Lead zinc sulfide ore flotation separation inhibitor and application

Abstract

The invention discloses a lead-zinc sulfide ore flotation separation inhibitor and application, and belongs to the technical field of mineral processing. The invention provides a method for applying sodium thiophosphate as a selective inhibitor for sphalerite and pyrite. The method comprises the steps that lead-zinc sulfide ore is ground, then in lead flotation operation, an effective amount of sodium thiophosphate is added into ore pulp so as to selectively inhibit flotation of sphalerite and pyrite, meanwhile, conventional dispersing agents, collecting agents and foaming agents are added in a matched mode, the lead sulfide ore is preferentially floated and recycled, and lead concentrate is obtained. By means of the selective adsorption effect of sodium thiophosphate on sphalerite and pyrite, the surface of the sodium thiophosphate is hydrophilic, adsorption of a collecting agent is hindered, and the influence of sodium thiophosphate on galena flotation is small. Compared with a traditional inhibitor, the sodium thiophosphate used in the method has the advantages of being small in dosage, high in selectivity, low in mutual content of lead and zinc in the concentrate, environmentally friendly and the like.

Description

Technical Field

[0001] The present invention relates to a depressant for the flotation separation of lead-zinc sulfide ore and its application, belonging to the technical field of mineral processing. Background Art

[0002] Lead and zinc are indispensable basic metals in the global industrial system and are widely used in many fields such as battery manufacturing, alloy production, galvanizing, and chemical industry. Sulfide lead-zinc ores are the main raw material sources for extracting lead and zinc globally. Therefore, efficiently, economically, and environmentally separating and recovering lead-zinc sulfide ores is crucial for ensuring the stable supply of global lead and zinc metals and meeting the growing industrial demands.

[0003] Currently, the mainstream industrial method for separating galena and sphalerite from lead-zinc sulfide ores is flotation. The core of this process lies in utilizing the differences in the physicochemical properties of the mineral surfaces and regulating the floatability of minerals by adding specific flotation reagents. In a typical preferential flotation process, the key lies in selectively depressing sphalerite and other sulfide minerals such as pyrite often associated with it, while keeping galena with good floatability.

[0004] The cyanide-free depressant systems widely used in industrial practice mainly include lime, zinc sulfate, sulfite, and sodium sulfide, etc. However, these traditional depressants have common technical limitations. Although lime and zinc sulfate are commonly used, relatively high dosages are often required to achieve a certain depressing effect, which not only increases the reagent cost but may also have an adverse impact on the subsequent flotation of minerals. Sulfite usually needs to be used in combination with other reagents, its single depressing effect is limited, and it may be unstable under certain conditions. Sodium sulfide, as a strong depressant, may also cause a certain degree of non-selective depression on the target mineral galena.

[0005] In view of the deficiencies of traditional depressants, researchers in the global mineral processing field have been actively exploring and developing new, efficient, and environmentally friendly depressants. For example, some organic small molecule depressants have been studied to improve selectivity. Chinese invention patent CN107442290A discloses a method of using sodium thioglycolate as a sphalerite depressant, which is said to improve the grade of lead concentrate, but this technology requires precise control of the reagent ratio to balance the beneficiation cost and metal recovery rate. In addition, composite depressant systems are also a hot research direction. For example, the polyepoxysuccinic acid-zinc sulfate-sodium sulfite combined depressant proposed in Chinese invention patent CN111715410A aims to reduce the total reagent dosage and improve the depressing performance through the synergistic effect between components, but its application may be limited by a narrow component ratio regulation window and strict control of process conditions.

[0006] Despite numerous studies and attempts, developing an ideal depressant that can efficiently and selectively inhibit sphalerite and pyrite, and has the advantages of low dosage, low cost, environmental friendliness, and convenient use, remains an important challenge and urgent need in the field of flotation separation of lead-zinc sulfide ores. Solving this technical problem is of great significance for improving the utilization efficiency of global lead-zinc resources, reducing production costs, and achieving sustainable development of the mining industry. Summary of the Invention

[0007] Aiming at the problems of large dosage and poor selectivity of traditional depressants (such as zinc sulfate, lime, sodium sulfide) in the flotation separation of lead-zinc sulfide ores, especially in the preferential flotation of lead process, one of the purposes of the present invention is to provide a depressant for the flotation separation of lead-zinc sulfide ores, and the depressant is sodium thiophosphate.

[0008] Another purpose of the present invention is to provide an application of the depressant in obtaining lead concentrate and zinc concentrate by flotation separation of lead-zinc sulfide ores.

[0009] Preferably, the application method is as follows:

[0010] (1) Grind the lead-zinc sulfide ore to prepare pulp.

[0011] (2) Add a dispersant, sodium thiophosphate, a collector, and a frother to the pulp in sequence, and obtain lead rougher concentrate and lead rougher tailings after one-stage lead rougher flotation.

[0012] (3) Subject the lead rougher concentrate obtained in step (2) to two-stage lead cleaning; in the lead cleaning I operation, add sodium thiophosphate and a frother in sequence; in the lead cleaning II operation, add sodium thiophosphate; after two-stage lead cleaning, obtain the final lead concentrate and lead cleaning tailings, and the lead cleaning tailings are returned to the previous operation.

[0013] (4) Subject the lead rougher tailings obtained in step (2) to two-stage lead scavenging. In the lead scavenging I operation, add a collector and a frother in sequence, and in the lead scavenging II operation, add a collector; after two-stage lead scavenging, obtain lead scavenging tailings and lead scavenging concentrate, and the lead scavenging concentrate is returned to the previous operation in sequence.

[0014] (5) Subject the lead scavenging tailings obtained in step (4) to zinc rougher flotation operation, add lime, an activator, a collector, and a frother in sequence, and separate to obtain zinc rougher concentrate and zinc rougher tailings after one-stage zinc rougher flotation.

[0015] (6) Subject the zinc rougher concentrate obtained in step (5) to two-stage zinc cleaning. In the zinc cleaning I operation, add lime and a frother in sequence; in the zinc cleaning II operation, add lime; after two-stage zinc cleaning, obtain the final zinc concentrate and zinc cleaning tailings, and the zinc cleaning tailings are returned to the previous operation in sequence.

[0016] (7) The zinc rougher tailings obtained in step (5) are subjected to two zinc scavenging operations; in the first zinc scavenging operation, an activator, a collector, and a frother are sequentially added; in the second zinc scavenging operation, a collector is added; after the two zinc scavenging operations, the final tailings are obtained, and the zinc scavenging concentrates are sequentially returned to the previous operation level.

[0017] Preferably, the proportion of the -0.074 mm particle size fraction in the pulp is 64% to 68%.

[0018] Preferably, the addition amount of sodium thiophosphate in the lead rougher is 200 to 400 g / t.

[0019] Preferably, in the lead rougher in step (2), the addition amount of the dispersant is 1000 to 1500 g / t; the addition amount of the collector is 50 to 60 g / t; the addition amount of the frother is 15 to 20 g / t.

[0020] Preferably, the addition amount of sodium thiophosphate in the first lead cleaner is 100 to 200 g / t; in the second lead cleaner, the addition amount of sodium thiophosphate is 50 to 100 g / t.

[0021] Preferably, in the first lead cleaner in step (3), the addition amount of the frother is 5 to 10 g / t.

[0022] Preferably, in the first lead scavenger in step (4), the addition amount of the collector is 20 to 30 g / t, and the addition amount of the frother is 5 to 10 g / t; in the second lead scavenger, the addition amount of the collector is 5 to 10 g / t.

[0023] Preferably, in step (5), the addition amount of lime is 500 to 1000 g / t, the addition amount of the activator is 400 to 600 g / t, the addition amount of the collector is 40 to 60 g / t; the addition amount of the frother is 15 to 20 g / t.

[0024] Preferably, in the first zinc cleaner in step (6), the addition amount of lime is 300 to 400 g / t, and the addition amount of the frother is 5 to 10 g / t; in the second zinc cleaner, the addition amount of lime is 100 to 200 g / t.

[0025] Preferably, in the first zinc scavenger in step (7), the addition amount of the activator is 50 to 100 g / t, the addition amount of the collector is 20 to 30 g / t, and the addition amount of the frother is 5 to 10 g / t; in the second zinc scavenger, the addition amount of the collector is 5 to 10 g / t.

[0026] The dispersant, collector, activator, and frother used in the separation process are all conventional reagents commonly used by those skilled in the art.

[0027] Principle of the present invention: The present invention is based on the basic principle of flotation separation, that is, by adding flotation reagents to selectively regulate the wettability of different mineral surfaces. The present invention uses sodium thiophosphate (Na3PO3S) as a selective inhibitor for sphalerite and pyrite when preferentially floating lead minerals. Specifically, the O and S atoms in sodium thiophosphate have lone pairs of electrons, which can coordinate with the Zn atoms on the surface of sphalerite and the Fe atom sites on the surface of pyrite to form surface bonds of types such as Zn-O, Zn-S, Fe-O, and Fe-S, and then form a chemisorbed layer. This chemisorbed layer makes the surfaces of sphalerite and pyrite more hydrophilic on the one hand, and on the other hand, sterically hinders the adsorption of activators on the surfaces of sphalerite and pyrite. In contrast, on the surface of galena, the adsorption of the activator is stronger than that of sodium thiophosphate under this condition, so that the surface of galena still maintains good hydrophobicity. Finally, during the flotation process, the highly hydrophobic galena preferentially floats up into the foam product, while the sphalerite and pyrite with hydrophilic surfaces remain in the pulp, thus realizing the efficient selective separation of galena from sphalerite and pyrite.

[0028] Advantages of the present invention:

[0029] (1) The sodium thiophosphate used in the present invention has excellent selective inhibitory effects on sphalerite and pyrite, while maintaining the floatability of galena.

[0030] (2) Through the effective inhibition of sphalerite and pyrite, the present invention significantly improves the separation effect of lead flotation operations, not only improving the quality and recovery rate of lead concentrates, but also reducing the loss of zinc minerals in lead flotation, which is beneficial to improving the zinc recovery rate of subsequent zinc flotation operations and ultimately enhancing the total recovery level of valuable metals in the ore.

[0031] (3) Compared with the traditional method of using a large amount of lime to inhibit pyrite in high-alkalinity pulp, the inhibitor sodium thiophosphate used in the present invention can reduce the lime consumption in lead flotation and zinc flotation operations, thereby reducing the pollution of highly alkaline beneficiation wastewater and pipeline blockage.

[0032] (4) The inhibitor provided by the present invention has low dosage, low cost, environmental friendliness and convenient use. Description of the drawings

[0033] Figure 1 It is a schematic diagram of the flotation process flow used in the embodiment of the present invention.

[0034] Figure 2 It is a schematic diagram of the flotation process flow used in the comparative example of the present invention. Detailed implementation manners

[0035] The present invention will be further described in detail below in conjunction with the accompanying drawings and specific embodiments. It should be understood that these embodiments are only used to explain the present invention and do not limit the scope of the present invention in any form. The protection scope of the present invention shall be subject to the claims. Unless otherwise specified, the technical means used in the embodiments are conventional means well-known to those skilled in the art, and the reagents used are all industrial products or commercially available.

[0036] Example 1

[0037] The ore sample used in this example is a lead-zinc sulfide ore in Inner Mongolia. The chemical multi-element analysis results of the original ore are as follows: Pb 1.81%, Zn 1.52%, S 3.72%. The flotation process flow chart is as Figure 1 shown, and the specific flotation separation steps are as follows:

[0038] (1) Grinding: Grind the original ore to a fineness where the content of the -0.074mm particle size fraction reaches 68%, and adjust it into a pulp with a mass concentration of 30%.

[0039] (2) Lead roughing: Sequentially add 1000 g / t of water glass, 200 g / t of sodium thiophosphate, 50 g / t of butyl xanthate, and 15 g / t of 2 # oil per ton of dry weight of the original ore to the pulp, stir and perform aerated flotation to obtain lead roughing concentrate and lead roughing tailings.

[0040] (3) Lead cleaning: Perform two-stage cleaning on the lead roughing concentrate. In the lead cleaning I operation, sequentially add 100 g / t of sodium thiophosphate and 10 g / t of 2 # oil per ton of dry weight of the original ore, stir and then perform flotation; in the lead cleaning II operation, add 50 g / t of sodium thiophosphate per ton of dry weight of the original ore, stir and then perform flotation to obtain the final lead concentrate. The tailings from the two-stage lead cleaning are sequentially returned to the previous operation.

[0041] (4) Lead scavenging: Perform two-stage scavenging on the lead roughing tailings. In the lead scavenging I operation, sequentially add 20 g / t of butyl xanthate and 10 g / t of 2 # oil per ton of dry weight of the original ore, stir and then perform flotation; in the lead scavenging II operation, add 10 g / t of butyl xanthate per ton of dry weight of the original ore, stir and then perform flotation to obtain lead scavenging tailings. The concentrates from the two-stage lead scavenging are sequentially returned to the previous operation.

[0042] (5) Zinc roughing: Use the lead scavenging tailings from step (4) as the zinc flotation feed. Sequentially add 500 g / t of lime, 400 g / t of copper sulfate, 50 g / t of butyl xanthate, and 15 g / t of 2 # oil per ton of dry weight of the original ore, stir and perform aerated flotation to obtain zinc roughing concentrate and zinc roughing tailings.

[0043] (6) Zinc beneficiation: The zinc rougher concentrate is beneficiated twice. In the first zinc beneficiation operation, 300 g / t of lime and 10 g / t of No. 2 oil are added successively per ton of dry raw ore, and after stirring, flotation is carried out. In the second zinc beneficiation operation, 100 g / t of lime is added per ton of dry raw ore, and after stirring, flotation is carried out to obtain the final zinc concentrate; the tailings from the two zinc beneficiation operations are returned to the previous operation level in sequence. # In the second zinc beneficiation operation, 100 g / t of lime is added per ton of dry raw ore, and after stirring, flotation is carried out to obtain the final zinc concentrate; the tailings from the two zinc beneficiation operations are returned to the previous operation level in sequence.

[0044] (7) Zinc scavenging: The zinc rougher tailings in step (5) are scavenged twice. In the first zinc scavenging operation, 50 g / t of copper sulfate, 20 g / t of butyl xanthate, and 10 g / t of No. 2 oil are added successively per ton of dry raw ore, and after stirring, flotation is carried out. In the second zinc scavenging operation, 10 g / t of butyl xanthate is added per ton of dry raw ore, and after stirring, flotation is carried out to obtain the final tailings. The concentrates from the two zinc scavenging operations are returned to the previous operation level in sequence. # In the second zinc scavenging operation, 10 g / t of butyl xanthate is added per ton of dry raw ore, and after stirring, flotation is carried out to obtain the final tailings. The concentrates from the two zinc scavenging operations are returned to the previous operation level in sequence.

[0045] The results of the closed-circuit flotation test in this example are shown in Table 1.

[0046] Example 2

[0047] The ore sample used in this example is a lead-zinc sulfide ore from a certain place in Guangxi, and the results of its chemical composition analysis are: Pb 2.04%, Zn 2.12%, S 5.21%; the flotation process flow is the same as that in Example 1. The reagent system is mainly adjusted as follows: the sodium thiophosphate in the lead rougher operation is adjusted to 300 g / t; the sodium thiophosphate in the first lead beneficiation operation is adjusted to 150 g / t; the sodium thiophosphate in the second lead beneficiation operation is adjusted to 75 g / t; the dosage of butyl xanthate in the zinc rougher operation is adjusted to 40 g / t. The types, dosages of other reagents and operation parameters are the same as those in Example 1.

[0048] The results of the closed-circuit flotation test in this example are shown in Table 1.

[0049] Example 3

[0050] The ore sample used in this example is a lead-zinc sulfide ore from a certain place in Yunnan, and the results of its chemical composition analysis are: Pb 2.16%, Zn 5.14%, S 8.63%; the flotation process flow is the same as that in Example 1. The reagent system is mainly adjusted as follows: the water glass in the lead rougher operation is adjusted to 1500 g / t, the sodium thiophosphate is adjusted to 400 g / t, the butyl xanthate is adjusted to 60 g / t, and the No. 2 oil is adjusted to 20 g / t; the sodium thiophosphate in the first lead beneficiation operation is adjusted to 200 g / t and the No. 2 oil is adjusted to 5 g / t; the sodium thiophosphate in the second lead beneficiation operation is adjusted to 100 g / t; the butyl xanthate in the first lead scavenging operation is adjusted to 30 g / t and the No. 2 oil is adjusted to 10 g / t; # In the first lead beneficiation operation, the sodium thiophosphate is adjusted to 200 g / t and the No. 2 oil is adjusted to 5 g / t; # In the second lead beneficiation operation, the sodium thiophosphate is adjusted to 100 g / t; in the first lead scavenging operation, the butyl xanthate is adjusted to 30 g / t and the No. 2 oil is adjusted to 10 g / t; #The dosage of oil is adjusted to 5 g / t; the dosage of butyl xanthate in the second lead scavenging operation is adjusted to 5 g / t; the dosage of lime in the first zinc roughing operation is adjusted to 1000 g / t, the dosage of copper sulfate is adjusted to 600 g / t, the dosage of butyl xanthate is adjusted to 60 g / t, 2 # The dosage of oil is adjusted to 20 g / t; the dosage of lime in the first zinc cleaning operation is adjusted to 400 g / t, 2 # The dosage of oil is adjusted to 5 g / t; the dosage of lime in the second zinc cleaning operation is adjusted to 200 g / t; the dosage of copper sulfate in the first zinc scavenging operation is adjusted to 100 g / t, the dosage of butyl xanthate is adjusted to 30 g / t, 2 # The dosage of oil is adjusted to 5 g / t; the dosage of butyl xanthate in the second zinc scavenging operation is adjusted to 5 g / t. The types, dosages of other reagents and operation parameters are the same as those in Example 1.

[0051] The results of the closed-circuit flotation test in this example are shown in Table 1.

[0052] Comparative Example 1

[0053] This comparative example aims to compare with Example 1 to illustrate the effect of the inhibitor of the present invention. The ore samples and flotation process flows used are the same as those in Example 1. The specific flotation process is as Figure 2 shown. The main difference is that instead of using sodium thiophosphate as the inhibitor in the lead flotation operation, zinc sulfate and lime are used as the inhibitors, and the corresponding dosage of lime is added in the second lead cleaning operation. The dosage of reagents is mainly adjusted as follows: the dosage of water glass in the first lead roughing operation is adjusted to 2000 g / t, the inhibitor is adjusted to 1500 g / t of lime and 1000 g / t of zinc sulfate; the inhibitor in the first lead cleaning operation is adjusted to 400 g / t of zinc sulfate; the inhibitor in the second lead cleaning operation is adjusted to 200 g / t of lime and 200 g / t of zinc sulfate; the dosage of lime in the first zinc roughing operation is adjusted to 2000 g / t; the dosage of lime in the first zinc cleaning operation is adjusted to 500 g / t; the dosage of lime in the second zinc cleaning operation is adjusted to 200 g / t. The types, dosages of other reagents and operation parameters are the same as those in Example 1.

[0054] The results of the closed-circuit flotation test in this comparative example are shown in Table 1.

[0055] Comparative Example 2

[0056] This comparative example aims to compare with Example 2 to illustrate the effect of the inhibitor of the present invention. The ore samples and flotation process flows used are the same as those in Example 2. The main difference is that in the lead flotation operation, sodium thiophosphate is not used as the inhibitor, but zinc sulfate and lime are used as inhibitors, and the corresponding amount of lime is added in the second lead cleaning operation. The dosage of the agents is mainly adjusted as follows: in the lead roughing operation, the water glass is adjusted to 2000 g / t, the inhibitor is adjusted to 1500 g / t of lime and 1000 g / t of zinc sulfate; in the first lead cleaning operation, the inhibitor is adjusted to 500 g / t of zinc sulfate; in the second lead cleaning operation, the inhibitor is adjusted to 200 g / t of lime and 250 g / t of zinc sulfate; in the zinc roughing operation, the lime is adjusted to 2000 g / t; in the first zinc cleaning operation, the lime is adjusted to 600 g / t; in the second zinc cleaning operation, the lime is adjusted to 300 g / t. The types, dosages and operation parameters of other agents are consistent with those in Example 2.

[0057] The results of the closed-circuit flotation test of this comparative example are shown in Table 1.

[0058] Comparative Example 3

[0059] This comparative example aims to compare with Example 3 to illustrate the effect of the inhibitor of the present invention. The ore samples and flotation process flows used are the same as those in Example 3. The main difference is that in the lead flotation operation, sodium thiophosphate is not used as the inhibitor, but zinc sulfate and lime are used as inhibitors, and the corresponding amount of lime is added in the second lead cleaning operation. The dosage of the agents is mainly adjusted as follows: in the lead roughing operation, the inhibitor is adjusted to 1500 g / t of lime and 1500 g / t of zinc sulfate; in the first lead cleaning operation, the inhibitor is adjusted to 600 g / t of zinc sulfate; in the second lead cleaning operation, the inhibitor is adjusted to 200 g / t of lime and 300 g / t of zinc sulfate. In the zinc roughing operation, the lime is adjusted to 2000 g / t; in the first zinc cleaning operation, the lime is adjusted to 600 g / t; in the second zinc cleaning operation, the lime is adjusted to 300 g / t. The types, dosages and operation parameters of other agents are consistent with those in Example 3.

[0060] The results of the closed-circuit flotation test of this comparative example are shown in Table 1.

[0061] Table 1 Closed-circuit flotation test indexes of each example and comparative example

[0062]

[0063] Table 1 clearly shows the main technical indexes obtained from the closed-circuit flotation test of lead-zinc sulfide ore using the method of the present invention and the traditional method, aiming to objectively evaluate the effectiveness of the application method using sodium thiophosphate as the inhibitor proposed by the present invention. The data comparison intuitively reflects that the technical solution proposed by the present invention shows significant superiority in the lead-zinc separation effect compared with the commonly used zinc sulfate inhibition system in the prior art.

[0064] For different ore samples, the method of the present invention has achieved a significant improvement in the grade of lead concentrate, while maintaining a high lead recovery rate. More importantly, the method of the present invention has an excellent inhibitory effect on sphalerite and also has a good inhibitory effect on pyrite, resulting in a significant reduction in the zinc content in lead concentrate, effectively reducing the mutual inclusion rate of lead and zinc concentrates, and creating favorable conditions for subsequent zinc flotation. While achieving high-quality lead concentrate and high recovery rate, the most prominent advantage of the method of the present invention lies in the significant reduction in the dosage of the inhibitor. Taking Example 1 as an example, the total dosages of sodium thiophosphate and lime are 21.9% and 20.4% of the total dosages of zinc sulfate and lime in Comparative Example 1 respectively, which indicates that sodium thiophosphate has a higher inhibitory efficiency and can achieve a better separation effect with less reagents, thereby reducing the beneficiation cost and potential environmental impact.

[0065] In summary, by using sodium thiophosphate as a selective inhibitor, the method of the present invention can efficiently inhibit sphalerite and pyrite, significantly improve the grade and recovery rate of lead concentrate, effectively reduce the mutual inclusion rate of lead and zinc concentrates, and show good compatibility with the subsequent recovery of zinc. More importantly, this method can greatly reduce the dosage of the inhibitor and has obvious advantages in terms of economy and environmental friendliness compared with traditional methods. Therefore, the technical solution provided by the present invention provides a promising solution for the efficient, economic and environmental-friendly separation of lead-zinc sulfide ores and has important industrial application value.

Claims

1. A flotation separation inhibitor for lead-zinc sulfide ores, characterized in that: The inhibitor is sodium thiophosphate.

2. Use of the inhibitor according to claim 1 in flotation separation of lead-zinc sulfide ore to obtain lead concentrate and zinc concentrate.

3. The use according to claim 2, characterized in that: The application method is as follows: (1) grinding the lead-zinc sulfide ore to prepare a slurry; (2) adding a dispersant, sodium thiophosphate, a collector and a frother to the slurry in sequence, and obtaining a lead roughing concentrate and a lead roughing tailing after a lead roughing process; (3) subjecting the lead roughing concentrate obtained in step (2) to lead concentration twice; in lead concentration I, sodium thiophosphate and a frother are added in sequence; in lead concentration II, sodium thiophosphate is added; after two lead concentrations, a final lead concentrate is obtained, and the tailings of the two lead concentrations are returned to the previous operation in sequence; (4) The lead roughing tailings obtained in step (2) are subjected to two lead scavenging operations. In the lead scavenging operation I, a collector and a frother are added in sequence. In the lead scavenging operation II, a collector is added. After two lead scavenging operations, lead scavenging tailings are obtained. The concentrates of the two lead scavenging operations are returned to the previous operation in sequence. (5) subjecting the lead scavenging tailings obtained in step (4) to zinc roughing, adding lime, an activator, a collector and a frother in sequence, and separating the zinc roughing concentrate and the zinc roughing tailings after a zinc roughing; (6) The zinc rougher concentrate obtained in step (5) is subjected to two zinc concentrations. In the zinc concentration I operation, lime and a frother are added in sequence; in the zinc concentration II operation, lime is added; after two zinc concentrations, a final zinc concentrate and zinc concentration tailings are obtained, and the zinc concentration tailings are returned to the previous operation in sequence; (7) The zinc rougher tailings obtained in step (5) are subjected to two zinc scavenging operations; an activator, a collector and a frother are added in sequence in the zinc scavenging operation I; and a collector is added in the zinc scavenging operation II; and the final tailings are obtained after two zinc scavenging operations, and the zinc scavenging concentrate is returned to the previous operation in sequence.

4. The use according to claim 3, characterized in that: The amount of sodium thiophosphate added in the lead roughing process of step (2) is 200-400 g / t.

5. The use according to claim 3, characterized in that: In the lead coarse selection of step (2), the amount of dispersant added is 1000-1500 g / t; the amount of collector added is 50-60 g / t; and the amount of foaming agent added is 15-20 g / t.

6. The use according to claim 3, characterized in that: In the lead concentration I operation described in step (3), the amount of sodium thiophosphate added is 100-200 g / t; in the lead concentration II operation, the amount of sodium thiophosphate added is 50-100 g / t.

7. The use according to claim 3, characterized in that: The amount of foaming agent added in the lead concentration I operation of step (3) is 5 to 10 g / t.

8. The use according to claim 3, characterized in that: In the lead scavenging I operation of step (4), the amount of collector added is 20-30 g / t, and the amount of foaming agent added is 5-10 g / t; in the lead scavenging II operation, the amount of collector added is 5-10 g / t.

9. The use according to claim 3, characterized in that: In step (5), the amount of lime added is 500-1000 g / t, the amount of activator added is 400-600 g / t, the amount of collector added is 40-60 g / t; and the amount of foaming agent added is 15-20 g / t.

10. The use according to claim 3, characterized in that: In the zinc concentration I operation of step (6), the amount of lime added is 300-400 g / t, and the amount of frother added is 5-10 g / t; in the zinc concentration II operation, the amount of lime added is 100-200 / t; in the zinc scavenging I operation of step (7), the amount of activator added is 50-100 g / t, the amount of collector added is 20-30 g / t, and the amount of frother added is 5-10 g / t; in the zinc scavenging II operation, the amount of collector added is 5-10 g / t.

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