A method for ultra-stable foam separation and flotation of lepidolite ore

Abstract

The present invention discloses a method for ultra-stable foam separation and flotation of lepidolite, belonging to the field of mineral processing technology. The method first utilizes an amine cationic collector, an anionic collector, and a polyoxyethylene ether defoamer to prepare a high-efficiency collector, Super Lithium Cheng-31. The reselected lepidolite ore is then deslimed, and the +0.030 mm particle size product is subjected to a first stage of roughing to obtain a roughing concentrate and roughing tailings. The roughing concentrate is subjected to two stages of fine separation to obtain a final concentrate. The roughing tailings are subjected to three stages of scavenging to obtain scavenged ore and tailings. The middlings are sequentially returned, and an inhibitor and a collector, Super Lithium Cheng-31, are added to the roughing. Only the collector, Super Lithium Cheng-31, is added to the scavenging, and only the inhibitor is added to the fine separation. The lithium ion oxide (Li2O) grade in the lepidolite concentrate obtained by the method is 3.0% to 3.5%, the recovery rate of Li2O is greater than 90%, and the grade of Li2O in the tailings is less than 0.05%. The grade and recovery rate of Li2O in the lepidolite concentrate are significantly improved, and the foam has low viscosity, good fluidity, and is relatively easy to eliminate, thereby having good application prospects.

Description

Technical Field

[0001] The invention belongs to the technical field of mineral processing, and in particular relates to a method for ultra-stable foam separation and flotation of lepidolite ore. Background Art

[0002] Lepidolite is currently attracting much attention due to its low cost and abundant mineral resources. Yichun, Jiangxi Province, is an important lepidolite production base in my country. Because lepidolite is a brittle ore, the front-end crushing and grinding process easily results in an increase in fine particles, leading to severe mudification. Current lepidolite flotation processes mostly use only oily amine collectors and sodium salts as regulators, resulting in dense, sticky flotation foam with poor fluidity that is difficult to eliminate. The production process is highly unstable, with frequent occurrences of trough runaway and concentrate tailing, resulting in significant resource waste and a serious impact on its industrialization process. Therefore, in order to comprehensively and efficiently recover lepidolite ore, a new flotation technology with ultra-stable foam and efficient separation must be developed for lepidolite ore.

[0003] In order to recycle lepidolite resources more efficiently, predecessors have done a lot of research work. For example, the invention patent with application date of January 13, 2023 and application number 202310055602.x discloses a lepidolite beneficiation method based on a hyperdispersant. The flotation dispersant used in this method is obtained by mixing sodium hexametaphosphate, sodium polyacrylate, and sodium lignosulfonate in proportion and stirring them evenly. This process can prevent the ore from being covered by mud and realize a non-de-sludge flotation process. However, this method adds a large number of reagents and the cost is relatively high. At the same time, the addition of a large amount of sodium salt tends to increase the viscosity of the foam, making subsequent filtration operations difficult, and the stability of the production process remains to be verified.

[0004] The invention patent, filed on November 18, 2022, with application number 202211445117.X, discloses a beneficiation method for high-mud-content, fine-grained lepidolite ore. This method utilizes a microbubble flotation column flotation process. A stirring barrel is used before each stage of the beneficiation process to defoam and ensure full interaction between the reagent and the material. This effectively stabilizes the concentration, reagent dosage, and other process conditions of the microbubble flotation slurry, ensuring the output of high-quality products. This method is only intended for the recovery of fine-grained materials with a -200 mesh particle size accounting for ≥80%, and its applicability to the flotation of most lepidolite ores remains to be verified.

[0005] Therefore, achieving efficient flotation of ultra-stable foam separation of current lepidolite minerals and comprehensive recovery of their valuable metal elements are of great significance to improving the utilization efficiency of lepidolite resources in my country. Summary of the Invention

[0006] The present invention provides a method for ultrastable foam separation and flotation of lepidolite ore. The method first prepares the collector Super Lithium Cheng-31 and adjusts the pH by adding CaO to the return water. The entire process does not require the addition of additional adjusting agents such as Na2CO3. This method stabilizes the slurry environment and achieves efficient ultrastable foam separation. Furthermore, the process is simple and efficient, cost-effective, and has excellent separation performance, demonstrating promising application prospects.

[0007] In order to solve the above technical problems, the present invention provides the following technical solutions:

[0008] A method for ultrastable foam separation and flotation of lepidolite ore, comprising the following steps:

[0009] S1. After gravity separation, lithium mica ore with a Li2O grade greater than 0.39% is deslimed by a 250 hydrocyclone, and the +0.030mm particle size product is used as flotation feed;

[0010] S2, subjecting the +0.030 mm particle size product obtained in step S1 to a roughing step to obtain a roughing concentrate and roughing tailings, and adding an inhibitor and a collector, Super Lithium Cheng-31, in the roughing step;

[0011] S3, the rougher concentrate is subjected to two stages of cleaning to obtain the final concentrate, and the cleaned middlings are returned in sequence, with only inhibitors added in each stage of cleaning;

[0012] S4. The roughing tailings are scavenged in three stages to obtain the final tailings. The tailings are returned in sequence during scavenging. Only the collector Super Lithium Cheng-31 is added in each stage of scavenging.

[0013] The collector Chao Li Cheng-31 is made of an amine cationic collector, an anionic collector and a polyoxyethylene ether defoaming agent, wherein, by mass ratio, the amine cationic collector accounts for 20-30%, the anionic collector accounts for 50%-60%, and the polyoxyethylene ether defoaming agent accounts for 10%-20%.

[0014] The preparation process of the collector Chao Li Cheng-31 is as follows:

[0015] S01, after mixing an anionic collector and an amine cationic collector according to a mass ratio, adding a polyoxyethylene ether defoamer to obtain a mixed agent;

[0016] S02, using 60-70 ° C water to prepare the mixed reagent into a reagent solution with a mass concentration of 3%, and then adding 1-2% of the mass of the reagent solution nitric acid;

[0017] S03. Heat and stir the reagent solution after adding nitric acid to prepare a milky white solution. After the mixed reagent is completely dissolved, the high-efficiency collector Chao Li Cheng-31 is obtained.

[0018] The amine cationic collector is one or both of dodecylamine and coconut amine;

[0019] The anionic collector is one or both of sodium oleate and oxidized paraffin soap;

[0020] The polyoxyethylene ether defoaming agent is one or both of isopentanol polyoxyethylene ether and tallow amine polyoxyethylene ether.

[0021] In step S03, water bath heating is adopted, the heating temperature is 60° C., the stirring speed is 500 r / min, and the stirring time is 30 min.

[0022] The inhibitor is sodium hexametaphosphate.

[0023] The pH value of the return water used for flotation in the capture S2-S4 is adjusted to 8-11 by CaO.

[0024] In the roughing step S2, the dosage of the inhibitor is 500 g / t, the dosage of the collector is 300-500 g / t, and the flotation time is 2 min.

[0025] In step S3, the dosage of the two stages of concentration inhibitor is 250 g / t, and the flotation time is 1-1.5 min.

[0026] In step S4, the dosage of the collector in the three stages of scavenging is 150-250 g / t, and the flotation time is 1-1.5 min.

[0027] The Li2O grade in the concentrate obtained in step S3 is greater than 3.0%, and the recovery rate exceeds 90%.

[0028] Compared with the prior art, the technical solution of the present invention has the following beneficial effects:

[0029] The above scheme utilizes the synergistic effect of anionic collectors, cationic collectors, and nonionic defoamers. Furthermore, by adding CaO to the recycled water to adjust the pH, it avoids the problems of dense, sticky foam, poor fluidity, and difficulty in removing foam caused by the large amounts of oily collectors and sodium salts in traditional lepidolite flotation processes. The production process is stable and controllable, achieving the goal of efficiently recovering lepidolite, ferrolepidolite, and other lepidolite-containing minerals. Using the ultra-stable foam high-efficiency separation collector Super Li Cheng-31 prepared by the present invention, compared with the direct addition of traditional amine collectors, the Li2O grade in the concentrate can be increased by more than 0.3%-0.5%, and the Li2O recovery rate can be increased by more than 5%-10%. The ultra-stable foam high-efficiency separation flotation process for lepidolite ore employed in the present invention offers advantages such as wide adaptability, a stable and controllable production process, a simple process, low cost, and excellent flotation performance. It can achieve efficient recovery of most lithium-containing resources, such as lepidolite and ferrolepidolite, thereby improving overall resource recovery efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the following briefly introduces the drawings required for use in the description of the embodiments. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without creative work.

[0031] Figure 1 The present invention is a process flow chart of the method for ultra-stable foam separation and flotation of lepidolite ore. DETAILED DESCRIPTION

[0032] In order to make the technical problems, technical solutions and advantages to be solved by the present invention clearer, a detailed description will be given below with reference to the accompanying drawings and specific embodiments.

[0033] The invention provides a method for ultra-stable foam separation and flotation of lepidolite ore.

[0034] like Figure 1 As shown, the method includes the following steps:

[0035] S1. After gravity separation, lithium mica ore with a Li2O grade greater than 0.39% is deslimed in a 250 hydrocyclone. The +0.030mm particle size product is used as flotation feed, and the -0.030mm particle size product is recovered separately as the final ore slime product.

[0036] S2, subjecting the +0.030 mm particle size product obtained in step S1 to a roughing step to obtain a roughing concentrate and roughing tailings, and adding an inhibitor and a collector, Super Lithium Cheng-31, in the roughing step;

[0037] S3, the rougher concentrate is subjected to two stages of cleaning to obtain the final concentrate, and the cleaned middlings are returned in sequence, with only inhibitors added in each stage of cleaning;

[0038] S4. The roughing tailings are scavenged in three stages to obtain the final tailings. The tailings are returned in sequence during scavenging. Only the collector Super Lithium Cheng-31 is added in each stage of scavenging.

[0039] Among them, the collector Chao Li Cheng-31 is made of amine cationic collector, anionic collector and polyoxyethylene ether defoaming agent, among which, by mass ratio, amine cationic collector accounts for 20-30%, anionic collector accounts for 50%-60%, and polyoxyethylene ether defoaming agent accounts for 10%-20%.

[0040] The preparation process of the collector Chao Li Cheng-31 is as follows:

[0041] S01, after mixing an anionic collector and an amine cationic collector according to a mass ratio, adding a polyoxyethylene ether defoamer to obtain a mixed agent;

[0042] S02, using 60-70 ° C water to prepare the mixed reagent into a reagent solution with a mass concentration of 3%, and then adding 1-2% of the mass of the reagent solution nitric acid;

[0043] S03. Heat and stir the reagent solution after adding nitric acid to prepare a milky white solution. After the mixed reagent is completely dissolved, the high-efficiency collector Chao Li Cheng-31 is obtained.

[0044] The following is an explanation of the specific embodiment of open circuit flotation of +0.030 mm particle size products.

[0045] The calculation method of lithium ore recovery rate is: the recovery rate of Li2O in scavenging concentrate + the recovery rate of Li2O in beneficiation concentrate.

[0046] Example 1

[0047] The mass percentage of the amine cationic collector is 20%, of which the mass percentage of dodecylamine is 10% and the mass percentage of coconut amine is 10%; the mass percentage of the anionic collector is 60%, of which the mass percentage of sodium oleate is 30% and the mass percentage of oxidized paraffin soap is 30%; the mass percentage of the polyoxyethylene ether defoaming agent is 20%, of which the mass percentage of isopentenol polyoxyethylene ether is 10% and the mass percentage of tallow amine polyoxyethylene ether is 10%.

[0048] The preparation method is as follows: dodecylamine, coconut amine, sodium oleate, oxidized paraffin soap, isopentanol polyoxyethylene ether, and tallow amine polyoxyethylene ether are mixed according to a predetermined mass percentage; the mixed agent is prepared into a 3% agent solution using 60°C tap water; 2% by mass of concentrated nitric acid (using 69wt.% nitric acid) is added to the agent solution to improve its solubility; the mixed agent after adding nitric acid is heated in a water bath and stirred to prepare a milky white solution, the water bath heating temperature is 60°C, the stirring intensity is 500r / min, the stirring time is 30min, and the high-efficiency collector Chao Li Cheng-31 is obtained after it is completely dissolved.

[0049] Example 2

[0050] The mass percentage of the amine cationic collector is 25%, of which the mass percentage of coconut amine is 25%; the mass percentage of the anionic collector is 55%, of which the mass percentage of sodium oleate is 55%; the mass percentage of the polyoxyethylene ether defoaming agent is 20%, of which the mass percentage of tallow amine polyoxyethylene ether is 20%.

[0051] The preparation method is as follows: coconut amine, sodium oleate, and tallow amine polyoxyethylene ether are mixed according to a predetermined mass percentage; the mixed agent is prepared into a 3% agent solution using 70°C tap water; 1.5% by mass of nitric acid (using 69wt.% nitric acid) is added to the agent solution to improve its solubility; the mixed agent after adding nitric acid is placed in a water bath and heated and stirred to prepare a milky white solution, the water bath heating temperature is 60°C, the stirring intensity is 500r / min, and the stirring time is 30min, and the high-efficiency collector Chao Li Cheng-31 is obtained after complete dissolution.

[0052] Example 3

[0053] The mass percentage of the amine cationic collector is 30%, of which the mass percentage of dodecylamine is 30%; the mass percentage of the anionic collector is 60%, of which the mass percentage of oxidized paraffin soap is 60%; the mass percentage of the polyoxyethylene ether defoaming agent is 10%, of which the mass percentage of isopentenol polyoxyethylene ether is 10%.

[0054] The preparation method comprises the following steps: mixing dodecylamine, oxidized paraffin soap, and isopentanol polyoxyethylene ether in predetermined mass percentages; using 65°C tap water to prepare the mixed reagents into a reagent solution with a concentration of 3%; adding 1% by mass nitric acid (using 69wt.% nitric acid) to the reagent solution to improve its solubility; heating the mixed reagent after adding nitric acid in a water bath and stirring it to prepare a milky white solution, wherein the water bath heating temperature is 60°C, the stirring intensity is 500r / min, and the stirring time is 30min. After the mixture is completely dissolved, the efficient collector Chao Li Cheng-31 is obtained.

[0055] Example 4

[0056] The tailings of a lithium mica beneficiation plant in Binjiang Industrial Park, Yichun City, Jiangxi Province (containing lithium mica after recovering tungsten and tin) were used as the application object, and the Li2O content was 0.39%-0.42%. This example is a comparative experiment on the effect of the collector Chaolicheng-31. The experimental process was strictly in accordance with Figure 1 The process shown includes the following steps:

[0057] 1) Weigh 500g of fine tailings product for classification, with the +0.030mm particle size product used as flotation feed and the -0.030mm particle size product treated separately as a sludge product;

[0058] 2) The +0.030 mm particle size product is prepared into a 30% concentration slurry, which is transferred to an XFD 1.5 L flotation cell for roughing. Collectors and depressants are added in sequence during the roughing process, and after stirring for 2 minutes each, aeration flotation is started to obtain a roughing concentrate and a roughing tailing. The roughing concentrate obtained by flotation is transferred to a 750 mL flotation cell for concentrating. The roughing tailing is scavenged three times, scavenged middling 3 is returned to the roughing, and scavenged middlings 4 and 5 are respectively returned to the previous scavenging level. The tailings obtained from scavenging 3 are the final tailings. The roughing concentrate is concentrating twice in a 750 mL flotation cell, concentrating middling 1 is returned to the roughing, and concentrating middling 2 is returned to concentrating 1. The concentrate obtained from concentrating 2 is the final concentrate.

[0059] The reagent conditions of this embodiment are: the collector prepared in Example 1 is Super Lithium Cheng-31. CaO is used to adjust the pH of industrial return water to 8, and the industrial return water is used to prepare the pulp concentration. No additional pH adjuster is added during the process implementation. Specifically, the reagent system for the roughing operation is: 500g / t of sodium hexametaphosphate, 500g / t of the collector Super Lithium Cheng-31 prepared in Example 1, and the flotation time is 2min; the scavenging operation is performed 3 times, and the reagent system is to add 250g / t of the collector Super Lithium Cheng prepared in Example 1 respectively, and the flotation time is 1min; the cleaning operation is performed 2 times, and the reagent system is to add 250g / t of sodium hexametaphosphate respectively, and the flotation time is 1min.

[0060] Comparative Condition 1: lepidolite using a conventional collector, cocoamine. Specifically, the roughing operation consisted of tap water slurry preparation, a reagent system consisting of 200g / t sodium carbonate, 500g / t sodium hexametaphosphate, and 500g / t cocoamine collector, with a flotation time of 2 minutes. The scavenging operation was repeated three times, using a reagent system of 250g / t cocoamine collector and a flotation time of 1 minute. The cleaning operation was repeated twice, using a reagent system of 250g / t sodium hexametaphosphate and a flotation time of 1 minute.

[0061] Table 1 Comparison of flotation effects of collector Chaolicheng-31 and coconut amine

[0062]

[0063] Analysis of Table 1 shows that, compared with the conventional coconut amine process, the use of the Super Lithium Cheng-31 and return water pH adjustment process prepared in Example 1 increased the LiO grade of the concentrate by 0.55% and the LiO recovery rate by 12.48%. This indicates that, compared with the conventional coconut amine process, the Super Lithium Cheng-31 and return water pH adjustment process prepared in Example 1 has a better selective capture effect on the flotation of lepidolite ore.

[0064] Example 5

[0065] The application object is a lithium mica mine tailings (containing lithium mica after tantalum and niobium recovery) in Yuanzhou District, Yichun City, Jiangxi Province, with a Li2O content of 0.4%-0.45%. This example is a comparative experiment on the effect of collector Chaolicheng-31. The experimental process is strictly in accordance with Figure 1 The specific flotation process is the same as that in Example 4.

[0066] The reagent conditions of this embodiment are: the collector prepared in Example 2 is Super Lithium Cheng-31. CaO is used to adjust the pH of industrial return water to 9, and the industrial return water is used to prepare the pulp concentration, so no additional pH adjuster is added during the process implementation. Specifically, the reagent system for the roughing operation is: 500g / t of sodium hexametaphosphate, 400g / t of the collector Super Lithium Cheng-31 prepared in Example 2, and the flotation time is 2min; the scavenging operation is performed 3 times, and the reagent system is respectively 200g / t of the collector prepared in Example 2, and the flotation time is 1.5min; the cleaning operation is performed 2 times, and the reagent system is respectively 250g / t of sodium hexametaphosphate, and the flotation time is 1.5min.

[0067] Comparative Condition 2: Lepidolite collectors were cocoamine and sodium oleate, both added directly according to conventional mineral processing reagent usage methods, without using the preparation method of this application. Specifically, the roughing operation was tap water slurry preparation, the reagent system was 300g / t Na2CO3, 500g / t sodium hexametaphosphate, 100g / t cocoamine collector, 300g / t sodium oleate, and the flotation time was 2 minutes; the scavenging operation was performed three times, the reagent system was 50g / t cocoamine collector, 150g / t sodium oleate, and the flotation time was 1.5 minutes; the cleaning operation was performed twice, the reagent system was 250g / t sodium hexametaphosphate, and the flotation time was 1.5 minutes.

[0068] Table 2 Comparison of flotation effects of collector Chaolicheng-31 and coconut amine and sodium oleate added directly

[0069]

[0070] Analysis of Table 2 shows that, compared with the conventional process of directly adding a collector sodium oleate in combination with coconut amine, the collector prepared in Example 2, Super Lithium Cheng-31, increased the LiO grade in the concentrate by 0.34% and the LiO recovery rate by 10.98%. This indicates that, compared with the conventional process of using anion-cation compatible collectors coconut amine and sodium oleate, the collector Super Lithium Cheng-31 prepared in Example 2 and the new process of adjusting the pH of the return water can better utilize the synergistic effect between the cationic, anionic, and nonionic agents and achieve a better selective capture effect for the flotation of lepidolite ore.

[0071] Example 6

[0072] The tailings of a lithium mica beneficiation plant in Huaqiao Township, Yichun City, Jiangxi Province (containing lithium mica after recovering tantalum and niobium) were used as the application object, and the Li2O content was 0.39-0.43%. This example is a comparative experiment on the effect of the collector Chaolicheng-31. The experimental process was strictly in accordance with Figure 1 The specific flotation process is the same as that in Example 4.

[0073] The reagent conditions of this embodiment are: the collector prepared in Example 3 is Super Lithium Cheng-31. CaO is used to adjust the pH of industrial return water to 11, and the industrial return water is used to prepare the pulp concentration, so no additional pH adjuster is added during the process implementation. Specifically, the reagent system for the roughing operation is: 500g / t of sodium hexametaphosphate, 300g / t of the collector Super Lithium Cheng-31 prepared in Example 3, and the flotation time is 2min; the scavenging operation is performed 3 times, and the reagent system is respectively 150g / t of the collector prepared in Example 3, and the flotation time is 1.5min; the cleaning operation is performed 2 times, and the reagent system is respectively 250g / t of sodium hexametaphosphate, and the flotation time is 1.5min.

[0074] Comparative Condition 3: The lepidolite collectors were oxidized paraffin soap and dodecylamine, both of which were added directly according to conventional mineral processing reagent usage methods, without using the preparation method of this application. Specifically, the roughing operation was tap water slurry mixing, the reagent system was 500g / t Na2CO3, 500g / t sodium hexametaphosphate, 220g / t oxidized paraffin soap collector, 80g / t dodecylamine, and the flotation time was 2 minutes; the scavenging operation was performed three times, the reagent system was 110g / t oxidized paraffin soap collector, 40g / t dodecylamine, and the flotation time was 1.5 minutes; the cleaning operation was performed twice, the reagent system was 250g / t sodium hexametaphosphate, and the flotation time was 1.5 minutes.

[0075] Table 3 Comparison of flotation effects of collector Chaolicheng-31, oxidized paraffin soap and dodecylamine added directly

[0076]

[0077] Analysis of Table 3 shows that, compared with the conventional process of directly adding oxidized paraffin soap and dodecylamine as collectors, the novel process of adding CaO to the return water for pH adjustment using Super Lithium-Cheng-31 employed in Example 3 increases the LiO grade of the concentrate by 0.35% and the LiO recovery rate by 9.62%. This indicates that, compared with the conventional process of directly adding oxidized paraffin soap and dodecylamine as collectors of a combined anion and cation combination, Super Lithium-Cheng-31 as collector prepared by the preparation method of the present invention is more capable of leveraging the synergistic effects of the cationic, anionic, and nonionic agents and exhibits a more selective capture effect in the flotation of lepidolite ore.

[0078] The above is a preferred embodiment of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principles of the present invention. These improvements and modifications should also be regarded as within the scope of protection of the present invention.

Claims

1. A method for ultrastable foam separation and flotation of lepidolite ore, characterized in that: The steps are as follows: S1. After gravity separation, lithium mica ore with a Li2O grade greater than 0.39% is deslimed by a 250 hydrocyclone, and the +0.030mm particle size product is used as flotation feed; S2, subjecting the +0.030 mm particle size product obtained in step S1 to a roughing step to obtain a roughing concentrate and roughing tailings, and adding an inhibitor and a collector, Super Lithium Cheng-31, in the roughing step; S3, the rougher concentrate is subjected to two stages of cleaning to obtain the final concentrate, and the cleaned middlings are returned in sequence, with only inhibitors added in each stage of cleaning; S4, the roughing tailings are scavenged in three stages to obtain the final tailings, and the scavenged tailings are returned in sequence. Only the collector Super Lithium Cheng-31 is added in each scavenging stage; The collector Chao Li Cheng-31 is made of an amine cationic collector, an anionic collector and a polyoxyethylene ether defoamer, wherein, by mass ratio, the amine cationic collector accounts for 20-30%, the anionic collector accounts for 50%-60%, and the polyoxyethylene ether defoamer accounts for 10%-20%; The preparation process of the collector Chao Li Cheng-31 is as follows: S01, after mixing an anionic collector and an amine cationic collector according to a mass ratio, adding a polyoxyethylene ether defoamer to obtain a mixed agent; S02, using 60-70 ° C water to prepare the mixed reagent into a reagent solution with a mass concentration of 3%, and then adding 1-2% of the mass of the reagent solution nitric acid; S03. Heat and stir the reagent solution after adding nitric acid to prepare a milky white solution. After the mixed reagent is completely dissolved, the high-efficiency collector Chao Li Cheng-31 is obtained.

2. The method for ultrastable foam separation and flotation of lepidolite according to claim 1, wherein: The amine cationic collector is one or both of dodecylamine and coconut amine; The anionic collector is one or both of sodium oleate and oxidized paraffin soap; The polyoxyethylene ether defoaming agent is one or both of isopentanol polyoxyethylene ether and tallow amine polyoxyethylene ether.

3. The method for ultrastable foam separation and flotation of lepidolite according to claim 1, wherein: In step S03, water bath heating is adopted, the heating temperature is 60° C., the stirring speed is 500 r / min, and the stirring time is 30 min.

4. The method for ultrastable foam separation and flotation of lepidolite according to claim 1, wherein: The inhibitor is sodium hexametaphosphate.

5. The method for ultrastable foam separation and flotation of lepidolite according to claim 1, wherein: In the roughing step S2, the dosage of the inhibitor is 500 g / t, the dosage of the collector is 300-500 g / t, and the flotation time is 2 min.

6. The method for ultrastable foam separation and flotation of lepidolite according to claim 1, wherein: In step S3, the dosage of the two stages of concentration inhibitor is 250 g / t, and the flotation time is 1-1.5 min.

7. The method for ultrastable foam separation and flotation of lepidolite according to claim 1, wherein: In step S4, the dosage of the collector in the three stages of scavenging is 150-250 g / t, and the flotation time is 1-1.5 min.

8. The method for ultrastable foam separation and flotation of lepidolite according to claim 1, wherein: The Li2O grade in the concentrate obtained in step S3 is greater than 3.0%, and the recovery rate exceeds 90%.

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