Reverse flotation separation upgrading method for high-silicon beryllium rough concentrate

Abstract

The invention discloses a reverse flotation separation upgrading method for high-silicon beryllium rough concentrate, and belongs to the technical field of mineral separation. According to the method, the high-silicon beryllium rough concentrate is subjected to regrinding and size mixing, obtained size is subjected to reverse flotation separation through flotation reagents including beryllium mineral inhibitors (including starch inhibitors and water glass inhibitors) and siliceous mineral collecting agents (including ether amine collecting agents and quaternary ammonium salt collecting agents), and the product in a reverse flotation tank is the beryllium concentrate. According to the method, efficient desiliconization of the high-silicon beryllium rough concentrate can be achieved, the grade of the beryllium concentrate is greatly improved, the beryllium recovery rate reaches 70% or above, the method is short in process, low in cost and easy to operate, a higher-quality beryllium concentrate raw material can be provided for follow-up beryllium smelting, and further application and popularization are facilitated.

Description

Technical Field

[0001] The invention relates to a desiliconization method for high-silicon beryllium rough concentrate, in particular to a reverse flotation separation and quality improvement method for high-silicon beryllium rough concentrate, belonging to the technical field of ore dressing. Background Art

[0002] Metallic beryllium and its alloys are of irreplaceable importance in high-tech fields such as aerospace, nuclear energy, and electronic communications due to their unique physical and chemical properties, and are critical strategic resources that are in short supply in the country. At present, the extraction of beryllium resources in my country is mainly based on the production of beryllium oxide by treating beryl concentrate obtained by mineral processing with sulfuric acid. Other methods, such as fluorosilicic acid roasting, direct concentrated sulfuric acid leaching, etc., such as the mixed acid decomposition method disclosed in the Chinese patent (publication number: CN116926345A), and the microwave leaching method disclosed in the Chinese patent (publication number: CN105734282A, CN112322893A), are mostly only in the laboratory stage. The principle of the sulfuric acid method is to first use the calcium in calcite to fix silicon under high-temperature roasting conditions, and promote the beryllium in beryl to enter the beryllium aluminate phase, then quench the slag with water, grind it finely, and then use concentrated sulfuric acid to leach out beryllium, iron, aluminum and other ions, further add ammonium sulfate to make alum to remove aluminum, and then use ammonia water to neutralize and remove iron, and then precipitate beryllium hydroxide. After calcining the beryllium hydroxide, the finished product beryllium oxide is obtained. However, the amount of silicon slag and aluminum alum slag generated during the sulfuric acid method is huge, and the amount of slag generated is close to 10 times the amount of raw material processing. In addition, this part of the waste slag has a high beryllium content and has been included in the list of hazardous wastes. It is difficult to dispose of it, and the environmental pollution caused is serious and the risk is high.

[0003] Most beryllium minerals are silicate / aluminate minerals, and the associated gangue minerals are mostly quartz, feldspar, muscovite, olivine, chlorite, etc. The differences in their surface physical and chemical properties are very small, and selective separation is difficult. However, it is worth noting that the structural structure of beryllium minerals is different from gangue minerals such as muscovite. For example, beryl has a hexagonal ring structure, chrysoberyl and hydroxysilicate beryllite are plate-like / short columnar crystals, while muscovite is a typical TOT structure layered silicate, and olivine is an island structure silicate. The degree of Al-O bond breaking is different, and there are differences in surface electrical properties and metal particle activity, which also provides a basis for selective separation. Therefore, if the silicon content entering the final beryllium concentrate can be reduced in the front-end beneficiation process, it will help to reduce the pressure at the subsequent beryllium smelting end and provide better quality raw materials for the furnace.

[0004] Chrysoberyl is an important beryllium resource second only to beryl, but chrysoberyl-type beryllium resources are complex in nature and difficult to develop and utilize. There is no precedent for development and utilization at home and abroad, and they are typical "stagnant" resources. The flotation enrichment of this part of beryllium resources is difficult, and the content of siliceous gangue in the concentrate product is high. For example, the literature ("Experimental Study on Comprehensive Recovery of Beryllium and Fluorite from a Fluorite-Containing Beryllium Ore", Shao Weihua et al., Mineral Conservation and Utilization, 2023, 43(01):98-104) reported that a chrysoberyl-type beryllium ore in Hunan contains 0.47% BeO and 44.86% CaF2. The main gangue minerals are chlorite, mica, calcite, etc. After flotation pre-enrichment, a beryllium concentrate containing 1.57% BeO and a recovery rate of 67.95% can be obtained. The literature (“Study on the Extraction Technology of Beryllium from Chrysoberyl Beryllium Ore”, Rui Haifeng, Xiangtan University, 2017) reported that the chrysoberyl beryllium ore in Xianghualing area of ​​Chenzhou, Hunan Province can only increase the BeO grade from 0.400% to about 0.889% after flotation pre-enrichment. It can be seen that the efficient removal of siliceous gangue in the pre-enriched concentrate is of great significance to the improvement of the quality of the beryllium concentrate, but the existing desiliconization and upgrading methods of high-silicon beryllium rough concentrate still have the defects of poor quality improvement effect, high cost and complex process. Summary of the invention

[0005] In view of the defects of the prior art, the purpose of the present invention is to provide a method for reverse flotation separation and upgrading of high-silicon beryllium rough concentrate. The method is based on the difference in metal particle activity between the target beryllium mineral and the siliceous gangue minerals in the high-silicon beryllium rough concentrate, and adopts reverse flotation to efficiently remove siliceous gangue minerals such as muscovite, so as to achieve the purpose of reducing silicon to improve the grade of beryllium concentrate.

[0006] In order to achieve the above technical objectives, the present invention provides a method for reverse flotation separation and quality improvement of high-silicon beryllium rough concentrate, which comprises re-grinding and slurrying the high-silicon beryllium rough concentrate, and the obtained slurry is subjected to reverse flotation separation using flotation reagents including beryllium mineral inhibitors and siliceous mineral collectors, and the product in the reverse flotation tank is the beryllium concentrate; the beryllium mineral inhibitors include starch inhibitors and water glass inhibitors; the siliceous mineral collectors include etheramine collectors and quaternary ammonium salt collectors.

[0007] The technical scheme of the present invention is based on the crystal structure characteristics of the target beryllium mineral and silicate gangue mineral in the high-silicon beryllium rough concentrate. The number of broken bonds and the reaction activity of the surface aluminum particles of the two are quite different (for example, muscovite, as a typical layered silicate, mostly breaks at the interlayer hydrogen bonds, and Al-O bonds and Si-O bonds are difficult to break). The key is to use a starch inhibitor and a water glass inhibitor as a beryllium mineral inhibitor, and use the physical adsorption and chemical adsorption of the two to target the metal active particles on the surface of the beryllium mineral. On this basis, a mixed amine collector formed by assembling an etheramine collector and a quaternary ammonium salt collector is used to strengthen the hydrophobic flotation of the siliceous gangue mineral. By optimizing the flotation reagent, it is helpful to selectively separate the target beryllium mineral and the siliceous gangue mineral, and realize the efficient silicon reduction and quality improvement of the beryllium concentrate.

[0008] As a preferred solution, the high-silicon beryllium rough concentrate contains at least one beryllium mineral selected from the group consisting of chrysoberyl, hydroxysilicate, beryl, calcite and beryl, and the mass content of BeO is ≥0.60%.

[0009] As a preferred solution, the silicon minerals contained in the high-silicon beryllium rough concentrate are mica silicate minerals, with a mass content of more than 45%.

[0010] The high-silicon beryllium rough concentrate involved in the present invention is obtained by conventional flotation pre-enrichment, and its beryllium mineral is mainly at least one of chrysoberyl, hydroxysilicate beryllite, blue stone, beryllium silicate and beryl, and the mass content of BeO is ≥0.60%. The silicon minerals contained therein are mainly mica silicate minerals, such as white mica, lepidolite, sodium pearl mica, etc., and the total mass accounts for more than 45%.

[0011] As a preferred solution, the regrinding is performed to control the particle size to meet the mass proportion of -0.074mm particle size greater than 90%. Based on the high-silicon beryllium rough concentrate pre-enriched by ordinary flotation, its beryllium minerals often exist in the form of fine-grained dissemination, and the intergrowth with the gangue minerals is complicated. By regrinding to an appropriate particle size, the full monomer dissociation of the target beryllium mineral can be ensured, and the selective separation efficiency of beryllium minerals and siliceous gangue minerals can be improved. At the same time, the regrinding process is also a de-drug process, which can effectively avoid the influence of the residual flotation reagents at the front end on the subsequent separation operation.

[0012] As a preferred solution, the pulping is to adjust the pulp concentration to 25-35wt / %, and the pH is 10.0-11.0. The adjusted pulp concentration of the present invention is relatively low. In a lower concentration pulp, it helps to enhance the full dispersion of fine mineral particles, the selectivity of the agent is better, the efficiency of reverse flotation separation is higher, and it is also beneficial to reduce the agglomeration and interference between mineral particles. The pH is generally adjusted with a weak base, preferably sodium carbonate. When the pH of the slurry is adjusted to within the range of 10.0-11.0, the surface electrical properties of beryllium minerals and siliceous minerals are quite different, the flotation performance of the desiliconization collector is good, and the separation efficiency is high. At this time, the RNH2 component of the mixed amine is dominant, reducing the RNH3 + The consumption of reagents caused by adsorption on the surface of negatively charged mineral mud is more beneficial to RNH3 + It associates with RNH2, promoting its co-adsorption / semi-micelle adsorption groups on the surface of siliceous minerals, and strengthening the hydrophobic floating of siliceous gangue minerals. At the same time, in addition to adjusting pH, sodium carbonate can also be used as a dispersant to reduce the generation of sticky foam.

[0013] As a preferred solution, the beryllium mineral inhibitor is composed of a starch inhibitor and a water glass inhibitor in a mass ratio of 1: (1~10). As a more preferred solution, the starch inhibitor includes at least one of potato starch, soybean starch, corn starch or soluble starch. Wherein the soluble starch is obtained by oxidation and other modifications of potato starch, soybean starch, corn starch, etc., and its hydrophilicity is improved relative to ordinary starch. As a more preferred solution, the modulus of the water glass inhibitor is 2.0~3.0. The negatively charged colloid particles formed by the hydrolysis of water glass can not only reduce the adsorption amount of the collector on the mineral surface, but also easily adsorb on the polymerization center of the colloidal silica polymer formed on the surface of the beryllium mineral, thereby enhancing the hydrophilicity of the mineral. However, water glass with different moduli has different affinity for beryllium. The preferred modulus of the water glass inhibitor is 2.0~3.0, which can better improve the hydrophilicity of the surface of the beryllium mineral. Starch can form a ring with metal particles on the surface of beryllium minerals through hydroxyl groups, and chemically adsorb on the surface of beryllium minerals to reduce the adsorption effect of collectors on metal particles on the surface of beryllium minerals. When starch inhibitors and water glass inhibitors are used in combination, the ratio of the two needs to be coordinated and controlled. When the amount of water glass inhibitor is high, it will have an inhibitory effect on siliceous minerals, resulting in a "crushing" phenomenon and low reverse flotation efficiency. When the amount of starch inhibitors is high, it will also have an inhibitory effect on iron-containing minerals such as hematite and limonite, resulting in a high iron content in beryllium concentrate, which creates a heavy burden on the subsequent iron removal separation at the smelting end. Under the preferred ratio of starch inhibitors and water glass inhibitors of the present invention, the hydrophilicity of the surface of beryllium minerals can be improved and the adsorption of collectors on the surface of beryllium minerals can be reduced, so as to achieve the purpose of synergistic and efficient selective inhibition of beryllium mineral flotation.

[0014] As a preferred solution, the siliceous mineral collector is composed of an etheramine collector and a quaternary ammonium salt collector in a mass ratio of (1-4):1. As a more preferred solution, the etheramine collector includes polyetheramine, C8-C 13 As a preferred solution, the quaternary ammonium salt collector includes C 12 ~C 18 At least one of the single long-chain alkyl quaternary ammonium salts. The introduction of ether groups in etheramine collectors improves their water solubility and dispersibility, and they have strong electrostatic adsorption and hydrogen bonding capabilities for siliceous minerals. Quaternary ammonium salt collectors have good solubility, and due to their tetrahedral structure and positive charge, they can selectively act on the surface of siliceous minerals very accurately. The HLB values ​​(hydrophilic and lipophilic values) of the two are similar. The mixed collector assembled in an appropriate ratio has good low-temperature performance, a lower CMC value (critical micelle concentration) and higher reactivity. The three-phase foam formed by it has strong stability and a long half-life. The amount of flotation foam is moderate, brittle, and easy to defoam, avoiding the serious entrainment caused by the large amount of foam of fatty amine collectors.

[0015] As a preferred solution, the reverse flotation includes 1 roughing selection, 1 to 3 cleaning selections and 1 to 3 scavenging selections.

[0016] As a preferred solution, the reagent system for roughing is: 20-60 g / t beryllium mineral inhibitor, 40-100 g / t siliceous mineral collector; the reagent system for fine selection is: only adding collector, following the principle of gradual decrease; the reagent system for scavenging is: only adding inhibitor, following the principle of gradual decrease. Under the preferred flotation reagent system, the grade of beryllium concentrate can be enriched by more than one time, and the operation recovery rate can reach more than 70%.

[0017] The starch inhibitor involved in the present invention can be either amylose or amylopectin.

[0018] The etheramine collector and quaternary ammonium salt collector of the present invention may contain an alkyl hydrocarbon chain which may be a straight-chain alkyl chain or a branched-chain alkyl chain.

[0019] Compared with the prior art, the present invention has the following beneficial effects: (1) In the technical solution of the present invention, the beryllium mineral depressant has good selectivity, the siliceous mineral collector has high reverse flotation efficiency, the final beryllium concentrate grade can be more than doubled, and the operating recovery rate reaches more than 70%.

[0020] (2) The technical solution of the present invention can reduce the generation of hazardous silicon slag waste in the subsequent beryllium smelting process by removing part of the siliceous gangue in the beryllium concentrate during the front-end mineral processing, thereby reducing the processing cost and environmental pollution risk.

[0021] (3) The mineral processing method of the technical solution of the present invention is simple to operate, has high flexibility and strong adaptability, and has a short process flow and low reagent cost, which is conducive to further promotion and use. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 This is the process flow chart of Example 1.

[0023] Figure 2 This is the phase analysis of the high silicon beryllium concentrate in Example 1.

[0024] Figure 3 2 is a flotation flow chart of Example 2 and Comparative Example 2.

[0025] Figure 4 1 is a flotation flow chart of Example 3 and Comparative Example 3. DETAILED DESCRIPTION

[0026] The following examples are provided to further illustrate the contents of the present invention in detail, but are not intended to limit the scope of protection of the claims of the present invention.

[0027] Example 1 The beryllium concentrate obtained by flotation in a beneficiation plant in Hunan was taken as the research object to explore the method of reducing silicon and improving quality. The following is the property analysis of the beryllium concentrate. The BeO grade of the beryllium concentrate is 1.1~1.2%, and the main mineral phases are diaspore, fluorite, sodium pearl mica, muscovite, lithium chlorite, feldspar, chrysoberyl and corundum. The proportion of silicate gangue minerals exceeds 45% ( Figure 2 ).

[0028] The MLA test results show that the main independent beryllium minerals in the beryllium concentrate are chrysoberyl, and there are also a small amount of hydroxysilicate beryllite, beryl, blue stone and beryllium calcium silicate. In addition, sodium pearl mica also contains a small amount of dispersed beryllium (Table 1). The beryllium minerals in the beryllium concentrate are embedded in a fine particle size, more than 80% of the beryllium is distributed in the -0.043mm particle size, and the grade of beryllium oxide in the -0.025mm particle size reaches 1.668% (Table 2). Therefore, fine embedded particle size and high content of siliceous gangue are important factors affecting its recovery.

[0029]

[0030]

[0031] Under stirring conditions, 5 g of solid water glass with a modulus of 2.3 and 1 g of soluble starch (commercial product) were weighed respectively, water was added to a total weight of 100 g of the solution, and the reaction was carried out for 10 minutes to obtain the beryllium mineral inhibitor aqueous solution.

[0032] Under stirring conditions, 2 g of polyetheramine (commercial product) and 1 g of hexadecyltrimethylammonium chloride were weighed respectively, water was added to make the total weight of the solution 100 g, and the reaction was carried out for 5 minutes to obtain the siliceous mineral collector aqueous solution.

[0033] The high silicon beryllium concentrate is treated by the process method. The specific process flow is as follows: Figure 1 shown.

[0034] After grinding the high silicon beryllium rough concentrate in the ball mill for 1 minute, the grinding fineness requirement of -0.074mm 90% is met, and the pulp concentration is readjusted to 35%, and the pulp pH is adjusted to 10.5 with sodium carbonate, and beryllium mineral inhibitors and siliceous mineral collectors are added for reverse flotation separation. The amount of beryllium mineral inhibitor added relative to the feed is 40g / t, and the amount of siliceous mineral collector added relative to the feed is 80g / t. After aeration and slurry adjustment for 5 minutes, reverse flotation roughing operation is carried out, and the foam product is further added with 20g / t and 10g / t of beryllium mineral inhibitors, and two sweeping operations are carried out. Siliceous mineral collectors of 40g / t and 20g / t are added to the product in the roughing operation tank, and two concentrating operations are carried out. The final foam product is the siliceous gangue impurities, and the product in the tank is the final beryllium concentrate. After filtering, drying and weighing, the beryllium oxide content is tested and the operation recovery rate is calculated. The specific test results are shown in Table 3 below.

[0035]

[0036] Control group 1 The control experiment group 1 is used for comparison with Example 1. The process flow is consistent with Example 1, and the only difference is that a single dodecylamine is used as a siliceous mineral collector.

[0037] After the high silicon beryllium rough concentrate was regrinded and slurried, the dosages of beryllium mineral inhibitor added were 40g / t, 20g / t and 10g / t respectively, the dosages of dodecylamine siliceous mineral collector were 80g / t, 40g / t and 20g / t respectively, the aeration and slurrying time was 5min, and after one roughing, two fine and two sweeping reverse flotation closed-circuit operation, the obtained foam product was siliceous gangue impurities, and the product in the tank was the final beryllium concentrate. The specific test results are shown in Table 4 below.

[0038]

[0039] It can be seen from the flotation test results in the table that the process of the present invention can obtain a beryllium concentrate product with a grade of 2.4%, which is more than twice the enrichment of the original ore, and the operating recovery rate reaches 70%. The conventional fatty amine reverse flotation system has almost no sorting ability, and it was found during the test that the foam layer of dodecylamine was too thick, and the foam viscosity was large and difficult to defoam, resulting in serious entrainment of fine particles, making it difficult to achieve the goal of reducing silicon and improving quality.

[0040] Control group 2 The control experimental group is used for comparison with Example 1. The only difference is that the beryllium mineral inhibitor in Example 1 is replaced by a single inhibitor, or the silicon mineral collector is replaced by a single collector. As a control, the superiority of the flotation performance of the combined flotation reagent of the present invention is evaluated. The flotation process and reagent dosage of the control experimental group are consistent with those of Example 1.

[0041] Taking water glass as a single beryllium mineral inhibitor control group as an example, the high silicon beryllium rough concentrate was re-grinded in a ball mill for 1 minute to meet the grinding fineness requirement of -0.074mm 90%, the pulp concentration was readjusted to 35%, the pulp pH was adjusted to 10.5 with sodium carbonate, and a single water glass inhibitor (modulus of 2.3) and a siliceous mineral collector were added for reverse flotation separation. The amount of water glass added relative to the feed was 40g / t, and the amount of siliceous mineral collector added relative to the feed was 80g / t. After aeration and slurry adjustment for 5 minutes, the roughing operation of reverse flotation was carried out, and the foam product was further added with 20g / t and 10g / t of water glass inhibitor, and two scavenging operations were carried out. The siliceous mineral collectors of 40g / t and 20g / t were added to the products in the roughing operation tank, and two concentrating operations were carried out. The specific test results are shown in Table 5 below.

[0042]

[0043] It can be seen from the flotation test results in the table that the grade and recovery rate of the beryllium concentrate flotated using a single inhibitor / collector are not as good as those of the combined flotation reagent of Example 1, which also shows that the combined flotation reagent of the present invention has a relatively advantageous synergistic effect, the water glass-starch inorganic-organic combined inhibitor has good selectivity for beryllium minerals, and the ether amine-quaternary ammonium salt mixed amine collector has high desiliconization efficiency.

[0044] Example 2 Under stirring conditions, 4 g of solid water glass with a modulus of 2.85 and 1 g of potato starch were weighed respectively, water was added to a total weight of 100 g of the solution, and the mixture was reacted for 10 minutes to obtain the beryllium mineral inhibitor aqueous solution.

[0045] Under stirring conditions, 3 g of polyetheramine and 1 g of dodecyltrimethylammonium chloride were weighed respectively, water was added to make the total weight of the solution 100 g, and the reaction was carried out for 5 minutes to obtain the siliceous mineral collector aqueous solution.

[0046] This process is used to treat a high silicon beryllium concentrate in Hunan. The specific flotation process is as follows: Figure 3 shown.

[0047] The high silicon beryllium rough concentrate was ground in a ball mill for 1.5 minutes to meet the grinding fineness requirement of -0.074mm 90%. The pulp concentration was readjusted to 33%, and the pulp pH was adjusted to 10.0 with sodium carbonate. The amount of beryllium mineral inhibitor beryllium added relative to the feed was 50g / t, and the amount of siliceous mineral collector added relative to the feed was 100g / t. After aeration and slurry adjustment for 5 minutes, a reverse flotation separation operation was carried out. The foam product obtained was the siliceous gangue impurities, and the product in the tank was the final beryllium concentrate. After filtering, drying and weighing, the beryllium oxide content was tested and the operation recovery rate was calculated. The specific test results are shown in Table 6 below.

[0048]

[0049] Control group The control experimental group is used for comparison with Example 2. The process flow is consistent with Example 2. The only difference is that metal ions are used to activate the flotation of siliceous gangue minerals, and fatty acid (NaOL) is used as a collector for reverse flotation separation. The dosage is 100 g / t. The specific test results are shown in Table 7 below.

[0050]

[0051] From the flotation test results in the table, it can be seen that the introduction of metal ions with different valence states has different effects on reverse flotation separation. 2+ and Mg 2+ It showed a positive enrichment trend, Fe 3+ and Al 3+ The reverse enrichment trend is obvious, but the overall effect of flotation separation of siliceous gangue minerals activated by metal ions is not good, the grade of beryllium concentrate is only slightly improved, and the recovery rate is not high. However, by using the method of this process, a beryllium concentrate product with a BeO grade of 2.1688% and a recovery rate of 62.99% can be obtained through a reverse flotation separation, which has a relatively advantageous separation efficiency.

[0052] Example 3 Under stirring conditions, 3 g of solid water glass with a modulus of 3.0 and 1 g of corn starch were weighed respectively, water was added to a total weight of 100 g of the solution, and the mixture was reacted for 10 minutes to obtain the beryllium mineral inhibitor aqueous solution.

[0053] Under stirring conditions, 2 g of decyl ether amine and 1 g of dodecyl trimethyl ammonium chloride were weighed respectively, water was added to make the total weight of the solution 100 g, and the reaction was carried out for 5 minutes to obtain the siliceous mineral collector aqueous solution.

[0054] This process is used to treat a low-grade high-silicon beryllium concentrate. The main beryllium minerals in the beryllium concentrate are chrysoberyl, and there are also a small amount of hydroxysilicate beryllite and blue stone. The specific flotation process is as follows: Figure 4 shown.

[0055] The high silicon beryllium rough concentrate was ground in a ball mill for 1 min to meet the grinding fineness requirement of -0.074 mm 90%. The pulp concentration was readjusted to 30%, and the pulp pH was adjusted to 11.0 with sodium carbonate. The amount of beryllium mineral depressant added relative to the feed was 40 g / t, and the amount of siliceous mineral collector added relative to the feed was 100 g / t. After aeration and slurry adjustment for 5 min, a reverse flotation separation operation was carried out. The foam product obtained was the siliceous gangue impurities, and the product in the tank was the final beryllium concentrate. After filtering, drying and weighing, the beryllium oxide content was tested and the operation recovery rate was calculated. The specific test results are shown in Table 8 below.

[0056]

[0057] Control group The control experimental group is used for comparison with Example 3. The process flow is consistent with Example 3. The only difference is that different types of beryllium mineral inhibitors are used. Conventional small molecule organic acid inhibitor oxalic acid (OA), high molecular polymer inhibitor polyacrylamide (PAM), inorganic inhibitor sodium fluorosilicate (SSF) and sodium hexametaphosphate (SHMP) are selected. The dosage is 40 g / t. The specific test results are shown in Table 9 below.

[0058]

[0059] From the flotation test results in the table, it can be seen that conventional beryllium mineral depressants are difficult to achieve targeted inhibition of beryllium minerals, and the efficiency of reverse flotation is not high. However, using this process, the enrichment effect of beryllium concentrate is obvious and the operation recovery rate is high. After one reverse flotation separation, the BeO grade can be increased from about 0.71% to 1.39%, and the recovery rate is close to 70%, which has a relatively advantageous separation efficiency.

Claims

1. A reverse flotation separation and upgrading method for high-silicon beryllium rough concentrate, characterized in that: The high silicon beryllium rough concentrate is re-grinded and slurried, and the obtained slurry is reversely flotated and separated using flotation reagents including beryllium mineral inhibitors and siliceous mineral collectors, and the product in the reverse flotation tank is the beryllium concentrate; The beryllium mineral inhibitors include starch inhibitors and water glass inhibitors; The siliceous mineral collectors include etheramine collectors and quaternary ammonium salt collectors.

2. The reverse flotation separation and upgrading method of a high-silicon beryllium rough concentrate according to claim 1, characterized in that: The high-silicon beryllium rough concentrate contains at least one beryllium mineral selected from the group consisting of chrysoberyl, hydroxysilicate, blue stone, beryl and beryl, and the mass content of BeO is ≥0.60%; and / or, The silicon minerals contained in the high-silicon beryllium rough concentrate are mica silicate minerals, with a mass content of more than 45%.

3. The reverse flotation separation and upgrading method of a high silicon beryllium rough concentrate according to claim 1 or 2, characterized in that: The regrinding is performed so as to control the particle size to meet the -0.074 mm particle size, and the mass proportion thereof is greater than 90%.

4. The reverse flotation separation and upgrading method of a high silicon beryllium rough concentrate according to claim 1 or 2, characterized in that: The slurry adjustment is to adjust the slurry concentration to 25-35wt / %, and the pH to 10.0-11.

0.

5. The reverse flotation separation and upgrading method of a high silicon beryllium rough concentrate according to claim 1, characterized in that: The beryllium mineral inhibitor is composed of a starch inhibitor and a water glass inhibitor in a mass ratio of 1: (1-10).

6. The reverse flotation separation and upgrading method of a high-silicon beryllium rough concentrate according to claim 5, characterized in that: The starch inhibitor includes at least one of potato starch, soybean starch, corn starch and soluble starch; The modulus of the water glass inhibitor is 2.0-3.

0.

7. The reverse flotation separation and upgrading method of a high-silicon beryllium rough concentrate according to claim 1, characterized in that: The siliceous mineral collector is composed of an ether amine collector and a quaternary ammonium salt collector in a mass ratio of (1-4):

1.

8. The reverse flotation separation and upgrading method of a high-silicon beryllium rough concentrate according to claim 7, characterized in that: The etheramine collector includes polyetheramine, C8~C 13 At least one of alkyl ether amines and ether diamines; The quaternary ammonium salt collector includes C 12 ~C 18 At least one of the mono-long-chain alkyl quaternary ammonium salts.

9. A reverse flotation separation and upgrading method for high silicon beryllium rough concentrate according to claim 1, 2, 5, 6, 7 or 8, characterized in that: The reverse flotation comprises 1 roughing selection, 1 to 3 cleaning selections and 1 to 3 scavenging selections.

10. The reverse flotation separation and upgrading method of a high silicon beryllium rough concentrate according to claim 9, characterized in that: The reagent system for the roughing is: 20-60 g / t of beryllium mineral inhibitor and 40-100 g / t of siliceous mineral collector; the reagent system for the fine selection is: only adding collector, following the principle of gradual reduction; The drug system for the scanning selection is: only inhibitors are added, following the principle of gradual reduction.

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