Method for separating and extracting titanium concentrate from aluminiferous rock series ore

Abstract

The invention relates to the technical field of aluminiferous rock series ore processing, in particular to a method for separating and extracting titanium concentrate from aluminiferous rock series ore. The aluminiferous rock series ores comprise titanium minerals, aluminum minerals and silicon minerals, and the method comprises the steps that the aluminiferous rock series ores are sequentially subjected to crushing and first grinding, and first ore pulp is obtained; grading the first ore pulp to obtain fine particle ore pulp and coarse particle ore pulp; the coarse particle ore pulp is subjected to second grinding, and second ore pulp is obtained; mixing the fine particle ore pulp with the second ore pulp to obtain third ore pulp; the third ore pulp is subjected to desiliconization reverse flotation through an acid-base regulator and a first collecting agent, part of silicon minerals are removed, and desiliconized rough concentrate pulp is obtained; wherein the first collecting agent comprises dodecyl trimethyl ammonium chloride and hexadecyl trimethyl ammonium bromide; the desiliconized rough concentrate pulp is subjected to microbubble flotation through an inhibitor, an activating agent and a second collecting agent, aluminum minerals and residual silicon minerals are removed, and titanium concentrate is obtained; wherein the second collecting agent comprises (2-hydroxy-2-methyl propyl) (phenyl) phosphinic acid, diphenyl phosphinic acid and diisooctyl phosphinic acid.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of processing of aluminum-bearing rock series ore, and particularly relates to a method for separating and extracting titanium concentrate from aluminum-bearing rock series ore. BACKGROUND

[0002] Titanium and its alloys have high strength, low density, corrosion resistance, high temperature resistance and other characteristics, and thus are distinguished from many metal materials, and are widely used in the fields of aerospace, chemical industry, metallurgy, medical treatment and the like. This makes titanium a metal material with great strategic value. The aluminum-bearing rock series ore is represented by rutile and anatase, and the rutile or anatase is almost composed of high-purity TiO2, which makes the rutile or anatase a high-quality raw material for high-end titanium materials.

[0003] However, the rutile or anatase generally contains titanium minerals, aluminum minerals and silicon minerals, and the conventional sorting method is difficult to realize effective separation among the titanium minerals, the aluminum minerals and the silicon minerals, and the yield and grade of the titanium concentrate obtained are low. SUMMARY

[0004] The present application provides a method for separating and extracting titanium concentrate from aluminum-bearing rock series ore, so as to solve the technical problem of how to simultaneously improve the yield and grade of the titanium concentrate extracted from the aluminum-bearing rock series ore. In a first aspect, the embodiments of the present application provide a method for separating and extracting titanium concentrate from aluminum-bearing rock series ore, the aluminum-bearing rock series ore comprising titanium minerals, aluminum minerals and silicon minerals, and the method comprising: crushing and first grinding the aluminum-bearing rock series ore in sequence to obtain a first ore slurry; grading the first ore slurry to obtain a fine particle ore slurry and a coarse particle ore slurry; second grinding the coarse particle ore slurry to obtain a second ore slurry; mixing the fine particle ore slurry and the second ore slurry to obtain a third ore slurry; using an acid-base regulator, a first collector to perform desiliconization reverse flotation on the third ore slurry to remove part of the silicon minerals, to obtain a desiliconization coarse concentrate slurry; wherein the first collector comprises dodecyltrimethylammonium chloride and hexadecyltrimethylammonium bromide; using an inhibitor, an activator and a second collector to perform micro-bubble flotation on the desiliconization coarse concentrate slurry to remove the aluminum minerals and the remaining silicon minerals, to obtain the titanium concentrate; wherein the second collector comprises (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid, diphenyl phosphinic acid and diisooctyl phosphinic acid.

[0005] Optionally, the first collector comprises, in terms of mass fraction: dodecyltrimethylammonium chloride: 60% to 80%, and hexadecyltrimethylammonium bromide: 20% to 40%; and / or The second collector is, in mass fraction, (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid: 30% to 40%, diphenyl phosphinic acid: 30% to 45%, and diisooctyl phosphinic acid: 15% to 30%.

[0006] Optionally, the mass m2 of the second collector and the mass m1 of the dry substance of the desilication rough concentrate pulp satisfy: m2:m1=(800 to 1500):1000000.

[0007] Optionally, the mass m4 of the first collector and the mass m3 of the dry substance of the third pulp satisfy: m4:m3=(600 to 1200):1000000.

[0008] Optionally, the acid-base regulator is sulfuric acid and / or hydrochloric acid; and / or The inhibitor includes sodium fluorosilicate and / or water glass; and / or The activator includes at least one of lead acetate, lead nitrate, copper sulfate, copper nitrate, and bismuth nitrate.

[0009] Optionally, the mass m5 of the inhibitor and the mass m1 of the dry substance of the desilication rough concentrate pulp satisfy: m5:m1=(500 to 1500):1000000; and / or The mass m6 of the activator and the mass m1 of the dry substance of the desilication rough concentrate pulp satisfy: m6:m1=(200 to 800):1000000.

[0010] Optionally, the target particle size of the classification is 0.40 mm to 0.50 mm.

[0011] Optionally, the mass of the first fine particles in the first pulp is 60% to 80% of the mass of the first pulp, the particle size of the first fine particles being less than 0.045 mm; and / or The mass of the second fine particles in the second pulp is 80% to 90% of the mass of the second pulp, the particle size of the second fine particles being less than 0.045 mm.

[0012] Optionally, the initial pH of the desilication reverse flotation is 2 to 5.

[0013] Optionally, the aluminum-bearing rock series ore includes a di-aluminum trioxide component, a silicon dioxide component, and a titanium dioxide component; the mass of the di-aluminum trioxide component is 30% to 45% of the mass of the aluminum-bearing rock series ore, the mass of the silicon dioxide component is 30% to 40% of the mass of the aluminum-bearing rock series ore, and the mass of the titanium dioxide component is 2% to 4% of the mass of the aluminum-bearing rock series ore.

[0014] The above technical solution provided by the embodiments of the present application has the following advantages compared with the prior art. The method for separating and extracting titanium concentrate from aluminum-bearing rock series ore provided by the embodiments of the present application first performs first grinding, grading and second grinding on the aluminum-bearing rock series ore, so that the dissociation degree between titanium minerals, silicon minerals and aluminum minerals and the yield of titanium minerals can be considered, and the monomer titanium minerals are enriched in the third ore slurry. In addition, the acid-base regulator and the first collector are used to perform desiliconization reverse flotation on the third ore slurry, so that the interference of silicon minerals on the extraction of titanium concentrate in micro-bubble flotation can be reduced, and the basic yield of titanium concentrate can be ensured. At the same time, the acid-base regulator can ensure that the third ore slurry is in an acidic environment, and the collecting performance of the first collector on silicon minerals can be ensured. In addition, the micro-bubble flotation technology can use the depressant, the activator and the second collector to efficiently separate and recover the titanium minerals in the desiliconization rough concentrate slurry obtained by desiliconization reverse flotation. Specifically, the hydroxyl group of (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid in the second collector can form a stable hydrophobic film on the surface of the titanium minerals, the hydrophobic chain of diphenyl phosphinic acid can avoid the collecting effect of the second collector on aluminum minerals and silicon minerals, and the long-chain hydrophobic group of diisooctyl phosphinic acid can improve the yield of the micro-fine particle level titanium minerals in the desiliconization rough concentrate slurry. The addition of the depressant can further inhibit the activity of silicon minerals and aluminum minerals, and reduce the possibility of the aluminum minerals and silicon minerals floating in the micro-bubble flotation process. In addition, the use of the activator can increase the adsorption sites on the surface of the titanium minerals, strengthen the adsorption stability, and further improve the yield of the titanium minerals in the micro-bubble flotation process. BRIEF DESCRIPTION OF DRAWINGS

[0015] The accompanying drawings, which are incorporated into and form a part of the specification, illustrate preferred embodiments of the present application and, together with the description, serve to explain the principles of the application.

[0016] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the drawings needed to be used in the embodiments or the prior art description will be briefly introduced as follows. Obviously, for those skilled in the art, other drawings can also be obtained from these drawings without creative labor.

[0017] Figure 1 A flowchart of a method for separating and extracting titanium concentrate from aluminum-bearing rock series ore provided by the embodiments of the present application is shown in the figure. Figure 2 An actual flowchart of a method for separating and extracting titanium concentrate from aluminum-bearing rock series ore provided by the embodiments of the present application is shown in the figure. DETAILED DESCRIPTION

[0018] In order to make the purposes, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application will be described clearly and completely below with reference to the drawings in the embodiments of the present application. Obviously, the described embodiments are some but not all of the embodiments of the present application. Based on the embodiments in the present application, all other embodiments obtained by those of ordinary skill in the art without creative work belong to the scope of protection of the present application.

[0019] The range descriptions described in the present application, such as numerical range, ratio range, etc., all include all possible sub-ranges and single values within the range, for example, the range description of "1 to 6" or "1~6" covers all sub-ranges (such as 1 to 3, 2 to 5, etc.) and single numbers (such as 1, 2, 3, 4, 5, 6) between 1 and 6. Unless otherwise specified, the terms "include", etc. used in the present application mean "include but not limited to"; the relationship terms "first", "second", etc. are only used to distinguish different entities or operations, and do not imply actual sequence or relationship; "and / or" means that multiple cases can exist alone or simultaneously; "at least one", "multiple", "at least one", etc. refer to any combination of the corresponding objects, including single or multiple combinations of objects. The proportional relationship involved in the present application, such as mass ratio, molar ratio, etc., should be understood as the corresponding relationship between the front and the back in the proportional form according to the sequence of description. The raw materials, reagents, instruments and equipment used in the present application can be purchased or prepared by existing methods.

[0020] It should be noted that the technical problems existing in the process of separating and extracting titanium from the aluminum-bearing rock series ore at present are: (1) In the aluminum-bearing rock series ore, complex intergrowth relationships are formed between titanium minerals and associated minerals such as aluminum minerals and silicon minerals, and the intergrowth particle size of titanium minerals in associated minerals is very fine, which makes it difficult to fully dissociate titanium minerals from associated minerals, and over-grinding phenomenon is prone to occur in the separation process of titanium minerals and associated minerals. (2) In the aluminum-bearing rock series ore, the physical and chemical properties of titanium minerals and associated minerals such as aluminum minerals and silicon minerals are similar, and in the separation process of the aluminum-bearing rock series ore, it is difficult to effectively separate titanium minerals from associated minerals by conventional separation methods. Therefore, the methods for separating and extracting titanium from the aluminum-bearing rock series ore at present generally have the problem of low yield of titanium concentrate.

[0021] Based on the problem of low yield and low grade of titanium concentrate in the method for extracting titanium from the aluminum-bearing rock series ore at present, the present application proposes the following technical solutions: Figure 1 An exemplary flowchart of a method for separating and extracting titanium concentrate from an aluminum-bearing rock series ore provided by the embodiments of the present application is shown; Figure 2An actual flow diagram of a method for separating and extracting titanium concentrate from aluminum-bearing rock series ore is exemplarily shown; As Figure 1 shown, the method for separating and extracting titanium concentrate from aluminum-bearing rock series ore provided by the embodiment of the application includes titanium minerals, aluminum minerals and silicon minerals, and the method includes: S1. The aluminum-bearing rock series ore is sequentially crushed and first ground to obtain a first ore slurry; S2. The first ore slurry is classified to obtain a fine particle ore slurry and a coarse particle ore slurry; S3. The coarse particle ore slurry is second ground to obtain a second ore slurry; S4. The fine particle ore slurry and the second ore slurry are mixed to obtain a third ore slurry; S5. The third ore slurry is subjected to desiliconization reverse flotation using an acid-base regulator, a first collector to remove part of the silicon minerals to obtain a desiliconized coarse concentrate slurry; wherein the first collector includes dodecyltrimethylammonium chloride and hexadecyltrimethylammonium bromide; S6. The desiliconized coarse concentrate slurry is subjected to micro-bubble flotation using an inhibitor, an activator and a second collector to remove the aluminum minerals and the remaining silicon minerals to obtain titanium concentrate; wherein the second collector includes (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid, diphenyl phosphinic acid and diisooctyl phosphinic acid.

[0022] It should be noted that the current method for extracting titanium from aluminum-bearing rock series ore is: preparation of a flotation recovery reagent for bauxite associated anatase and application method thereof. The flotation recovery reagent is applied to the flotation process of bauxite associated anatase. The flotation process includes a pretreatment process, a direct flotation process and a gravity separation process. This process can effectively recover titanium minerals with a particle size of 0.02mm to 0.03mm associated with bauxite. However, the particle size of titanium minerals in aluminum-bearing rock series ore is generally less than 0.01mm. In the primary grinding stage of the pretreatment process, the aluminum-bearing rock series ore is prone to over-grinding, resulting in excessive surface energy of the fine particles produced in the primary grinding stage. The fine particles are easily combined with the adsorption reagent in the flotation recovery reagent, reducing the selectivity of the collector in the flotation recovery reagent. In the direct flotation process and the gravity separation process, the kinetic energy is insufficient in the collision process between the bubbles and the fine particles, and the fine particles cannot break through the hydration film on the surface of the fine particles, resulting in poor separation of the titanium minerals.

[0023] It should be noted that the first grinding can be rod grinding. The first grinding can preliminarily dissociate the aluminum minerals, silicon minerals and titanium minerals in the crushed aluminum-bearing rock series ore. At the same time, the first grinding can also control the particle size distribution of the titanium minerals to avoid over-grinding and the formation of fine mud of the titanium minerals.

[0024] It should be noted that the second grinding can be a ball mill. The second grinding can finely grind the titanium minerals with poor dissociation degree in the coarse particle slurry, realize complete dissociation of aluminum minerals, silicon minerals and titanium minerals, and make the fine particle titanium minerals enter the second slurry.

[0025] It should be noted that the combination of the first grinding and the second grinding can avoid over-grinding of titanium minerals caused by direct grinding, so that titanium minerals of different particle sizes can enter the second slurry as high-quality raw materials for subsequent desiliconization reverse flotation.

[0026] It should be noted that the third slurry can also be mineralized before desiliconization reverse flotation, so that the third slurry, the acid-base regulator and the first collector are fully mixed.

[0027] It should be noted that the desiliconization rough concentrate slurry can also be mineralized before micro-bubble flotation, so that the desiliconization rough concentrate slurry, the depressant, the activator and the second collector are fully mixed.

[0028] It should be noted that the desiliconization reverse flotation process can be one desiliconization roughing, one desiliconization scavenging and two desiliconization cleanings. In one desiliconization roughing, the acid-base regulator is used to adjust the pH of the first slurry, and then part of the first collector is used, and the remaining first collector is added in one desiliconization scavenging and two desiliconization cleanings. Among them, in the three desiliconization cleanings, the amount of the first collector added in the first desiliconization cleaning is generally greater than that in the second desiliconization cleaning, so as to ensure that most of the silicon minerals in the first slurry are removed by desiliconization reverse flotation.

[0029] It should be noted that the micro-bubble flotation process can be one micro-bubble roughing, one micro-bubble scavenging and three micro-bubble cleanings. In one micro-bubble roughing, the second acid-base regulator is used to adjust the pH of the second slurry, and then the depressant, the activator and part of the second collector are added for roughing, and the remaining second collector is added in one micro-bubble scavenging and three micro-bubble cleanings. Among them, in the three micro-bubble cleanings, the amount of the second collector added in the second micro-bubble cleaning is generally the same as that in the third micro-bubble cleaning, but the amount of the second collector added in the first micro-bubble cleaning is greater than that in the second micro-bubble cleaning or the third micro-bubble cleaning, so as to ensure that the fine particle titanium minerals can be floated by micro-bubble flotation after the three micro-bubble cleanings.

[0030] It should be noted that the micro-bubble flotation will also obtain a micro-bubble tailing in addition to the titanium concentrate, and the desiliconization reverse flotation will also obtain a desiliconization tailing in addition to the desiliconization rough concentrate slurry. The desiliconization tailing obtained by the desiliconization reverse flotation and the micro-bubble tailing obtained by the micro-bubble flotation can be combined to obtain a tailing enriched with aluminum minerals and silicon minerals.

[0031] It should be noted that the method for separating and extracting titanium concentrate from aluminum-bearing rock series ore provided by the embodiments of the present application solves the traditional technical problem of mutual restriction between yield and grade of titanium concentrate in the process of separating and extracting titanium concentrate from aluminum-bearing rock series ore through the process structure optimization strategy of staged regrinding + two-stage flotation, combined with the precise adaptation strategy of reagent of cation desilication + phosphinic acid titanium capture + microbubble strengthening recovery. The specific mechanism is as follows: 1. Stage grinding and classification closed circuit: considering both dissociation degree and recovery rate.

[0032] (1) Avoid overgrinding and mudification: through the first grinding and classification of the staged grinding method, the dissociated fine particle size titanium minerals can be promptly separated, avoiding the overgrinding of coarse particle slurry in the second grinding stage, which causes the overgrinding of fine particle size titanium minerals to form titanium mineral mud. Titanium mineral mud can seriously deteriorate desilication reverse flotation and microbubble flotation, resulting in the loss of part of the titanium minerals in the tailings, reducing the yield of titanium concentrate.

[0033] (2) Strengthening coarse particle dissociation: the coarse particle slurry obtained by the first grinding and classification contains coarse particle intergrowths, which can be further dissociated by the second grinding to improve the monomer dissociation degree of titanium minerals and obtain high-dissociation-degree second slurry, laying the foundation for obtaining high-grade titanium concentrate. At the same time, the second grinding can optimize the particle size distribution of the final titanium concentrate, meeting the separation requirements of subsequent desilication reverse flotation and microbubble flotation, and maximizing the reduction of titanium mineral loss, while simultaneously improving the yield and grade of titanium minerals.

[0034] 2. Two-stage flotation combined with desilication reverse flotation and microbubble flotation: realizing the upgrading and quantity preservation of titanium minerals.

[0035] (1) First stage flotation (desilication reverse flotation): using quaternary ammonium salt cationic collectors (dodecyltrimethylammonium chloride and hexadecyltrimethylammonium bromide) can preferentially make silicon minerals (such as kaolinite, illite, pyrophyllite, etc.) float. This step directly reduces the amount of silicon minerals entering the subsequent microbubble flotation, improves the grade of desilication rough concentrate slurry entering the microbubble flotation, and reduces the interference of silicon minerals on the extraction of titanium concentrate in the microbubble flotation. In addition, desilication reverse flotation has little effect on titanium minerals, avoiding the misplacement of titanium minerals in the microwave flotation process, and ensuring the basic yield of titanium concentrate.

[0036] (2) Second-stage flotation (micro-bubble flotation): The micro-bubble flotation uses a secondary phosphinic acid collector (such as (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid, diphenyl phosphinic acid, and diisooctyl phosphinic acid) that has strong selectivity and adsorption capacity for titanium minerals, can improve the collecting capacity of the micro-bubble flotation for fine particles of titanium minerals, and significantly improve the recovery rate of fine particles of titanium minerals. Meanwhile, the strong selectivity of the secondary phosphinic acid collector can ensure that aluminum minerals and silicon minerals in the desiliconized rough concentrate slurry are not entrained and floated in the micro-bubble flotation process, thereby ensuring the grade of the titanium concentrate.

[0037] 3. Precise adaptation of the medication regimen: Strengthening the selective recovery of titanium minerals.

[0038] (1) First collector: The first collector of quaternary ammonium salt cations can specifically act on silicon minerals but not on titanium minerals, so that the silicon minerals float while the titanium minerals remain in the third slurry phase, thereby achieving selective desiliconization of the desiliconization reverse flotation.

[0039] (2) Second collector: The secondary phosphinic acid compound has strong chemical chelation with metal titanium ions on the surface of the aluminum-bearing rock series ore, so that the second collector can firmly adsorb the titanium minerals in the aluminum-bearing rock series ore. Compared with traditional fatty acid collectors, the second collector has higher selectivity for titanium minerals, can effectively repel residual aluminum minerals and silicon minerals, and can improve the grade of the titanium concentrate produced by the micro-bubble flotation while ensuring a high recovery rate of the titanium minerals.

[0040] 4. Progressive optimization of process logic: Overall yield improvement.

[0041] In the case of pursuing the yield of the titanium concentrate, the conventional single positive flotation is prone to result in a low grade of the titanium concentrate due to an insufficient enrichment ratio of the titanium concentrate. In the case of pursuing the grade of the titanium concentrate, the titanium minerals are lost due to excessive cleaning, resulting in a decrease in the yield of the titanium minerals.

[0042] The method provided in the application decouples the purposes of improving the quality and ensuring the quantity of the titanium concentrate through the desiliconization reverse flotation: a large amount of silicon minerals is removed at a low cost through the first grinding, classification, and second grinding to improve the grade of the titanium concentrate, and the third slurry enriched with titanium minerals is subjected to desiliconization reverse flotation and efficient collection by micro-bubble flotation, which can improve the yield of the titanium concentrate. The method provided in the application takes the optimization of the recovery timing of the titanium minerals as the core, avoids the trade-off between the yield and the grade of the titanium concentrate, and thus simultaneously improves the yield and the grade of the titanium concentrate.

[0043] In some optional embodiments, the first collector includes, in terms of mass fraction, 60% to 80% of dodecyltrimethylammonium chloride and 20% to 40% of hexadecyltrimethylammonium bromide; and / or The second collector comprises, by mass fraction, (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid: 30% to 40%, diphenyl phosphinic acid: 30% to 45%, and diisooctyl phosphinic acid: 15% to 30%.

[0044] In these embodiments, dodecyl trimethyl ammonium chloride with a mass fraction of 60% to 80% and hexadecyl trimethyl ammonium bromide with a mass fraction of 20% to 40% can provide sufficient quaternary ammonium salt cations for the first collector, which can specifically capture the silicon minerals, in particular: the short carbon chain of dodecyl trimethyl ammonium chloride can quickly diffuse on the surface of the silicon minerals, and can quickly cover the surface of the silicon minerals, while the long carbon chain of hexadecyl trimethyl ammonium bromide can provide a longer hydrophobic chain on the surface of the silicon minerals, and can significantly improve the hydrophobicity of the silicon minerals, thus the combination of dodecyl trimethyl ammonium chloride and hexadecyl trimethyl ammonium bromide can have a synergistic effect of rapid adsorption + enhanced hydrophobicity, and can achieve specific and efficient collection of the silicon minerals.

[0045] In addition, (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid with a mass fraction of 30% to 40% and diphenyl phosphinic acid with a mass fraction of 30% to 45% can provide sufficient phosphinic acid groups for the second collector, which can selectively adsorb titanium exposed on the surface of the titanium minerals in the desiliconized rough concentrate slurry, so that the second collector can firmly adhere to the surface of the titanium minerals; in addition, the phenyl and alkyl groups in (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid and diphenyl phosphinic acid can act as nonpolar groups, which can impart a certain hydrophobicity to the surface of the titanium minerals in the desiliconized rough concentrate slurry, so that the titanium minerals are more easily attached to the surface of the gas bubbles in the microbubble flotation process; in addition, the hydroxyl group of (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid can improve the hydrophilicity of the second collector, so that the second collector can better dissolve in the desiliconized rough concentrate slurry. In addition, diisooctyl phosphinic acid with a mass fraction of 15% to 30% can improve the performance of the second collector, on the one hand, the phosphinic acid groups of diisooctyl phosphinic acid can assist the phosphinic acid groups of (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid and diphenyl phosphinic acid, further improving the adhesion of the second collector to the surface of the titanium minerals, and improving the total amount of adsorption of the second collector to the titanium minerals, on the other hand, the long carbon chain nonpolar group of diisooctyl phosphinic acid can further increase the hydrophobic area of the surface of the titanium minerals, and strengthen the binding stability of the titanium minerals and the collector, which is finally beneficial to improving the yield of the fine particle grade titanium minerals.

[0046] The mass fraction of the dodecyl trimethyl ammonium chloride can be 60%, 61%, 62%, 63%, 64%, 65%, 70%, 75%, or 80%.

[0047] The mass fraction of the cetyltrimethylammonium bromide can be 20%, 21%, 22%, 23%, 24%, 25%, 30%, 35%, or 40% The mass fraction of the (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid can be 30%, 31%, 32%, 33%, 34%, 35%, 36%, 37%, 38%, 39%, or 40%.

[0048] The mass fraction of the diphenyl phosphinic acid can be 30%, 31%, 32%, 33%, 34%, 35%, 40%, or 45%.

[0049] The mass fraction of the diisooctyl phosphinic acid can be 15%, 16%, 17%, 18%, 19%, 20%, 25%, or 30%.

[0050] It should be noted that, due to the differences in the adaptability of quaternary ammonium salt cations with different carbon chain lengths to the acid-base environment and ionic strength of the third ore pulp, and the first collector is matched between dodecyltrimethylammonium chloride and cetyltrimethylammonium bromide, the first collector can widen the tolerance range of the first collector to various environments in the third ore pulp by the different carbon chain lengths of dodecyltrimethylammonium chloride and cetyltrimethylammonium bromide, reduce the fluctuation of the collecting effect of the first collector caused by the fluctuation of the acid-base degree or the interference of impurity ions, and improve the stability of the first collector. In addition, there are slight differences in the selective adsorption of dodecyltrimethylammonium chloride and cetyltrimethylammonium bromide to silicate minerals and titanium minerals, and by adjusting the mass fraction between dodecyltrimethylammonium chloride and cetyltrimethylammonium bromide, the specific adsorption capacity of the first collector to silicate minerals can be enhanced, thereby improving the separation efficiency between silicate minerals and titanium minerals and aluminum minerals in the desiliconization reverse flotation process. In addition, compared with the use of dodecyltrimethylammonium chloride and cetyltrimethylammonium bromide alone, the use of dodecyltrimethylammonium chloride and cetyltrimethylammonium bromide to form the first collector can reduce the reagent usage amount of the first collector in the desiliconization reverse flotation process through the synergistic effect of dodecyltrimethylammonium chloride and cetyltrimethylammonium bromide.

[0051] It should be noted that, compared with the conventional flotation titanium mineral collector, (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid and diphenyl phosphinic acid have higher solubility in the second ore pulp, which can make the second collector quickly dissolve and form an effective mass concentration in the second ore pulp, so that the second collector can fully contact with the surface of the titanium minerals, avoiding the problem of insufficient adsorption between the titanium minerals and the second collector due to the slow dissolution of the second collector.

[0052] It should be noted that the synergistic complementary action of the collecting ability is formed by the intermolecular interaction between (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid, diphenyl phosphinic acid and diisooctyl phosphinic acid and the synergistic regulation on the surface properties of titanium minerals, so that the efficient separation and recovery of the titanium minerals in the second ore slurry in the microbubble flotation process is realized, and the yield of titanium extracted from the aluminum-bearing rock series ore is improved.

[0053] In some optional embodiments, the mass m2 of the second collector and the mass m1 of the dry substance of the desilicated rough concentrate slurry satisfy: m2:m1= (800 to 1500):1000000.

[0054] In these embodiments, the second collector with a mass ratio of (800 to 1500):1000000 of the dry substance of the desilicated rough concentrate slurry can be fully contacted and adsorbed with the surface of the titanium minerals through the synergistic effect of chemical adsorption complementation, hydrophobic synergistic enhancement and selective improvement between (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid, diphenyl phosphinic acid and diisooctyl phosphinic acid, which is conducive to the subsequent microbubble flotation and improves the yield of titanium concentrate extracted from the aluminum-bearing rock series ore.

[0055] The mass m2 of the second collector can be 800, 900, 1000, 1100, 1200, 1300, 1400 or 1500.

[0056] It should be noted that when the mass m2 of the second collector and the mass m1 of the dry substance of the desilicated rough concentrate slurry satisfy: m2:m1<800:1000000, the amount of the second collector is too small, and a small amount of the second collector is difficult to contact and adsorb with the surface of the titanium minerals, which is not conducive to the subsequent microbubble flotation and reduces the yield of the titanium concentrate; when the mass m2 of the second collector and the mass m1 of the dry substance of the desilicated rough concentrate slurry satisfy: m2:m1>1500:1000000, the amount of the second collector is too large, and too much second collector will adsorb aluminum minerals or silicon minerals, so that the titanium concentrate obtained by microbubble flotation is mixed with silicon minerals and aluminum minerals, thereby reducing the grade of the titanium concentrate.

[0057] In some optional embodiments, the mass m4 of the first collector and the mass m3 of the dry substance of the third ore slurry satisfy: m4:m3= (600 to 1200):1000000.

[0058] In these embodiments, the first collector with a mass ratio of (600 to 1200):1000000 of the dry substance of the third ore slurry can be quickly adsorbed and synergistically enhanced by hydrophobicity through the compounding of dodecyltrimethylammonium chloride and hexadecyltrimethylammonium bromide, so that the specific and efficient collection of silicon minerals is realized.

[0059] The mass m4 of the first collector can be 600, 700, 800, 900, 1000, 1100, or 1200.

[0060] It should be noted that, in the case where the mass m4 of the first collector and the mass m3 of the dry substance of the third ore slurry satisfy: m4:m3<600:1000000, the amount of the first collector is too small, and it is difficult for a small amount of the first collector to contact and adsorb to the surface of the silicon mineral, which is not conducive to the floating removal of the silicon mineral and reduces the grade of the titanium concentrate; in the case where the mass m4 of the first collector and the mass m3 of the dry substance of the third ore slurry satisfy: m4:m3>1200:1000000, the amount of the first collector is too large, and an excessive amount of the first collector not only contacts and adsorbs to the surface of the silicon mineral, but also contacts and adsorbs to the surface of the titanium mineral, so that the desiliconization flotation removes part of the titanium mineral, reducing the yield of the titanium concentrate.

[0061] In some optional embodiments, the acid-base regulator is sulfuric acid and / or hydrochloric acid; and / or The depressant includes sodium fluorosilicate and / or water glass; and / or The activator includes at least one of lead acetate, lead nitrate, copper sulfate, copper nitrate, and bismuth nitrate.

[0062] In these embodiments, the use of the acid-base regulator including sulfuric acid and / or hydrochloric acid can regulate the pH value of the third ore slurry, so that the third ore slurry is in an acidic environment, and the third ore slurry in the acidic environment can make the surface of the silicon mineral have a stable negative charge, while the surface of the titanium mineral has a positive charge. The silicon mineral with a negative charge can combine with the quaternary ammonium salt cation provided by the dodecyltrimethylammonium chloride and the cetyltrimethylammonium bromide in the first collector, so as to complete the adsorption of the silicon mineral to the first collector and achieve the removal of the silicon mineral in the third ore slurry. In addition, the use of the depressant including sodium fluorosilicate and / or water glass can enhance the hydrophilicity of the aluminum mineral and the silicon mineral in the aluminum-bearing rock series ore, and reduce the floating probability of the aluminum mineral and the silicon mineral in the desiliconization rough concentrate slurry in the micro-bubble flotation process. In addition, the use of the activator including at least one of lead acetate, lead nitrate, copper sulfate, copper nitrate, and bismuth nitrate can provide a large amount of activation ions (such as lead, copper, and bismuth), which can be adsorbed to the surface of the titanium mineral in the desiliconization rough concentrate slurry, increasing the adsorption sites of the titanium mineral to the second collector.

[0063] In some optional embodiments, the mass m5 of the depressant and the mass m1 of the dry substance of the desiliconization rough concentrate slurry satisfy: m5:m1=(500 to 1500):1000000; and / or The mass m6 of the activator and the mass m1 of the dry substance of the desilicated rough concentrate slurry satisfy: m6:m1=(200 to 800):1000000.

[0064] In these embodiments, the inhibitor with a mass ratio of (500 to 1500):1000000 of the dry substance of the desilicated rough concentrate slurry can enhance the hydrophilicity of the surfaces of the aluminum minerals and the silicon minerals in the desilicated rough concentrate slurry, and inhibit the floating of the aluminum minerals and the silicon minerals in the desilicated rough concentrate slurry in the micro-bubble flotation process. In addition, the activator with a mass ratio of (200 to 800):1000000 of the dry substance of the desilicated rough concentrate slurry can provide a large amount of activated ions, which can be adsorbed on the surfaces of the titanium minerals in the desilicated rough concentrate slurry, and increase the adsorption sites of the titanium minerals and the collector in the desilicated rough concentrate slurry.

[0065] The mass m5 of the inhibitor can be 500, 600, 700, 800, 900, 1000, 1100, 1200, 1300, 1400, or 1500.

[0066] The mass m6 of the activator can be 200, 250, 300, 350, 400, 450, 500, 550, 600, 650, 700, 750, or 800.

[0067] It should be noted that, in the case where the mass m5 of the inhibitor and the mass m2 of the dry substance of the desilicated rough concentrate slurry satisfy: m5:m2<500:1000000, the inhibitor is insufficient, which leads to the easy floating of the silicon minerals and the aluminum minerals in the desilicated rough concentrate slurry in the micro-bubble flotation process, so that the silicon minerals and the aluminum minerals are mixed in the titanium concentrate obtained by the micro-bubble flotation, thereby reducing the grade of the titanium concentrate; in the case where the mass m5 of the inhibitor and the mass m1 of the dry substance of the desilicated rough concentrate slurry satisfy: m3:m1>1500:1000000, the inhibitor is excessive, and part of the fine particles of the titanium minerals in the desilicated rough concentrate slurry are inhibited, thereby reducing the yield of the titanium concentrate.

[0068] It should be noted that, in the case where the mass m6 of the activator and the mass m2 of the dry substance of the desilicated rough concentrate slurry satisfy: m6:m2<200:1000000, the activator is insufficient, which reduces the activation effect of the titanium minerals in the desilicated rough concentrate slurry, thereby reducing the yield of the titanium concentrate; in the case where the mass m6 of the activator and the mass m2 of the dry substance of the desilicated rough concentrate slurry satisfy: m6:m2>800:1000000, the activator is excessive, which affects the performance of the second collector, and reduces the collection amount of the titanium minerals, thereby reducing the yield of the titanium concentrate.

[0069] In some optional embodiments, the target particle size of the classification is 0.40 mm to 0.50 mm.

[0070] In these embodiments, the fractionating of the target particle size of 0.40 mm to 0.50 mm can separate the fine particle fraction of the first slurry from the coarse particle fraction of the first slurry, avoiding overgrinding of the fine particle fraction into the second grinding.

[0071] The target particle size of the fractionating can be 0.040 mm, 0.041 mm, 0.042 mm, 0.043 mm, 0.044 mm, 0.045 mm, or 0.050 mm.

[0072] In some alternative embodiments, the first fine particles in the first slurry have a mass of 60% to 80% of the mass of the first slurry, the first fine particles having a particle size of less than 0.045 mm; and / or the second fine particles in the second slurry have a mass of 80% to 90% of the mass of the second slurry, the second fine particles having a particle size of less than 0.045 mm.

[0073] In these embodiments, in the first slurry, the first fine particles having a mass of 65% to 80% of the mass of the first slurry and a particle size of less than 0.045 mm can indicate that the first grinding has completed the preliminary dissociation of the aluminum minerals, the silicon minerals, and the titanium minerals in the aluminum-bearing rock series, resulting in a suitable particle size for the monomer dissociation of the silicon minerals and the titanium minerals and the aluminum minerals, avoiding overgrinding that leads to the sliming of the titanium minerals; in addition, in the second slurry, the second fine particles having a mass of 80% to 90% of the mass of the second slurry and a particle size of less than 0.045 mm can indicate that the second grinding has completed the complete dissociation of the aluminum minerals, the silicon minerals, and the titanium minerals in the coarse particle fraction of the slurry, resulting in the complete dissociation of the aluminum minerals and the titanium minerals remaining in the coarse particle fraction of the slurry, improving the selectivity of the separation of the titanium minerals.

[0074] The mass of the first fine particles in the first slurry can be 60%, 61%, 62%, 63%, 64%, 65%, 66%, 67%, 68%, 69%, 70%, 75%, or 80% of the mass of the first slurry.

[0075] The mass of the second fine particles in the second slurry can be 80%, 81%, 82%, 83%, 84%, 85%, 86%, 87%, 88%, 89%, or 90% of the mass of the second slurry.

[0076] In some alternative embodiments, the initial pH of the desiliconization reverse flotation is 2 to 5.

[0077] In these embodiments, the desilication reverse flotation with an initial pH of 2 to 5 can make the third slurry in an acidic environment, the third slurry in the acidic environment can make the surface of the silicon minerals carry a stable negative charge, while the surface of the titanium minerals carries a positive charge, the silicon minerals with the negative charge can be combined with the quaternary ammonium salt cations provided by the dodecyltrimethylammonium chloride and the hexadecyltrimethylammonium bromide in the first collector, and the combination trend of the silicon minerals and the first collector is greater than the combination trend of the titanium minerals and the first collector, so that the adsorption of the silicon minerals and the first collector can be completed, and the removal of the silicon minerals in the third slurry can be realized.

[0078] The initial pH of the desilication reverse flotation can be 2, 3, 4, or 5.

[0079] It should be noted that in the case where the initial pH of the desilication reverse flotation is greater than 5, at this time part of the titanium minerals will be adsorbed with the dodecyltrimethylammonium chloride and the hexadecyltrimethylammonium bromide in the first collector, resulting in the loss of titanium minerals in the desilication flotation.

[0080] In some optional embodiments, the aluminum-bearing rock series ore includes a diaspore component, a silicon dioxide component, and a titanium dioxide component; the mass of the diaspore component is 30% to 45% of the mass of the aluminum-bearing rock series ore, the mass of the silicon dioxide component is 30% to 40% of the mass of the aluminum-bearing rock series ore, and the mass of the titanium dioxide component is 2% to 4% of the mass of the aluminum-bearing rock series ore.

[0081] In these embodiments, the diaspore component with a mass of 30% to 45% of the mass of the aluminum-bearing rock series ore can indicate that the aluminum-bearing rock series ore contains a large amount of aluminum minerals, in addition, the silicon dioxide component with a mass of 30% to 40% of the mass of the aluminum-bearing rock series ore can indicate that the aluminum-bearing rock series ore contains a large amount of silicon minerals, and further, the titanium dioxide component with a mass of 2% to 4% of the mass of the aluminum-bearing rock series ore indicates that the titanium minerals in the aluminum-bearing rock series ore are in a low content. This indicates that the method for separating and extracting titanium concentrate from the aluminum-bearing rock series ore provided in the embodiments can extract titanium from the aluminum-bearing rock series ore with a low content of titanium minerals, thereby realizing the high-yield recovery of the titanium concentrate in the aluminum-bearing rock series ore.

[0082] The mass of the diaspore component can be 30%, 31%, 32%, 33%, 34%, 35%, 40%, or 45% of the mass of the aluminum-bearing rock series ore.

[0083] The mass of the silicon dioxide component can be 30%, 31%, 32%, 33%, 34%, 35%, or 40% of the mass of the aluminum-bearing rock series ore.

[0084] The mass of the titanium dioxide component can be 2.0%, 2.5%, 3%, 3.5%, or 4.0% of the mass of the aluminum-bearing rock ore.

[0085] The present application is further illustrated below with reference to specific embodiments. Experimental methods in the following embodiments that do not specify specific conditions are generally determined according to national / industry standards; if there is no corresponding national / industry standard, they are performed according to general international standards, conventional conditions, or conditions recommended by the manufacturer.

[0086] Example 1 The aluminum-bearing rock series ore includes aluminum oxide, silicon dioxide, and titanium dioxide components; the mass of aluminum oxide component is 39.35% of the mass of the aluminum-bearing rock series ore, the mass of silicon dioxide component is 36.17% of the mass of the aluminum-bearing rock series ore, and the mass of titanium dioxide component is 2.39% of the mass of the aluminum-bearing rock series ore.

[0087] like Figure 1 and Figure 2 As shown, a method for separating and extracting titanium concentrate from aluminum-bearing rock ore, the aluminum-bearing rock ore including titanium minerals, aluminum minerals and silicon minerals, including: S1. The aluminum-bearing rock ore is crushed and ground in sequence to obtain the first slurry; S2. The first slurry is classified to obtain fine-particle slurry and coarse-particle slurry; S3. The coarse-particle slurry is subjected to a second grinding to obtain a second slurry; S4. Mix the fine-particle slurry and the second slurry to obtain the third slurry; S5. The third slurry is subjected to desilication reverse flotation using an acid-base regulator and a first collector to remove some silica minerals and obtain a desilication rough concentrate slurry; wherein the first collector includes dodecyltrimethylammonium chloride and hexadecyltrimethylammonium bromide; S6. Using inhibitors, activators, and a second collector, the desilication rough concentrate slurry is subjected to microbubble flotation to remove aluminum minerals and the remaining silica minerals, thereby obtaining titanium concentrate; wherein, the second collector includes (2-hydroxy-2-methylpropyl(phenyl)phosphine, diphenylphosphine, and diisooctylphosphine.

[0088] The first collector, by mass fraction, is: dodecyltrimethylammonium chloride: 60%, hexadecyltrimethylammonium bromide: 40%; The second collector, by mass fraction, is: (2-hydroxy-2-methylpropyl)(phenyl)phosphine: 30%, diphenylphosphine: 40%, and diisooctylphosphine: 30%.

[0089] The mass m2 of the second collector and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m2:m1 = 1000 g:1000000 g.

[0090] The process of the microbubble flotation is one microbubble roughing, one microbubble scavenging and three microbubble cleaning; in the one microbubble roughing, the mass of the second collector is 400 g, in the one microbubble scavenging, the mass of the second collector is 200 g, in the three microbubble cleaning, the mass of the second collector used in the first microbubble cleaning is 200 g, the mass of the second collector used in the second microbubble cleaning is 100 g, and the mass of the second collector used in the third microbubble cleaning is 100 g.

[0091] The mass m4 of the first collector and the mass m3 of the third slurry satisfy: m4:m3 = 600 g:1000000 g.

[0092] The process of the desiliconization reverse flotation is one desiliconization roughing, one desiliconization scavenging and two desiliconization cleanings; in the one desiliconization roughing, the mass of the first collector is 300 g, in the one desiliconization scavenging, the mass of the first collector is 70 g, in the two desiliconization cleanings, the mass of the first collector used in the first desiliconization cleaning is 150 g, and the mass of the first collector used in the second desiliconization cleaning is 80 g.

[0093] The acid-base regulator is hydrochloric acid. The depressant includes sodium fluosilicate and water glass; wherein the mass m7 of the sodium fluosilicate and the mass m8 of the water glass satisfy: m7:m8 = 1000 g:500 g. The activator is lead nitrate.

[0094] The mass m5 of the depressant and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m5:m1 = 1500 g:1000000 g. The mass m6 of the activator and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m6:m1 = 400 g:1000000 g.

[0095] The target particle size of the classification is 0.45 mm.

[0096] The mass of the first fine particles in the first slurry is 67.53% of the mass of the first slurry, and the particle size of the first fine particles is less than 0.045 mm. The mass of the second fine particles in the second slurry is 82.67% of the mass of the second slurry, and the particle size of the second fine particles is less than 0.045 mm.

[0097] The initial pH of the desiliconization reverse flotation is 2.

[0098] Example 2 Compared with embodiment 1, the differences of embodiment 2 are as follows, and the rest are the same: The aluminum-bearing rock series ore includes an aluminum oxide component, a silicon dioxide component, and a titanium dioxide component; the mass of the aluminum oxide component is 30.34% of the mass of the aluminum-bearing rock series ore, the mass of the silicon dioxide component is 42.14% of the mass of the aluminum-bearing rock series ore, and the mass of the titanium dioxide component is 2.16% of the mass of the aluminum-bearing rock series ore.

[0099] The first collector is, in terms of mass fraction: dodecyltrimethylammonium chloride: 70%, and hexadecyltrimethylammonium bromide: 30%; The second collector is, in terms of mass fraction: (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid: 40%, diphenyl phosphinic acid: 40%, and diisooctyl phosphinic acid: 20%.

[0100] The mass m2 of the second collector and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m2:m1=800g:1000000g.

[0101] The process of microbubble flotation is one-time microbubble roughing, one-time microbubble scavenging, and three-time microbubble cleaning; in the one-time microbubble roughing, the mass of the second collector is 320g, in the one-time microbubble scavenging, the mass of the second collector is 160g, in the three-time microbubble cleaning, the mass of the second collector used in the first-time microbubble cleaning is 160g, the mass of the second collector used in the second-time microbubble cleaning is 80g, and the mass of the second collector used in the third-time microbubble cleaning is 80g.

[0102] The mass m4 of the first collector and the mass m3 of the dry substance of the third slurry satisfy: m4:m3=1200g:1000000g.

[0103] The process of desiliconization reverse flotation is one-time desiliconization roughing, one-time desiliconization scavenging, and two-time desiliconization cleaning; in the one-time desiliconization roughing, the mass of the first collector is 600g, in the one-time desiliconization scavenging, the mass of the first collector is 150g, in the two-time desiliconization cleaning, the mass of the first collector used in the first-time desiliconization cleaning is 300g, and the mass of the first collector used in the second-time desiliconization cleaning is 150g.

[0104] The acid-base regulator is sulfuric acid; The depressant includes sodium fluosilicate and water glass; wherein the mass m7 of the sodium fluosilicate and the mass m8 of the water glass satisfy: m7:m8=1000g:500g; The activator is lead acetate.

[0105] The mass m5 of the depressant and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m5:m1=1500g:1000000g; The mass m6 of the activator and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m6:m1=200g:1000000g.

[0106] The mass of the first fine particles in the first slurry is 62.12% of the mass of the first slurry, and the particle size of the first fine particles is less than 0.045mm; The mass of the second fine particles in the second slurry is 84.33% of the mass of the second slurry, and the particle size of the second fine particles is less than 0.045mm.

[0107] The initial pH of the desiliconization reverse flotation is 4.

[0108] Example 3 Compared with Example 1, the differences of Example 2 are as follows, and the rest are the same: The aluminum-bearing rock series ore includes an aluminum oxide component, a silicon dioxide component, and a titanium dioxide component; the mass of the aluminum oxide component is 37.41% of the mass of the aluminum-bearing rock series ore, the mass of the silicon dioxide component is 38.61% of the mass of the aluminum-bearing rock series ore, and the mass of the titanium dioxide component is 2.89% of the mass of the aluminum-bearing rock series ore.

[0109] The first collector is, in mass fraction: dodecyltrimethylammonium chloride: 75%, and hexadecyltrimethylammonium bromide: 25%; The second collector is, in mass fraction: (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid: 40%, diphenyl phosphinic acid: 40%, and diisooctyl phosphinic acid: 20%.

[0110] The mass m2 of the second collector and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m2:m1=1500g:1000000g.

[0111] The process of the microbubble flotation is one-time microbubble roughing, one-time microbubble scavenging, and three-time microbubble cleaning; in the one-time microbubble roughing, the mass of the second collector is 600g, in the one-time microbubble scavenging, the mass of the second collector is 300g, in the three-time microbubble cleaning, the mass of the second collector used in the first-time microbubble cleaning is 300g, the mass of the second collector used in the second-time microbubble cleaning is 150g, and the mass of the second collector used in the third-time microbubble cleaning is 150g.

[0112] The mass m4 of the first collector and the mass m3 of the dry substance of the third slurry satisfy: m4:m3=800g:1000000g.

[0113] The process of the desilication reverse flotation is one desilication roughing, one desilication scavenging and two desilication cleaning; in the one desilication roughing, the mass of the first collector is 400 g, in the one desilication scavenging, the mass of the first collector is 100 g, in the two desilication cleaning, the mass of the first collector used in the first desilication cleaning is 200 g, and the mass of the first collector used in the second desilication cleaning is 100 g.

[0114] The acid-base regulator is hydrochloric acid. The inhibitor includes sodium fluorosilicate and water glass; wherein the mass m7 of the sodium fluorosilicate and the mass m8 of the water glass satisfy: m7:m8=500 g:500 g. The activator is lead acetate.

[0115] The mass m5 of the inhibitor and the mass m1 of the dry substance of the desilication rough concentrate pulp satisfy: m5:m1=1000 g:1000000 g. The mass m6 of the activator and the mass m1 of the dry substance of the desilication rough concentrate pulp satisfy: m6:m1=800 g:1000000 g.

[0116] The target particle size of the classification is 0.45 mm.

[0117] The mass of the first fine particle in the first ore pulp is 72.91% of the mass of the first ore pulp, and the particle size of the first fine particle is less than 0.045 mm. The mass of the second fine particle in the second ore pulp is 85.79% of the mass of the second ore pulp, and the particle size of the second fine particle is less than 0.045 mm.

[0118] The initial pH of the desilication reverse flotation is 4.

[0119] Example 4 Compared with Example 1, the differences of Example 2 are as follows, and the rest are the same: The aluminum-bearing rock series ore includes an aluminum oxide component, a silicon dioxide component and a titanium dioxide component; the mass of the aluminum oxide component is 33.63% of the mass of the aluminum-bearing rock series ore, the mass of the silicon dioxide component is 44.24% of the mass of the aluminum-bearing rock series ore, and the mass of the titanium dioxide component is 2.76% of the mass of the aluminum-bearing rock series ore.

[0120] The first collector is: dodecyltrimethylammonium chloride: 80%, hexadecyltrimethylammonium bromide: 20% by mass; The second collector is: (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid: 40%, diphenyl phosphinic acid: 40% and diisooctyl phosphinic acid: 15% by mass.

[0121] The mass m2 of the second collector and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m2:m1=1200g:1000000g.

[0122] The process of microbubble flotation is one microbubble roughing, one microbubble scavenging and three microbubble cleaning; in the one microbubble roughing, the mass of the second collector is 480g, in the one microbubble scavenging, the mass of the second collector is 240g, in the three microbubble cleaning, the mass of the second collector used in the first microbubble cleaning is 240g, the mass of the second collector used in the second microbubble cleaning is 120g, and the mass of the second collector used in the third microbubble cleaning is 120g.

[0123] The mass m4 of the first collector and the mass m3 of the third slurry satisfy: m4:m3=990g:1000000g.

[0124] The process of desiliconized reverse flotation is one desiliconized roughing, one desiliconized scavenging and two desiliconized cleanings; in the one desiliconized roughing, the mass of the first collector is 500g, in the one desiliconized scavenging, the mass of the first collector is 120g, in the two desiliconized cleanings, the mass of the first collector used in the first desiliconized cleaning is 250g, and the mass of the first collector used in the second desiliconized cleaning is 120g.

[0125] The acid-base regulator is hydrochloric acid; The depressant includes sodium fluosilicate and water glass; wherein the mass m7 of the sodium fluosilicate and the mass m8 of the water glass satisfy: m7:m8=500g:500g; The activator is lead nitrate.

[0126] The mass m5 of the depressant and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m5:m1=1000g:1000000g; The mass m6 of the activator and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m6:m1=700g:1000000g.

[0127] The mass of the first fine particle in the first slurry is 73.14% of the mass of the first slurry, and the particle size of the first fine particle is less than 0.045mm; The mass of the second fine particle in the second slurry is 88.66% of the mass of the second slurry, and the particle size of the second fine particle is less than 0.045mm.

[0128] The initial pH of the desiliconized reverse flotation is 3.

[0129] Example 5 Compared with Example 1, the difference of Example 2 is as follows, and the rest is the same: The bauxite-containing rock series ore includes an aluminum trioxide component, a silicon dioxide component, and a titanium dioxide component; the mass of the aluminum trioxide component is 35.51% of the mass of the bauxite-containing rock series ore, the mass of the silicon dioxide component is 42.07% of the mass of the bauxite-containing rock series ore, and the mass of the titanium dioxide component is 2.61% of the mass of the bauxite-containing rock series ore.

[0130] The first collector is, in terms of mass fraction, dodecyltrimethylammonium chloride: 80%, and hexadecyltrimethylammonium bromide: 20%; The second collector is, in terms of mass fraction, (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid: 40%, diphenyl phosphinic acid: 45%, and diisooctyl phosphinic acid: 15%.

[0131] The mass m2 of the second collector and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m2:m1 = 1500g:1000000g.

[0132] The process of microbubble flotation is one-time microbubble roughing, one-time microbubble scavenging, and three-time microbubble cleaning; in the one-time microbubble roughing, the mass of the second collector is 600g, in the one-time microbubble scavenging, the mass of the second collector is 300g, in the three-time microbubble cleaning, the mass of the second collector used in the first-time microbubble cleaning is 300g, the mass of the second collector used in the second-time microbubble cleaning is 150g, and the mass of the second collector used in the third-time microbubble cleaning is 150g.

[0133] The mass m4 of the first collector and the mass m3 of the dry substance of the third slurry satisfy: m4:m3 = 850g:1000000g.

[0134] The process of desiliconization reverse flotation is one-time desiliconization roughing, one-time desiliconization scavenging, and two-time desiliconization cleaning; in the one-time desiliconization roughing, the mass of the first collector is 450g, in the one-time desiliconization scavenging, the mass of the first collector is 100g, in the two-time desiliconization cleaning, the mass of the first collector used in the first-time desiliconization cleaning is 200g, and the mass of the first collector used in the second-time desiliconization cleaning is 100g.

[0135] The acid-base regulator is hydrochloric acid; The depressant includes sodium fluosilicate; The activator is lead acetate.

[0136] The mass m5 of the depressant and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m5:m1 = 500g:1000000g; The mass m6 of the activator and the mass m1 of the dry substance of the desiliconized rough concentrate slurry satisfy: m6:m1 = 800g:1000000g.

[0137] The mass of the first fine particles in the first slurry is 78.63% of the mass of the first slurry, and the particle size of the first fine particles is less than 0.045 mm; The mass of the second fine particles in the second slurry is 89.63% of the mass of the second slurry, and the particle size of the second fine particles is less than 0.045 mm.

[0138] The initial pH of the desilication reverse flotation is 5.

[0139] Comparative Example 1 The differences between Comparative Example 1 and Example 1 are as follows, and the rest are the same: The second collector only uses diphenyl phosphinic acid.

[0140] Comparative Example 2 The differences between Comparative Example 2 and Example 1 are as follows, and the rest are the same: The second collector only uses diisooctyl phosphinic acid.

[0141] Comparative Example 3 The differences between Comparative Example 3 and Example 1 are as follows, and the rest are the same: The second collector only uses (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid.

[0142] Comparative Example 4 The differences between Comparative Example 4 and Example 1 are as follows, and the rest are the same: The process of microbubble flotation is one-time microbubble roughing, one-time microbubble scavenging, and three-time microbubble cleaning; in the one-time microbubble roughing, the mass of the second collector is 600 g, in the one-time microbubble scavenging, the mass of the second collector is 300 g, in the three-time microbubble cleaning, the mass of the second collector used in the first-time microbubble cleaning is 300 g, the mass of the second collector used in the second-time microbubble cleaning is 300 g, and the mass of the second collector used in the third-time microbubble cleaning is 300 g.

[0143] Comparative Example 5 The differences between Comparative Example 5 and Example 1 are as follows, and the rest are the same: The process of microbubble flotation is one-time microbubble roughing, one-time microbubble scavenging, and three-time microbubble cleaning; in the one-time microbubble roughing, the mass of the second collector is 300 g, in the one-time microbubble scavenging, the mass of the second collector is 140 g, in the three-time microbubble cleaning, the mass of the second collector used in the first-time microbubble cleaning is 140 g, the mass of the second collector used in the second-time microbubble cleaning is 60 g, and the mass of the second collector used in the third-time microbubble cleaning is 60 g.

[0144] Comparative Example 6 The differences between Comparative Example 6 and Example 1 are as follows, and the rest are the same: The first collector is only dodecyl trimethyl ammonium chloride.

[0145] Comparative Example 7 Comparative Example 6 is different from Example 1 as follows, and the rest is the same: The first collector is only dodecyl trimethyl ammonium chloride.

[0146] Comparative Example 8 Comparative Example 8 is different from Example 1 as follows, and the rest is the same: The process of desilication reverse flotation is once desilication roughing, once desilication scavenging and twice desilication cleaning; in the once desilication roughing, the mass of the first collector is 650g, in the once desilication scavenging, the mass of the first collector is 200g, in the twice desilication cleaning, the mass of the first collector used in the first desilication cleaning is 350g, and the mass of the first collector used in the second desilication cleaning is 200g.

[0147] Comparative Example 9 Comparative Example 9 is different from Example 1 as follows, and the rest is the same: The process of desilication reverse flotation is once desilication roughing, once desilication scavenging and twice desilication cleaning; in the once desilication roughing, the mass of the first collector is 300g, in the once desilication scavenging, the mass of the first collector is 50g, in the twice desilication cleaning, the mass of the first collector used in the first desilication cleaning is 100g, and the mass of the first collector used in the second desilication cleaning is 50g.

[0148] Related experiments and effect data: Titanium concentrates and tailings obtained in each example and comparative example are collected respectively, and the yield of titanium concentrate and tailings and the mass content of titanium dioxide in the titanium concentrate and tailings are counted, and the results are shown in Table 1, wherein the tailings are obtained by combining the desilication tailings obtained by desilication reverse flotation and the micro-bubble tailings obtained by micro-bubble flotation.

[0149] Table 1: Yield of titanium concentrate and tailings and mass content of titanium dioxide obtained in each example and comparative example

[0150] As can be seen from Table 1, the method for separating and extracting titanium concentrate from aluminum-bearing rock series ore provided in the examples of the present application, through the process structure optimization strategy of grading regrinding + two-stage flotation, combined with the precise adaptation strategy of cation desilication + phosphinic acid titanium capture + micro-bubble strengthening recovery, systematically solves the traditional technical problem of mutual restriction between the yield and grade of titanium concentrate in the process of separating and extracting titanium concentrate from aluminum-bearing rock series ore. The titanium concentrate product with a yield of more than 1.0% and a grade of about 53.00% can be obtained.

[0151] Compared with Example 1, the second collector of Comparative Example 1 only uses diphenyl phosphinic acid. Although the second collector using only diphenyl phosphinic acid has higher selectivity than the second collector of the present application, the second collector using only diphenyl phosphinic acid has poor collecting ability, which leads to a significant decrease in the yield of the titanium concentrate. The second collector of Comparative Example 2 only uses diisooctyl phosphinic acid. Although the second collector using only diisooctyl phosphinic acid has higher collecting ability than the second collector of the present application, the second collector using only diisooctyl phosphinic acid has poor selectivity, which leads to a significant decrease in the grade of the titanium concentrate. In addition, the second collector of Comparative Example 3 only uses (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid. Although the second collector using only (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid has higher selectivity than the second collector of the present application, the second collector using only (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid has poor collecting ability, which leads to a significant decrease in the yield of the titanium concentrate.

[0152] Compared with Example 1, Comparative Example 4 adds an excessive amount of the second collector in the micro-bubble flotation process. The excessive second collector can adsorb aluminum minerals or silicon minerals, so that the titanium concentrate obtained by micro-bubble flotation is mixed with silicon minerals and aluminum minerals, thereby reducing the grade of the titanium concentrate. Comparative Example 5 adds a small amount of the second collector in the micro-bubble flotation process. The small amount of the second collector is difficult to contact and adsorb the surface of the titanium minerals, which is not conducive to the subsequent micro-bubble flotation, thereby reducing the yield of the titanium concentrate.

[0153] Compared with Example 1, the first collector of Comparative Example 6 only uses dodecyl trimethyl ammonium chloride. Although the single dodecyl trimethyl ammonium chloride first collector can quickly cover the surface of the silicon minerals, the collecting ability of dodecyl trimethyl ammonium chloride for silicon minerals is general, which can cause part of the silicon minerals in the third slurry to enter the titanium concentrate, thereby reducing the grade of the titanium concentrate. The first collector of Comparative Example 7 only uses hexadecyl trimethyl ammonium bromide. Although the single hexadecyl trimethyl ammonium bromide first collector can greatly improve the hydrophobicity of the silicon minerals, which is conducive to the floating of the silicon minerals, the diffusion speed of hexadecyl trimethyl ammonium bromide is slow, which makes it difficult for the desiliconization reverse flotation to be fully carried out, thereby leading to poor removal effect of the silicon minerals in the desiliconization reverse flotation process, and reducing the grade of the titanium concentrate.

[0154] Compared with embodiment 1, the excessive first collector is added in the desilication reverse flotation process of comparative example 8, and the excessive first collector can collect the titanium minerals, so that the titanium minerals in the desilication rough concentrate slurry obtained by desilication reverse flotation are reduced, thereby reducing the yield of the titanium concentrate. And a small amount of first collector is added in the desilication reverse flotation process of comparative example 9, and the small amount of first collector is difficult to selectively remove the silicon minerals in the third slurry, which is not conducive to the subsequent micro-bubble flotation, and reduces the grade of the titanium concentrate.

[0155] In summary, the method for separating and extracting titanium concentrate from aluminum-bearing rock series ore provided by the embodiment of the application solves the traditional technical problem that the yield and grade of titanium concentrate are mutually restricted in the process of separating and extracting titanium concentrate from aluminum-bearing rock series ore by using the process structure optimization strategy, combined with the precise adaptation strategy of desilication flotation and micro-bubble flotation.

[0156] In addition, the method for separating and extracting titanium concentrate from aluminum-bearing rock series ore provided by the embodiment of the application precisely controls the surface property difference of titanium minerals, aluminum minerals and silicon minerals by using the process optimization of grinding and classification + the core design idea of precise adaptation of flotation reagents, and realizes the efficient development of titanium resources in aluminum-bearing rock series ore, thereby providing a technical paradigm for the comprehensive utilization of similar ores.

[0157] In addition, the method for separating and extracting titanium concentrate from aluminum-bearing rock series ore provided by the embodiment of the application can process titanium minerals in aluminum-bearing rock series ore with different embedded particle sizes, and compared with the traditional flotation process, the method has a significant recovery effect on fine and micro-fine particle size titanium minerals by using the composite flotation mode of desilication flotation combined with micro-bubble flotation.

[0158] The above only describes the specific embodiments of the application, so that those skilled in the art can understand or implement the application. Various modifications to these embodiments will be apparent to those skilled in the art, and the general principles defined in the application can be implemented in other embodiments without departing from the spirit or scope of the application. Therefore, the application will not be limited to these embodiments shown in the application, but will conform to the widest scope consistent with the principles and novel features of the application claimed.

Claims

1. A process for the separation of titanium values from an aluminium-bearing rock series ore, characterised in that, The aluminum-containing rock series ore includes titanium minerals, aluminum minerals and silicon minerals, and the method comprises: sequentially crushing and first grinding the aluminum-containing rock series ore to obtain a first ore slurry; grading the first ore slurry to obtain a fine particle ore slurry and a coarse particle ore slurry; second grinding the coarse particle ore slurry to obtain a second ore slurry; mixing the fine particle ore slurry and the second ore slurry to obtain a third ore slurry; using an acid-base regulator, a first collector to perform desiliconization reverse flotation on the third ore slurry to remove part of the silicon minerals to obtain a desiliconization coarse concentrate slurry; wherein the first collector comprises dodecyltrimethylammonium chloride and hexadecyltrimethylammonium bromide; using an inhibitor, an activator and a second collector to perform micro-bubble flotation on the desiliconization coarse concentrate slurry to remove the aluminum minerals and the remaining silicon minerals to obtain a titanium concentrate; wherein the second collector comprises (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid, diphenyl phosphinic acid and diisooctyl phosphinic acid.

2. The method of claim 1, wherein, The first collector comprises, in mass fraction: dodecyltrimethylammonium chloride: 60% to 80%, and hexadecyltrimethylammonium bromide: 20% to 40%; and / or The second collector comprises, in mass fraction: (2-hydroxy-2-methylpropyl) (phenyl) phosphinic acid: 30% to 40%, diphenyl phosphinic acid: 30% to 45%, and diisooctyl phosphinic acid: 15% to 30%.

3. The method of claim 1, wherein, The mass m2 of the second collector and the mass m1 of the dry substance of the desiliconization coarse concentrate slurry satisfy: m2:m1=(800 to 1500):1000000.

4. The method of claim 1, wherein, The mass m4 of the first collector and the mass m3 of the dry substance of the third ore slurry satisfy: m4:m3=(600 to 1200):1000000.

5. The method of claim 1, wherein, The acid-base regulator is sulfuric acid and / or hydrochloric acid; and / or The inhibitor comprises sodium fluorosilicate and / or water glass; and / or The activator comprises at least one of lead acetate, lead nitrate, copper sulfate, copper nitrate and bismuth nitrate.

6. The method of claim 1, wherein, The mass m5 of the inhibitor and the mass m1 of the dry substance of the desiliconization coarse concentrate slurry satisfy: m5:m1=(500 to 1500):1000000; and / or The mass m6 of the activator and the mass m1 of the dry substance of the desiliconization coarse concentrate slurry satisfy: m6:m1=(200 to 800):1000000.

7. The method of claim 1, wherein, The target particle size of the grading is 0.40 mm to 0.50 mm.

8. The method of claim 1, wherein, The mass of the first fine particles in the first ore slurry is 60% to 80% of the mass of the first ore slurry, and the particle size of the first fine particles is less than 0.045 mm; and / or The mass of the second fine particles in the second ore slurry is 80% to 90% of the mass of the second ore slurry, and the particle size of the second fine particles is less than 0.045 mm.

9. The method of claim 1, wherein, The initial acid-base degree of the desiliconization reverse flotation is 2 to 5.

10. The method of claim 1, wherein, The aluminum-bearing rock series ore includes an aluminum oxide component, a silicon dioxide component, and a titanium dioxide component; the mass of the aluminum oxide component is 30% to 45% of the mass of the aluminum-bearing rock series ore, the mass of the silicon dioxide component is 30% to 40% of the mass of the aluminum-bearing rock series ore, and the mass of the titanium dioxide component is 2% to 4% of the mass of the aluminum-bearing rock series ore.

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