A mineral separation method for separating sphalerite

Abstract

The present invention discloses a mineral processing method for the separation of iron sphalerite, which belongs to the field of mineral processing technology. The present invention pre-removes sphalerites with different iron contents and different floatation activities by means of the technical means of cascade flotation. At the same time, the present invention innovatively uses unconventional collectors, inhibitors, and activators such as arylhydroxamic acid, glucomannan, sodium dithionite, and silver chloride. The collectors, inhibitors, and activators with different properties are combined together to selectively activate sphalerites with different iron contents, change the floatation properties of sphalerites with different iron contents, and make sphalerites with different iron contents float out in sequence. This technical circuit not only reduces the difficulty of separating iron-containing sphalerite from pyrite and improves separation efficiency, but also saves reagent costs, thereby improving the economic and social benefits of mining enterprises.

Description

Technical Field

[0001] The present invention relates to the technical field of mineral processing, and in particular to a mineral processing method for separating sphalerite. Background Art

[0002] Sphalerite is a sulfide mineral. In nature, sphalerite usually contains a variety of impurity elements such as Fe, Mn, Cd, Ga, Ge, In, Se, and Te. Among them, Fe is the easiest to enter the sphalerite lattice to form a mixed crystal system of ZnS-FeS. The iron content of sphalerite depends on the FeS content. According to the different iron content of sphalerite, it can be divided into iron sphalerite (iron content>6%), high-iron sphalerite (iron content>12%) and ultra-high-iron sphalerite (iron content>18%). When iron enters the sphalerite lattice to form iron sphalerite, the size of the sphalerite becomes smaller, the specific surface area becomes larger, the hydration effect is enhanced, and the natural floatability decreases; and because of Fe 2+ Radius larger than Zn 2+ , the copper activation process of sphalerite will be hindered, which in turn will weaken the xanthate capture process, making the separation of sphalerite and pyrite more difficult. As the iron content increases, the difference in surface properties between sphalerite and pyrite continues to decrease, making the separation of the two minerals more difficult. Because the high alkaline environment inhibits pyrite while also reducing the flotation of sphalerite, the traditional lime-alkali process that can separate sphalerite and pyrite cannot achieve a good separation of sphalerite, especially high-iron sphalerite, from pyrite.

[0003] To improve the separation efficiency of sphalerite and pyrite in such ores, a deep dissociation-strong inhibition method is currently often used to enhance the inhibition of pyrite. For example, patent CN107442267B discloses a flotation method for fine-grained, refractory sphalerite. This method uses lime, hydroxyalkyl dithiocarbamate, and sodium humate to separate sphalerite and pyrite by regrinding the concentrate. While this separation process addresses the issues of high separation difficulty and low separation accuracy to a certain extent, it requires regrinding the mixed concentrate, which consumes high energy and is complex. Furthermore, the inhibitor used is a combined inhibitor, resulting in a high flotation pH and low zinc recovery, making it difficult to commercialize. Patent CN111632748A discloses a method for treating sphalerite using a combined magnetic-flotation process. This method treats zinc roughing tailings by adding magnetic separation to remove some pyrrhotite with higher magnetism, and then separates the pyrite through a flotation process. Although this solution reduces the interference of pyrrhotite on the zinc flotation process to a certain extent, the method is only applicable to zinc ores with low pyrrhotite and pyrite contents in the material, and is not applicable to zinc ores with weak magnetism and high pyrite contents.

[0004] In addition, the material containing sphalerite is mainly lead-zinc sulfide ore, and the pyrite content in most lead-zinc sulfide ores is much higher than that of lead-zinc minerals. Therefore, in the lead flotation process, in order to obtain qualified lead concentrate products, a large amount of sphalerite and pyrite inhibitors need to be added; correspondingly, a large amount of copper sulfate needs to be added in the zinc flotation process, resulting in an extremely high actual copper sulfate usage, even as high as 1000-2000g / t. Copper sulfate also has a significant activation effect on pyrite. Pyrite activated by copper sulfate has excellent floatability, resulting in a very high cost of the reagent used to inhibit the pyrite activated by copper sulfate.

[0005] Therefore, how to further improve the utilization rate of lead-zinc mineral resources containing sphalerite and pyrite, reduce the difficulty of separating sphalerite and pyrite, improve the separation efficiency of sphalerite and pyrite, reduce the separation cost of sphalerite and pyrite, and carry out separation and high-value comprehensive recycling of sphalerite and pyrite is one of the major problems that need to be solved urgently in the current mineral resources industry. In response to the above problems, the present invention provides a mineral processing method for separation of sphalerite. Summary of the Invention

[0006] The purpose of the present invention is to provide a mineral processing method for separating sphalerite by quality, which can achieve preferential and rapid flotation of partially activated sphalerite by changing the flotation performance of sphalerite with different iron contents, and at the same time reduce the separation difficulty for subsequent zinc flotation, improve the separation efficiency, and reduce production costs, thereby solving the problems of low separation efficiency, great separation difficulty and high separation cost in existing mineral processing processes.

[0007] To achieve the above object, the present invention provides a mineral separation method for marmatite separation, comprising the following steps:

[0008] S1. Slurrying the sulfide ore containing sphalerite to a slurry mass concentration of 30-45%;

[0009] S2, stirring the slurry obtained in step S1, adding an inhibitor, an activator, and a collector in sequence, and starting the first stage of flotation after the reagents have fully reacted with the slurry to obtain a low-iron sphalerite concentrate and tailings with an iron content of less than 6%;

[0010] S3, adding an inhibitor, an activator and a collector to the tailings obtained in step S2, and starting the second flotation operation after the reagents have fully reacted with the slurry to obtain a sphalerite concentrate and tailings with an iron content of 6-12%;

[0011] S4, adding an inhibitor, an activator and a collector to the tailings obtained in step S3, and starting the third flotation operation after the reagents have fully reacted with the slurry to obtain a high-iron sphalerite concentrate and tailings with an iron content of 12-18%;

[0012] S5. Add an inhibitor, an activator, and a collector to the tailings obtained in step S4 in sequence. After the reagents fully react with the slurry, start the fourth flotation operation to obtain an ultra-high iron sphalerite concentrate with an iron content of >18% and a final tailings.

[0013] Preferably, in step S2, the inhibitor is sodium metabisulfite, and the dosage is 0-500 g / t; the activator is lead nitrate, and the dosage is 0-500 g / t; the collector is diesel and butyl xanthate, wherein the dosage of diesel is 0-10 g / t, and the dosage of butyl xanthate is 0-30 g / t.

[0014] Preferably, in step S3, the inhibitor is sodium dithionite, and the dosage is 0-800 g / t; the activator is copper sulfate, and the dosage is 0-500 g / t; and the collector is allyl isobutyl thiocarbamate, and the dosage is 0-50 g / t.

[0015] Preferably, in step S4, the inhibitor is sodium sulfite, and the amount is 0-800 g / t; the activator is ammonium sulfite, and the amount is 0-800 g / t; the collector is aryl hydroxamic acid, and the amount is 0-100 g / t, and the structural formula is shown in Formula 1.

[0016]

[0017]

[0018] Among them, R1 and R2 are C n H 2n+2 Alkanes with structure, n≥1.

[0019] Preferably, in step S5, the inhibitor is glucomannan, and the amount is 0-500 g / t; the activator is silver chloride, and the amount is 0-800 g / t; the collector is a combination of sodium butyrate, allyl isobutyl thiocarbamate, and aryl hydroxamic acid, and the amount is 0-50 g / t. The structural formula of aryl hydroxamic acid is shown in Formula 1.

[0020]

[0021] Among them, R1 and R2 are C n H 2n+2 Alkanes with structure, n≥1.

[0022] Preferably, the glucomannan is a high molecular weight heteropolysaccharide formed by polymerization of glucose and mannose residues in a molecular ratio of 1:1.6 to 1.7 through β-1,4 glycosidic bonds.

[0023] Preferably, the specific operation of the first stage flotation operation in step S2 is as follows: the rougher concentrate enters the zinc concentration operation, and after one concentration operation, a low-iron sphalerite concentrate with an iron content of less than 6% is obtained, and the tailings from the zinc concentration are returned to the previous operation; the rougher tailings enter the second scavenging operation, the scavenged concentrate is returned to the previous operation, and the scavenged tailings enter the next operation.

[0024] Preferably, the specific operation of the second flotation operation in step S3 is as follows: the roughing concentrate enters the zinc concentration operation, and after two concentration operations, a sphalerite concentrate with an iron content of 6-12% is obtained, and the tailings from the zinc concentration are returned to the previous operation in sequence; the roughing tailings enter two scavenging operations, the scavenged concentrate is returned to the previous operation, and the scavenged tailings enter the next operation.

[0025] Preferably, the specific operation of the third stage flotation operation in step S4 is as follows: the roughing concentrate enters the zinc concentration operation, and after three concentration operations, a sphalerite concentrate with an iron content of 12-18% is obtained, and the tailings from the zinc concentration are returned to the previous operation in sequence; the roughing tailings enter two scavenging operations, the scavenged concentrate is returned to the previous operation, and the scavenged tailings enter the next operation.

[0026] Preferably, the specific operation of the fourth stage flotation operation in step S5 is: the roughing concentrate enters the concentrating operation, the concentrate from the nth concentrating enters the n+1th lead concentrating operation, and the tailings from the nth lead concentrating return to the n-1th lead concentrating operation; the tailings from the roughing enters the scavenging operation, the concentrate from the nth lead scavenging enters the n-1th scavenging operation, and the tailings from the nth lead scavenging enters the n+1th lead scavenging operation, wherein n is a natural number and is greater than or equal to 3.

[0027] Therefore, the present invention provides a mineral separation method for marmatite separation, which has the following beneficial effects:

[0028] (1) The mineral processing method of the present invention abandons the traditional high-alkali technical idea of ​​"heavy pulling and heavy pressing" and adopts a "starvation" drug administration method. By combining several collectors, inhibitors and activators with different collecting properties, inhibitory properties and activation properties, sphalerite with different iron contents is selectively activated, the floating properties of sphalerite with different iron contents are changed, and sphalerite with different iron contents is floated out in sequence. This technical line not only reduces the difficulty of separating iron-containing sphalerite from pyrite, improves separation efficiency, and increases product types, but also greatly reduces the amount of copper sulfate used, avoids the high-alkali effect brought by the use of lime, saves the cost of reagents, and reduces the pollution of residual heavy metal ions in mineral processing wastewater, thereby improving the economic and social benefits of mining enterprises.

[0029] (2) The present invention innovatively uses unconventional collectors, inhibitors and activators such as aromatic hydroxamic acid, glucomannan, sodium dithionite and silver chloride, and innovatively uses these agents in combination, which cleverly makes up for the shortcomings of poor selectivity of existing flotation agents, not only achieving the purpose of quality separation, but also reducing the environmental pollution of agents and lowering the requirements of flotation on the pH value of the pulp.

[0030] (3) The present invention removes sphalerite with different iron contents and different floatation activities in advance through the technical means of step S2, S3, S4, and S5 cascade flotation, greatly reducing the amount of copper sulfate used in the traditional process and avoiding the activation of gangue minerals such as pyrite by high copper sulfate dosage. Not only is the production process simple, adaptable, and efficient, but it can also reduce the loss of other valuable minerals in the tailings, improve the comprehensive utilization efficiency of resources, and achieve efficient comprehensive recovery of valuable metals. It is particularly suitable for ores with a large span of embedded particle size, complex structure, and a large amount of associated valuable metals.

[0031] The technical solution of the present invention is further described in detail below through the accompanying drawings and embodiments. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] Figure 1 Schematic diagram of the process flow of an embodiment of the present invention;

[0033] Figure 2 Schematic diagram of the process flow of the comparative example of the present invention. DETAILED DESCRIPTION

[0034] The present invention provides a method for separating and separating sphalerite, comprising the following steps:

[0035] S1. The prepared sphalerite sulfide ore is transported to a slurry mixing tank for mixing and slurrying. During the slurrying process, the slurry mass concentration is adjusted to 30-45% by concentration or dilution with clean water.

[0036] If the concentration of the material to be processed is higher than 45%, a certain amount of clean water is added to dilute the material to the specified concentration. If the concentration of the material to be processed is lower than 30%, a certain amount of clarified liquid is removed by sedimentation concentration to concentrate the pulp to a mass percentage concentration of 30-45% for the next operation.

[0037] S2. The slurry obtained in step S1 is stirred, and an inhibitor, an activator, and a collector are added in succession during the stirring process. After the reagents fully react with the slurry, the first flotation operation is started to obtain a low-iron sphalerite concentrate and tailings with an iron content of less than 6%.

[0038] In the present invention, the specific operation of the first stage flotation operation is as follows: the roughing concentrate enters the zinc concentration operation, and after the first concentration operation, a low-iron sphalerite concentrate with an iron content of less than 6% is obtained, and the tailings of the zinc concentration are returned to the previous operation; the roughing tailings enter the second scavenging operation, the scavenged concentrate is returned to the previous operation, and the scavenged tailings enter the next operation.

[0039] The inhibitor is sodium metabisulfite, and the dosage is 0-500 g / t, preferably 200-300 g / t; the activator is lead nitrate, and the dosage is 0-500 g / t, preferably 200-300 g / t; the collector is diesel and butyl xanthate, wherein the dosage of diesel is 0-10 g / t, and the dosage of butyl xanthate is 0-30 g / t.

[0040] S3. Add an inhibitor, an activator and a collector to the tailings obtained in step S2 in sequence, and start the second flotation operation after the reagents fully react with the slurry to obtain sphalerite concentrate and tailings with an iron content of 6-12%.

[0041] In the present invention, the specific operation of the second stage flotation operation is as follows: the roughing concentrate enters the zinc concentration operation, and after two concentration operations, the marmatite concentrate with an iron content of 6-12% is obtained, and the tailings of the zinc concentration are returned to the previous operation in sequence; the roughing tailings enter the two scavenging operations, the scavenged concentrate is returned to the previous operation, and the scavenged tailings enter the next operation.

[0042] In the present invention, the inhibitor is sodium dithionite, and the dosage is 0-800 g / t, preferably 300-500 g / t; the activator is copper sulfate, and the dosage is 0-500 g / t, preferably 200-300 g / t; the collector is allyl isobutyl thiocarbamate, and the dosage is 0-50 g / t, preferably 10-20 g / t.

[0043] S4. Add an inhibitor, an activator and a collector to the tailings obtained in step S3 in sequence, and start the third flotation operation after the reagents fully react with the slurry to obtain a high-iron sphalerite concentrate and tailings with an iron content of 12-18%.

[0044] In the present invention, the specific operation of the third stage flotation operation is as follows: the roughing concentrate enters the zinc concentration operation, and after three concentration operations, the marmatite concentrate with an iron content of 12-18% is obtained, and the tailings of the zinc concentration are returned to the previous operation in sequence; the roughing tailings enter the second scavenging operation, the scavenged concentrate is returned to the previous operation, and the scavenged tailings enter the next operation.

[0045] The inhibitor is sodium sulfite, and the dosage is 0-800 g / t, preferably 100-300 g / t; the activator is ammonium sulfite, and the dosage is 0-800 g / t, preferably 200-500 g / t; the collector is aryl hydroxamic acid, and the dosage is 0-100 g / t, preferably 20-60 g / t. The structural formula is shown in Formula 1.

[0046]

[0047] Among them, R1 and R2 are C n H 2n+2 Alkanes with structure, n≥1.

[0048] S5. Add an inhibitor, an activator, and a collector to the tailings obtained in step S4 in sequence. After the reagents fully react with the slurry, start the fourth flotation operation to obtain an ultra-high iron sphalerite concentrate with an iron content of >18% and a final tailings.

[0049] In the present invention, the specific operation of the fourth stage flotation operation is as follows: the rougher concentrate enters the concentration operation, the concentrate from the nth concentration enters the n+1th lead concentration operation, and the tailings from the nth lead concentration return to the n-1th lead concentration operation; the tailings from the rougher concentration enters the scavenging operation, the concentrate from the nth lead scavenging enters the n-1th scavenging operation, and the tailings from the nth lead scavenging enters the n+1th lead scavenging operation, where n is a natural number and is greater than or equal to 3.

[0050] The inhibitor is glucomannan, which is a high-molecular-weight heteropolysaccharide polymerized by glucose and mannose residues in a molecular ratio of 1:1.6-1.7 through β-1,4 glycosidic bonds, and the dosage is 0-500 g / t, preferably 300-500 g / t; the activator is silver chloride, and the dosage is 0-800 g / t, preferably 300-500 g / t; the collector is a combination collector of sodium butyrate, allyl isobutyl thiocarbamate and aromatic hydroxamic acid of formula 1, and the dosage of the combination collector is 0-50 g / t, preferably 10-20 g / t.

[0051] In order to make the purpose, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and specific embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the scope of the invention claimed for protection, but merely represent selected embodiments of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of the present invention.

[0052] The ore used in the following experiments was obtained from tailings from a lead-zinc mine in Chenzhou, Hunan Province. It contained approximately 5.3% zinc, 11.5% iron, and 14.2% sulfur. The inhibitors used in the experiments were sodium sulfite, sodium metabisulfite, sodium dithionite, and glucomannan. The activators used were copper sulfate, lead nitrate, ammonium sulfite, and silver chloride. The collectors used included diesel fuel, butyl xanthate, sodium butyl black salt, allyl isobutyl thiocarbamate, and N-oxylauroyl-C-phenylarylhydroxamic acid.

[0053] Example

[0054] 500 g of dry lead tailings were taken, mixed with water at a ratio of 1:1 and ground, and then the pulp was transferred to a flotation machine, the pulp concentration was adjusted to 30-45%, and 300 g / t of sodium metabisulfite, 300 g / t of lead nitrate, 4 g / t of diesel, and 20 g / t of butyl xanthate were added in sequence. After the reagents were fully acted on, low-iron sphalerite flotation was started with one coarse and one fine two-sweep to obtain a zinc concentrate with an Fe content of less than 6%, which was recorded as concentrate I, and the obtained tailings were recorded as tailings I; then 300 g / t of sodium dithionite, 300 g / t of copper sulfate, and 20 g / t of allyl isobutyl sulfamide were added to the tailings I in sequence, and after the reagents were fully acted on, medium-iron sphalerite flotation was started with one coarse and two fine two-sweep to obtain a medium-iron zinc concentrate with an Fe content of 6%-12%, which was recorded as concentrate II, and the obtained tailings were recorded as tailings II; then 300g / t of sodium sulfite, 300g / t of ammonium sulfite, and 50g / t of N-oxylauroyl-C-phenylaryl hydroxamic acid were added to the tailings II in sequence. After the reagents were fully reacted, the high-iron sphalerite flotation with one coarse, three fines, and two sweeps was started to obtain a high-iron zinc concentrate with an Fe content of 12% to 18%, which was recorded as concentrate III, and the obtained tailings were recorded as tailings III; then 400g / t of glucomannan, 500g / t of silver chloride, 10g / t of sodium butyrate, 10g / t of allyl isobutyl sulfonate, and 10g / t of N-oxylauroyl-C-phenylaryl hydroxamic acid were added to the tailings III in sequence. After the reagents were fully reacted, the ultra-high iron sphalerite flotation with one coarse, four fines, and three sweeps was started to obtain an ultra-high iron zinc concentrate with an Fe content of more than 18%, which was recorded as concentrate IV. The obtained tailings were the final tailings. The experimental process is as follows: Figure 1 The test results are shown in Table 1.

[0055] Comparative Example

[0056] Take 500g of dry lead tailings, mix them with water at a ratio of 1:1 and grind them. Then transfer the pulp to a flotation machine and adjust the pulp concentration to 30-45%. Then add 3000g / t lime, 1500g / t copper sulfate and 100g / t xanthate in sequence. After the reagents have fully acted, start the roughing operation. The roughing time is 15 minutes. After adding 1000g / t lime to the obtained roughing concentrate, enter the first refining operation. After adding 500g / t lime to the obtained concentrate, the concentrate obtained from the second refining operation is subjected to a blank selection to obtain the final concentrate. The selected middlings are returned to the previous operation in sequence. The roughing tailings undergo three scavenging operations. The first scavenging operation adds 20g / t xanthate, and the next two operations are blank scavenging. The test process is as follows: Figure 2 The test results are shown in Table 1.

[0057] Table 1

[0058]

[0059]

[0060] As can be seen from the test data results obtained in Table 1, the mineral processing method of the present invention has a good separation effect on sphalerite with different iron contents, and can significantly improve the recovery rate of sphalerite. Four types of zinc concentrates with different iron contents can be obtained using the technical solution of the present invention, namely: a low-iron zinc concentrate with a zinc grade of 53.26%, an iron grade of 3.28%, and a sulfur grade of 27.88%; a medium-iron zinc concentrate with a zinc grade of 48.97%, an iron grade of 8.91%, and a sulfur grade of 26.48%; a high-iron zinc concentrate with a zinc grade of 43.25%, an iron grade of 14.67%, and a sulfur grade of 29.90%; and an ultra-high-iron zinc concentrate with a zinc grade of 40.77%, an iron grade of 21.33%, and a sulfur grade of 24.38%. The cumulative zinc recovery rate reaches 94.29%, which is 5.33% higher than that of the traditional zinc flotation process.

[0061] The present invention innovatively uses unconventional collectors, inhibitors and activators such as aromatic hydroxamic acid, glucomannan, sodium dithionite and silver chloride, and cleverly combines several collectors, inhibitors and activators with different properties to selectively activate sphalerite with different iron contents, change the floatation properties of sphalerite with different iron contents, and make sphalerite with different iron contents float out in sequence. This technical route not only reduces the difficulty of separating iron-containing sphalerite from pyrite and improves separation efficiency, but also saves reagent costs and improves the economic and social benefits of mining enterprises.

[0062] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention rather than to limit the same. Although the present invention has been described in detail with reference to the preferred embodiments, those skilled in the art should understand that they can still modify or replace the technical solutions of the present invention with equivalents, and these modifications or equivalent replacements cannot cause the modified technical solutions to deviate from the spirit and scope of the technical solutions of the present invention.

Claims

1. A mineral separation method for marmatite separation, characterized in that: The following steps are involved: S1. Slurry the sulfide ore containing sphalerite to a slurry mass concentration of 30-45%; S2, stirring the slurry obtained in step S1, adding an inhibitor, an activator and a collector in sequence, and starting the first stage of flotation operation after the reagents have fully reacted with the slurry to obtain a low-iron sphalerite concentrate and tailings with an iron content of less than 6%; the inhibitor is sodium metabisulfite, and the amount is 0-500g / t; the activator is lead nitrate, and the amount is 0-500g / t; the collectors are diesel and butyl xanthate, wherein the amount of diesel is 0-10g / t, and the amount of butyl xanthate is 0-30g / t; S3, adding an inhibitor, an activator and a collector to the tailings obtained in step S2, and starting the second flotation operation after the reagents have fully reacted with the slurry to obtain a sphalerite concentrate and tailings with an iron content of 6-12%; the inhibitor is sodium dithionite in an amount of 0-800 g / t; the activator is copper sulfate in an amount of 0-500 g / t; the collector is allyl isobutyl thiocarbamate in an amount of 0-50 g / t; S4, adding an inhibitor, an activator and a collector to the tailings obtained in step S3, and starting the third flotation operation after the reagents have fully reacted with the slurry to obtain a high-iron sphalerite concentrate and tailings with an iron content of 12-18%; the inhibitor is sodium sulfite in an amount of 0-800 g / t; the activator is ammonium sulfite in an amount of 0-800 g / t; the collector is arylhydroxamic acid in an amount of 0-100 g / t, and the structural formula is shown in Formula 1, Formula 1 Among them, R1 and R2 are C n H 2n+2 Alkanes of structure, n≥1; S5. Add an inhibitor, an activator, and a collector to the tailings obtained in step S4, and start the fourth flotation operation after the reagents fully react with the slurry to obtain an ultra-high iron sphalerite concentrate with an iron content of>18% and a final tailings; the inhibitor is glucomannan in an amount of 0-500 g / t; the activator is silver chloride in an amount of 0-800 g / t; the collector is a combination of sodium butyrate, allyl isobutyl thiocarbamate, and aryl hydroxamic acid in an amount of 0-50 g / t, and the structural formula of aryl hydroxamic acid is shown in Formula 1. Formula 1 Among them, R1 and R2 are C n H 2n+2 Alkanes with structure, n≥1.

2. The mineral processing method for separating sphalerite according to claim 1, characterized in that: The glucomannan is a high molecular weight heteropolysaccharide formed by polymerization of glucose and mannose residues in a molecular ratio of 1:1.6-1.7 through β-1,4 glycosidic bonds.

3. The mineral processing method for separating sphalerite according to claim 1, characterized in that: The specific operation of the first stage flotation operation in step S2 is as follows: the rougher concentrate enters the zinc concentration operation, and after one concentration operation, a low-iron sphalerite concentrate with an iron content of less than 6% is obtained, and the tailings of the zinc concentration are returned to the previous operation; the rougher tailings enter the second scavenging operation, the scavenged concentrate is returned to the previous operation, and the scavenged tailings enter the next operation.

4. The mineral processing method for separating sphalerite according to claim 1, characterized in that: The specific operation of the second flotation operation in step S3 is as follows: the rougher concentrate enters the zinc concentration operation, and after two concentration operations, a sphalerite concentrate with an iron content of 6-12% is obtained, and the tailings from the zinc concentration are returned to the previous operation in sequence; the rougher tailings enter two scavenging operations, the scavenged concentrate is returned to the previous operation, and the scavenged tailings enter the next operation.

5. The mineral processing method for separating sphalerite according to claim 1, characterized in that: The specific operation of the third flotation operation in step S4 is as follows: the rougher concentrate enters the zinc concentration operation, and after three concentration operations, a sphalerite concentrate with an iron content of 12-18% is obtained, and the tailings from the zinc concentration are returned to the previous operation in sequence; the rougher tailings enter the second scavenging operation, the scavenged concentrate is returned to the previous operation, and the scavenged tailings enter the next operation.

6. The mineral processing method for separating sphalerite according to claim 1, characterized in that: The specific operation of the fourth stage flotation operation in step S5 is as follows: the rougher concentrate enters the concentrating operation, the concentrate from the nth concentrating enters the n+1th lead concentrating operation, and the tailings from the nth lead concentrating return to the n-1th lead concentrating operation; the tailings from the rougher concentrate enters the scavenging operation, the concentrate from the nth lead scavenging enters the n-1th scavenging operation, and the tailings from the nth lead scavenging enters the n+1th lead scavenging operation, where n is a natural number and is greater than or equal to 3.

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