals are primarily dolomite, calcite, and muscovite. Figure 2 The wastewater from the new mineral processing process (lead concentrate wastewater) has a pH of 7.58, a COD content of 62 mg / L, and a Ca content of... 2+ The content is 79 mg / L, Pb 2+ The content is 9.25 mg / L, Zn 2+ The content was 4.26 mg / L, Cu 2+ The concentration of SS (suspended solids) was 0.54 mg / L, and the concentration of COD was 56 mg / L; Wastewater 2 (zinc concentrate wastewater) had a pH of 7.79, a COD concentration of 72 mg / L, and a Ca concentration of 0.54 mg / L. 2+ The content is 70 mg / L, Pb 2+ The content is 5.9 mg / L, Zn 2+ The content is 9.7 mg / L, Cu 2+ The concentration was 0.47 mg / L, and the suspended solids (SS) concentration was 62 mg / L; the pH of wastewater 3 + wastewater 4 (sulfur concentrate wastewater + tailings wastewater) was 7.91, the COD concentration was 158 mg / L, and the Ca concentration was... 2+ The content is 81 mg / L, Pb 2+ The content is 5.3 mg / L, Zn 2+ The content is 6.7 mg / L, Cu 2+ The concentration was 0.6 mg / L, and the suspended solids (SS) concentration was 69 mg / L. The treatment, resource utilization, and lead-zinc recovery methods for lead-zinc ore beneficiation wastewater are carried out according to the following steps:

[0083] (1) In the process, the lead concentrate thick water is pumped into the collection tank 1 and does not need to be treated as supplementary water for lead beneficiation. In the process, the zinc concentrate thick water is pumped into the collection tank 2 and does not need to be treated as supplementary water for zinc flotation operations. In the process, the sulfur concentrate and tailings water are pumped into the high-level water tank and used as supplementary water for grinding and classification operations, lead rough scavenging operations and sulfur flotation operations.

[0084] (2) Add the raw ore and water from the collection pool to the mill in a certain proportion, add 800g / t of modifier Ts3 and grind to obtain a slurry with a grinding fineness of 0.074mm and a particle size of 73%.

[0085] (3) The slurry obtained in step (2) was added to a flotation machine for lead-preferred flotation. The lead-preferred flotation consisted of one roughing, three scavenging, and three cleaning processes to obtain lead concentrate and lead scavenging tailings. The slurry obtained in step (2) was added to 1200 g / t inhibitor Ts2 and 120 g / t collector P1 for lead roughing to obtain lead roughing concentrate and lead roughing tailings.

[0086] (4) Add 40g / t collector P1 to the lead roughing tailings obtained in step (3) for lead scavenging 1 to obtain lead scavenging 1 concentrate and lead scavenging 1 tailings; add 20g / t collector P1 to the lead scavenging 1 tailings for lead scavenging 2 to obtain lead scavenging 2 concentrate and lead scavenging 2 tailings; add 15g / t collector P1 to the lead scavenging 2 tailings for lead scavenging 3 to obtain lead scavenging 3 concentrate and lead scavenging 3 tailings, which is the final lead scavenging tailings; the lead scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0087] (5) Add 300g / t inhibitor Ts2 to the lead roughing concentrate obtained in step (3) for lead beneficiation 1 to obtain lead beneficiation 1 concentrate and lead beneficiation 1 tailings; add 200g / t inhibitor Ts2 to the lead beneficiation 1 concentrate for lead beneficiation 2 to obtain lead beneficiation 2 concentrate and lead beneficiation 2 tailings; add 100g / t inhibitor Ts2 to the lead beneficiation 2 concentrate for lead beneficiation 3 to obtain lead beneficiation 3 concentrate and lead beneficiation 3 tailings. The lead beneficiation 3 concentrate is the final lead concentrate; the lead beneficiation tailings of each level are returned to the previous level in sequence as middlings.

[0088] (6) The lead scavenging tailings obtained in step (4) are subjected to zinc preferential flotation. The zinc preferential flotation consists of two roughing processes, three scavenging processes, and one cleaning process to obtain zinc concentrate and zinc scavenging tailings. The lead scavenging tailings obtained in step (4) are added to 600 g / t activator CuSO4 and 100 g / t collector LY for zinc roughing 1 to obtain zinc roughing 1 concentrate and zinc roughing 1 tailings. The zinc roughing 1 tailings are added to 30 g / t collector LY for zinc roughing 2 to obtain zinc roughing 2 concentrate and zinc roughing 2 tailings. The zinc roughing 1 concentrate and zinc roughing 2 concentrate are combined into zinc roughing concentrate.

[0089] (7) Add 40g / t collector LY to the zinc roughing tailings obtained in step (6) for zinc scavenging 1 to obtain zinc scavenging 1 concentrate and zinc scavenging 1 tailings; add 25g / t collector LY to the zinc scavenging 1 tailings for zinc scavenging 2 to obtain zinc scavenging 2 concentrate and zinc scavenging 2 tailings; add 15g / t collector LY to the zinc scavenging 2 tailings for zinc scavenging 3 to obtain zinc scavenging 3 concentrate and zinc scavenging 3 tailings, which is the final zinc scavenging tailings; each zinc scavenging concentrate is returned to the previous stage as middlings in sequence.

[0090] (8) The zinc roughing concentrate obtained in step (6) is subjected to zinc beneficiation 1 without adding reagents to obtain zinc beneficiation 1 concentrate and zinc beneficiation 1 tailings; zinc beneficiation 1 concentrate is the final zinc concentrate; zinc beneficiation 1 tailings are returned to zinc roughing 1.

[0091] (9) The zinc scavenging tailings obtained in step (7) were subjected to sulfur flotation. The sulfur flotation consisted of one roughing, two scavenging, and one cleaning stage to obtain sulfur concentrate and tailings. 180 g / t of collector butyl xanthate and 20 g / t of frother were added to the zinc scavenging tailings obtained in step (7).# The oil undergoes sulfur roughing to obtain sulfur roughing concentrate and sulfur roughing tailings.

[0092] (10) Add 50g / t of collector butyl xanthate to the sulfur roughing tailings obtained in step (9) for sulfur scavenging 1 to obtain sulfur scavenging 1 concentrate and sulfur scavenging 1 tailings; add 30g / t of collector butyl xanthate to the sulfur scavenging 1 tailings for sulfur scavenging 2 to obtain sulfur scavenging 2 concentrate and sulfur scavenging 2 tailings, and sulfur scavenging 2 tailings are the final tailings; the sulfur scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0093] (11) The sulfur roughing concentrate obtained in step (9) is subjected to sulfur refining without adding reagents to obtain sulfur refined concentrate and sulfur refined tailings. The sulfur refined concentrate is the final sulfur concentrate, and the sulfur refined tailings are returned to the sulfur roughing operation as middlings.

[0094] Comparative Example 2: The raw ore was the same as in Example 2.

[0095] Comparative Example 2 Figure 1 The process flow includes water treatment and mineral processing. The resulting total wastewater from mineral processing (wastewater 1 + wastewater 2 + wastewater 3 + wastewater 4) has a pH of 12.8, a COD content of 458 mg / L, and a Ca content of... 2+ The content is 758 mg / L, Pb 2+ The content is 9.58 mg / L, Zn 2+ The content is 12.25 mg / L, Cu 2+ The concentration was 0.66 mg / L, and the suspended solids (SS) concentration was 358 mg / L. The treatment, resource utilization, and lead-zinc recovery methods for lead-zinc ore beneficiation wastewater are carried out according to the following steps:

[0096] (1) In the process, lead concentrate, zinc concentrate, sulfur concentrate, and tailings are thickened and dewatered to obtain mineral processing wastewater. The wastewater is pumped into a collection tank and then flows into a regulating tank. In the regulating tank, 8000 g / t sodium carbonate is added for calcium removal. The water after calcium removal enters a coagulation reaction tank, where 3000 g / t sulfuric acid is added to adjust the pH value. Then, 150 g / t PAM and 75 g / t PAC are added for three-stage flocculation and sedimentation. The clarified water obtained after sedimentation enters an aeration tank, where ozone is introduced for aeration. After that, it enters an adsorption tank, where 200 g / t activated carbon is added for adsorption and impurity removal. The water after the above water treatment process is pumped into a high-level water tank for use in various parts of the mineral processing production.

[0097] (2) The raw ore and water from the high-level water tank are added to the mill in a certain proportion for grinding to obtain a slurry with a grinding fineness of 0.074 mm and a particle size of 73%.

[0098] (3) The slurry obtained in step (2) was added to a flotation machine for lead-preferred flotation. The lead-preferred flotation consisted of one roughing, three scavenging, and three cleaning processes to obtain lead concentrate and lead scavenging tailings. The slurry obtained in step (2) was then mixed with 2000 g / t lime, 1200 g / t zinc sulfate, 150 g / t collector SN-9, and 50 g / t frother 2. # The oil is subjected to lead roughing to obtain lead roughing concentrate and lead roughing tailings.

[0099] (4) Add 60g / t collector SN-9 to the lead roughing tailings obtained in step (3) for lead scavenging 1 to obtain lead scavenging 1 concentrate and lead scavenging 1 tailings; add 30g / t collector SN-9 to the lead scavenging 1 tailings for lead scavenging 2 to obtain lead scavenging 2 concentrate and lead scavenging 2 tailings; add 20g / t collector SN-9 to the lead scavenging 2 tailings for lead scavenging 3 to obtain lead scavenging 3 concentrate and lead scavenging 3 tailings, which is the final lead scavenging tailings; the lead scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0100] (5) Add 500g / t lime and 200g / t zinc sulfate to the lead roughing concentrate obtained in step (3) for lead beneficiation 1 to obtain lead beneficiation 1 concentrate and lead beneficiation 1 tailings; add 300g / t lime and 100g / t zinc sulfate to the lead beneficiation 2 to obtain lead beneficiation 2 concentrate and lead beneficiation 2 tailings; add 200g / t lime and 50g / t zinc sulfate to the lead beneficiation 3 to obtain lead beneficiation 3 concentrate and lead beneficiation 3 tailings. The lead beneficiation 3 concentrate is the final lead concentrate; the lead beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0101] (6) The lead scavenging tailings obtained in step (4) were subjected to zinc preferential flotation. The zinc preferential flotation consisted of two roughing processes, three scavenging processes, and one cleaning process to obtain zinc concentrate and zinc scavenging tailings. 5000 g / t lime, 800 g / t activator CuSO4, 150 g / t collector butyl xanthate, and 30 g / t frother 2 were added to the lead scavenging tailings obtained in step (4). # The oil is subjected to zinc roughing 1 to obtain zinc roughing 1 concentrate and zinc roughing 1 tailings; the zinc roughing 1 tailings are added to 30g / t collector butyl xanthate for zinc roughing 2 to obtain zinc roughing 2 concentrate and zinc roughing 2 tailings; the zinc roughing 1 concentrate and zinc roughing 2 concentrate are combined into zinc roughing concentrate.

[0102] (7) Add 50g / t of collector butyl xanthate to the zinc roughing tailings obtained in step (6) for zinc scavenging 1 to obtain zinc scavenging 1 concentrate and zinc scavenging 1 tailings; add 30g / t of collector butyl xanthate to the zinc scavenging 1 tailings for zinc scavenging 2 to obtain zinc scavenging 2 concentrate and zinc scavenging 2 tailings; add 20g / t of collector butyl xanthate to the zinc scavenging 2 tailings for zinc scavenging 3 to obtain zinc scavenging 3 concentrate and zinc scavenging 3 tailings, which is the final zinc scavenging tailings; each zinc scavenging concentrate is returned to the previous stage as middlings in sequence.

[0103] (8) The zinc roughing concentrate obtained in step (6) is subjected to zinc beneficiation 1 without adding reagents to obtain zinc beneficiation 1 concentrate and zinc beneficiation 1 tailings; zinc beneficiation 1 concentrate is the final zinc concentrate; zinc beneficiation 1 tailings are returned to zinc roughing 1.

[0104] (9) The zinc scavenging tailings obtained in step (7) were subjected to sulfur flotation. The sulfur flotation consisted of one roughing, two scavenging, and one cleaning stage to obtain sulfur concentrate and tailings. 800 g / t of activator sulfuric acid, 200 g / t of collector butyl xanthate, and 20 g / t of frother were added to the zinc scavenging tailings obtained in step (7). # The oil undergoes sulfur roughing to obtain sulfur roughing concentrate and sulfur roughing tailings.

[0105] (10) Add 60g / t of collector butyl xanthate to the sulfur roughing tailings obtained in step (9) for sulfur scavenging 1 to obtain sulfur scavenging 1 concentrate and sulfur scavenging 1 tailings; add 30g / t of collector butyl xanthate to the sulfur scavenging 1 tailings for sulfur scavenging 2 to obtain sulfur scavenging 2 concentrate and sulfur scavenging 2 tailings, and sulfur scavenging 2 tailings are the final tailings; the sulfur scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0106] (11) The sulfur roughing concentrate obtained in step (9) is subjected to sulfur refining without adding reagents to obtain sulfur refined concentrate and sulfur refined tailings. The sulfur refined concentrate is the final sulfur concentrate, and the sulfur refined tailings are returned to the sulfur roughing operation as middlings.

[0107] Example 3: An experimental study was conducted on the wastewater treatment process and mineral processing technology of a lead-zinc mine in Inner Mongolia.

[0108] A lead-zinc mine in Inner Mongolia has Pb, Zn, and S contents of 3.35%, 2.85%, and 24.65%, respectively. The main useful minerals are galena, sphalerite, and pyrite, while the gangue minerals are primarily quartz, muscovite, and kaolinite. The wastewater from the new beneficiation process (lead concentrate wastewater) has a pH of 7.95, a COD content of 62 mg / L, and a Ca content of... 2+ The content is 74 mg / L, Pb 2+ The content is 8.6 mg / L, Zn 2+ The content is 3.3 mg / L, Cu 2+The concentration of the first wastewater was 0.3 mg / L, and the suspended solids (SS) concentration was 46 mg / L; the pH of wastewater 2 (zinc concentrate wastewater) was 7.69, the COD concentration was 69 mg / L, and the Ca concentration was... 2+ The content is 71 mg / L, Pb 2+ The content is 6.2 mg / L, Zn 2+ The content is 7.9 mg / L, Cu 2+ The concentration was 0.2 mg / L, and the suspended solids (SS) concentration was 53 mg / L; the pH of wastewater 3 + wastewater 4 (sulfur concentrate wastewater + tailings wastewater) was 7.48, the COD concentration was 118 mg / L, and the Ca concentration was... 2+ The content is 67 mg / L, Pb 2+ The content is 5.1 mg / L, Zn 2+ The content is 4.5 mg / L, Cu 2+ The concentration was 0.25 mg / L, and the suspended solids (SS) concentration was 76 mg / L. The treatment, resource utilization, and lead-zinc recovery methods for lead-zinc ore beneficiation wastewater are carried out according to the following steps:

[0109] (1) In the process, the lead concentrate thick water is pumped into the collection tank 1 and does not need to be treated as supplementary water for lead beneficiation. In the process, the zinc concentrate thick water is pumped into the collection tank 2 and does not need to be treated as supplementary water for zinc flotation operations. In the process, the sulfur concentrate and tailings water are pumped into the high-level water tank and used as supplementary water for grinding and classification operations, lead rough scavenging operations and sulfur flotation operations.

[0110] (2) Add the raw ore and water from the collection pool to the mill in a certain proportion, add 500g / t of modifier Ts3 and grind to obtain a slurry with a grinding fineness of -0.074mm particle size accounting for 70%.

[0111] (3) The slurry obtained in step (2) was added to a flotation machine for lead-preferred flotation. The lead-preferred flotation consisted of one roughing, three scavenging, and three cleaning processes to obtain lead concentrate and lead scavenging tailings. The slurry obtained in step (2) was added to 800 g / t inhibitor Ts2 and 70 g / t collector P1 for lead roughing to obtain lead roughing concentrate and lead roughing tailings.

[0112] (4) Add 20 g / t collector P1 to the lead roughing tailings obtained in step (3) for lead scavenging 1 to obtain lead scavenging 1 concentrate and lead scavenging 1 tailings; add 10 g / t collector P1 to the lead scavenging 1 tailings for lead scavenging 2 to obtain lead scavenging 2 concentrate and lead scavenging 2 tailings; add 5 g / t collector P1 to the lead scavenging 2 tailings for lead scavenging 3 to obtain lead scavenging 3 concentrate and lead scavenging 3 tailings, which is the final lead scavenging tailings; the lead scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0113] (5) Add 130 g / t inhibitor Ts2 to the lead roughing concentrate obtained in step (3) for lead beneficiation 1 to obtain lead beneficiation 1 concentrate and lead beneficiation 1 tailings; add 80 g / t inhibitor Ts2 to the lead beneficiation 1 concentrate for lead beneficiation 2 to obtain lead beneficiation 2 concentrate and lead beneficiation 2 tailings; add 50 g / t inhibitor Ts2 to the lead beneficiation 2 concentrate for lead beneficiation 3 to obtain lead beneficiation 3 concentrate and lead beneficiation 3 tailings. The lead beneficiation 3 concentrate is the final lead concentrate; the lead beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0114] (6) The lead scavenging tailings obtained in step (4) are subjected to zinc preferential flotation. The zinc preferential flotation consists of one roughing, three scavenging, and two cleaning processes to obtain zinc concentrate and zinc scavenging tailings. The lead scavenging tailings obtained in step (4) are added to 300 g / t activator CuSO4 and 60 g / t collector LY for zinc roughing to obtain zinc roughing concentrate and zinc roughing tailings.

[0115] (7) Add 20g / t collector LY to the zinc roughing tailings obtained in step (6) for zinc scavenging 1 to obtain zinc scavenging 1 concentrate and zinc scavenging 1 tailings; add 10g / t collector LY to the zinc scavenging 1 tailings for zinc scavenging 2 to obtain zinc scavenging 2 concentrate and zinc scavenging 2 tailings; add 5g / t collector LY to the zinc scavenging 2 tailings for zinc scavenging 3 to obtain zinc scavenging 3 concentrate and zinc scavenging 3 tailings, which is the final zinc scavenging tailings; each zinc scavenging concentrate is returned to the previous stage as middlings in sequence.

[0116] (8) The zinc roughing concentrate obtained in step (6) is subjected to zinc beneficiation 1 without adding reagents to obtain zinc beneficiation 1 concentrate and zinc beneficiation 1 tailings; the zinc beneficiation 1 concentrate is subjected to zinc beneficiation 2 without adding reagents to obtain zinc beneficiation 2 concentrate and zinc beneficiation 2 tailings. The zinc beneficiation 2 concentrate is the final zinc concentrate; the zinc beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0117] (9) The zinc scavenging tailings obtained in step (7) were subjected to sulfur flotation. The sulfur flotation consisted of one roughing, two scavenging, and one cleaning stage to obtain sulfur concentrate and tailings. 140 g / t of collector butyl xanthate and 20 g / t of frother were added to the zinc scavenging tailings obtained in step (7). # The oil undergoes sulfur roughing to obtain sulfur roughing concentrate and sulfur roughing tailings.

[0118] (10) Add 45g / t of collector butyl xanthate to the sulfur roughing tailings obtained in step (9) for sulfur scavenging 1 to obtain sulfur scavenging 1 concentrate and sulfur scavenging 1 tailings; add 15g / t of collector butyl xanthate to the sulfur scavenging 1 tailings for sulfur scavenging 2 to obtain sulfur scavenging 2 concentrate and sulfur scavenging 2 tailings, and sulfur scavenging 2 tailings are the final tailings; the sulfur scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0119] (11) The sulfur roughing concentrate obtained in step (9) is subjected to sulfur refining without adding reagents to obtain sulfur refined concentrate and sulfur refined tailings. The sulfur refined concentrate is the final sulfur concentrate, and the sulfur refined tailings are returned to the sulfur roughing operation as middlings.

[0120] Comparative Example 3: The raw ore was the same as in Example 3.

[0121] Comparative Example 3 Figure 1 The process flow includes water treatment and mineral processing. The resulting total wastewater from mineral processing (wastewater 1 + wastewater 2 + wastewater 3 + wastewater 4) has a pH of 11.58, a COD content of 306 mg / L, and a Ca content of... 2+ The content is 568 mg / L, Pb 2+ The content is 7.9 mg / L, Zn 2+ The content is 5.7 mg / L, Cu 2+ The concentration was 0.1 mg / L, and the suspended solids (SS) concentration was 233 mg / L. The treatment, resource utilization, and lead-zinc recovery methods for lead-zinc ore beneficiation wastewater are carried out according to the following steps:

[0122] (1) In the process, lead concentrate, zinc concentrate, sulfur concentrate, and tailings are concentrated and dewatered to obtain mineral processing wastewater. The wastewater is pumped into a collection tank and then flows into an equalization tank. In the equalization tank, 1500 g / t sodium carbonate is added for calcium removal. The water after calcium removal enters a coagulation reaction tank, where 600 g / t sulfuric acid is added to adjust the pH value. Then, 80 g / t PAM and 40 g / t PAC are added for three-stage flocculation and sedimentation. The clarified water obtained after sedimentation enters an aeration tank, where ozone is introduced for aeration. After that, it enters an adsorption tank, where 100 g / t activated carbon is added for adsorption and impurity removal. The water after the above water treatment process is pumped into a high-level water tank for use in various parts of the mineral processing production.

[0123] (2) The raw ore and water from the high-level water tank are added to the mill in a certain proportion for grinding to obtain a slurry with a grinding fineness of 0.074 mm and a particle size of 70%.

[0124] (3) The slurry obtained in step (2) was added to a flotation machine for lead-preferred flotation. The lead-preferred flotation consisted of one roughing, three scavenging, and three cleaning processes to obtain lead concentrate and lead scavenging tailings. The slurry obtained in step (2) was then mixed with 1500 g / t lime, 700 g / t zinc sulfate, 90 g / t collector SN-9, and 40 g / t frother 2. # The oil is subjected to lead roughing to obtain lead roughing concentrate and lead roughing tailings.

[0125] (4) Add 30g / t collector SN-9 to the lead roughing tailings obtained in step (3) for lead scavenging 1 to obtain lead scavenging 1 concentrate and lead scavenging 1 tailings; add 15g / t collector SN-9 to the lead scavenging 1 tailings for lead scavenging 2 to obtain lead scavenging 2 concentrate and lead scavenging 2 tailings; add 10g / t collector SN-9 to the lead scavenging 2 tailings for lead scavenging 3 to obtain lead scavenging 3 concentrate and lead scavenging 3 tailings, which is the final lead scavenging tailings; the lead scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0126] (5) Add 200g / t lime and 100g / t zinc sulfate to the lead roughing concentrate obtained in step (3) to carry out lead beneficiation 1, and obtain lead beneficiation 1 concentrate and lead beneficiation 1 tailings; add 100g / t lime and 50g / t zinc sulfate to the lead beneficiation 1 concentrate to carry out lead beneficiation 2, and obtain lead beneficiation 2 concentrate and lead beneficiation 2 tailings; add 50g / t lime and 30g / t zinc sulfate to the lead beneficiation 2 concentrate to carry out lead beneficiation 3, and obtain lead beneficiation 3 concentrate and lead beneficiation 3 tailings. The lead beneficiation 3 concentrate is the final lead concentrate; the lead beneficiation tailings of each level are returned to the previous level in sequence as middlings.

[0127] (6) The lead scavenging tailings obtained in step (4) were subjected to zinc preferential flotation. The zinc preferential flotation consisted of one roughing, three scavenging, and two cleaning processes to obtain zinc concentrate and zinc scavenging tailings. 2000 g / t lime, 450 g / t activator CuSO4, 80 g / t collector butyl xanthate, and 25 g / t frother 2 were added to the lead scavenging tailings obtained in step (4). # The oil is subjected to zinc roughing to obtain zinc roughing concentrate and zinc roughing tailings.

[0128] (7) Add 25g / t of collector butyl xanthate to the zinc roughing tailings obtained in step (6) for zinc scavenging 1 to obtain zinc scavenging 1 concentrate and zinc scavenging 1 tailings; add 10g / t of collector butyl xanthate to the zinc scavenging 1 tailings for zinc scavenging 2 to obtain zinc scavenging 2 concentrate and zinc scavenging 2 tailings; add 10g / t of collector butyl xanthate to the zinc scavenging 2 tailings for zinc scavenging 3 to obtain zinc scavenging 3 concentrate and zinc scavenging 3 tailings, and the zinc scavenging 3 tailings are the final zinc scavenging tailings; each zinc scavenging concentrate is returned to the previous stage as middlings in sequence.

[0129] (8) The zinc roughing concentrate obtained in step (6) is subjected to zinc beneficiation 1 without adding reagents to obtain zinc beneficiation 1 concentrate and zinc beneficiation 1 tailings; the zinc beneficiation 1 concentrate is subjected to zinc beneficiation 2 without adding reagents to obtain zinc beneficiation 2 concentrate and zinc beneficiation 2 tailings. The zinc beneficiation 2 concentrate is the final zinc concentrate; the zinc beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0130] (9) The zinc scavenging tailings obtained in step (7) were subjected to sulfur flotation. The sulfur flotation consisted of one roughing, two scavenging, and one cleaning stage to obtain sulfur concentrate and tailings. 400 g / t of activator sulfuric acid, 150 g / t of collector butyl xanthate, and 20 g / t of frother were added to the zinc scavenging tailings obtained in step (7). # The oil undergoes sulfur roughing to obtain sulfur roughing concentrate and sulfur roughing tailings.

[0131] (10) Add 40g / t of collector butyl xanthate to the sulfur roughing tailings obtained in step (9) for sulfur scavenging 1 to obtain sulfur scavenging 1 concentrate and sulfur scavenging 1 tailings; add 20g / t of collector butyl xanthate to the sulfur scavenging 1 tailings for sulfur scavenging 2 to obtain sulfur scavenging 2 concentrate and sulfur scavenging 2 tailings, and sulfur scavenging 2 tailings are the final tailings; the sulfur scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0132] (11) The sulfur roughing concentrate obtained in step (9) is subjected to sulfur refining without adding reagents to obtain sulfur refined concentrate and sulfur refined tailings. The sulfur refined concentrate is the final sulfur concentrate, and the sulfur refined tailings are returned to the sulfur roughing operation as middlings.

[0133] Example 4: An experimental study was conducted on the wastewater treatment process and mineral processing technology of a lead-zinc mine in Guangxi.

[0134] A lead-zinc mine in Guangxi has Pb, Zn, and S contents of 0.65%, 2.45%, and 7.10%, respectively. The main useful minerals are galena, sphalerite, and pyrite, while the gangue minerals are primarily barite, dolomite, quartz, and mica. The wastewater from the new beneficiation process (lead concentrate wastewater) has a pH of 7.36, a COD content of 66 mg / L, and a Ca content of... 2+ The content is 65 mg / L, Pb 2+ The content is 6.5 mg / L, Zn 2+ The content is 2.6 mg / L, Cu 2+ The concentration of the first wastewater was 0.2 mg / L, and the suspended solids (SS) concentration was 35 mg / L; the pH of wastewater 2 (zinc concentrate wastewater) was 7.9, the COD concentration was 68 mg / L, and the Ca concentration was... 2+ The content is 65 mg / L, Pb 2+ The content is 4.6 mg / L, Zn 2+ The content is 6.2 mg / L, Cu 2+ The concentration was 0.1 mg / L, and the suspended solids (SS) concentration was 42 mg / L; Wastewater 3 + Wastewater 4 (sulfur concentrate wastewater + tailings wastewater) had a pH of 7.8, a COD concentration of 112 mg / L, and a Ca concentration of 0.1 mg / L. 2+ The content is 65 mg / L, Pb 2+ The content is 5.1 mg / L, Zn 2+ The content is 3.8 mg / L, Cu 2+The concentration was 0.1 mg / L, and the suspended solids (SS) concentration was 68 mg / L. The treatment, resource utilization, and lead-zinc recovery methods for lead-zinc ore beneficiation wastewater are carried out according to the following steps:

[0135] (1) In the process, the lead concentrate thick water is pumped into the collection tank 1 and does not need to be treated as supplementary water for lead beneficiation. In the process, the zinc concentrate thick water is pumped into the collection tank 2 and does not need to be treated as supplementary water for zinc flotation operations. In the process, the sulfur concentrate and tailings water are pumped into the high-level water tank and used as supplementary water for grinding and classification operations, lead rough scavenging operations and sulfur flotation operations.

[0136] (2) Add the raw ore and water from the collection pool to the mill in a certain proportion, add 550g / t of modifier Ts3 and grind to obtain a slurry with a grinding fineness of -0.074mm particle size accounting for 80%.

[0137] (3) The slurry obtained in step (2) was added to a flotation machine for lead-preferred flotation. The lead-preferred flotation consisted of one roughing, three scavenging, and three cleaning processes to obtain lead concentrate and lead scavenging tailings. The slurry obtained in step (2) was added to 800 g / t inhibitor Ts2 and 60 g / t collector P1 for lead roughing to obtain lead roughing concentrate and lead roughing tailings.

[0138] (4) Add 20 g / t collector P1 to the lead roughing tailings obtained in step (3) for lead scavenging 1 to obtain lead scavenging 1 concentrate and lead scavenging 1 tailings; add 10 g / t collector P1 to the lead scavenging 1 tailings for lead scavenging 2 to obtain lead scavenging 2 concentrate and lead scavenging 2 tailings; add 5 g / t collector P1 to the lead scavenging 2 tailings for lead scavenging 3 to obtain lead scavenging 3 concentrate and lead scavenging 3 tailings, which is the final lead scavenging tailings; the lead scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0139] (5) Add 150g / t inhibitor Ts2 to the lead roughing concentrate obtained in step (3) for lead beneficiation 1 to obtain lead beneficiation 1 concentrate and lead beneficiation 1 tailings; add 80g / t inhibitor Ts2 to the lead beneficiation 1 concentrate for lead beneficiation 2 to obtain lead beneficiation 2 concentrate and lead beneficiation 2 tailings; add 30g / t inhibitor Ts2 to the lead beneficiation 2 concentrate for lead beneficiation 3 to obtain lead beneficiation 3 concentrate and lead beneficiation 3 tailings. The lead beneficiation 3 concentrate is the final lead concentrate; the lead beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0140] (6) The lead scavenging tailings obtained in step (4) are subjected to zinc preferential flotation. The zinc preferential flotation consists of one roughing, three scavenging, and three cleaning processes to obtain zinc concentrate and zinc scavenging tailings. The lead scavenging tailings obtained in step (4) are then subjected to zinc roughing by adding 300 g / t activator CuSO4 and 60 g / t collector LY to obtain zinc roughing concentrate and zinc roughing tailings.

[0141] (7) Add 30g / t collector LY to the zinc roughing tailings obtained in step (6) for zinc scavenging 1 to obtain zinc scavenging 1 concentrate and zinc scavenging 1 tailings; add 20g / t collector LY to the zinc scavenging 1 tailings for zinc scavenging 2 to obtain zinc scavenging 2 concentrate and zinc scavenging 2 tailings; add 10g / t collector LY to the zinc scavenging 2 tailings for zinc scavenging 3 to obtain zinc scavenging 3 concentrate and zinc scavenging 3 tailings, and the zinc scavenging 3 tailings are the final zinc scavenging tailings; each zinc scavenging concentrate is returned to the previous stage as middlings in sequence.

[0142] (8) The zinc roughing concentrate obtained in step (6) is subjected to zinc beneficiation 1 without reagents to obtain zinc beneficiation 1 concentrate and zinc beneficiation 1 tailings; the zinc beneficiation 1 concentrate is subjected to zinc beneficiation 2 without reagents to obtain zinc beneficiation 2 concentrate and zinc beneficiation 2 tailings; the zinc beneficiation 2 concentrate is subjected to zinc beneficiation 3 without reagents to obtain zinc beneficiation 3 concentrate and zinc beneficiation 3 tailings. The zinc beneficiation 3 concentrate is the final zinc concentrate; the zinc beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0143] (9) The zinc scavenging tailings obtained in step (7) were subjected to sulfur flotation. The sulfur flotation consisted of one roughing, three scavenging, and two cleaning processes to obtain sulfur concentrate and tailings. 80 g / t of collector butyl xanthate and 20 g / t of frother were added to the zinc scavenging tailings obtained in step (7). # The oil undergoes sulfur roughing to obtain sulfur roughing concentrate and sulfur roughing tailings.

[0144] (10) Add 30g / t of collector butyl xanthate to the sulfur roughing tailings obtained in step (9) for sulfur scavenging 1 to obtain sulfur scavenging 1 concentrate and sulfur scavenging 1 tailings; add 10g / t of collector butyl xanthate to the sulfur scavenging 1 tailings for sulfur scavenging 2 to obtain sulfur scavenging 2 concentrate and sulfur scavenging 2 tailings; add 5g / t of collector butyl xanthate to the sulfur scavenging 2 tailings for sulfur scavenging 3 to obtain sulfur scavenging 3 concentrate and sulfur scavenging 3 tailings, which is the final tailings; the sulfur scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0145] (11) The sulfur rough concentrate obtained in step (9) is subjected to sulfur beneficiation 1 without reagents to obtain sulfur beneficiation 1 concentrate and sulfur beneficiation 1 tailings; the sulfur beneficiation 1 concentrate is subjected to sulfur beneficiation 2 without reagents to obtain sulfur beneficiation 2 concentrate and sulfur beneficiation 2 tailings. The sulfur beneficiation 2 concentrate is the final sulfur concentrate. The sulfur beneficiation tailings of each level are returned to the previous level in sequence.

[0146] Comparative Example 4: The raw ore was the same as in Example 4.

[0147] Comparative Example 4 Figure 1 The process involves water treatment and mineral processing. The resulting total wastewater (wastewater 1 + wastewater 2 + wastewater 3 + wastewater 4) has a pH of 12.2, a COD content of 254 mg / L, and a Ca content of... 2+ The content is 365 mg / L, Pb2+ The content is 7.5 mg / L, Zn 2+ The content is 4.8 mg / L, Cu 2+ The concentration was 0.3 mg / L, and the suspended solids (SS) concentration was 218 mg / L. The treatment, resource utilization, and lead-zinc recovery methods for lead-zinc ore beneficiation wastewater are carried out according to the following steps:

[0148] (1) In the process, lead concentrate, zinc concentrate, sulfur concentrate, and tailings are thickened and dewatered to obtain mineral processing wastewater. The wastewater is pumped into a collection tank and then flows into a regulating tank. In the regulating tank, 2000 g / t sodium carbonate is added for calcium removal. The water after calcium removal enters a coagulation reaction tank, where 1000 g / t sulfuric acid is added to adjust the pH value. Then, 60 g / t PAM and 30 g / t PAC are added for three-stage flocculation and sedimentation. The clarified water obtained after sedimentation enters an aeration tank, where ozone is introduced for aeration. After that, it enters an adsorption tank, where 80 g / t activated carbon is added for adsorption and impurity removal. The water after the above water treatment process is pumped into a high-level water tank for use in various parts of the mineral processing production.

[0149] (2) The raw ore and water from the high-level water tank are added to the mill in a certain proportion for grinding to obtain a slurry with a grinding fineness of 0.074 mm and a particle size of 80%.

[0150] (3) The slurry obtained in step (2) was added to a flotation machine for lead-preferred flotation. The lead-preferred flotation consisted of one roughing, three scavenging, and three cleaning stages to obtain lead concentrate and lead scavenging tailings. The slurry obtained in step (2) was then mixed with 1000 g / t lime, 600 g / t zinc sulfate, 70 g / t collector SN-9, and 30 g / t frother 2. # The oil is subjected to lead roughing to obtain lead roughing concentrate and lead roughing tailings.

[0151] (4) Add 30g / t collector SN-9 to the lead roughing tailings obtained in step (3) for lead scavenging 1 to obtain lead scavenging 1 concentrate and lead scavenging 1 tailings; add 15g / t collector SN-9 to the lead scavenging 1 tailings for lead scavenging 2 to obtain lead scavenging 2 concentrate and lead scavenging 2 tailings; add 10g / t collector SN-9 to the lead scavenging 2 tailings for lead scavenging 3 to obtain lead scavenging 3 concentrate and lead scavenging 3 tailings, which is the final lead scavenging tailings; the lead scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0152] (5) Add 200g / t lime and 100g / t zinc sulfate to the lead roughing concentrate obtained in step (3) for lead beneficiation 1 to obtain lead beneficiation 1 concentrate and lead beneficiation 1 tailings; add 100g / t lime and 50g / t zinc sulfate to the lead beneficiation 1 concentrate for lead beneficiation 2 to obtain lead beneficiation 2 concentrate and lead beneficiation 2 tailings; add 100g / t lime to the lead beneficiation 2 concentrate for lead beneficiation 3 to obtain lead beneficiation 3 concentrate and lead beneficiation 3 tailings. The lead beneficiation 3 concentrate is the final lead concentrate; the lead beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0153] (6) The lead scavenging tailings obtained in step (4) were subjected to zinc preferential flotation. The zinc preferential flotation consisted of one roughing, three scavenging, and three cleaning processes to obtain zinc concentrate and zinc scavenging tailings. 1500 g / t lime, 400 g / t activator CuSO4, 60 g / t collector butyl xanthate, and 20 g / t frother 2 were added to the lead scavenging tailings obtained in step (4). # The oil is subjected to zinc roughing to obtain zinc roughing concentrate and zinc roughing tailings.

[0154] (7) Add 20g / t of collector butyl xanthate to the zinc roughing tailings obtained in step (6) for zinc scavenging 1 to obtain zinc scavenging 1 concentrate and zinc scavenging 1 tailings; add 10g / t of collector butyl xanthate to the zinc scavenging 1 tailings for zinc scavenging 2 to obtain zinc scavenging 2 concentrate and zinc scavenging 2 tailings; add 2g / t of collector butyl xanthate to the zinc scavenging 2 tailings for zinc scavenging 3 to obtain zinc scavenging 3 concentrate and zinc scavenging 3 tailings, which is the final zinc scavenging tailings; each zinc scavenging concentrate is returned to the previous stage as middlings in sequence.

[0155] (8) The zinc roughing concentrate obtained in step (6) is subjected to zinc beneficiation 1 without reagents to obtain zinc beneficiation 1 concentrate and zinc beneficiation 1 tailings; the zinc beneficiation 1 concentrate is subjected to zinc beneficiation 2 without reagents to obtain zinc beneficiation 2 concentrate and zinc beneficiation 2 tailings; the zinc beneficiation 2 concentrate is subjected to zinc beneficiation 3 without reagents to obtain zinc beneficiation 3 concentrate and zinc beneficiation 3 tailings. The zinc beneficiation 3 concentrate is the final zinc concentrate; the zinc beneficiation tailings of each level are returned to the previous level as middlings in sequence.

[0156] (9) The zinc scavenging tailings obtained in step (7) were subjected to sulfur flotation. The sulfur flotation consisted of one roughing, three scavenging, and two cleaning processes to obtain sulfur concentrate and tailings. 300 g / t of activator sulfuric acid, 100 g / t of collector butyl xanthate, and 20 g / t of frother were added to the zinc scavenging tailings obtained in step (7). # The oil undergoes sulfur roughing to obtain sulfur roughing concentrate and sulfur roughing tailings.

[0157] (10) Add 30g / t of collector butyl xanthate to the sulfur roughing tailings obtained in step (9) for sulfur scavenging 1 to obtain sulfur scavenging 1 concentrate and sulfur scavenging 1 tailings; add 15g / t of collector butyl xanthate to the sulfur scavenging 1 tailings for sulfur scavenging 2 to obtain sulfur scavenging 2 concentrate and sulfur scavenging 2 tailings; add 15g / t of collector butyl xanthate to the sulfur scavenging 2 tailings for sulfur scavenging 3 to obtain sulfur scavenging 3 concentrate and sulfur scavenging 3 tailings, which is the final tailings; the sulfur scavenging concentrates of each level are returned to the previous level as middlings in sequence.

[0158] (11) The sulfur rough concentrate obtained in step (9) is subjected to sulfur beneficiation 1 without reagents to obtain sulfur beneficiation 1 concentrate and sulfur beneficiation 1 tailings; the sulfur beneficiation 1 concentrate is subjected to sulfur beneficiation 2 without reagents to obtain sulfur beneficiation 2 concentrate and sulfur beneficiation 2 tailings. The sulfur beneficiation 2 concentrate is the final sulfur concentrate. The sulfur beneficiation tailings of each level are returned to the previous level in sequence.

[0159] Table 2 Experimental Results

[0160]

[0161] The results of the above examples and comparative experiments show that the method provided by this invention produces wastewater with a pH value of 6-8 (natural pH), and low levels of COD, metal ions, and suspended solids. Only wastewater 3 and wastewater 4 have slightly higher COD levels. After Ts3 treatment during the grinding and classification process, the wastewater produced by this method has virtually no adverse impact on the lead-zinc processing. The wastewater produced in the comparative example is high-pH wastewater with low COD and Ca content. 2+ The high content of lead and suspended solids makes it difficult to meet the needs of mineral processing without wastewater treatment. The lead, zinc, and sulfur concentrates obtained in the examples show significantly higher grades and recoveries than those in the comparative experiments. This further illustrates that the mineral processing and water treatment method provided by this invention enables efficient resource utilization of mineral processing wastewater through simple treatment. Furthermore, the beneficiation indicators for lead, zinc, and sulfur after reuse are higher than those of conventional processes, resulting in high-quality lead and zinc concentrates. Compared to the comparative examples, the wastewater treatment cost and reagent cost of the examples are also significantly reduced.

Claims

1. A method for reusing lead-zinc ore beneficiation wastewater, comprising grinding the raw ore to obtain a raw ore slurry, then performing lead flotation on the raw ore slurry, performing zinc flotation on the lead flotation tailings, and performing sulfur flotation on the zinc flotation tailings, characterized in that: Wastewater 1, obtained from the lead concentrate obtained by lead flotation after thickening and dewatering, is returned to the lead flotation operation. Wastewater 2, obtained from the zinc concentrate obtained by zinc flotation after thickening and dewatering, is returned to the zinc flotation operation. Wastewater 3, obtained from the sulfur concentrate obtained by sulfur flotation after thickening and dewatering, and wastewater 4, obtained from the tailings obtained by sulfur flotation after thickening and dewatering, are recycled to a high-level water tank. Then, according to the water consumption and requirements of grinding, the wastewater recycled from the high-level water tank is adjusted and returned to the grinding operation. The sulfur flotation uses xanthate as a collector; the wastewater returned from the high-level water tank to the grinding operation is treated with a modifier Ts3, which causes micro-flocculation; the dosage of modifier Ts3 is 600~800g / t; the modifier Ts3, calculated by weight percentage, includes: sodium carbonate 70~80%, sodium sulfide 5~20%, and high polyaluminum sulfate 5~20%.

2. The method for reusing lead-zinc ore beneficiation wastewater according to claim 1, characterized in that: The wastewater 1 is clarified in the collection tank 1 before being returned to the lead flotation operation.

3. The method for reusing lead-zinc ore beneficiation wastewater according to claim 1, characterized in that: The wastewater 2 is clarified in the collection tank 2 before being returned to the zinc flotation operation.

4. A method for reusing lead-zinc ore beneficiation wastewater according to claim 1, characterized in that: The lead flotation process includes: adding depressants to the raw ore slurry, stirring, adding lead collectors, and performing lead roughing to obtain lead roughing concentrate and lead roughing tailings; repeatedly adding depressants to the lead roughing concentrate for multiple lead cleaning operations, and repeatedly adding lead collectors to the lead roughing tailings for multiple lead scavenging operations to finally obtain lead concentrate and lead tailings; thickening and dewatering the lead concentrate to obtain wastewater 1, which is then returned to the lead cleaning operation for reuse; the lead tailings are then used in the zinc flotation operation; and the wastewater from the high-level water tank is returned to the lead roughing and scavenging operation for reuse.

5. A method for reusing lead-zinc ore beneficiation wastewater according to claim 1, characterized in that: The zinc flotation steps include: adding copper sulfate to the lead tailings obtained after lead flotation, stirring, adding zinc collector, and then performing zinc roughing to obtain zinc roughing concentrate and zinc roughing tailings; performing multiple zinc cleaning operations on the zinc roughing concentrate, and adding zinc collector to the zinc roughing tailings multiple times to perform multiple zinc scavenging operations to finally obtain zinc concentrate and zinc tailings; thickening and dewatering the zinc concentrate to obtain wastewater 2, which is then returned to the zinc cleaning and zinc roughing operations for use; and finally, the zinc tailings are used in the sulfur flotation operation.

6. A method for reusing lead-zinc ore beneficiation wastewater according to claim 1, characterized in that: The sulfur flotation steps include: adding sulfur collectors and frothers to the zinc tailings obtained after zinc flotation for sulfur roughing to obtain sulfur roughing concentrate and sulfur roughing tailings; performing multiple sulfur cleaning operations on the sulfur roughing concentrate and multiple sulfur scavenging operations on the sulfur roughing tailings by adding sulfur collectors multiple times to finally obtain sulfur concentrate and tailings; obtaining wastewater 3 after thickening and dewatering the sulfur concentrate and obtaining wastewater 4 after thickening and dewatering the tailings; recycling wastewater 3 and wastewater 4 to a high-level water tank; and returning the wastewater from the high-level water tank to the sulfur cleaning and sulfur roughing operations of sulfur flotation.

7. A method for reusing lead-zinc ore beneficiation wastewater according to claim 1, characterized in that: Grinding the raw ore yields a raw ore slurry with a particle size of -0.074 mm accounting for 60% to 85%.

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