A beneficiation process method of lead ore, zinc ore and fluorite ore in polymetallic ore

Abstract

The application discloses a beneficiation process method for lead ore, zinc ore and fluorite ore in polymetallic ore, and relates to the technical field of ore dressing. The method comprises the following steps: S1, crushing; S2, grinding; S3, lead flotation: flotation reagents comprise 25# black medicine, butyl xanthate, a foaming agent and a zinc inhibitor, 1 roughing, 2 scavenging and 3 cleaning flotation are adopted, and lead concentrate and lead tailings are output; S4, zinc flotation: flotation reagents comprise copper sulfate, butyl xanthate and a foaming agent, 1 roughing, 2 scavenging and 3 cleaning flotation are adopted, zinc concentrate and zinc tailings are output; S5, desulfurization; S6, fluorite flotation: 2 roughing, 2 scavenging and 8 cleaning flotation are adopted, fluorite concentrate and fluorite tailings are output; wherein, the flotation reagents in the two roughing and the two scavenging comprise sodium silicate, tannic acid, aluminum sulfate and oleic acid; the flotation reagents in the cleaning comprise tannic acid and sodium silicate; and S7, tailings and wastewater treatment, realizing efficient separation and recovery of the three valuable minerals of lead, zinc and fluorite in turn, improving the comprehensive utilization rate of mineral resources and improving the economic benefits of the mining enterprises.

Description

Technical Field

[0001] This invention relates to the field of mineral processing technology, specifically to a mineral processing method for lead, zinc, and fluorite in polymetallic ores. Background Technology

[0002] Lead and zinc are indispensable basic metal materials in modern industry, widely used in electrical, mechanical, chemical, and defense fields. Fluorite, as a strategic mineral resource, is a core raw material for the fluorochemical industry and plays an irreplaceable role in emerging industries such as new energy and new materials. my country is a major producer of lead and zinc and a major consumer of fluorite. However, with the increasing depletion of easily beneficiated single mineral resources, the efficient and comprehensive recovery of complex and difficult-to-beneficial polymetallic ores has become an inevitable trend in my country's mining development.

[0003] The Mabian area of ​​Leshan, Sichuan Province, is located in the core area of ​​the southwestern Sichuan metallogenic belt and is rich in mineral resources. Fifteen types of minerals, including phosphorus, lead, zinc, and fluorite, have been discovered, with four large deposits and three medium-sized deposits. In recent years, with the deepening of geological exploration, a large amount of fluorite resources associated with lead and zinc mines have been discovered in the area. For example, the northern section of the Maiziping mining area has abundant associated fluorite resources, with huge potential for exploration in its deeper and peripheral areas. However, for a long time, mineral development in the Mabian area has mainly focused on the mining and processing of single phosphate deposits, with only a few mines incidentally mining lead and zinc. There has been almost no effective comprehensive recovery and utilization of the fluorite resources associated with lead and zinc mines. In the lead-zinc beneficiation process, most mines discard fluorite as gangue minerals with the tailings, resulting in a serious waste of valuable strategic resources and increasing the capacity pressure and environmental risks of tailings ponds.

[0004] Currently, there are relatively mature lead and zinc beneficiation technologies, as well as separate fluorite beneficiation technologies. However, these beneficiation processes cannot be directly combined, making it impossible to achieve the efficient sequential separation and recovery of these three valuable minerals (lead, zinc, and fluorite). Preliminary research by the technical staff of Mabian Fuma Phosphate Co., Ltd. has revealed the following problems that can easily arise when integrating existing technologies: 1. The lead-zinc fluorite deposit in Mabian area is characterized by fine mineral intergrowth and complex symbiotic relationships. Lead-zinc minerals and fluorite minerals are intertwined, and conventional grinding fineness is insufficient to achieve sufficient individual liberation of useful minerals, resulting in low lead-zinc recovery rate and ineffective fluorite recovery. 2. Due to improper flotation reagents and process control, there is a problem of poor lead-zinc separation, resulting in excessive lead content in zinc concentrate and reducing the quality of zinc concentrate; 3. The ore in the Mabian area contains a large amount of calcium-bearing gangue minerals such as calcite and dolomite, whose surface properties are very similar to fluorite. Conventional flotation reagents are insufficient to effectively separate fluorite from calcium-bearing gangue. To improve the grade of fluorite concentrate, the amount of depressant needs to be significantly increased, but this will lead to a significant decrease in fluorite recovery. If the recovery rate is to be guaranteed, the calcium carbonate content in the fluorite concentrate will exceed the standard, failing to meet the requirements for industrial-grade fluorite concentrate. 4. Conventional processes use large quantities of reagents, especially cyanide, which is a highly toxic agent. This not only increases the cost of mineral processing but also poses serious safety hazards and environmental risks, which does not meet the requirements of current green mine construction. 5. Due to the ineffective recovery of fluorite resources, mining companies can only rely on the sale of lead-zinc concentrates for revenue, resulting in a single product structure and weak resilience to market risks. Furthermore, the low comprehensive utilization rate of resources also hinders the sustainable development of mining companies.

[0005] Therefore, developing an efficient, environmentally friendly, and economical integrated recycling and beneficiation process suitable for lead-zinc-fluorite polymetallic deposits in Mabian County, Sichuan Province, to achieve the sequential and efficient separation and recovery of the three valuable minerals, lead, zinc, and fluorite, is of great significance for improving the comprehensive utilization rate of mineral resources in the region, enhancing the economic benefits of mining enterprises, and ensuring the security of my country's strategic mineral resource supply. Summary of the Invention

[0006] The purpose of this invention is to solve the above-mentioned technical problems and to propose a beneficiation process for lead, zinc and fluorite in polymetallic ores.

[0007] This invention is achieved through the following technical solution: A beneficiation process for lead, zinc, and fluorite in polymetallic ores includes the following steps: S1. Crushing: The raw ore is sent to the crushing station for processing to make the particle size of the raw ore <20mm; S2. Grinding: Control the particle size distribution of the grinding product to meet the requirement that the mass fraction of the -0.074mm particle size is 75~80%, and adjust the mass concentration of the grinding discharge slurry to 30~33%; S3, Lead Flotation: The slurry after grinding is fed to the lead flotation cell at a rate of 20-21 tons / h, and the flotation reagents are fed to the flotation cell at a rate of 210-420 mL / h. The flotation reagents include No. 25 black reagent, butyl xanthate, frother and zinc inhibitor. The pH is controlled at 7.5-8. The flotation process is 1 roughing, 2 scavenging and 3 cleaning to produce lead concentrate and lead tailings. S4. Zinc Flotation: Lead tailings are fed to the zinc flotation cell at a rate of 20-21 tons / h, and flotation reagents are fed to the flotation cell at a rate of 210-420 mL / h. The flotation reagents include copper sulfate, butyl xanthate and frother. The pH is controlled at 7.5-8. The flotation process is 1 roughing, 2 scavenging and 3 cleaning to produce zinc concentrate and zinc tailings. S5. Desulfurization: The zinc tailings are sent to the desulfurization tank, and butyl xanthate and No. 2 oil are added for desulfurization treatment. The preferred treatment time is 5-10 minutes. S6. Fluorite flotation: The slurry after step S5 is fed to the fluorite flotation cell at a rate of 20-21 tons / h, and the flotation reagent is fed to the flotation cell at a rate of 210-420 mL / h. The flotation is carried out using 2 roughing, 2 scavenging and 8 cleaning flotation, and the pH is controlled at 7.5-8. Fluorite concentrate and fluorite tailings are produced. The flotation reagents used in the two roughing and two scavenging processes include sodium silicate, tannic acid, aluminum sulfate, and oleic acid. The flotation reagents used in the fine selection process include tannic acid and sodium silicate; S7. Tailings and wastewater treatment: The fluorite tailings produced by flotation are separated into solid and liquid phases. The liquid phase is sent to the wastewater treatment plant for treatment, and the treated water is recycled to the mineral processing section. The solid phase is sent to the mine for backfilling or used as building material.

[0008] Furthermore, in steps S3 and S4, the foaming agent is No. 2 oil; in step S3, the zinc inhibitor is zinc sulfate.

[0009] Furthermore, in step S3, the reagents used in the lead flotation process include 25# black reagent, butyl xanthate, 2# oil, and zinc sulfate. In the lead roughing, lead scavenging, and lead cleaning sections, the dosage of each reagent is as follows, based on the mass of the ore pulp: 10-20 g / ton for 25# black reagent, 50-100 g / ton for butyl xanthate, 5-10 g / ton for 2# oil, and 400-600 g / ton for zinc sulfate.

[0010] Furthermore, in step S4, the reagents used in the zinc flotation process include copper sulfate, butyl xanthate, and No. 2 oil; wherein, in the zinc roughing, zinc scavenging, and zinc cleaning sections, the dosage of each reagent is as follows, based on the slurry mass: copper sulfate 250~400g / ton, butyl xanthate 50~60g / ton, and No. 2 oil 8~15g / ton.

[0011] Furthermore, in step S5, the dosage of butyl xanthate is 20-30 g / ton and the dosage of No. 2 oil is 3-5 g / ton, based on the mass of the slurry.

[0012] Furthermore, in step S6, during the two-stage roughing and two-stage scavenging, the reagents used are sodium silicate, tannic acid, aluminum sulfate, and oleic acid. Based on the mass of the slurry, the dosage of each reagent is as follows: sodium silicate 2000~2300 g / ton, tannic acid 100~130 g / ton, aluminum sulfate 200~230 g / ton, and oleic acid 20~30 g / ton. During the eighth-stage beneficiation process, the reagents used are sodium silicate and tannic acid. Based on the mass of the slurry, the dosage of each reagent is as follows: 400-450 g / ton for tannic acid and 4000-4100 g / ton for sodium silicate.

[0013] Furthermore, in step S6, during the two-stage roughing and two-stage scavenging, the reagents used are sodium silicate, tannic acid, aluminum sulfate, and oleic acid. Based on the mass of the slurry, the dosage of each reagent is as follows: sodium silicate 2000~2300 g / ton, tannic acid 100~130 g / ton, aluminum sulfate 200~230 g / ton, and oleic acid 20~30 g / ton. During the eighth-stage refining process, the reagents used are acidified water glass, tannic acid, and sodium silicate. The acidified water glass is prepared by mixing 7.5% sodium silicate, 2.5% sulfuric acid, and 90% water by mass. The dosage of each reagent is as follows, based on the mass of the slurry: acidified water glass 0.3~0.5g / ton, tannic acid 300~350g / ton, and sodium silicate 4000~4100g / ton.

[0014] Furthermore, in steps S3, S4, and S6, the height of the lead flotation cell, zinc flotation cell, and fluorite flotation cell is 1500mm, and the liquid level in the cell is kept stable during the flotation operation. During lead flotation, zinc flotation, and fluorite flotation, the liquid level is controlled at 1300~1350mm for roughing operation, 1400~1460mm for scavenging operation, and 1100~1200mm for cleaning operation.

[0015] Furthermore, in the fluorite concentrate obtained in step S6, the mass fraction of calcium fluoride is not less than 91%, the mass fraction of sulfur is not more than 0.08%, the mass fraction of calcium carbonate is not more than 1.5%, and the mass fraction of silicon dioxide is not more than 1.2%.

[0016] Furthermore, in step S7, the fluorite tailings produced by flotation are sent to a thickener to be concentrated to a concentration of 50-60%, and then sent to a filter press workshop for filter pressing. The treated tailings are then transported to the mine for backfilling. The wastewater generated throughout the process is sent to a wastewater treatment plant for treatment, and the treated water is recycled back to the mineral processing section.

[0017] Furthermore, in step S7, the wastewater treatment plant includes, in sequence, a first equalization tank, a pH equalization tank, a stirring tank, a catalytic oxidation tank, a neutralization reaction tank, a first reaction tank, an inclined tube sedimentation tank, a pH adjustment tank, a softening reaction tank, a first filter, and an activated carbon filter. The first equalization tank is equipped with a filter press water inlet pipe, a thickener water inlet pipe, and a first sulfuric acid inlet pipe; the pH equalization tank is equipped with a second sulfuric acid inlet pipe; the stirring tank is equipped with a ferrous sulfate inlet pipe; the catalytic oxidation tank is equipped with a hydrogen peroxide inlet pipe; the neutralization reaction tank is equipped with a sodium hydroxide inlet pipe and a lime inlet pipe; the first reaction tank is equipped with a calcium chloride inlet pipe, a sodium sulfide inlet pipe, and a sodium hypochlorite inlet pipe; the inclined tube sedimentation tank is equipped with a first polyacrylamide inlet pipe; the pH adjustment tank is equipped with a third sulfuric acid inlet pipe; the softening reaction tank is equipped with a sodium carbonate inlet pipe; and the first filter is equipped with a polyferric sulfate inlet pipe and a second polyacrylamide inlet pipe. Wastewater treatment plants use the following methods to treat wastewater: S7.1 The first equalization tank receives filter press water and thickener overflow water, adds sulfuric acid, and after preliminary pH adjustment, sends it to the pH equalization tank. S7.2. Continue to add sulfuric acid to the pH adjustment tank to adjust the pH of the wastewater to acidic, and then send the wastewater through the stirring tank and the catalytic oxidation tank in sequence. S7.3 The wastewater is degraded for COD and organic pollutants in the mixing tank and catalytic oxidation tank, and then sent to the neutralization reaction tank; S7.4 Add sodium hydroxide and lime to the neutralization reaction tank to adjust the pH of the liquid in the tank to 9-10, so that the heavy metal ions form hydroxide precipitates, and then send the liquid phase to the first reaction tank. S7.5. Add calcium chloride, sodium sulfide, and sodium hypochlorite to the first reaction tank to remove fluoride, mercury, and cadmium from the wastewater and oxidize CN. - Alternatively, after decolorization, the treated material is transported to an inclined tube sedimentation tank; S7.6 Add polyacrylamide to the inclined tube sedimentation tank to achieve mud-water separation, and the supernatant enters the pH adjustment tank. S7.7 Add sulfuric acid to the pH adjustment tank to adjust the pH of the effluent in the tank to 6.5~7.5, and send the liquid phase to the softening reaction tank. S7.8. Add sodium carbonate to the softening reaction tank to react with Ca in the water. 2+ Mg 2+ The reaction is carried out, and the resulting material is then sent to the first filter and the activated carbon filter in sequence. S7.9 Add polyferric sulfate and polyacrylamide to the first filter. After the liquid phase is treated by the first filter and the activated carbon filter in sequence, residual suspended solids, colloids and trace organic matter in the water are removed to obtain purified water.

[0018] Compared with the prior art, the present invention has the following advantages and beneficial effects: I. In this invention, the yield of the -0.074mm particle size in the grinding section of the mineral processing is controlled within the range of 75-80%. Within this range, the degree of liberation of fluorite monomers can reach more than 85%, the grade of fluorite concentrate is stable at 91% or above, the recovery rate is increased to 70% or above, and the grinding cost only increases by about 8%. The overall benefits are optimal, which solves the problems of insufficient fluorite concentrate recovery rate (generally less than 60%) and low grade (difficult to break through 85%, mainly sold as a low-end flux) in traditional processes.

[0019] Second, this invention innovatively employs a weakly alkaline flotation system of 7.5-8.0, eliminating the need for lime slurry conditioning. Combined with a self-optimized reagent combination, the total reagent usage is reduced by more than 18% compared to conventional processes. The tailings wastewater pH is close to neutral, significantly reducing the use of neutralizing reagents and lowering overall beneficiation costs by more than 10%. In contrast, existing flotation processes for lead-zinc-fluorite polymetallic ores generally use lime to adjust the pulp pH to a strongly alkaline environment of 9.0 or higher. This not only consumes large amounts of lime but also leads to a surge in the use of fatty acid collectors. Furthermore, the treatment of high-calcium, high-alkaline wastewater is difficult and costly.

[0020] Third, by optimizing the flotation reagent formulation of the lead flotation section, this invention breaks through the technical limitation of existing conventional processes that can only recover lead sulfide minerals, and realizes the simultaneous recovery of lead sulfide and some difficult-to-process lead oxide minerals, which greatly improves the comprehensive utilization rate of lead resources and increases the economic benefits of mining enterprises.

[0021] Fourth, in this invention, a desulfurization section is added to the fluorite flotation stage, which significantly reduces the sulfur content in the final fluorite concentrate and improves its quality. Simultaneously, in the fluorite flotation stage, by selecting reagents with a specific formulation and adjusting their proportions, the pH of the slurry in the flotation tank is controlled to 7.5-8.0. No other reagents need to be added. After a "2-roughing, 2-scavenging, 8-cleaning flotation" process, fluorite concentrate is flotated from zinc tailings with a recovery rate exceeding 75%. Furthermore, the mass fraction of calcium fluoride in the fluorite concentrate is not less than 91%, the mass fraction of sulfur is not higher than 0.08%, the mass fraction of calcium carbonate is not higher than 1.5%, and the mass fraction of silica is not higher than 1.2%.

[0022] V. In this invention, a superior reagent formulation for fluorite flotation is proposed, comprising acidified water glass, tannic acid, and sodium silicate. The acidified water glass is prepared by mixing 7.5% sodium silicate, 2.5% sulfuric acid, and 90% water by mass. After adding the flotation reagent to the flotation cell, the concentration of acidified water glass is 0.3~0.5 g / ton, the concentration of tannic acid is 300~350 g / ton, and the concentration of water glass is 4000~4100 g / ton. This can increase the mass fraction of calcium fluoride in fluorite concentrate to 93% or more, thus broadening the application of this high-grade fluorite concentrate and further improving the recovery rate.

[0023] VI. This invention proposes a preferred wastewater treatment plant structure and wastewater treatment method. In the first equalization tank, filter press water and thickener overflow are received, homogenized, and the pH is initially adjusted to prevent subsequent shocks. In the pH equalization tank, the wastewater pH is adjusted to acidic (approximately pH 4) to create optimal conditions for Fenton oxidation. In the stirring tank and catalytic oxidation tank, a Fenton system is formed, generating •OH free radicals that powerfully degrade COD and organic pollutants. In the neutralization reaction tank, the pH is adjusted to alkaline (approximately pH 9-10) to cause heavy metal ions to precipitate as hydroxides. In the first reaction tank, calcium chloride (for fluoride removal), sodium sulfide (for mercury / cadmium removal), and sodium hypochlorite (for CN oxidation) are added. - (Or decolorization) to target and remove specific pollutants; flocculation and sedimentation are aided in the inclined tube sedimentation tank to achieve mud-water separation, with the supernatant entering subsequent treatment; the pH of the effluent is adjusted to neutral (6.5~7.5) in the pH adjustment tank to meet the requirements of subsequent softening and filtration; calcium and magnesium hardness are removed in the softening reaction tank to prevent membrane / filter scaling; polyferric sulfate (PFS) + PAM (coagulant aid) are used in the first filter and activated carbon filter to remove residual suspended solids, colloids, and trace organic matter, ensuring clear effluent. Wastewater from mineral processing is treated and reused, achieving "zero discharge" and reducing production water consumption. Attached Figure Description

[0024] Figure 1 This is a flowchart of Example 1.

[0025] Figure 2 This is a schematic diagram of the sewage treatment plant in Example 3. Detailed Implementation

[0026] The present invention will be further described in detail below with reference to embodiments, but the implementation of the present invention is not limited thereto.

[0027] To facilitate public understanding of the present invention, this embodiment uses a lead, zinc, and fluorite ore beneficiation production line of Mabian Fuma Phosphate Co., Ltd. as an example for further explanation.

[0028] Multiple batches of sampling and testing revealed that, by mass percentage, the grade of lead ore in the region was 1.0-1.5%, zinc ore was 0.8-1.5%, and fluorite ore was 20-30%.

[0029] A beneficiation process for lead, zinc, and fluorite in polymetallic ores, with a beneficiation flow chart as reference. Figure 1 This includes the following steps: Step S1: Crushing.

[0030] The raw ore is sent to a crushing station for processing to reduce the particle size of the raw ore to <20mm.

[0031] Step S2: Grinding.

[0032] The crushed raw ore is transported to the grinding section, where a closed-circuit grinding system consisting of a ball mill and a hydrocyclone is used for grinding and classification. The particle size distribution of the grinding product is controlled to meet the requirement that the mass fraction of the -0.074mm particle size is 75~80%, and the mass concentration of the grinding discharge slurry is adjusted to 30~33%.

[0033] This step involves grinding and classifying the ore, with the core control parameter being the yield of the -0.074mm particle size. If this parameter is too low, fluorite and gangue minerals will not be sufficiently liberated, leading to a decrease in the flotation rate of fluorite minerals during subsequent flotation, ultimately resulting in a lower fluorite concentrate recovery rate and substandard grade. The application value of fluorite concentrate is directly related to its grade: high-quality fluorite concentrate with a calcium fluoride mass fraction ≥90% can be used as a raw material for high-end glass and optical materials, while fluorite concentrate with a calcium fluoride mass fraction ≤80% can only be used in low-end fields such as fluxing agents in steel smelting. Limited by the ball mill's processing capacity, the efficiency of the classifying equipment, and on-site production conditions, increasing the yield of the -0.074mm particle size to over 80% would significantly increase grinding energy consumption and equipment wear, resulting in a significant decrease in economic efficiency. Therefore, considering equipment load, product quality requirements, and beneficiation production costs, this embodiment controls the yield of the -0.074mm particle size of the ore at 75-80%.

[0034] Step S3: Lead flotation.

[0035] Objective: To perform priority flotation on qualified grinding pulp to selectively enrich lead minerals such as lead ore, separate and remove gangue and zinc mineral impurities, and produce lead concentrate products that meet industrial grade requirements. At the same time, the lead tailings produced are transported to the subsequent zinc flotation section.

[0036] The slurry after grinding is fed to the lead flotation cell at a rate of 20-21 tons / h, and the flotation reagents are fed to the flotation cell at a rate of 210-420 mL / h. The flotation reagents include No. 25 black reagent, butyl xanthate, frother and zinc inhibitor. The pH is controlled at 7.5-8. The flotation process is 1 roughing, 2 scavenging and 3 cleaning to produce lead concentrate and lead tailings.

[0037] In this embodiment, the pH value of the pulp is uniformly controlled at 7.5~8.0 throughout the flotation process to maintain a weakly alkaline pulp environment. The pulp pH value is closely related to the dissolution, dispersion, and adsorption behavior of flotation reagents. Under these weakly alkaline conditions, the collectors and depressants selected in this invention can achieve optimal selectivity. Compared with conventional strongly alkaline flotation processes, the total reagent dosage can be reduced by 15~20%. At the same time, the weakly alkaline pulp does not require the addition of large amounts of lime for pulp conditioning, reducing the introduction of calcium and magnesium ions and significantly reducing the difficulty and cost of subsequent tailings wastewater treatment.

[0038] In this step, the frother is No. 2 oil (pine oil), and the zinc depressant is zinc sulfate. After adding the flotation reagents to the lead flotation cell, the dosage of each reagent, based on the mass of the ore pulp, is as follows: 10-20 g / ton of No. 25 black reagent, 50-100 g / ton of butyl xanthate, 5-10 g / ton of No. 2 oil, and 400-600 g / ton of zinc sulfate. During the lead roughing stage, the flotation reagents of this invention are added for flotation treatment. This reagent has good collecting performance for lead sulfide minerals and also has a certain collecting ability for some difficult-to-react lead oxide minerals associated with the ore. However, the reagents used in existing conventional lead flotation processes are only effective for lead sulfide minerals and cannot recover lead oxide minerals. Compared with existing technologies, the total recovery rate of lead minerals using the reagents of this invention is significantly improved (by approximately 8%).

[0039] The lead flotation cell has a height of 1500mm, and the liquid level in the cell is kept stable during the flotation operation. The liquid level is controlled at 1300~1350mm for roughing operation, 1400~1460mm for scavenging operation, and 1100~1200mm for cleaning operation.

[0040] The specific implementation method is as follows: I. Preparations before the assignment.

[0041] Equipment status check: Confirm that the roughing mixing tank, each flotation tank, slurry transfer pump, reagent metering pump, online pH meter and flow meter are operating normally, the flotation tank level adjustment device and the froth scraping mechanism are sensitive, and the equipment is well lubricated and sealed.

[0042] Reagent preparation and storage: Prepare flotation reagents according to the following standards and pump them into the corresponding reagent storage tanks for later use: Zinc inhibitor (zinc sulfate): Prepare a 10-15% aqueous solution; Butyl xanthate: Prepare a 5-10% aqueous solution and use immediately. 25# Black Powder: Use the undiluted solution directly or prepare a 10% aqueous solution; Foaming agent (2# oil): Use the undiluted solution directly.

[0043] II. The operating procedure is as follows.

[0044] S3.1 System startup and feeding.

[0045] Start the stirring motor, aeration motor and foam scraping motor of each section of the flotation tank in sequence, and adjust the aeration amount to form a uniform and fine foam layer on the surface of the flotation tank.

[0046] Start the slurry transfer pump from the grinding section to the lead flotation roughing mixing tank, and transport the qualified slurry from the grinding section to the lead roughing mixing tank No. 1 at a constant rate of 20~21 tons / h.

[0047] Simultaneously start the metering pumps of each reagent to deliver zinc inhibitor, butyl xanthate, 25# black powder and foaming agent to the corresponding mixing tanks according to the preset ratio. The total delivery rate of the four reagents is stably controlled within the range of 210~420mL / h.

[0048] S3.2 Lead roughing operation.

[0049] Add the aforementioned reagents (25# black reagent, butyl xanthate, frother, and zinc inhibitor) to the No. 1 mixing tank of lead roughing, precisely controlling the pH of the roughing pulp within the range of 7.5~8.0, and the flotation time within 15~20 minutes. Adjust the froth scraping speed to promptly scrape off the lead-rich froth product from the surface. The lead roughing froth product is the lead concentrate, which is transported to the No. 1 mixing tank of lead finishing; the lead roughing underflow (tailings) is transported to the first lead scavenging operation.

[0050] S3.3 Lead sweeping operation (2 times in total).

[0051] Objective: To recover low-grade lead minerals lost in roughing tailings and improve the overall lead recovery rate.

[0052] First scavenging: The reagents used are the same as those used in the lead roughing operation, but adjustments can be made based on the flotation foam condition on site. Scavenging foam #1 is returned to the lead roughing mixing tank; the underflow from scavenging foam #1 is transported to the second lead scavenging operation, with a flotation time of 12-15 minutes.

[0053] Second scavenging: The same reagents are used as in the lead roughing operation. The foam from scavenging #2 is returned to the first lead scavenging operation. The underflow from scavenging #2 is the final lead tailings, which are transported to the subsequent zinc flotation section. The flotation time is 12-15 minutes.

[0054] S3.4 Lead Refining Operation (3 times in total).

[0055] Objective: To gradually remove zinc minerals and gangue impurities from the rough concentrate and improve the grade of lead concentrate.

[0056] First cleaning operation: Lead rough concentrate enters the No. 1 cleaning mixing tank, and reagents are added (the reagent dosage is the same as in the lead cleaning section. In this section, the dosage of zinc inhibitor may be reduced or omitted depending on the specific situation). After stirring for 3 minutes, it is sent to the No. 1 cleaning flotation tank, where flotation time is 12-15 minutes. The froth from the No. 1 cleaning tank enters the second cleaning process; the underflow from the No. 1 cleaning tank is returned to the lead roughing mixing tank. In practice, a separate reagent mixing tank / vessel can be designed according to actual needs, or the corresponding reagents can be added to the flotation tank and stirred first using a stirring mechanism before adding the slurry.

[0057] Second purification operation: The foam from Purification 1# enters Purification 2# mixing tank, where reagents are added (same as in the first purification operation). After mixing for 3 minutes, it is sent to Purification 2# flotation tank for 10-12 minutes. Purification 2# foam then enters the third purification operation; the underflow from Purification 2# is returned to Purification 1# mixing tank.

[0058] The third refining operation: The No. 2 froth from the refining process is fed into the No. 3 mixing tank, where reagents are added (same as in the first refining operation). After stirring for 3 minutes, it is sent to the No. 3 flotation tank for flotation, where the flotation time is 10-12 minutes. The No. 3 froth is the final qualified lead concentrate and is transported to the concentrate filtration and dewatering section; the No. 3 underflow is returned to the No. 2 mixing tank.

[0059] Step S4: Zinc flotation.

[0060] Lead tailings are fed to the zinc flotation cell at a rate of 20-21 tons / h, and flotation reagents, including copper sulfate, butyl xanthate and frother, are fed to the flotation cell at a rate of 210-420 mL / h. The pH is controlled at 7.5-8. The flotation process consists of 1 roughing, 2 scavenging, and 3 cleaning flotation steps to produce zinc concentrate and zinc tailings.

[0061] In this step, No. 2 oil is selected as the foaming agent.

[0062] The height of the zinc flotation tank is 1500mm, and the liquid level in the tank is kept stable during the flotation operation. The liquid level is controlled at 1300~1350mm for roughing operation, 1400~1460mm for scavenging operation, and 1100~1200mm for cleaning operation.

[0063] The specific steps are as follows: S4.1 Zinc roughing operation.

[0064] Objective: To maximize the activation and harvesting of sphalerite in lead tailings to obtain zinc concentrate.

[0065] After adding the flotation reagents to the zinc flotation cell, the dosage of each reagent, based on the mass of the slurry, is as follows: copper sulfate 250-400 g / ton, butyl xanthate 50-60 g / ton, and No. 2 oil 8-15 g / ton. The flotation time is controlled at 18-20 minutes. The surface foam rich in zinc minerals is promptly skimmed off. The zinc roughing froth product is zinc concentrate, which is transported to the No. 1 mixing tank for zinc refining. The zinc roughing underflow is transported to the first zinc scavenging operation.

[0066] S4.2 Zinc scavenging operation (2 times in total).

[0067] Objective: To recover insufficiently activated and collected sphalerite lost in the roughing tailings, thereby improving the overall zinc recovery rate. The reagents and their concentrations used in the zinc scavenging operation are the same as those in the zinc roughing section.

[0068] First scavenging: Scavenger No. 1 foam is returned to the zinc roughing mixing tank; Scavenger No. 1 underflow is transported to the second zinc scavenging operation, with a flotation time of 15~18 minutes.

[0069] Second scavenging: The foam from scavenging #2 is returned to the zinc from the first scavenging operation; the underflow from scavenging #2 is the final zinc tailings, which is transported to the desulfurization section in step S5.

[0070] S4.3 Zinc Refining Operation (3 times in total).

[0071] Objective: To gradually remove impurities from zinc roughing concentrate and improve the zinc concentrate grade to industrial requirements. The reagents and their concentrations used in zinc beneficiation are the same as those in the zinc roughing section.

[0072] First cleaning: Zinc rough concentrate enters the No. 1 cleaning tank and is floated for 12-15 minutes. The froth from the No. 1 cleaning tank enters the second cleaning tank; the underflow from the No. 1 cleaning tank is returned to the zinc roughing tank.

[0073] Second purification: Selected foam #1 enters the mixing tank of purification #2, with a flotation time of 10-12 minutes. Selected foam #2 enters the third purification; the underflow of selected foam #2 is returned to the first purification operation.

[0074] Third refining: The No. 2 froth from the refining process enters the No. 3 refining mixing tank, where flotation takes 10-12 minutes. The No. 3 refining froth is the final qualified zinc concentrate and is transported to the concentrate filtration and dewatering section; the No. 3 refining underflow is returned to the second refining operation.

[0075] Step S5: Desulfurization.

[0076] Zinc tailings are fed into a desulfurization mixing tank, where butyl xanthate and No. 2 oil are added. The dosage of each reagent, based on the mass of the slurry, is: 20-30 g / ton of butyl xanthate and 3-5 g / ton of No. 2 oil. After treatment for 5-10 minutes, the tailings are sent to a desulfurization flotation tank for flotation. The froth product obtained from flotation is sulfur concentrate (sent to the tailings treatment in step S7), while the desulfurization underflow enters the fluorite flotation section in step S6.

[0077] Step S6: Fluorite flotation.

[0078] The slurry processed in step S5 is fed to the fluorite flotation cell at a rate of 20-21 tons / h, and the flotation reagent is fed to the fluorite flotation cell at a rate of 210-420 mL / h. The flotation process is 2 roughing, 2 scavenging and 8 cleaning, with the pH controlled at 7.5-8, producing fluorite concentrate and fluorite tailings.

[0079] S6.1 Fluorite coarse selection operation.

[0080] Objective: To maximize the recovery of fluorite minerals from the ore and obtain crude concentrate products.

[0081] S6.1.1 First coarse selection.

[0082] The desulfurized underflow enters the No. 1 fluorite roughing flotation tank. First, flotation reagents sodium silicate (water glass), tannic acid, aluminum sulfate, and oleic acid are added. Based on the mass of the slurry, the dosages of each reagent are: sodium silicate 2000-2300 g / ton, tannic acid 100-130 g / ton, aluminum sulfate 200-230 g / ton, and oleic acid 20-30 g / ton (generally, the minimum dosage is sufficient). Flotation lasts for 20 minutes. The froth product from roughing tank No. 1 is fluorite rough concentrate 1, which enters the cleaning system. The underflow from roughing tank No. 1 enters the No. 2 fluorite roughing flotation tank for further processing.

[0083] S6.1.2 Second coarse selection.

[0084] The selection and dosage of reagents are the same as those in the first roughing stage. In practice, the dosage can be adjusted according to the flotation foam state on site. The dosage of reagents is generally not less than 1 / 3 of that in the first roughing stage.

[0085] Flotation time: 20 min.

[0086] The froth product from roughing stage #2 is fluorite rough concentrate 2, which is combined with rough concentrate 1 and enters the cleaning system; the underflow from roughing stage #2 enters the scavenging operation.

[0087] S6.2 Fluorite scanning operation (2 times in total).

[0088] Objective: To recover fluorite minerals lost in roughing tailings and improve the overall recovery rate.

[0089] First scavenging: The reagents used are sodium silicate (water glass with a modulus of 2.8-3.2), tannic acid, and aluminum sulfate. These reagents are added to the No. 1 fluorite scavenging flotation tank, along with water glass, tannic acid, aluminum sulfate, and oleic acid. The dosage of each reagent, based on the pulp mass, is as follows: sodium silicate 2000-2300 g / ton, tannic acid 100-130 g / ton, aluminum sulfate 200-230 g / ton, and oleic acid 20-30 g / ton. The froth from scavenging No. 1 is returned to the No. 2 roughing flotation tank; the underflow from scavenging No. 1 enters the No. 2 fluorite scavenging flotation tank for the No. 2 scavenging flotation operation. The first scavenging time is controlled to be 20-22 minutes.

[0090] Second scavenging: Oleic acid is used as the reagent. It is added to the No. 2 fluorite scavenging flotation cell, with the same reagent and dosage as in the first scavenging operation. The froth from the No. 2 scavenging cell is returned to the No. 1 scavenging operation. The underflow from the No. 2 scavenging cell is the final tailings, which is discharged from the system and proceeds to step S7. The second scavenging time is controlled to be 20-22 minutes.

[0091] S6.3, Selected Fluorite Tasks (8 in total).

[0092] Objective: To gradually improve the grade of fluorite concentrate, remove residual gangue impurities, and ultimately obtain qualified fluorite concentrate.

[0093] The flotation reagents used in the fine-grained process include tannic acid and sodium silicate (industrial water glass with a modulus of 2.8 to 3.2). These reagents are added to each stage of the fluorite fine-grained flotation tank. The dosage of each reagent, based on the pulp mass, is: 400-450 g / ton of tannic acid and 4000-4100 g / ton of sodium silicate. (This dosage is applied for each fine-grained process, but can be adjusted slightly according to the froth condition of each process).

[0094] Work process: a. The combined fluorite rough concentrate enters the No. 1 fluorite refining flotation tank. Add the reagent according to the above dosage and stir for 3-5 minutes. The flotation time is 15-20 minutes.

[0095] b. Select the No. 1 foam and move it to the No. 2 selection operation; select the No. 1 undercurrent and return it to the No. 1 coarse selection operation.

[0096] c. The process for selecting #2 to #7 is the same: the foam from the previous selection enters the current selection, and the bottom current from the current selection returns to the previous selection operation.

[0097] d. Select 8# foam as the final fluorite concentrate, filter and dehydrate it as the product; the underflow of 8# is returned to the 7# selection process.

[0098] Step S7: Tailings and wastewater treatment.

[0099] The fluorite tailings produced by flotation are sent to a thickener to be concentrated to a concentration of 50-60%, and then sent to a filter press workshop for filtration. The treated tailings are then transported to the mine for backfilling. The wastewater generated throughout the process is sent to a wastewater treatment plant for treatment, and the treated water is recycled back to the mineral processing section.

[0100] The yield, grade, and recovery rate of lead concentrate, zinc concentrate, fluorite concentrate, and tailings produced from multiple batches of raw ore were examined. The statistical results are shown in Table 1.

[0101] Table 1

[0102] As shown in Table 1, the process method of this embodiment can simultaneously float lead, zinc, and fluorite concentrates. The recovery rate of fluorite concentrate is high, reaching over 75%, and even as high as 83%, representing a significant breakthrough in the field of mineral processing. Furthermore, the obtained fluorite concentrate contains no less than 91% calcium fluoride, no more than 0.08% sulfur, no more than 1.5% calcium carbonate, and no more than 1.2% silica, classifying it as a high-grade fluorite concentrate with promising applications in high-end glass manufacturing and related fields.

[0103] In this embodiment, the lead concentrate recovery rate reaches 50% or higher, even as high as 60%. The recovered lead concentrate contains not only conventional lead sulfide but also some lead oxide, with the recovered lead oxide accounting for 20-30% of the lead concentrate, significantly improving the lead recovery rate. Compared to traditional processes, the lead recovery rate is increased by approximately 50%.

[0104] In addition, compared with traditional flotation processes, this invention uses reagents with specific formulations and adjusts their ratios to control the pH value of the slurry in the flotation cell to 7.5~8.0. No other reagents need to be added, the reagent cost is relatively low, the post-treatment pressure is less, and the wastewater is treated and reused in the upstream mineral processing flotation section, reducing external discharge and production costs are also relatively low.

[0105] Example 2 The difference between this embodiment and Embodiment 1 is that: In step S6.1, the flotation reagents include acidified water glass, tannic acid, and sodium silicate. The acidified water glass is prepared by mixing 7.5% sodium silicate (industrial water glass with a modulus of 2.8 to 3.2), 2.5% sulfuric acid, and 90% water. When preparing the acidified water glass, the raw sulfuric acid can be concentrated sulfuric acid with a mass fraction of 98% or industrial sulfuric acid with a mass fraction of 93%.

[0106] Based on the mass of the slurry, the dosage of each reagent is as follows: acidified water glass 0.3~0.5g / ton, tannic acid 300~350g / ton, sodium silicate 4000~4100g / ton. (Add according to this dosage for each refining process, and adjust the dosage slightly according to the foam state of each refining process). This example is based on Example 1, further optimizing the reagents for fluorite flotation to further improve the grade of fluorite concentrate.

[0107] The yield, grade, and recovery rate of lead concentrate, zinc concentrate, fluorite concentrate, and tailings produced from multiple batches of raw ore were investigated. The statistical results are shown in Table 2.

[0108] Table 2

[0109] As shown in Table 2, the adjusted reagent formula can further improve the grade of fluorite concentrate in the fluorite beneficiation section, enabling it to be used in high-end applications and creating better economic value. At the same time, the recovery rate of fluorite concentrate is also improved to a certain extent.

[0110] As can be seen from the above embodiments: This lead, zinc, and fluorite beneficiation process not only significantly improves concentrate grade and recovery rate, but also features stable process, convenient control, high reagent consumption, high energy consumption, and full utilization of recycled water. It effectively solves the problems of long flotation process, low concentration, insufficient beneficiation index, high reagent and water consumption, high energy consumption, and unstable operation in lead, zinc, and fluorite flotation. It is of great significance for improving the recovery rate and concentrate quality of lead, zinc, and fluorite, saving energy and reducing consumption, and promoting clean production.

[0111] Example 3 In this embodiment, a preferred wastewater treatment plant structure is proposed for treating the wastewater obtained in step S7 of embodiment 1, and the treated clean water is recycled back to the mineral processing section.

[0112] refer to Figure 2 The wastewater treatment plant includes a first equalization tank, a pH equalization tank, a stirring tank, a catalytic oxidation tank, a neutralization reaction tank, a first reaction tank, an inclined tube sedimentation tank, a pH adjustment tank, a softening reaction tank, a first filter, and an activated carbon filter, which are connected in sequence.

[0113] In this embodiment, the first regulating tank is equipped with a filter press water inlet pipe, a thickener water inlet pipe, and a first sulfuric acid inlet pipe; the pH regulating tank is equipped with a second sulfuric acid inlet pipe; the stirring tank is equipped with a ferrous sulfate inlet pipe; the catalytic oxidation tank is equipped with a hydrogen peroxide inlet pipe; the neutralization reaction tank is equipped with a sodium hydroxide inlet pipe and a lime inlet pipe; the first reaction tank is equipped with a calcium chloride inlet pipe, a sodium sulfide inlet pipe, and a sodium hypochlorite inlet pipe; the inclined tube sedimentation tank is equipped with a first polyacrylamide inlet pipe; the pH adjustment tank is equipped with a third sulfuric acid inlet pipe; the softening reaction tank is equipped with a sodium carbonate inlet pipe; and the first filter is equipped with a polyferric sulfate inlet pipe and a second polyacrylamide inlet pipe.

[0114] In one preferred embodiment, an aeration device is provided on the first conditioning tank, pH conditioning tank, stirring tank, catalytic oxidation tank, neutralization reaction tank and first reaction tank.

[0115] One preferred embodiment is that a first clear water tank, a first sedimentation tank, a second clear water tank, and a recycled water tank are sequentially arranged after the activated carbon filter.

[0116] In one preferred embodiment, a transfer pump is provided between the first conditioning tank, pH conditioning tank, stirring tank, catalytic oxidation tank, neutralization reaction tank, first reaction tank, inclined tube sedimentation tank, pH adjustment tank, softening reaction tank, first filter, activated carbon filter, first clear water tank, first sedimentation tank, second clear water tank and recycled water tank.

[0117] In one preferred embodiment, pH meters are installed on the first conditioning tank, pH conditioning tank, neutralization reaction tank, first reaction tank and pH adjustment tank to monitor the pH value of the fluid in the tank.

[0118] Wastewater treatment plants use the following methods to treat wastewater: S7.1 The first equalization tank receives filter press water and thickener overflow water, adds sulfuric acid, and after preliminary pH adjustment, sends it to the pH equalization tank. S7.2. Continue to add sulfuric acid to the pH adjustment tank to adjust the pH of the wastewater to acidic, and then send the wastewater through the stirring tank and the catalytic oxidation tank in sequence. S7.3 The wastewater is degraded for COD and organic pollutants in the mixing tank and catalytic oxidation tank, and then sent to the neutralization reaction tank; S7.4 Add sodium hydroxide and lime to the neutralization reaction tank to adjust the pH of the liquid in the tank to 9-10, so that the heavy metal ions form hydroxide precipitates, and then send the liquid phase to the first reaction tank. S7.5. Add calcium chloride, sodium sulfide, and sodium hypochlorite to the first reaction tank to remove fluoride, mercury, and cadmium from the wastewater and oxidize CN. - Alternatively, after decolorization, the treated material is transported to an inclined tube sedimentation tank; S7.6 Add polyacrylamide to the inclined tube sedimentation tank to achieve mud-water separation, and the supernatant enters the pH adjustment tank. S7.7 Add sulfuric acid to the pH adjustment tank to adjust the pH of the effluent in the tank to 6.5~7.5, and send the liquid phase to the softening reaction tank. S7.8. Add sodium carbonate to the softening reaction tank to react with Ca in the water. 2+ Mg 2+ The reaction is carried out, and the resulting material is then sent to the first filter and the activated carbon filter in sequence. S7.9 Add polyferric sulfate and polyacrylamide to the first filter. After the liquid phase is treated by the first filter and the activated carbon filter in sequence, residual suspended solids, colloids and trace organic matter in the water are removed to obtain purified water.

[0119] The above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention in any way. Any simple modifications or equivalent changes made to the above embodiments based on the technical essence of the present invention shall fall within the protection scope of the present invention.

Claims

1. A beneficiation process for lead, zinc, and fluorite in polymetallic ores, characterized in that, Includes the following steps: S1. Crushing: The raw ore is sent to the crushing station for processing to make the particle size of the raw ore <20mm; S2. Grinding: Control the particle size distribution of the grinding product to meet the requirement that the mass fraction of the -0.074mm particle size is 75~80%, and adjust the mass concentration of the grinding discharge slurry to 30~33%; S3, Lead Flotation: The slurry after grinding is fed to the lead flotation cell at a rate of 20-21 tons / h, and the flotation reagents are fed to the flotation cell at a rate of 210-420 mL / h. The flotation reagents include No. 25 black reagent, butyl xanthate, frother and zinc inhibitor. The pH is controlled at 7.5-8. The flotation process is 1 roughing, 2 scavenging and 3 cleaning to produce lead concentrate and lead tailings. S4. Zinc Flotation: Lead tailings are fed to the zinc flotation cell at a rate of 20-21 tons / h, and flotation reagents are fed to the flotation cell at a rate of 210-420 mL / h. The flotation reagents include copper sulfate, butyl xanthate and frother. The pH is controlled at 7.5-8. The flotation process is 1 roughing, 2 scavenging and 3 cleaning to produce zinc concentrate and zinc tailings. S5. Desulfurization: Zinc tailings are sent to a desulfurization tank, where butyl xanthate and No. 2 oil are added for desulfurization treatment. S6. Fluorite flotation: The slurry after step S5 is fed to the fluorite flotation cell at a rate of 20-21 tons / h, and the flotation reagent is fed to the flotation cell at a rate of 210-420 mL / h. The flotation is carried out using 2 roughing, 2 scavenging and 8 cleaning flotation, and the pH is controlled at 7.5-8. Fluorite concentrate and fluorite tailings are produced. The flotation reagents used in the two roughing and two scavenging processes include sodium silicate, tannic acid, aluminum sulfate, and oleic acid. The flotation reagents used in the fine selection process include tannic acid and sodium silicate; S7. Tailings and wastewater treatment: Solid-liquid separation is performed on the fluorite tailings produced by flotation. The liquid phase is sent to the wastewater treatment plant for treatment, and the treated water is recycled to the mineral processing section. The solid phase is sent to the mine for backfilling or used as building material.

2. The mineral processing method according to claim 1, characterized in that: In steps S3 and S4, the foaming agent is No. 2 oil; in step S3, the zinc inhibitor is zinc sulfate.

3. The mineral processing method according to claim 2, characterized in that: In step S3, the reagents used in the lead flotation process include No. 25 black reagent, butyl xanthate, No. 2 oil, and zinc sulfate. In the lead roughing, lead scavenging and lead cleaning processes, the dosage of each reagent, based on the slurry quality, is as follows: 25# black reagent 10~20g / ton, butyl xanthate 50~100g / ton, 2# oil 5~10g / ton, and zinc sulfate 400~600g / ton.

4. The mineral processing method according to claim 2, characterized in that: In step S4, the reagents used in the zinc flotation process include copper sulfate, butyl xanthate, and No. 2 oil; In the zinc roughing, zinc scavenging and zinc cleaning processes, the dosage of each reagent, based on the slurry quality, is as follows: copper sulfate 250~400g / ton, butyl xanthate 50~60g / ton, and No. 2 oil 8~15g / ton.

5. The mineral processing method according to claim 1, characterized in that: In step S5, the dosage of butyl xanthate is 20-30 g / ton and the dosage of No. 2 oil is 3-5 g / ton, based on the mass of the slurry.

6. The mineral processing method according to claim 1, characterized in that: In step S6, during the two-stage roughing and two-stage scavenging, the reagents used are sodium silicate, tannic acid, aluminum sulfate, and oleic acid. Based on the mass of the slurry, the dosage of each reagent is as follows: sodium silicate 2000~2300 g / ton, tannic acid 100~130 g / ton, aluminum sulfate 200~230 g / ton, and oleic acid 20~30 g / ton. During the eighth-stage beneficiation process, the reagents used are sodium silicate and tannic acid. Based on the mass of the slurry, the dosage of each reagent is as follows: 400-450 g / ton for tannic acid and 4000-4100 g / ton for sodium silicate.

7. The mineral processing method according to claim 1, characterized in that: In step S6, during the two-stage roughing and two-stage scavenging, the reagents used are sodium silicate, tannic acid, aluminum sulfate, and oleic acid. Based on the mass of the slurry, the dosage of each reagent is as follows: sodium silicate 2000~2300g / ton, tannic acid 100~130g / ton, aluminum sulfate 200~230g / ton, and oleic acid 20~30g / ton. During the eighth-stage refining process, the reagents used are acidified water glass, tannic acid, and sodium silicate. The acidified water glass is prepared by mixing 7.5% sodium silicate, 2.5% sulfuric acid, and 90% water by mass. The dosage of each reagent is as follows, based on the mass of the slurry: acidified water glass 0.3~0.5g / ton, tannic acid 300~350g / ton, and sodium silicate 4000~4100g / ton.

8. The mineral processing method according to claim 1, characterized in that: In steps S3, S4, and S6, the height of the lead flotation cell, zinc flotation cell, and fluorite flotation cell is 1500mm, and the liquid level in the cell is kept stable during the flotation operation. During lead flotation, zinc flotation, and fluorite flotation, the liquid level is controlled at 1300~1350mm for roughing, 1400~1460mm for scavenging, and 1100~1200mm for cleaning.

9. The mineral processing method according to claim 1, characterized in that: In the fluorite concentrate obtained in step S6, the mass fraction of calcium fluoride is not less than 91%, the mass fraction of sulfur is not more than 0.08%, the mass fraction of calcium carbonate is not more than 1.5%, and the mass fraction of silicon dioxide is not more than 1.2%.

10. The mineral processing method according to claim 1, characterized in that: In step S7, the wastewater treatment plant includes, in sequence, a first equalization tank, a pH equalization tank, a stirring tank, a catalytic oxidation tank, a neutralization reaction tank, a first reaction tank, an inclined tube sedimentation tank, a pH adjustment tank, a softening reaction tank, a first filter, and an activated carbon filter. The first equalization tank is equipped with a filter press water inlet pipe, a thickener water inlet pipe, and a first sulfuric acid inlet pipe; the pH equalization tank is equipped with a second sulfuric acid inlet pipe; the stirring tank is equipped with a ferrous sulfate inlet pipe; the catalytic oxidation tank is equipped with a hydrogen peroxide inlet pipe; the neutralization reaction tank is equipped with a sodium hydroxide inlet pipe and a lime inlet pipe; the first reaction tank is equipped with a calcium chloride inlet pipe, a sodium sulfide inlet pipe, and a sodium hypochlorite inlet pipe; the inclined tube sedimentation tank is equipped with a first polyacrylamide inlet pipe; the pH adjustment tank is equipped with a third sulfuric acid inlet pipe; the softening reaction tank is equipped with a sodium carbonate inlet pipe; and the first filter is equipped with a polyferric sulfate inlet pipe and a second polyacrylamide inlet pipe. Wastewater treatment plants treat wastewater using the following methods: S7.1 The first equalization tank receives filter press water and thickener overflow water, adds sulfuric acid, and after preliminary pH adjustment, sends it to the pH equalization tank. S7.

2. Continue to add sulfuric acid to the pH adjustment tank to adjust the pH of the wastewater to acidic, and then send the wastewater through the stirring tank and the catalytic oxidation tank in sequence. S7.3 The wastewater is degraded for COD and organic pollutants in the mixing tank and catalytic oxidation tank, and then sent to the neutralization reaction tank; S7.4 Add sodium hydroxide and lime to the neutralization reaction tank to adjust the pH of the liquid in the tank to 9-10, so that the heavy metal ions form hydroxide precipitates, and then send the liquid phase to the first reaction tank. S7.

5. Add calcium chloride, sodium sulfide, and sodium hypochlorite to the first reaction tank to remove fluoride, mercury, and cadmium from the wastewater and oxidize CN. - Alternatively, after decolorization, the treated material is transported to an inclined tube sedimentation tank; S7.6 Add polyacrylamide to the inclined tube sedimentation tank to achieve mud-water separation, and the supernatant enters the pH adjustment tank. S7.7 Add sulfuric acid to the pH adjustment tank to adjust the pH of the effluent in the tank to 6.5~7.5, and send the liquid phase to the softening reaction tank. S7.

8. Add sodium carbonate to the softening reaction tank to react with Ca in the water. 2+ Mg 2+ The reaction is carried out, and the resulting material is then sent to the first filter and the activated carbon filter in sequence. S7.9 Add polyferric sulfate and polyacrylamide to the first filter. After the liquid phase is treated by the first filter and the activated carbon filter in sequence, residual suspended solids, colloids and trace organic matter in the water are removed to obtain purified water.

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