A high-sulfur white tungsten coarse concentrate lime sulfur suppression-regrinding drug removal-normal temperature cleaning method

Abstract

The application discloses a high-sulfur white tungsten rough concentrate lime sulfur suppression-regrinding drug removal-normal temperature cleaning method and belongs to the technical field of mineral processing. The method is characterized in that high-concentration lime is added to high-sulfur white tungsten rough concentrate for desulfurization flotation to obtain white tungsten concentrate; the white tungsten concentrate is subjected to drug removal treatment and then normal temperature cleaning to obtain white tungsten concentrate; the method utilizes the high-concentration lime to strengthen the inhibition of pyrite and other sulfide minerals to realize effective separation of the white tungsten ore and the sulfide minerals, and on this basis, regrinding is utilized to promote the desorption of the mineral surface residual fatty acid collector, and after the reaction with calcium ions, the concentrated discharge slurry is discharged, so that efficient drug removal is realized, which is favorable for the subsequent white tungsten ore normal temperature cleaning process. The method avoids the problems of high energy consumption and complex process of the traditional heating cleaning process, has the advantages of simple process, stable reagent system, low energy consumption and the like, and has a good industrial application prospect.

Description

Technical Field

[0001] This invention relates to a mineral processing method, and more particularly to a method for lime-sulfur suppression-re-refining-room-temperature beneficiation of high-sulfur scheelite rough concentrate, belonging to the field of mineral processing technology. Background Technology

[0002] Scheelite (CaWO4) is an important tungsten resource mineral, playing a crucial role in tungsten resource development and utilization. However, because scheelite resources are often associated with sulfide minerals and calcium-bearing gangue minerals, its complex mineral composition and close intergrowth make flotation separation difficult. Especially in molybdenum-tungsten associated deposits, sulfide minerals such as pyrite tend to accumulate in the rough concentrate during scheelite flotation, resulting in high sulfur content in the rough concentrate and negatively impacting subsequent beneficiation and concentrate quality.

[0003] Currently, the main industrial method for recovering scheelite is the fatty acid-based collector flotation process, with a typical flow being "roughing-heated cleaning." In the roughing stage, fatty acid-based collectors are used to recover scheelite, while the cleaning stage typically employs high temperature, high concentration, large amounts of water glass, and prolonged stirring to achieve selective separation between scheelite and calcareous gangue minerals. In traditional heated cleaning, the pulp temperature is usually 75–90℃, the pulp concentration is 55–75%, and a large amount of water glass is added for pulp conditioning. Simultaneously, the pulp is kept at a constant temperature and stirred for 30–60 minutes. The main purpose is to enhance the desorption of fatty acid-based collectors from the surface of calcareous gangue minerals such as calcite and fluorite. Since the collectors adsorbed on the surface of scheelite are relatively stable, flotation separation between scheelite and gangue minerals is achieved. Although this process is widely used in industrial production, it suffers from high energy consumption, a long process, and stringent operating conditions. Especially for high-sulfur scheelite rough concentrate, sulfide minerals such as pyrite are prone to entering the scheelite concentrate product during the heating and beneficiation process, leading to an increase in the sulfur content of the concentrate and an adverse effect on the grade of the concentrate.

[0004] In addition, traditional heating and refining processes usually require long-term heat preservation and stirring under high temperature and high concentration conditions, which not only consumes a lot of energy, but also has high requirements for equipment and on-site operating conditions. Summary of the Invention

[0005] To address the technical problems of traditional scheelite heating and beneficiation processes, such as complex processes, high energy consumption, and difficulties in beneficiating high-sulfur scheelite rough concentrates, the present invention aims to provide a lime-based sulfur suppression-re-removal-room-temperature beneficiation method for high-sulfur scheelite rough concentrates. This method utilizes the high-alkali and high-calcium conditions provided by lime to regulate the flotation behavior of scheelite and sulfide minerals, effectively suppressing sulfide minerals such as pyrite and preferentially flotating scheelite. Re-removal through regrinding and washing avoids the influence of aliphatic collectors on subsequent beneficiation processes, and achieves efficient separation of scheelite at room temperature, thereby reducing process energy consumption and simplifying the process structure.

[0006] To achieve the above-mentioned technical objectives, the present invention provides a method for high-sulfur scheelite rough concentrate with lime desulfurization-re-grinding and de-refining-room-temperature purification, the method comprising the following steps:

[0007] 1) Add lime to high-sulfur scheelite rough concentrate at a rate of 10,000–100,000 g / t for desulfurization flotation. The frothy product is scheelite concentrate. ;

[0008] 2) Calcium tungsten concentrate The slurry is then de-treated to obtain a de-treated slurry.

[0009] 3) The de-refined slurry is then subjected to ambient temperature cleaning using flotation reagents including scheelite collectors and composite depressants to obtain scheelite concentrate. ;

[0010] The composite inhibitor includes aluminum sulfate and an auxiliary inhibitor;

[0011] The scheelite collector is a hydroxamic acid collector or a hydroxamic acid collector-lead salt complex.

[0012] Because high-sulfur scheelite rough concentrates contain high levels of sulfide minerals such as pyrite and have a high amount of residual fatty acid collectors, and because traditional heated beneficiation methods for high-sulfur scheelite rough concentrates allow sulfide minerals to easily enter the scheelite concentrate product, thus affecting the concentrate grade; furthermore, residual fatty acid collectors increase the complexity of the pulp system, which is detrimental to the selective separation of scheelite from calcium-bearing gangue minerals. Therefore, high-sulfur scheelite rough concentrates are generally difficult to be effectively beneficiated under normal temperature conditions. The key to this invention lies in using lime to create a high-alkalinity, high-calcium-ion-concentration flotation environment for high-sulfur scheelite rough concentrate. This effectively inhibits sulfide minerals such as pyrite, while scheelite maintains a certain degree of hydrophobicity thanks to the residual fatty acid collectors from the roughing stage. This allows the scheelite to continue into the froth product after flotation, thus achieving effective separation of scheelite from sulfide minerals. Furthermore, the high alkalinity and high calcium-ion concentration of the pulp system promotes the desorption of residual fatty acid collectors from the mineral surface into the pulp during subsequent de-reagent processing, under mechanical grinding and scrubbing or high-speed stirring. The desorbed residual fatty acid collectors react with calcium ions in the pulp, and the reaction products are discharged with the concentrate overflow, reducing the impact of residual collectors on subsequent cleaning processes. Finally, under ambient temperature conditions, a composite inhibitor system and a metal complex collector system are used for selective flotation of scheelite, achieving effective separation between scheelite and calcium-bearing gangue minerals, thereby obtaining high-grade scheelite concentrate. In summary, this invention achieves efficient separation of high-sulfur scheelite rough concentrate under ambient temperature conditions through lime-suppressed flotation and subsequent de-drug treatment, solving the technical problems of high energy consumption, complex process, and difficulty in the beneficiation of high-sulfur scheelite rough concentrate in traditional heated beneficiation processes.

[0013] As a preferred embodiment, the high-sulfur scheelite rough concentrate contains scheelite coexisting with metallic sulfide minerals, and the minerals contain residual fatty acid collectors. Metallic sulfides include, for example, pyrite. Fatty acid collectors are the main collectors used in scheelite recovery, such as sodium oleate. The main minerals in the high-sulfur scheelite rough concentrate include scheelite, metallic sulfide minerals, and calcium-bearing gangue minerals; wherein the metallic sulfide minerals include at least one of pyrite and pyrrhotite; and the calcium-bearing gangue minerals include at least one of fluorite, calcite, and dolomite.

[0014] As a preferred embodiment, the lime is added at a rate of 30,000–80,000 g / t. The amount of lime has a significant impact on the separation effect between scheelite and metallic sulfide minerals. With increasing lime dosage, the inhibitory effect on metallic sulfide minerals such as pyrite gradually strengthens, and more sulfide minerals are inhibited from entering the tailings system, thus achieving effective separation of scheelite and sulfide minerals. However, with increasing lime dosage, the WO3 recovery rate of tungsten concentrate gradually decreases. When the lime dosage is low, the surface of scheelite still retains a strong residual fatty acid collector effect, thus allowing scheelite to fully enter the foam product. With further increases in lime dosage, the high-alkali environment and large amounts of Ca... 2+ The residual hydrophobicity on the surface of scheelite will gradually weaken, thus inhibiting some scheelite formation and reducing the WO3 recovery rate. Therefore, the lime is further preferably added at a rate of 40,000–50,000 g / t, which ensures both the separation efficiency of the metal sulfide ore and the tungsten recovery rate.

[0015] As a preferred embodiment, the decanting treatment includes regrinding and concentration. Regrinding can be replaced by common decanting methods such as high-speed stirring and scrubbing. Concentration can be replaced by other solid-liquid separation methods, but regrinding and concentration are the most effective. Regrinding promotes the desorption of fatty acid collectors adsorbed on the mineral surface, while calcium ions in the lime system react with residual fatty acid collectors in the slurry. Concentration removes the removed collectors from the slurry system.

[0016] As a preferred embodiment, the hydroxamic acid collector-lead salt complex is composed of a hydroxamic acid collector and a lead salt at a mass ratio of 0.5 to 2:1. The lead salt primarily provides lead ions, such as lead nitrate. The lead ions mainly act as activators, and their combination with the hydroxamic acid collector can improve the collection effect of a single hydroxamic acid collector on scheelite. More preferably, the hydroxamic acid collector and the lead salt are premixed before being added to the slurry to form a hydroxamic acid-lead complex collector.

[0017] As a preferred embodiment, the hydroxamic acid collector includes at least one of benzohydroxyxamic acid, alkylhydroxyxamic acid, and salicylic acid.

[0018] As a preferred embodiment, the composite inhibitor is composed of aluminum sulfate and an auxiliary inhibitor in a mass ratio of 1:(1~3). The combined use of aluminum sulfate and the auxiliary inhibitor, through their synergistic effect, inhibits the flotation of calcium-bearing gangue minerals such as fluorite and calcite in the scheelite flotation system, thereby improving the flotation selectivity of scheelite.

[0019] As a preferred embodiment, the auxiliary inhibitor includes at least one of water glass, sodium hexametaphosphate, and starch.

[0020] As a preferred option, the ambient temperature selection temperature is 10–35°C.

[0021] As a preferred embodiment, the ambient temperature cleaning process includes one roughing stage, two to four cleaning stages, and one to two scavenging stages. Specifically, in the roughing stage, hydroxamic acid collectors and lead salts are added for flotation; in the cleaning stage, the concentrate grade is improved by adjusting the amount of depressant; and in the scavenging stage, a small amount of collector is added to improve the recovery rate of scheelite, thereby achieving efficient enrichment of scheelite.

[0022] As a preferred embodiment, the reagent formulation for the rough selection is as follows: sodium carbonate 1000-3000 g / t, hydroxamic acid collector-lead salt complex 1000-4000 g / t, compound inhibitor 2000-5000 g / t, and foaming agent 10-50 g / t.

[0023] The selected pharmaceutical regimen:

[0024] Selected ingredients: Hydroxyxamic acid collectors 600-1000 g / t, compound inhibitors 800-3000 g / t.

[0025] For two or more rounds of selection, the dosage of medicine should be halved for each level of selection compared to one round.

[0026] The aforementioned drug formulation:

[0027] One scavenging step using hydroxamic acid collectors: 300–1000 g / t.

[0028] For two or more sweeps, the amount of reagent used should be halved for each sweep compared to a single sweep.

[0029] Compared with the prior art, the present invention has the following beneficial effects:

[0030] (1) The present invention achieves the fine flotation of high sulfur scheelite rough concentrate under normal temperature conditions, avoiding the high energy consumption problem caused by high temperature heating, high concentration slurry adjustment and long-term heat preservation and stirring in the traditional heating fine process, thereby significantly reducing production energy consumption and simplifying the mineral processing process, while reducing the investment and operating costs of heating equipment.

[0031] (2) This invention utilizes the differential regulation effect of lime on the flotation behavior of scheelite and sulfide minerals under high alkaline conditions to effectively suppress sulfide minerals such as pyrite, so that they mainly enter the tailings, while scheelite continues to enter the foam product, thereby effectively reducing the probability of sulfide minerals entering scheelite concentrate in the subsequent beneficiation process and improving the quality of scheelite concentrate.

[0032] (3) The present invention promotes the desorption of residual fatty acid collectors on the mineral surface by re-grinding and washing, and utilizes the calcium ions in the lime system to react with the residual fatty acid collectors, and discharges the reaction products with the concentration overflow, thereby reducing the impact of residual collectors in the slurry on the subsequent beneficiation process.

[0033] (4) In the process of room temperature scheelite beneficiation, the present invention adopts a composite inhibitor system and a metal complex collector system. The synergistic effect of aluminum sulfate and auxiliary inhibitors inhibits calcium-containing gangue minerals such as fluorite and calcite. At the same time, the metal complex formed by the hydroxamic acid collector and lead salt is used to selectively collect scheelite, thereby improving the flotation separation effect between scheelite and gangue minerals.

[0034] (5) The present invention, through the process flow design of “lime-sulfur-suppressing flotation-re-grinding and de-removal-room-temperature scheelite beneficiation”, achieves stable separation of high-sulfur scheelite rough concentrate under room temperature conditions on the basis of reducing the interference of sulfide minerals and the influence of residual collectors, which can effectively improve the grade and recovery rate of scheelite concentrate.

[0035] (6) The process flow of the present invention is reasonable, the operating conditions are mild and the reagent system is stable. It is suitable for the flotation and upgrading of high-sulfur scheelite rough concentrate and has good industrial adaptability and application prospects.

[0036] In summary, this invention achieves efficient separation of high-sulfur scheelite rough concentrate under ambient temperature conditions through a process design of "lime-suppressed flotation—re-grinding and de-reagenting—room temperature scheelite beneficiation". Attached Figure Description

[0037] Figure 1 This is a flowchart of the desulfurization flotation test for high-sulfur scheelite rough concentrate in Example 1.

[0038] Figure 2 This is a flowchart of the ambient temperature beneficiation test of scheelite rough and concentrate at a tungsten mine in Xinjiang in Example 2. Detailed Implementation

[0039] To enable those skilled in the art to better understand the technical solutions of the present invention, the following specific embodiments are intended to further illustrate the content of the present invention, rather than to limit the scope of protection of the claims.

[0040] Example 1

[0041] This study focuses on a high-sulfur scheelite rough concentrate produced by a molybdenum-tungsten mine in Henan Province. The rough concentrate has a WO3 grade of 1.158% and a sulfur grade of 2.157%. This rough concentrate originates from the scheelite roughing concentrate produced by the beneficiation plant: after crushing and grinding, kerosene and ethyl thiocyanate are used as the main flotation reagents to preferentially recover molybdenum minerals. The resulting molybdenum flotation tailings are then fed into the subsequent scheelite roughing process. Sodium carbonate is used to adjust the pulp pH, water glass is used as a gangue depressant, and fatty acid collectors are used as scheelite collectors. Because no dedicated desulfurization process is implemented after molybdenum flotation, residual pyrite and other sulfide minerals in the molybdenum tailings directly enter the scheelite roughing process and float to the surface along with the scheelite, ultimately forming a high-sulfur scheelite rough concentrate. Furthermore, the slurry contains residual fatty acid collectors added during the scheelite roughing stage, which has a certain impact on subsequent desulfurization flotation. Therefore, subsequent sulfur suppression, descaling, and ambient temperature beneficiation tests were carried out using this high-sulfur scheelite rough concentrate as raw material.

[0042] For the desulfurization flotation process, please refer to [link / reference]. Figure 1 Lime was added to high-sulfur scheelite rough concentrate at dosages of 0, 20, 30, 40, 50, and 60 kg / t, with the 0 kg / t group serving as a control group without lime addition. All other operating conditions remained consistent. After adding lime, the mixture was stirred for 5 minutes to create a highly alkaline calcium ion environment in the slurry, thereby enhancing the inhibition of sulfide minerals such as pyrite. Subsequently, flotation was performed directly, allowing the scheelite to continue floating to the top and enter the froth product, while the inhibited sulfide minerals mainly entered the tailings, thus achieving effective separation of scheelite and sulfide minerals.

[0043] To investigate the effect of lime dosage on the separation of scheelite and sulfide minerals, a batch of high-sulfur scheelite rough concentrate was used as the test sample. After slurry preparation, different amounts of lime were added for sulfur suppression flotation tests. No additional sulfide mineral collectors were added during the flotation process. Under the same flotation conditions, the effects of different lime dosages on the flotation behavior of scheelite and the inhibition effect on sulfide minerals were investigated, with the WO3 recovery rate and sulfur content of the froth product used as evaluation indicators. Higher WO3 recovery rate and lower sulfur content in the froth product indicate a better separation effect of lime on scheelite and sulfide minerals.

[0044] Multiple gradients were set for lime dosage; the experimental procedure is as follows. Figure 1 The experimental results are shown in Table 1.

[0045] Table 1. Results of the test on the dosage of sulfur-suppressing lime for scheelite rough concentrate.

[0046]

[0047] The results in the table show that the amount of lime used has a significant impact on the separation effect of scheelite and sulfide minerals. As the amount of lime used increases, the overall S recovery rate of the concentrate gradually decreases, indicating that under high alkaline conditions, the inhibitory effect of lime on sulfide minerals such as pyrite gradually increases, and more sulfide minerals are inhibited from entering the tailings system, thus achieving effective separation of scheelite and sulfide minerals.

[0048] Meanwhile, the WO3 recovery rate of tungsten concentrate gradually decreased with increasing lime dosage. When the lime dosage was low, the surface of scheelite still retained a strong residual fatty acid collector effect, thus allowing the scheelite to fully enter the foam product; however, with further increases in lime dosage, the high-alkali environment and large amounts of Ca... 2+ This will gradually weaken the residual hydrophobicity on the surface of scheelite, thereby inhibiting some scheelite and reducing the WO3 recovery rate.

[0049] Furthermore, the yield of tungsten concentrate showed a significant decreasing trend with increasing lime dosage. When the lime dosage increased from 20 kg / t to 40 kg / t, the sulfur recovery rate of the concentrate decreased significantly, indicating that at this stage, lime mainly enhanced the inhibitory effect on sulfide minerals, while having a relatively limited impact on scheelite flotation. When the lime dosage continued to increase to 50–60 kg / t, both the yield of tungsten concentrate and the WO3 recovery rate decreased significantly, indicating that excessive lime would inhibit scheelite flotation to a certain extent, thereby increasing scheelite loss.

[0050] A comprehensive comparison shows that when the lime dosage is 40 kg / t, the WO3 recovery rate of tungsten concentrate still reaches 98.11%, while the S recovery rate of concentrate is only 14.54%. This indicates that under these conditions, sulfide minerals can be effectively suppressed while ensuring high recovery of scheelite. Therefore, 40 kg / t is a suitable lime dosage.

[0051] Example 2

[0052] A room-temperature beneficiation test of scheelite rough and concentrate at a tungsten mine in Xinjiang:

[0053] Taking scheelite rough concentrate from a tungsten mine in Xinjiang as the research object, a flotation test was conducted on the high-sulfur scheelite rough concentrate using lime desulfurization, regrinding and deretting, and room-temperature cleaning. The main minerals in this rough concentrate include scheelite, pyrite, and calcium-bearing gangue minerals such as fluorite and calcite, with pyrite being the primary sulfide mineral. The raw material has a WO3 grade of approximately 1.15% and a high sulfur content. If direct room-temperature cleaning is performed, sulfide minerals will easily enter the scheelite concentrate product, and the calcium-bearing gangue minerals will also affect the scheelite cleaning effect, making it difficult to obtain a high-grade scheelite concentrate. Therefore, this embodiment uses a combined process of lime desulfurization flotation, regrinding and deretting, and room-temperature scheelite cleaning to upgrade the high-sulfur scheelite rough concentrate. The experimental process is described below. Figure 2 .

[0054] (1) Lime-based sulfur-suppressing flotation

[0055] First, lime is added to the above-mentioned high-sulfur scheelite rough concentrate as a sulfide mineral inhibitor at a dosage of 40,000 g / t. The slurry is prepared for approximately 5 minutes to create a highly alkaline calcium ion environment, thereby enhancing the inhibition of sulfide minerals such as pyrite. Under these conditions, sulfide minerals such as pyrite are effectively inhibited and mainly enter the tailings, while scheelite, relying on residual fatty acid collectors from the roughing stage, maintains a certain degree of hydrophobicity and continues to enter the froth product, achieving effective separation of scheelite and sulfide minerals.

[0056] (2) Re-grinding and drug removal treatment

[0057] The foam product obtained in step (1) is subjected to regrinding and de-agent treatment. First, the slurry is stirred by regrinding and scrubbing to desorb the fatty acid collectors adsorbed on the mineral surface; at the same time, the Ca in the lime system is utilized. 2+ It reacts with residual fatty acid collectors in the slurry, and then the desorbed and reacted reagents are discharged from the slurry system through a concentration operation, thereby reducing the content of residual collectors in the slurry and creating favorable conditions for subsequent room temperature scheelite beneficiation.

[0058] (3) Room temperature scheelite selection

[0059] The slurry after regrinding and de-refining was subjected to ambient temperature scheelite beneficiation. In the roughing stage, sodium carbonate was first added as a pH adjuster at a dosage of 2000 g / t; subsequently, a composite inhibitor formed by a pre-mixed mixture of aluminum sulfate and water glass was added, with aluminum sulfate at a dosage of 1500 g / t and water glass at a dosage of 3000 g / t; then, a metal complex collector system formed by a pre-mixed mixture of lead nitrate and benzohydroxyxamic acid was added, with lead nitrate at a dosage of 2000 g / t and benzohydroxyxamic acid at a dosage of 2000 g / t, and 2... # Oil was used as a foaming agent at a dosage of 20g / t, followed by roughing of scheelite.

[0060] The scheelite roughing concentrate undergoes three cleaning processes. In the first cleaning, 1000 g / t of aluminum sulfate, 2000 g / t of water glass, and 800 g / t of benzohydroxyxamic acid are added. In the second and third cleaning processes, the reagent dosages are halved each time. The scheelite roughing tailings undergo a scavenging operation, with 500 g / t of benzohydroxyxamic acid added to improve scheelite recovery. Using the above flotation process (1 roughing, 3 cleaning, 1 scavenging), the final scheelite concentrate product is obtained.

[0061] Under the above flotation conditions, the final scheelite concentrate obtained had a WO3 grade of 25.84%, and the refining recovery rate was 94.86%. Simultaneously, the sulfur content in the concentrate was significantly reduced. The experimental results demonstrate that the method described in this invention can effectively separate high-sulfur scheelite rough concentrate without heating, and obtain scheelite concentrate with high grade and recovery rate.

Claims

1. A method for sulfur suppression, regrinding, and room-temperature refining of high-sulfur scheelite rough concentrate, characterized in that: Includes the following steps: 1) Add lime to high-sulfur scheelite rough concentrate at a rate of 10,000–100,000 g / t for desulfurization flotation. The frothy product is scheelite concentrate. ; 2) Calcium tungsten concentrate The slurry is then de-treated to obtain a de-treated slurry. 3) The de-refined slurry is then subjected to ambient temperature cleaning using flotation reagents including scheelite collectors and composite depressants to obtain scheelite concentrate. ; The composite inhibitor includes aluminum sulfate and an auxiliary inhibitor; The scheelite collector is a hydroxamic acid collector or a hydroxamic acid collector-lead salt complex.

2. The method for high-sulfur scheelite rough concentrate with lime desulfurization-re-grinding and room-temperature refining according to claim 1, characterized in that: The high-sulfur scheelite rough concentrate contains scheelite coexisting with metallic sulfide minerals, and the minerals contain residual fatty acid collectors.

3. The method for high-sulfur scheelite rough concentrate with lime desulfurization-re-grinding and room-temperature refining according to claim 1, characterized in that: The lime is added at a rate of 30,000 to 80,000 g / t.

4. The method for high-sulfur scheelite rough concentrate with lime desulfurization-re-grinding and room-temperature refining according to claim 1, characterized in that: The de-drug treatment includes regrinding and concentration.

5. The method for high-sulfur scheelite rough concentrate with lime desulfurization-re-grinding and room-temperature refining according to claim 1, characterized in that: The hydroxamic acid collector-lead salt complex is composed of a hydroxamic acid collector and a lead salt in a mass ratio of 0.5 to 2:

1. The hydroxamic acid collectors include at least one of benzohydroxyxamic acid, alkylhydroxyxamic acid, and salicylic acid.

6. The method for high-sulfur scheelite rough concentrate with lime desulfurization-re-grinding and room-temperature refining according to claim 1, characterized in that: The composite inhibitor is composed of aluminum sulfate and an auxiliary inhibitor in a mass ratio of 1:(1~3).

7. The method for high-sulfur scheelite rough concentrate with lime desulfurization-re-grinding and room-temperature refining according to claim 6, characterized in that: The auxiliary inhibitors include at least one of water glass, sodium hexametaphosphate, and starch.

8. The method for high-sulfur scheelite rough concentrate with lime desulfurization-re-grinding and room-temperature refining according to claim 1, characterized in that: The selected room temperature range is 10–35°C.

9. A method for high-sulfur scheelite rough concentrate with lime desulfurization-re-grinding and room-temperature refining according to any one of claims 1 to 8, characterized in that: The ambient temperature selection process includes one coarse selection, two to four fine selections, and one to two sweeping selections.

10. The method for high-sulfur scheelite rough concentrate with lime desulfurization-re-grinding and room-temperature refining according to claim 1, characterized in that: The reagent regimen for the roughing process is as follows: sodium carbonate 1000-3000 g / t, hydroxamic acid collector-lead salt complex 1000-4000 g / t, compound inhibitor 2000-5000 g / t, and foaming agent 10-50 g / t. The selected pharmaceutical regimen: Selected ingredients: Hydroxyxamic acid collectors 600-1000 g / t, compound inhibitors 800-3000 g / t. For two or more rounds of selection, the dosage of medicine should be halved for each level of selection compared to one round. The aforementioned drug formulation: One scavenging step using hydroxamic acid collectors: 300–1000 g / t. For two or more sweeps, the amount of reagent used should be halved for each sweep compared to a single sweep.

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