A method for flotation separation of tungsten ore and iron sulfide ore in tungsten ore heated beneficiation tailings

Abstract

The present invention belongs to the field of flotation, and in particular relates to a method for flotation separation of tungsten ore and iron sulfide ore in tungsten ore heating and concentrating tailings, wherein an activated collector is used to carry out mixed flotation of tungsten ore and iron sulfide ore on the tungsten ore heating and concentrating tailings to obtain a mixed concentrate of tungsten ore and iron sulfide ore; a desorbent is then used to desorb the mixed concentrate of tungsten ore and iron sulfide ore, and an inhibitor and a sulfide ore collector are added to suppress tungsten flotation and iron, thereby obtaining a tungsten concentrate and a sulfide concentrate; the activated collector is at least one of a Pb-hydroxamic acid collector and a C8-C16 alkylamine collector; the inhibitor is a C2-C8 compound containing two or more phosphate groups, or at least one phosphate group and at least one carboxyl group. The present invention provides a new method for recovering tungsten ore heating and concentrating tailings, and the method can effectively separate tungsten and sulfur therein.

Description

Technical Field

[0001] The present invention belongs to the field of flotation, and in particular relates to the field of flotation separation of tailings containing tungsten ore and iron sulfide minerals. Background Art

[0002] Tungsten is a rare and strategic metal, primarily sourced from scheelite (approximately 70%), followed by wolframite. Wolframite and scheelite often coexist, though the proportions vary. Scheelite is the primary tungsten mineral phase, commonly referred to as scheelite. Scheelite is primarily separated from the gangue minerals calcite, fluorite, and quartz by flotation using the "fatty acid + water glass" method. However, the poor selectivity of fatty acids and water glass results in a rough scheelite concentrate with a grade that falls short of product requirements and often contains iron sulfides, primarily pyrite. Therefore, to improve the final grade of the scheelite concentrate, thermal concentrating is often used to further concentrate the rough tungsten concentrate. While thermal concentrating improves the grade of the scheelite concentrate, the large amount of water glass and strong alkali added during the thermal concentrating process suppresses the wolframite, some fine scheelite, and iron sulfides in the rough scheelite concentrate, causing them to enter the scheelite thermal concentrating tailings. This not only results in a significant loss of tungsten resources, but also easily oxidizes the iron sulfides in the tailings, leading to acidic wastewater and heavy metal pollution.

[0003] The traditional method for treating scheelite tailings from heated concentration is gravity separation, which uses shaking tables or disc concentrators to recover as much of the remaining tungsten as possible. However, because the remaining tungsten in the tailings is primarily in the form of fine particles, the recovery efficiency of these gravity separation equipment is very low. Furthermore, the large amount of water glass in the tailings easily causes equipment scaling, severely reducing its service life and efficiency, further compromising the recovery of residual tungsten resources in the tailings. Therefore, the development of new recovery methods to address these issues is urgently needed. Summary of the Invention

[0004] In response to the problems of very low recovery efficiency of tungsten and iron sulfide resources in tungsten ore, such as tungsten ore heated and concentrated tailings, and serious impact of a large amount of residual water glass on recovery equipment, the purpose of the present invention is to provide a method for comprehensively recovering difficult-to-select fine-grained tungsten ore and iron sulfide ore in tungsten ore heated and concentrated tailings, aiming to achieve comprehensive recovery of difficult-to-select tungsten and iron sulfide resources in tungsten ore heated and concentrated tailings.

[0005] A method for flotation separation of tungsten ore and iron sulfide ore in tungsten ore heated and concentrated tailings, wherein an activated collector is used to perform mixed flotation of tungsten ore and iron sulfide ore on the tungsten ore heated and concentrated tailings to obtain a mixed concentrate of tungsten ore and iron sulfide ore;

[0006] Subsequently, a desorbent is used to desorb the mixed concentrate of tungsten ore and iron sulfide ore, and then an inhibitor and a sulfide ore collector are added to suppress tungsten and float iron to obtain tungsten concentrate and iron sulfide concentrate;

[0007] The activated collector is at least one of a Pb-hydroxamic acid collector and a C8-C16 alkylamine collector;

[0008] The inhibitor is a C2-C8 group containing two or more phosphate groups and / or phosphono groups.

[0009] In response to the problems that the tailings of tungsten ore heated and concentrated have small particle size, low grade, high water glass content, and are difficult to effectively float, recover and selectively separate, the present invention breaks away from the conventional separation idea of gravity separation in the industry and innovatively proposes a new idea of tungsten ore-iron sulfide ore mixed flotation-tungsten ore-iron sulfide ore selective flotation separation. It is further found that the innovative use of the activated collector as a collector helps to obtain a mixed ore of tungsten ore-iron sulfide ore with high yield from the difficult-to-select tungsten ore heated and concentrated tailings. Subsequently, through desorption, the combination of the inhibitor and the collector can unexpectedly effectively inhibit the flotation of tungsten without inhibiting the flotation of iron sulfide ore. In this way, the positive flotation of iron sulfide ore and the reverse flotation of tungsten ore can be achieved, thereby achieving high-selective separation of tungsten ore and iron sulfide ore. The technical solution of the present invention provides a new idea of tungsten ore-iron sulfide ore mixed flotation-tungsten ore-iron sulfide ore separation, and based on the control of the process and components, it can recover tungsten ore-iron sulfide ore from the difficult-to-flotation tailings with a high recovery rate and improve the separation selectivity of tungsten ore-iron sulfide ore.

[0010] The tungsten ore is at least one of scheelite and wolframite;

[0011] Preferably, the iron sulfide ore is at least one of pyrite, pyrrhotite and arsenopyrite.

[0012] In the present invention, the pH of the slurry containing the heated beneficiated tungsten ore tailings is controlled in advance at 6 to 11, and then an activated collector is added to carry out mixed floatation of the tungsten ore and the iron sulfide ore.

[0013] Preferably, the concentration of the slurry containing the heated tungsten ore beneficiated tailings is 20-40%, preferably 25-35%.

[0014] The present invention has found that pre-controlling the pH of the slurry and then adding an activated collector can help improve the mixed flotation recovery rate of tungsten ore and iron sulfide ore. On this basis, further combined with the pH control, the mixed flotation recovery rate of tungsten ore and iron sulfide ore in the tungsten ore heated beneficiation tailings can be further synergistically improved. Preferably, in the tungsten ore and iron sulfide ore mixed flotation stage, the pH is 7.5 to 9.5, more preferably 8.5 to 9.5, and even more preferably 9 to 9.2. The study found that under the condition of the activated collector, further controlling the pH within the preferred range can further synergistically improve the mixed flotation recovery rate of tungsten ore and iron sulfide ore in the difficult-to-float tailings.

[0015] In the Pb-hydroxamic acid collector, the hydroxamic acid collector is a collector of formula 1;

[0016]

[0017] Said Ar is phenyl, substituted phenyl, naphthyl or substituted naphthyl;

[0018] The substituent in the substituted phenyl group or substituted naphthyl group is at least one of a C1-C6 alkyl group, an alkoxy group, and a hydroxyl group;

[0019] Preferably, the molar ratio of Pb to hydroxamic acid collector in the Pb-hydroxamic acid collector is 0.2 to 2.5:1; preferably 0.6 to 1.3:1;

[0020] Preferably, the activated collector is at least one of a benzyl lead complex collector and dodecylamine;

[0021] Preferably, in the tungsten ore-iron sulfide ore mixed flotation stage, the amount of activated collector used is 200-800 g / t; preferably 300-700 g / t;

[0022] In the present invention, in order to improve the efficiency of mixed flotation, a foaming agent is added in the tungsten ore-iron sulfide ore mixed flotation stage;

[0023] Preferably, in the tungsten ore-iron sulfide ore mixed flotation stage, the dosage of the foaming agent is 10-15 g / L.

[0024] In the present invention, a desorbent is added to the slurry containing the mixed concentrate to perform a desorption treatment.

[0025] In the present invention, the mixed concentrate is subjected to desorption treatment in advance, which helps to cooperate with the inhibitor and the sulfide ore collector to help synergistically improve the tungsten ore-iron sulfide ore separation selectivity in the tungsten ore-iron sulfide ore composite concentrate.

[0026] Preferably, the desorbent is at least one of sodium carbonate, sodium hydroxide, and lime;

[0027] Preferably, the amount of the desorbent is 400 to 900 g / t; preferably 600 to 800 g / t;

[0028] Preferably, the desorption treatment time is 15 to 30 minutes.

[0029] In the present invention, the concentration of the ore pulp after desorption is controlled to be 50% to 70%, preferably 55% to 65%, and then the inhibitor and sulfide ore collector are added to perform tungsten suppression and iron flotation.

[0030] The inhibitor is at least one of Formula A, Formula B, and Formula C;

[0031]

[0032] Preferably, in the tungsten suppression and iron flotation stage, the amount of the inhibitor is 700-1500 g / t, preferably 900-1200 g / t.

[0033] In the present invention, the sulfide ore collector can be a reagent known in the industry that can be used for the flotation of iron sulfide ores. For example, the sulfide ore collector is a xanthate collector, preferably at least one of ethyl xanthate and butyl xanthate.

[0034] Preferably, the dosage of the xanthate collector is 50-400 g / t; more preferably 100-300 g / t.

[0035] Preferably, the pH value in the tungsten suppression and iron flotation stage is 5-9, more preferably 6-8.

[0036] Preferably, a frother is added in the tungsten suppression and iron flotation stage, with an amount of 5 to 10 g / t.

[0037] The present invention provides a preferred method for comprehensively recovering refractory fine-grained tungsten ore and iron sulfide ore from scheelite heated concentration tailings, comprising the following steps:

[0038] Step (1): Tungsten ore-iron sulfide ore mixed floatation:

[0039] The concentration and pH of the slurry A containing the heated scheelite tailings are adjusted, and then an activated collector is added to perform mixed flotation of the tungsten ore and the iron sulfide ore to obtain a tungsten ore-iron sulfide ore mixed ore;

[0040] The concentration of slurry A is 20-40%, preferably 25-35%;

[0041] The pH is 6 to 11; preferably 7.5 to 9.5;

[0042] The activated collector refers to at least one of a benzyl lead complex collector and dodecylamine, and the amount used is 200 to 800 g / t; preferably, the amount of the activated collector is 300 to 700 g / t;

[0043] The benzoyl lead complex collector refers to a coordination collector of lead nitrate and benzohydroxamic acid, with a mass ratio of lead nitrate to benzohydroxamic acid of 0.2 to 2.5; preferably, the mass ratio of lead nitrate to benzohydroxamic acid is 0.6 to 1.3.

[0044] Step (2): Separation of tungsten ore and iron sulfide ore:

[0045] Add a desorbent to the slurry B containing the mixed tungsten ore and iron sulfide ore for desorption, and control the slurry to be 50% to 70% after desorption, then add an inhibitor and a sulfide ore collector to perform tungsten suppression and iron flotation to obtain tungsten concentrate and sulfide ore concentrate;

[0046] The desorbent is at least one of sodium carbonate, sodium hydroxide, and lime, and the amount used is 400-900 g / t; preferably, the amount of the desorbent is 600-800 g / t;

[0047] After the desorbent is added and stirred for 15 to 30 minutes, the tungsten ore-iron sulfide ore mixed concentrate is concentrated to a concentration of 50% to 70% (preferably 55% to 65%), and then the tungsten ore-iron sulfide ore is separated;

[0048] The inhibitor is at least one of Formula A, Formula B, and Formula C; the dosage is 700-1500 g / t;

[0049] Preferably, the dosage of the inhibitor is 900-1200 g / t;

[0050] The sulfide ore collector is at least one of ethyl xanthate and butyl xanthate, and the dosage is 50-400 g / t, preferably 100-300 g / t;

[0051] The pH of the slurry in the tungsten ore-iron sulfide ore separation stage is 5-9, preferably 6-8.

[0052] Beneficial effects:

[0053] 1. In order to solve the problem that tungsten ore and iron sulfide ore in tungsten ore heated beneficiation tailings are difficult to recover and separate, the present invention provides a tungsten ore and iron sulfide ore mixed flotation and selective separation method for the first time to achieve efficient recovery and separation of tungsten and sulfur in the tailings.

[0054] 2. The present invention innovatively adopts the activated collector to achieve high recovery of tungsten ore and iron sulfide ore from the difficult-to-select tungsten ore heated concentration tailings, and further based on the pre-adjustment of pH and the joint control of pH parameters, it helps to further improve the mixed flotation recovery rate of tungsten ore-iron sulfide ore.

[0055] 3. The present invention pre-desorbs the mixed tungsten ore and iron sulfide ore obtained by mixed flotation, and then adopts the synergistic control of the inhibitor and the sulfide ore collector to achieve selective separation of tungsten ore and iron sulfide ore.

[0056] 4. The present invention creatively proposes a flotation process for mixed flotation of tungsten ore and iron sulfide ore and separation of tungsten ore and iron sulfide ore, breaking through the traditional idea of pre-desulfurization and then flotation of tungsten, and solving the defect of pre-desulfurization process causing large-scale loss of tungsten resources.

[0057] 5. The desorbent and tungsten inhibitor described in the present invention solve the problem that tungsten ore and iron sulfide ore are difficult to separate, resulting in high sulfur content in tungsten concentrate and substandard products. BRIEF DESCRIPTION OF THE DRAWINGS

[0058] Figure 1 The tungsten concentrate (left) and sulfur concentrate (right) obtained by sorting in step 2 of Example 1; DETAILED DESCRIPTION

[0059] The following examples are provided to further illustrate the present invention, but are not intended to limit the scope of protection of the claims of the present invention.

[0060] Example 1

[0061] Step (1):

[0062] The tailings of scheelite from a tungsten concentrator in Hengyang (WO3 grade is 1.2%, of which scheelite accounts for 40%, wolframite accounts for 60%; the iron sulfide ore is mainly pyrite with a content of 3.0%; the pulp concentration is about 15%) were concentrated to a concentration of 30% (mass percentage), the pulp pH was adjusted to 9.0, and then 600g / t of phenylmethyl lead coordination collector (the mass ratio of lead to benzohydroxamic acid is 1:1) was added. After stirring for 5 minutes, 15g / t of 2 # The mixed concentrate of tungsten ore and iron sulfide ore is obtained after one coarse, three fine and one scavenging closed-circuit flotation with oil foaming agent. Among them, 150g / t of benzyl lead coordination collector needs to be added for scavenging, and the concentrating is blank.

[0063] Step (2):

[0064] 650 g / t of sodium hydroxide was added to the obtained tungsten ore-iron sulfide ore mixed concentrate, and the pulp concentration was concentrated to 65% after stirring for 20 minutes. 1000 g / t of formula A was added, and after stirring for 5 minutes, 150 g / t of butyl xanthate and 5 g / t of 2 # The oil foaming agent was added, and the stirring was continued for 3 minutes before aeration flotation. After a coarse and fine open circuit flotation, an iron sulfide ore concentrate with an S grade (i.e., iron sulfide ore) and a recovery rate of 43.78% and 84.35% was obtained. The rougher tailings and the selected middlings were combined into tungsten concentrate (WO3 grade of 17.02% and a recovery rate of 60.94%). The tungsten concentrate and iron sulfide concentrate samples are shown in Figure 1 shown.

[0065] Example 2

[0066] The tailings of scheelite (WO3 grade is 0.8%, of which scheelite accounts for 70%, wolframite accounts for 30%; the iron sulfide ore is mainly pyrite, with a content of 4.8%) from a tungsten concentrator in Luoyang were concentrated to a concentration of 26% (mass percentage), the pH of the pulp was adjusted to 8.5, and then 300g / t of dodecylamine collector was added. After stirring for 5 minutes, a tungsten ore-iron sulfide ore mixed concentrate was obtained after one roughing, three fines and one sweeping closed-circuit flotation. The sweeping process required the addition of 100g / t of dodecylamine collector, and the selection was blank. 600g / t of sodium carbonate was added to the obtained tungsten ore-iron sulfide ore mixed concentrate, and after stirring for 15 minutes, the pulp concentration was concentrated to 55%, 900g / t of formula C was added, and after stirring for 5 minutes, 250g / t of ethyl xanthate and 10g / t of 2 were added. # The oil frother was added, and stirring was continued for 3 minutes before aeration flotation. After coarse and fine open circuit flotation, an iron sulfide ore concentrate with an S grade of 49.39% and a recovery rate of 91.02% was obtained. The rougher tailings and the fine middlings were combined into tungsten concentrate (WO3 grade of 16.75% and recovery rate of 56.38%).

[0067] Example 3

[0068] The tailings of scheelite (WO3 grade of 1.7%, of which scheelite accounts for 25%, wolframite accounts for 70%, and tungsten ore accounts for 5%; the iron sulfide ore is mainly pyrite with a content of 3.6%) from a tungsten concentrator in Jiujiang were concentrated to a concentration of 32% (mass percentage), the pH of the slurry was adjusted to 9.2, and then 700g / t of benzyl lead coordination collector (the mass ratio of lead to benzohydroxamic acid is 0.7:1) was added. After stirring for 5 minutes, a tungsten ore-iron sulfide ore mixed concentrate was obtained after one roughing, three finishing and one scavenging closed-circuit flotation. Among them, 300g / t of benzyl lead coordination collector needs to be added for scavenging, and the concentrating is blank. 800g / t of lime was added to the obtained tungsten ore-iron sulfide ore mixed concentrate, and the pulp concentration was concentrated to 60% after stirring for 15 minutes. 1000g / t of formula B was added, and after stirring for 5 minutes, 200g / t of ethyl xanthate and 10g / t of 2 # The oil frother was added, and stirring was continued for 3 minutes before aeration flotation. After one coarse and one fine open circuit flotation, an iron sulfide ore concentrate with an S grade and a recovery rate of 45.60% and 88.32% was obtained. The rougher tailings and the fine middlings were combined into tungsten concentrate (WO3 grade was 20.95%, and the recovery rate was 69.03%).

[0069] Example 4

[0070] Compared with Example 1, the only difference is that the pH of step (1) is changed. The parameters and results are shown in Table 1.

[0071] Table 1 Flotation recovery of tungsten concentrate and iron sulfide concentrate at different pH

[0072]

[0073] Comparing the results in Table 1 and Example 1, it can be seen that the activated collector has good selective collection ability for tungsten ore and iron sulfide ore in a wide pH range. However, the optimal pH for tungsten ore-iron sulfide ore mixed floatation is 6-11; more preferably 7.5-9.5.

[0074] Example 5

[0075] Compared with Example 1, the only difference is that in step 1, a phenylmethyl lead coordination collector is added to the ore pulp in advance, and then the pH of the ore pulp is controlled to 9.0. Other operations and parameters are the same as in Example 1.

[0076] The grade and recovery rate of the tungsten concentrate obtained by flotation were 16.15% and 53.94%, respectively, and the grade and recovery rate of the iron sulfide ore concentrate were 40.19% and 79.45%, respectively. Compared with the results of Example 1, it can be seen that the method of adding the activated collector first and then adjusting the pH results in a decrease in the capture and selectivity of the activated collector for tungsten and sulfur.

[0077] Example 6

[0078] Except for reducing the dosage of Formula C in Example 2 to 500 g / t, all other aspects were consistent with Example 2. The grade and recovery rate of the tungsten concentrate obtained by flotation were 12.33% and 42.18%, respectively, while the grade and recovery rate of the iron sulfide concentrate were 43.65% and 94.37%, respectively. Comparing the results of Example 2, it can be seen that reducing the dosage of tungsten inhibitor will lead to a significant decrease in the grade and recovery rate of the tungsten concentrate, especially the recovery rate; the recovery rate of the iron sulfide concentrate slightly increased, but the grade decreased. These results indicate that reducing the dosage of tungsten inhibitor will worsen the tungsten ore-iron sulfide ore separation effect. Therefore, the dosage of tungsten inhibitor is a relatively critical factor.

[0079] Comparative Example 1

[0080] Except for replacing the benzyl lead coordination collector in Example 3 with the anionic collector sodium oleate, all other aspects were consistent with Example 3. The tungsten concentrate grade and recovery rate obtained by flotation were 7.89% and 35.20%, respectively, and the grade and recovery rate of the iron sulfide concentrate were 21.34% and 62.15%, respectively. Comparing the results of Example 3, it can be seen that the use of other collectors will lead to a significant decrease in the grade and recovery rate of the tungsten concentrate and the iron sulfide concentrate, that is, the tungsten and sulfur minerals cannot be effectively recovered. These results indicate that the recovery of tungsten and sulfur from scheelite thermal concentrator tailings requires a selected collector.

[0081] Comparative Example 2

[0082] Except for replacing the depressant of Formula B in Example 3 with carboxymethyl cellulose, all other procedures were consistent with Example 3. The tungsten concentrate grade and recovery rate obtained by flotation were 12.04% and 53.16%, respectively, while the grade and recovery rate of the iron sulfide concentrate were 30.15% and 80.33%, respectively. Comparison with the results of Example 3 shows that the use of other depressants will lead to poor tungsten-iron sulfide ore separation, resulting in relatively low grades for both the tungsten concentrate and the iron sulfide concentrate. These results demonstrate that the recovery of tungsten and sulfur from scheelite thermal concentrator tailings requires selective depressants.

Claims

1. A method for flotation separation of tungsten ore and iron sulfide ore in tungsten ore tailings by heating and concentrating, characterized in that: The activated collector is used to carry out mixed flotation of tungsten ore and iron sulfide ore on the tailings of tungsten ore after heating and concentration, so as to obtain a mixed concentrate of tungsten ore and iron sulfide ore; Subsequently, a desorbent is used to desorb the mixed concentrate of tungsten ore and iron sulfide ore, and then an inhibitor and a sulfide ore collector are added to suppress tungsten and float iron to obtain tungsten concentrate and iron sulfide concentrate; The activated collector is at least one of a coordinated collector and an alkylamine collector; wherein the coordinated collector is a coordinated collector of a Pb-hydroxamic acid collector, and the alkylamine collector is C8~C 16 Alkylamine collector; The inhibitor is a C2-C8 group containing two or more phosphate groups and / or phosphono groups.

2. The method according to claim 1, wherein The tungsten ore is at least one of scheelite and wolframite.

3. The method according to claim 1, wherein The iron sulfide ore is at least one of pyrite, pyrrhotite and arsenopyrite.

4. The method according to claim 1, wherein The pH of the slurry containing the heated tungsten ore tailings is controlled in advance at 6-11, and then an activated collector is added to carry out tungsten ore-iron sulfide ore mixed floatation.

5. The method according to claim 4, wherein The concentration of the slurry containing the heated tungsten ore tailings is 20~40%.

6. The method according to claim 4, wherein The concentration of the slurry containing the heated tungsten ore tailings is 25~35%.

7. The method according to claim 4, wherein The pH of the slurry is 7.5~9.

5.

8. The method according to claim 1, wherein In the Pb-hydroxamic acid collector, the hydroxamic acid collector is a collector of formula 1; Formula 1 Said Ar is phenyl, substituted phenyl, naphthyl or substituted naphthyl; The substituent in the substituted phenyl group and the substituted naphthyl group is at least one of a C1-C6 alkyl group, an alkoxy group, and a hydroxyl group.

9. The method according to claim 8, wherein The molar ratio of Pb to hydroxamic acid collector in the Pb-hydroxamic acid collector is 0.2~2.5:

1.

10. The method according to claim 9, wherein The molar ratio of Pb to hydroxamic acid collector in the Pb-hydroxamic acid collector is 0.6~1.3:

1.

11. The method according to claim 1, wherein The activated collector is at least one of a benzyl lead complex collector and dodecylamine.

12. The method according to claim 1, wherein In the tungsten ore-iron sulfide ore mixed flotation stage, the dosage of activated collector is 200~800 g / t.

13. The method according to claim 12, wherein: In the tungsten ore-iron sulfide ore mixed flotation stage, the dosage of activated collector is 300~700 g / t.

14. The method according to claim 1, wherein A frother is also added during the tungsten ore-iron sulfide ore mixed flotation stage.

15. The method according to claim 14, wherein In the tungsten ore-iron sulfide ore mixed flotation stage, the dosage of the foaming agent is 10~15g / L.

16. The method according to claim 1, wherein A desorbent is added to the slurry containing the mixed concentrate to perform a desorption treatment.

17. The method according to claim 16, wherein The desorbent is at least one of sodium carbonate, sodium hydroxide and lime.

18. The method according to claim 16, wherein The dosage of desorbent is 400~900 g / t.

19. The method according to claim 16, wherein The dosage of desorbent is 600~800 g / t.

20. The method of claim 16, wherein: The desorption treatment time is 15~30min.

21. The method according to any one of claims 16 to 20, wherein: The concentration of the ore pulp after desorption is controlled to be 50% to 70%, and then the inhibitor and sulfide ore collector are added to perform tungsten suppression and iron flotation.

22. The method of claim 1, wherein The inhibitor is at least one of Formula A, Formula B, and Formula C; Formula A Formula B Formula C.

23. The method according to claim 22, wherein In the tungsten suppression and iron flotation stage, the dosage of the inhibitor is 700~1500 g / t.

24. The method according to claim 23, wherein In the tungsten suppression and iron flotation stage, the dosage of the inhibitor is 900~1200 g / t.

25. The method of claim 1, wherein The sulfide ore collector is a xanthate collector.

26. The method of claim 25, wherein: The sulfide ore collector is at least one of ethyl xanthate and butyl xanthate.

27. The method of claim 25, wherein: The dosage of xanthate collector is 50~400 g / t.

28. The method of claim 25, wherein: The dosage of xanthate collector is 100~300 g / t.

29. The method of claim 1, wherein The pH value of the tungsten suppression and iron flotation stage is 5~9.

30. The method of claim 29, wherein: The pH value of the tungsten suppression and iron flotation stage is 6~8.

31. The method of claim 1, wherein A frother is also added in the tungsten suppression and iron flotation stage, with a dosage of 5~10 g / t.

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