Cationic combined collector and application thereof, cationic combined collector solution

Abstract

The application provides a cationic combined collector and application thereof and a cationic combined collector solution, and belongs to the technical field of lithium mica flotation. The cationic combined collector provided by the application comprises octadecylamine and an auxiliary component; the auxiliary component comprises cocamine and / or dodecylamine; and the mass ratio of the octadecylamine and the auxiliary component is (5-20):1. The cationic combined collector of the application is a cation-cation combined collector compounded by taking long-chain amine octadecylamine (ODA) as a main component and cocamine and / or dodecylamine as an auxiliary component, the foaming property of the auxiliary component is complementary to the strong hydrophobic property of the octadecylamine, so that the flotation separation effect of the cationic combined collector on lithium mica is improved; and by limiting the mass ratio of the octadecylamine and the auxiliary component, the flotation separation effect of the cationic combined collector on lithium mica can be further improved.

Description

Technical Field

[0001] This invention belongs to the field of lithium mica flotation technology, specifically relating to a cationic combined collector and its application, and a cationic combined collector solution. Background Technology

[0002] Lepidolite is an important mineral raw material for extracting lithium and its compounds. With the rapid development of the new energy industry, global lithium demand continues to grow, and the efficient recovery of lithium from low-grade lepidolite ore has become a research hotspot in the field of mineral processing. Flotation is the main industrial method for enriching lepidolite. Currently, the main approach is to use a combination of anion and cation collectors, leveraging the co-adsorption effect and electrostatic neutralization of the two types of reagents to improve flotation selectivity. This direction has accumulated a wealth of research results. Compared to the extensive research on the anion-cation combination route, research on cation-cation (cation-cation) amine-based combination collectors in lepidolite flotation is rarely reported. Summary of the Invention

[0003] The purpose of this invention is to provide a cationic combined collector and its application, as well as a cationic combined collector solution. The cationic combined collector provided by this invention can improve the flotation and separation effect of lepidolite when used in the flotation of lepidolite.

[0004] To achieve the above-mentioned objectives, the present invention provides the following technical solution: This invention provides a cationic combined collector comprising octadecylamine and an auxiliary component; The excipients include cocoylamine and / or dodecylamine; The mass ratio of the octadecylamine to the excipient is (5~20):1.

[0005] Preferably, the mass ratio of the octadecylamine to the excipient is (6~15):1.

[0006] The present invention also provides a cationic combined collector solution, which is obtained by mixing the cationic combined collector as described in claim 1 or 2, an acid and water.

[0007] Preferably, the mass concentration of the acid is 36-38%, and the mass ratio of the acid to the cationic collector is (1-5):1.

[0008] Preferably, the total mass concentration of octadecylamine and cofactors in the cationic combined collector solution is 1-10%.

[0009] This invention also provides the application of the cationic combined collector described in the above technical solution in the flotation of lepidolite.

[0010] Preferably, the amount of the cationic combined collector is 200~500g / t, based on the mass of the lepidolite ore during lepidolite flotation.

[0011] Preferably, the application includes: Lithium mica ore is slurry prepared to obtain lithium mica slurry; A cationic combined collector, acid, and water are mixed to obtain a cationic combined collector solution; The cationic combined collector solution and lepidolite slurry are mixed and then subjected to flotation.

[0012] Preferably, the mass concentration of the lithium mica slurry is 25-40%.

[0013] Preferably, the application includes: Lithium mica ore is slurry prepared to obtain lithium mica slurry; Octadecylamine, acid, and water are mixed to obtain a first ammonium salt solution; The auxiliary components, acid, and water are mixed to obtain a second ammonium salt solution; The first ammonium salt solution and the second ammonium salt solution are mixed to obtain a cationic combined collector solution; The lithium mica slurry and the cationic combined collector solution are mixed and then subjected to flotation.

[0014] This invention provides a cationic combined collector comprising octadecylamine and an auxiliary component; the auxiliary component includes cocoylamine and / or dodecylamine; the mass ratio of octadecylamine to the auxiliary component is (5~20):1. This cationic combined collector is a cation-cation combined collector formulated with long-chain amine octadecylamine (ODA) as the main component and cocoylamine and / or dodecylamine as auxiliary components. It utilizes the complementary foaming properties of the auxiliary component and the strong hydrophobic properties of octadecylamine to improve the flotation separation effect of the cationic combined collector on lepidolite. By limiting the mass ratio of octadecylamine to the auxiliary component, the flotation separation effect of the cationic combined collector on lepidolite can be further improved. The results of the embodiments show that the lepidolite rough concentrate obtained by one roughing process using the cationic combined collector provided by this invention has a Li2O grade of 1.42%, a recovery rate of 87.59%, and a separation efficiency of 82.31%. Detailed Implementation

[0015] This invention provides a cationic combined collector comprising octadecylamine and an auxiliary component; The excipients include cocoamine (COA) and / or dodecylamine (DDA). The mass ratio of the octadecylamine to the excipient is (5~20):1.

[0016] This invention does not impose any special restrictions on the source of the raw materials; commercially available products familiar to those skilled in the art can be used.

[0017] In one embodiment, the mass ratio of octadecylamine to the excipient can be 6:1, 6.14:1, 7:1, 8:1, 9:1, 10:1, 11:1, 12:1, 13:1, 14:1, 15:1, 16:1, 16.7:1, 17:1, 18:1, or 19:1. This invention, by limiting the mass ratio of octadecylamine to the excipient, can further improve the flotation separation effect of the cationic combined collector on lepidolite.

[0018] In this invention, the excipients are cocoamine and dodecylamine. There is no particular limitation on the mass ratio of cocoamine and dodecylamine; any ratio is acceptable. As one embodiment, the mass ratio of cocoamine and dodecylamine can be (1~0.1):(0.1~1).

[0019] The cationic combined collector of the present invention is a cationic-cationic combined collector with long-chain amine octadecylamine (ODA) as the main component and cocoylamine and / or dodecylamine as auxiliary components. It utilizes the complementary foaming properties of the auxiliary components and the strong hydrophobic properties of octadecylamine to improve the flotation and separation effect of the cationic combined collector on lepidolite.

[0020] This invention also provides a cationic combined collector solution, obtained by mixing a cationic combined collector, an acid, and water. In this invention, the use of an acid can improve the water solubility and collecting performance of the cationic combined collector.

[0021] In this invention, the preferred mass concentration of the acid is 36-38%; the preferred mass ratio of the acid to the cationic combined collector is (1-5):1. As one embodiment, the mass concentration of the acid can be 37%; the acid can be hydrochloric acid; and the mass ratio of the acid to the cationic combined collector can be 2:1, 3:1, or 4:1. This invention can further improve water solubility and collecting performance by controlling the mass ratio of the acid to the cationic combined collector.

[0022] The present invention does not have a special limitation on the amount of water used; it can be selected according to the mass concentration of the required cationic combined collector solution.

[0023] In this invention, the preferred method for mixing the cationic combined collector, acid, and water is to mix octadecylamine and the cofactor, and then add the acid and water.

[0024] In this invention, the mixing temperature of the octadecylamine and the cofactor is preferably 40-80°C. As one embodiment, the mixing temperature of the octadecylamine and the cofactor can be 45°C, 50°C, 55°C, 60°C, 65°C, 70°C, or 75°C. This invention does not have a particular limitation on the mixing time, as long as a homogeneous solution is obtained.

[0025] In this invention, the addition of acid and water is preferably carried out under stirring conditions. The stirring operation is not particularly limited in this invention, as long as a homogeneous solution is obtained. As one embodiment, the stirring time can be 30-60 minutes.

[0026] In this invention, the total mass concentration of octadecylamine and cofactors in the cationic combined collector solution is preferably 1-10%. As one embodiment, the total mass concentration of octadecylamine and cofactors in the cationic combined collector solution can be 2%, 3%, 4%, 5%, 6%, 7%, 8%, or 9%.

[0027] This invention also provides the application of the cationic combined collector described in the above technical solution in the flotation of lepidolite.

[0028] In this invention, based on the mass of lepidolite ore during lepidolite flotation, the preferred dosage of the cationic combined collector is 200-500 g / t. As one embodiment, based on the mass of lepidolite ore during lepidolite flotation, the dosage of the cationic combined collector can be 250 g / t, 275 g / t, 300 g / t, 350 g / t, 375 g / t, 400 g / t, or 450 g / t. Limiting the dosage of the cationic combined collector within the above range further improves the collecting performance.

[0029] In one embodiment of the present invention, the application preferably includes: Lithium mica ore is slurry prepared to obtain lithium mica slurry; A cationic combined collector, acid, and water are mixed to obtain a cationic combined collector solution; The cationic combined collector solution and lepidolite slurry are mixed and then subjected to flotation.

[0030] The present invention preferably involves adjusting the lepidolite ore into a slurry to obtain a lepidolite slurry.

[0031] The present invention does not impose any special limitations on the slurry preparation operation. Operations familiar to those skilled in the art can be used, as long as the required slurry concentration is obtained.

[0032] In this invention, the mass concentration of the lepidolite slurry is preferably 25-40%. As one embodiment, the mass concentration of the lepidolite slurry can be 26%, 28%, 30%, 32%, 34%, 36%, or 38%.

[0033] The present invention preferably involves mixing a cationic combined collector, an acid, and water to obtain a cationic combined collector solution.

[0034] In this invention, the preparation method of the cationic combined collector solution is preferably the same as the aforementioned operation, and will not be repeated here.

[0035] After obtaining the lepidolite slurry and the cationic combined collector solution, the present invention preferably mixes the cationic combined collector solution and the lepidolite slurry for flotation.

[0036] The present invention does not impose any particular limitation on the operation of mixing the cationic combined collector solution and the lepidolite slurry; any technical solution for preparing the mixture well known to those skilled in the art can be used. As one embodiment, the mixing of the cationic combined collector solution and the lepidolite slurry can be carried out under stirring conditions; the stirring time can be 2-5 minutes, or even 3 minutes.

[0037] The present invention does not impose any special limitations on the flotation operation; any flotation operation well known to those skilled in the art can be used. As one embodiment, the flotation can be aeration flotation.

[0038] In another technical solution of the present invention, the application preferably includes: Lithium mica ore is slurry prepared to obtain lithium mica slurry; Octadecylamine, acid, and water are mixed to obtain a first ammonium salt solution; The auxiliary components, acid, and water are mixed to obtain a second ammonium salt solution; The first ammonium salt solution and the second ammonium salt solution are mixed to obtain a cationic combined collector solution; The lithium mica slurry and the cationic combined collector solution are mixed and then subjected to flotation.

[0039] The present invention preferably involves adjusting the lepidolite ore into a slurry to obtain a lepidolite slurry.

[0040] In this invention, the slurry preparation operation is preferably the same as the aforementioned operation, and will not be repeated here.

[0041] The present invention does not impose any special limitations on the slurry preparation operation. Operations familiar to those skilled in the art can be used, as long as the required slurry concentration is obtained.

[0042] The present invention preferably involves mixing octadecylamine, acid, and water to obtain a first ammonium salt solution.

[0043] In this invention, the preferred mass concentration of the acid is 36-38%; the preferred mass ratio of the acid to octadecylamine is (1-5):1. As one embodiment, the mass concentration of the acid can be 37%; the acid can be hydrochloric acid; and the mass ratio of the acid to octadecylamine can be 2:1, 3:1, or 4:1. In this invention, the use of acid can improve the water solubility and collecting performance of octadecylamine; by controlling the mass ratio of acid to octadecylamine, the water solubility and collecting performance can be further improved.

[0044] The present invention does not impose any special limitation on the amount of water used; any amount known to those skilled in the art can be used.

[0045] In this invention, the preferred mixing temperature for the octadecylamine, acid, and water is 40-80°C. As one embodiment, the mixing temperature for the octadecylamine, acid, and water can be 45°C, 50°C, 55°C, 60°C, 65°C, 70°C, or 75°C. This invention does not impose a specific limitation on the mixing time for the octadecylamine, acid, and water, as long as a homogeneous solution is obtained.

[0046] The present invention preferably involves mixing the auxiliary components, acid, and water to obtain a second ammonium salt solution.

[0047] In this invention, the preferred mass concentration of the acid is 36-38%; the preferred mass ratio of the acid to the cofactor is (1-5):1. As one embodiment, the mass concentration of the acid can be 37%; the acid can be hydrochloric acid; and the mass ratio of the acid to octadecylamine can be 2:1, 3:1, or 4:1. In this invention, the use of acid can improve the water solubility and collecting performance of the cofactor; by controlling the mass ratio of the acid to the cofactor, the water solubility and collecting performance can be further improved.

[0048] The present invention does not impose any special limitation on the amount of water used; any amount known to those skilled in the art can be used.

[0049] In this invention, the preferred mixing temperature for the auxiliary component, acid, and water is 40-80°C. As one embodiment, the mixing temperature for the auxiliary component, acid, and water can be 45°C, 50°C, 55°C, 60°C, 65°C, 70°C, or 75°C. This invention does not impose a specific limitation on the mixing time for the auxiliary component, acid, and water, as long as a homogeneous solution is obtained.

[0050] After obtaining the first ammonium salt solution and the second ammonium salt solution, the present invention preferably mixes the first ammonium salt solution and the second ammonium salt solution to obtain a cationic combined collector solution.

[0051] The present invention does not have any special limitations on the operation of mixing the first ammonium salt solution and the second ammonium salt solution; any technical solution for preparing the mixture well known to those skilled in the art can be used.

[0052] After obtaining the lepidolite slurry and the cationic combined collector solution, the present invention preferably mixes the lepidolite slurry and the cationic combined collector solution for flotation.

[0053] In this invention, the operation of mixing the lithium mica slurry and the cationic combined collector solution for flotation is preferably the same as the aforementioned operation, and will not be repeated here.

[0054] The beneficial effects of this invention are as follows: (1) The efficient flotation of lepidolite can be achieved under neutral slurry conditions without the need to add pH adjusters such as sulfuric acid. This avoids the problems of equipment corrosion and high wastewater treatment costs associated with traditional acidic cation flotation methods, simplifies the on-site operation process, and provides a new technical solution and process reference for the flotation and recovery of low-grade lepidolite ore.

[0055] (2) The formulation design, with long-chain amine octadecylamine as the main component and medium- and short-chain amines as auxiliary components, fully leverages the selective collection advantage of long-chain amines on lepidolite. At the same time, medium- and short-chain amines improve the dispersion state and foam properties of the reagent in the slurry. The two work synergistically to significantly improve the separation efficiency. For low-grade lepidolite ore from Yichun tantalum-niobium mine with a Li2O grade of 0.24%, industrial-grade coconut oil amine (COA) was used as an auxiliary component. After flotation according to the optimized process of this invention, the Li2O grade of the rough concentrate can reach 1.42%, the recovery rate reaches 87.14%, and the separation efficiency reaches 82.31%, which is far superior to the flotation effect of single amine collectors.

[0056] (3) Easy to operate and adaptable to the needs of on-site industrial applications.

[0057] The technical solutions of this invention will be clearly and completely described below with reference to the embodiments thereof. Obviously, the described embodiments are only a part of the embodiments of this invention, and not all of them. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without creative effort are within the scope of protection of this invention.

[0058] The flotation effect of this invention uses the Hancock-Luikon separation efficiency η as a comprehensive evaluation index, and the calculation formula is η=(ε-γ) / (1-α / β) max )×100%, where ε is the concentrate recovery rate, γ is the concentrate yield, α is the feed grade, and β is the feed grade. max This represents the theoretical highest grade for lithium-bearing minerals. Based on the properties of the research object, β max The value is 2.0%. This sorting efficiency can take into account both grade and recovery rate, avoiding the one-sided evaluation of a single indicator.

[0059] Example 1 The cationic collector is a combination of ODA and COA in a mass ratio of 10:1.

[0060] Application Example 1 The cationic combined collector from Example 1 was applied to the flotation of lepidolite, and the steps are as follows: Mix ODA and COA, then add 36% hydrochloric acid (the mass ratio of hydrochloric acid to the cationic combined collector is 4:1) and an appropriate amount of water, and stir in a water bath at 50°C for 45 minutes to obtain a cationic combined collector solution with a total mass concentration of 2% for ODA and COA. Lithium mica ore (containing 0.24% Li2O, with lithium-containing minerals mainly consisting of lepidolite and muscovite, the mineral content ratio of lepidolite to muscovite is 1:2, and the yield of -0.074mm particle size is 28.65%) was added to an XFD-0.5L flotation machine, and tap water was used to adjust the slurry to a mass concentration of 38% to obtain lepidolite slurry. A cationic combined collector solution was added to the lepidolite slurry, stirred for 3 minutes, and aerated and skimmed to obtain a rough concentrate; wherein, based on the mass of lepidolite ore during lepidolite flotation, the amount of cationic combined collector was 300 g / t.

[0061] The crude concentrate obtained in Application Example 1 has a Li2O grade of 1.42%, a recovery rate of 87.14%, and a separation efficiency of 82.31%.

[0062] Application Example 2 Based on Application Example 1, the mass concentration of the lepidolite slurry was modified to 33%, and the mass of the lepidolite ore during lepidolite flotation was used as the benchmark. The dosage of the cationic combined collector was 250 g / t, and other conditions remained unchanged.

[0063] The crude concentrate obtained in Application Example 2 has a Li2O grade of 1.41%, a recovery rate of 82.92%, and a separation efficiency of 78.35%.

[0064] Application Example 3 Based on Application Example 1, the mass concentration of the lepidolite slurry was modified to 28%, the mass ratio of hydrochloric acid to cationic combined collector was 3:1, the dosage of cationic combined collector was 300 g / t based on the mass of lepidolite ore during lepidolite flotation, and other conditions remained unchanged.

[0065] The crude concentrate obtained in Application Example 3 has a Li2O grade of 1.21%, a recovery rate of 79.65%, and a separation efficiency of 72.21%.

[0066] Comparative Application Example 1 The cationic combined collector from Example 1 was applied to the flotation of lepidolite, and the steps are as follows: Lithium mica ore (containing 0.24% Li2O, with lithium-containing minerals mainly consisting of lepidolite and muscovite, the mineral content ratio of lepidolite to muscovite is 1:2, and the yield of -0.074mm particle size is 28.65%) was added to an XFD-0.5L flotation machine, and tap water was used to adjust the slurry to a mass concentration of 38% to obtain lepidolite slurry. Mix ODA, hydrochloric acid (mass concentration 37%, mass ratio of hydrochloric acid to ODA 2:1) and an appropriate amount of water in a 50°C water bath until homogeneous; mix COA, hydrochloric acid (mass concentration 37%, mass ratio of hydrochloric acid to COA 2:1) and an appropriate amount of water in a 50°C water bath until homogeneous. First, acidified COA is added to the lepidolite slurry and stirred for 3 minutes; then acidified ODA is added and stirred for 3 minutes; aeration and foam removal are performed to obtain a rough concentrate; based on the mass of lepidolite ore during lepidolite flotation, the dosage of the cationic combined collector is 275 g / t.

[0067] Compared with the crude concentrate obtained in Application Example 1, the Li2O grade was 0.88%, the recovery rate was 87.59%, and the separation efficiency was 71.76%.

[0068] Comparative Application Example 2 Based on Comparative Application Example 1, only acidified ODA was added. The amount of ODA used was 300 g / t, based on the mass of lepidolite ore during lepidolite flotation. Additionally, 30 g / t of No. 2 oil was added as a frother. The mixture was stirred for 3 minutes, aerated, and foamed, with other conditions remaining unchanged.

[0069] Under neutral conditions, the crude concentrate obtained in Comparative Application Example 2 had a Li2O grade of 0.75%, a recovery rate of 65.26%, and a separation efficiency of 49.85%. The grade was average, and the recovery rate was significantly lower than that of the embodiments of the present invention, indicating insufficient separation capacity.

[0070] Comparative Application Example 3 Based on Comparative Application Example 1, only acidified COA was added. The amount of COA was 300 g / t, based on the mass of lepidolite ore during lepidolite flotation. The mixture was stirred for 3 minutes, aerated and skimmed, with other conditions remaining unchanged.

[0071] Under neutral conditions, compared with the crude concentrate obtained in Application Example 3, the Li2O grade was 0.30%, the recovery rate was 96.11%, the separation efficiency was 17.54%, and there was almost no enrichment effect. The grade of the crude concentrate was close to that of the original ore, with no separation and enrichment effect, and a large amount of gangue floated to the surface.

[0072] Comparative Application Example 4 Based on Comparative Application Example 1, only acidified DDA was added. The amount of DDA used was 300 g / t, based on the mass of lepidolite ore during lepidolite flotation. The mixture was stirred for 3 minutes, aerated and skimmed, with other conditions remaining unchanged.

[0073] Under neutral conditions, compared with the crude concentrate obtained in Application Example 4, the Li2O grade was 0.30%, the recovery rate was 95.62%, the separation efficiency was 16.34%, and there was almost no enrichment effect. The grade of the crude concentrate was close to that of the original ore, with no separation and enrichment effect, and a large amount of gangue floated to the surface.

[0074] Comparative Application Example 5 Based on Comparative Application Example 1, the pH of the lepidolite slurry was adjusted to 5 using 10% H2SO4. Only acidified ODA was added, with the ODA dosage being 300 g / t based on the mass of the lepidolite ore during flotation. Additionally, 30 g / t of No. 2 oil was added as a foaming agent. The mixture was stirred for 3 minutes, aerated, and foamed, while other conditions remained unchanged.

[0075] Compared with the crude concentrate Li2O grade obtained in Application Example 5, the recovery rate was 61.21% and the separation efficiency was 59.48%. The crude concentrate Li2O grade was higher than that of the present invention, but the recovery rate and separation efficiency were significantly weaker than those of the embodiments of the present invention.

[0076] Comparative Application Example 6 Based on Comparative Application Example 1, the pH of the lepidolite slurry was adjusted to 5 using 10% H2SO4. Only acidified COA was added. The amount of COA was 300 g / t, based on the mass of the lepidolite ore during flotation. The mixture was stirred for 3 minutes, aerated and skimmed, with other conditions remaining unchanged.

[0077] Compared with the crude concentrate obtained in Application Example 6, the Li2O grade was 1.13%, the recovery rate was 77.14%, and the separation efficiency was 68.76%. All indicators were weaker than those of the present invention.

[0078] Comparative Application Example 7 Based on Comparative Application Example 1, the pH of the lepidolite slurry was adjusted to 5 using 10% H2SO4. Only acidified DDA was added, with the mass of the lepidolite ore during flotation as the benchmark. The amount of DDA used was 300 g / t. The mixture was stirred for 3 minutes, aerated, and skimmed, while other conditions remained unchanged.

[0079] Compared with the crude concentrate obtained in Application Example 7, the Li2O grade was 0.84%, the recovery rate was 83.44%, and the separation efficiency was 67.78%. All indicators were weaker than those of the present invention.

[0080] Example 2 Based on Example 1, the COA was modified to DDA, while other conditions remained unchanged.

[0081] Comparative Application Example 8 Based on Application Example 1, the cationic combined collector of Example 1 was modified to Example 2. Tap water was used to adjust the slurry to a mass concentration of 33%. DDA, hydrochloric acid (mass concentration of 37%, mass ratio of hydrochloric acid to DDA of 2:1) and an appropriate amount of water were stirred and mixed in a 50°C water bath until homogeneous. Acidified DDA was added to the lepidolite slurry first and stirred for 3 min. Then acidified ODA was added and stirred for 3 min. Aeration and foam removal were performed to obtain a rough concentrate, with other conditions remaining unchanged.

[0082] Compared with the crude concentrate obtained in Application Example 8, the Li2O grade was 0.95%, the recovery rate was 83.67%, and the separation efficiency was 70.09%.

[0083] Example 3 The cationic collector is ODA and COA in a mass ratio of 6.14:1.

[0084] Application Example 4 Based on Application Example 1, the cationic combined collector of Example 1 was modified to the cationic combined collector of Example 3, while other conditions remained unchanged.

[0085] The crude concentrate obtained in Application Example 4 has a Li2O grade of 1.33%, a recovery rate of 87.29%, and a separation efficiency of 81.49%.

[0086] Application Example 5 Based on Application Example 4, the mass concentration of the lepidolite slurry was modified to 33%, the mass ratio of hydrochloric acid to cationic combined collector was 3:1, the amount of cationic combined collector used was 275 g / t based on the mass of lepidolite ore during lepidolite flotation, and other conditions remained unchanged.

[0087] The crude concentrate obtained in Application Example 5 has a Li2O grade of 1%, a recovery rate of 85.59%, and a separation efficiency of 74.48%.

[0088] Example 4 The cationic collector is a combination of ODA and COA in a mass ratio of 19:1.

[0089] Application Example 6 Based on Application Example 1, the cationic combined collector of Example 1 was modified to the cationic combined collector of Example 4. The dosage of the cationic combined collector was 250 g / t, with other conditions remaining unchanged, based on the mass of lepidolite ore during lepidolite flotation.

[0090] The crude concentrate obtained in Application Example 6 has a Li2O grade of 1.38%, a recovery rate of 79.60%, and a separation efficiency of 74.71%.

[0091] Example 5 The cationic collector is a combination of ODA and DDA in a mass ratio of 16.7:1.

[0092] Application Example 7 The cationic combined collector from Example 5 was applied to the flotation of lepidolite, and the steps are as follows: DDA and ODA were mixed, and then hydrochloric acid with a mass concentration of 36% (the mass ratio of hydrochloric acid to cationic combined collector was 4:1) and an appropriate amount of water were added. The mixture was stirred in a water bath at 50°C for 45 minutes to obtain a cationic combined collector solution with a total mass concentration of 2% for ODA and DDA. Lithium mica ore (containing 0.24% Li2O, with lithium-containing minerals mainly consisting of lepidolite and muscovite, the mineral content ratio of lepidolite to muscovite is 1:2, and the yield of -0.074mm particle size is 28.65%) was added to an XFD-0.5L flotation machine, and tap water was used to adjust the slurry to a mass concentration of 38% to obtain lepidolite slurry. A cationic combined collector solution was added to the lepidolite slurry, stirred for 3 minutes, and aerated and skimmed to obtain a rough concentrate; wherein, based on the mass of lepidolite ore during lepidolite flotation, the amount of cationic combined collector was 250 g / t.

[0093] The crude concentrate obtained in Application Example 7 has a Li2O grade of 1.29%, a recovery rate of 80.81%, and a separation efficiency of 74.66%.

[0094] Example 6 The cationic collector is a combination of ODA and COA in a mass ratio of 12:1.

[0095] Comparative Application Example 9 The cationic combined collector from Example 6 was applied to the flotation of lepidolite, and the steps are as follows: Based on Comparative Application Example 1, acidified ODA was first added and stirred for 3 minutes, followed by acidified COA and stirred for 3 minutes. The amount of the cationic combined collector was 325 g / t, with other conditions remaining unchanged, based on the mass of lepidolite ore during lepidolite flotation.

[0096] Compared with the crude concentrate obtained in Application Example 9, the Li2O grade was 0.95%, the recovery rate was 77.16%, and the separation efficiency was 65.08%, which is low.

[0097] Example 7 The cationic collector is a combination of ODA and DDA in a mass ratio of 12:1.

[0098] Comparative Application Example 10 The cationic combined collector from Example 7 was applied to the flotation of lepidolite, and the steps are as follows: Based on Comparative Application Example 1, acidified ODA was added first, and the mixture was stirred for 3 minutes. Then, acidified DDA was added. The amount of the cationic combined collector was 325 g / t, with other conditions remaining unchanged, based on the mass of lepidolite ore during lepidolite flotation.

[0099] Compared with the crude concentrate obtained in Application Example 10, the Li2O grade was 0.86%, the recovery rate was 83.36%, and the separation efficiency was 67.55%, which is low.

[0100] As can be seen from the above embodiments and comparative examples, the cationic combined collector provided by the present invention can improve the flotation and separation effect of lepidolite when used for lepidolite flotation.

[0101] The above description is only a preferred embodiment of the present invention. It should be noted that for those skilled in the art, several improvements and modifications can be made without departing from the principle of the present invention, and these improvements and modifications should also be considered within the scope of protection of the present invention.

Claims

1. A cationic combined collector, comprising octadecylamine and an auxiliary component; The excipients include cocoylamine and / or dodecylamine; The mass ratio of the octadecylamine to the excipient is (5~20):

1.

2. The cationic combined collector according to claim 1, characterized in that, The mass ratio of the octadecylamine to the excipient is (6~15):

1.

3. A cationic combined collector solution, obtained by mixing the cationic combined collector of claim 1 or 2, an acid, and water.

4. The cationic combined collector solution according to claim 3, characterized in that, The mass concentration of the acid is 36-38%, and the mass ratio of the acid to the cationic collector is (1-5):

1.

5. The cationic combined collector solution according to claim 3, characterized in that, The total mass concentration of octadecylamine and cofactors in the cationic combined collector solution is 1-10%.

6. The application of the cationic combined collector as described in claim 1 or 2 in the flotation of lepidolite.

7. The application according to claim 6, characterized in that, Based on the mass of lepidolite ore during lepidolite flotation, the dosage of the cationic combined collector is 200~500g / t.

8. The application according to claim 6 or 7, characterized in that, The applications include: Lithium mica ore is slurry prepared to obtain lithium mica slurry; A cationic combined collector, acid, and water are mixed to obtain a cationic combined collector solution; The cationic combined collector solution and lepidolite slurry are mixed and then subjected to flotation.

9. The application according to claim 8, characterized in that, The mass concentration of the lithium mica slurry is 25-40%.

10. The application according to claim 6 or 7, characterized in that, The applications include: Lithium mica ore is slurry prepared to obtain lithium mica slurry; Octadecylamine, acid, and water are mixed to obtain a first ammonium salt solution; The auxiliary components, acid, and water are mixed to obtain a second ammonium salt solution; The first ammonium salt solution and the second ammonium salt solution are mixed to obtain a cationic combined collector solution; The lithium mica slurry and the cationic combined collector solution are mixed and then subjected to flotation.