Direct flotation process of high-magnesium and high-silicon collophosphate

Abstract

The present invention provides a positive flotation process for high-magnesium, high-silicon collophanite. The raw ore is first crushed and wet-ground, and water is added to prepare a slurry. The slurry is then subjected to roughing to obtain a roughing concentrate and roughing tailings. The roughing concentrate is then subjected to two stages of concentrating to obtain a phosphate concentrate. The selected middlings obtained from the two stages of concentrating are combined and then subjected to two stages of middling reselection. The reselected tailings from the second stage of middling reselection serve as the final tailings II. The roughing tailings are then subjected to two stages of scavenging to obtain the final tailings I. The present invention utilizes an acid-free positive flotation process. Through the synergistic combination of process and reagents, the process achieves efficient separation of collophanite from dolomite and quartz, improving the concentrate grade and recovery rate of the collophanite. Furthermore, through the combined action of an effective depressant (DP) and a collector, the total reagent consumption is only 30% of that of existing processes, significantly reducing reagent consumption and saving reagent costs. The process of the present invention has the advantages of a simple process, low reagent consumption, high economic efficiency, environmental friendliness, and high practicality.

Description

Technical Field

[0001] The present invention relates to the technical field of collophanite flotation, in particular to a positive flotation process of high-magnesium and high-silicon collophanite. Background Art

[0002] For high-magnesium phosphate ores, the existing technology generally uses an acidic reverse flotation process, which involves adding sulfuric acid (the higher the magnesium content, the greater the amount of sulfuric acid) and phosphoric acid to the slurry, followed by the addition of oxidized paraffin soap-based oxidized ore collectors, for reverse flotation to remove dolomite and obtain qualified phosphate concentrate. For high-silicon phosphate ores, the existing technology generally uses an alkaline direct flotation process, which involves adding sodium carbonate and water glass to the slurry, followed by the addition of oxidized paraffin soap-based oxidized ore collectors, for direct flotation. For high-magnesium and high-silicon phosphate ores, the existing technology generally uses a combination of alkaline direct flotation and acidic reverse flotation.

[0003] The invention patent (application number CN 201611229832.6) discloses a process for treating phosphate ore by combining reverse flotation for desiliconization and acid leaching for magnesium removal. This process combines reverse flotation to remove silicate minerals and acid chemical leaching to remove magnesium-containing carbonate minerals. The acid chemical leaching preferably uses waste acid. While this process achieves the phosphorus and magnesium content of phosphate concentrate meeting the quality requirements for acid processing, improving the grade of the phosphate concentrate and reducing the magnesium content, while also treating some of the waste acid solution, even with waste acid, the acidic slurry is highly corrosive to mechanical equipment, resulting in a shortened equipment life and high costs. Furthermore, the acidic wastewater has a significant environmental impact, necessitating wastewater treatment and increasing costs.

[0004] In addition, in industry, alkaline direct flotation generally requires a relatively fine grinding fineness of less than 200 mesh with a content of more than 90%, which reduces flotation efficiency. Furthermore, the high dosage of reagents, high foam viscosity, and poor fluidity lead to unstable production processes, large fluctuations in separation indicators, and difficult production management. Furthermore, the existing technology for the flotation of high-magnesium, high-silicon phosphate ore generally requires two steps, namely, demagnesium removal and desiliconization. The flotation conditions are inconsistent, and large amounts of reagents need to be added to change the pH of the slurry, resulting in high reagent consumption. Furthermore, the flotation process still relies on a combination of direct and reverse flotation, or a combination of reverse flotation and reverse flotation, which has the disadvantages of a long process flow, high reagent consumption, and high acid wastewater treatment costs.

[0005] In view of this, it is necessary to design an improved positive flotation process for high-magnesium and high-silicon collophosphate to solve the above problems. Summary of the Invention

[0006] The object of the present invention is to provide a direct flotation process for high-magnesium and high-silicon collophanite. The process adopts an acid-free direct flotation process and, under the joint action of an effective inhibitor, achieves efficient separation of the collophanite from dolomite and quartz, thereby improving the concentrate grade and recovery rate of the collophanite. At the same time, the process avoids the problems of a long process flow, high reagent consumption and poor environmental friendliness caused by the need to carry out combined direct and reverse flotation of this type of phosphate rock in a strong acid and strong alkaline slurry environment.

[0007] To achieve the above-mentioned object of the invention, the present invention provides a positive flotation process for high-magnesium and high-silicon collophosphate ore, comprising the following steps:

[0008] S1. Crushing the high-magnesium and high-silicon collophosphate ore to be selected, and wet grinding it to a certain fineness, and adding water to the pulp concentration of 30% to 35%;

[0009] S2, adding a roughing agent to the ore pulp of step S1 to perform roughing to obtain a roughing concentrate and a roughing tailing; the roughing agent includes water glass, an inhibitor DP and sodium tetradecyl fatty acid;

[0010] S3, the rougher concentrate obtained in step S2 is subjected to two-stage concentrating to obtain phosphate concentrate, and the selected middlings obtained in the two stages of concentrating are combined and further subjected to two-stage middling reselection; wherein the reselected concentrate from the first stage of middling reselection is returned to the rougher process in step S2, and the reselected concentrate from the second stage of middling reselection is returned to the first stage of middling reselection, and the reselected tailings from the second stage of middling reselection are the final tailings II;

[0011] The reagents for the two-stage selection include the inhibitor DP, the reagents for the first-stage middling reselection include the inhibitor DP and sodium tetradecyl fatty acid, and the reagents for the second-stage middling reselection include sodium tetradecyl fatty acid;

[0012] S4, the roughing tailings obtained in step S2 are subjected to two-stage scavenging to obtain final tailings I, and the scavenged tailings obtained by scavenging are returned to the previous operation step by step; the scavenging agent includes sodium tetradecyl fatty acid;

[0013] In step S2 and step S3, the components of the inhibitor DP include aluminum sulfate, citric acid, tannic acid and hydroxypropyl cellulose.

[0014] As a further improvement of the present invention, the components of the inhibitor DP include, by mass percentage, 45% to 55% of aluminum sulfate, 15% to 25% of citric acid, 7% to 12% of tannic acid, and 7% to 12% of hydroxypropyl cellulose.

[0015] As a further improvement of the present invention, the components of the inhibitor DP include, by mass percentage, 50% aluminum sulfate, 20% citric acid, 10% tannic acid, and 10% hydroxypropyl cellulose.

[0016] As a further improvement of the present invention, in step S2, the mass ratio of the water glass, the inhibitor DP and the sodium tetradecyl fatty acid in the roughing agent is 15:8:3.6.

[0017] As a further improvement of the present invention, in step S3, in the reagent for reselection of the first-stage middlings, the mass ratio of the inhibitor DP to sodium tetradecyl fatty acid is (1.1-1.3):1.

[0018] As a further improvement of the present invention, in step S1, after the raw ore is wet-ground, the mass of the ore powder with a grinding fineness of -0.074 mm accounts for 90% to 92% of the total mass of the ore powder.

[0019] As a further improvement of the present invention, in step S3, in the two-stage concentration process, the amount of inhibitor DP added in the second stage of concentration is 0.5 to 1.0 times the amount of inhibitor DP added in the first stage of concentration.

[0020] As a further improvement of the present invention, the components of the high-magnesium and high-silicon collophosphate ore include, by mass percentage, 17% to 19.5% P2O5, 5.5% to 8% MgO, 18% to 40% SiO2, and 34% to 37% CaO.

[0021] As a further improvement of the present invention, in the rough selection, the amount of water glass added is 1000-2000 g / t, the amount of inhibitor DP added is 700-1000 g / t, and the amount of sodium tetradecyl fatty acid added is 300-500 g / t.

[0022] As a further improvement of the present invention, in the two-stage concentration process, the amount of inhibitor DP added in the first stage concentration is 100-300 g / t, and the amount of inhibitor DP added in the second stage concentration is 100-300 g / t; in the first stage middling reselection, the amount of inhibitor DP added is 100-200 g / t, and the amount of sodium tetradecyl fatty acid added is 80-160 g / t; in the second stage middling reselection, the amount of sodium tetradecyl fatty acid added is 60-120 g / t; and in both stages of sweeping, the amount of sodium tetradecyl fatty acid added is 80-160 g / t.

[0023] The beneficial effects of the present invention are:

[0024] 1. The present invention provides a direct flotation process for high-magnesium, high-silica collophosphate. The process involves first crushing the raw ore, wet-grinding it, and adding water to prepare a slurry. The slurry is then subjected to roughing to obtain a rougher concentrate and rougher tailings. The rougher concentrate is then subjected to two stages of concentrating to obtain a phosphate concentrate. The selected middlings from the two stages of concentrating are combined and then subjected to two stages of middling reselection. The reselected tailings from the second stage of middling reselection serve as final tailings II. The rougher tailings are then subjected to two stages of scavenging to obtain final tailings I. The present invention flots the collophosphate in a neutral slurry environment, achieving acid-free direct flotation of high-magnesium, high-silica collophosphate. This process effectively avoids corrosion to equipment and environmental impacts caused by strongly acidic slurries, avoids the excessively sticky foam that occurs in alkaline direct flotation processes, and ensures the stability of the production process. Compared with the existing combined forward and reverse flotation or reverse flotation combined process, this process is simple, does not require desiliconization and dephosphorization in separate steps, and the entire process is carried out in neutral slurry, avoiding the problem of excessive acid or alkali consumption caused by the exchange of strongly acidic slurry and strongly alkaline slurry, and has higher economic benefits.

[0025] 2. The positive flotation process for high-magnesium, high-silicon collophanite of the present invention uses water glass as an effective inhibitor for quartz, effectively suppressing quartz. The inhibitor DP, a novel, independently developed combined inhibitor, contains aluminum sulfate and citric acid that can dissolve magnesium ions on the surface of dolomite without reacting with the collophanite. Tannic acid and hydroxypropyl cellulose selectively adsorb on the surface of the dissolved dolomite, negatively charging it and preventing it from interacting with the collector, sodium tetradecyl fatty acid. The collophanite, on the other hand, undergoes chemical adsorption with the collector, floating upward under the action of the collector and entering the phosphate concentrate. Thus, through the synergistic combination of these effective agents, the efficient separation of the collophanite from dolomite and quartz is achieved, enabling efficient flotation of the phosphate concentrate.

[0026] 3. The present invention utilizes an acid-free direct flotation process. Through the synergistic combination of process and reagents, it achieves efficient separation of collophanite from dolomite and quartz, improving the concentrate grade and recovery rate of the collophanite. Furthermore, thanks to the combined action of an effective inhibitor (DP) and a collector, the total reagent consumption is only 30% of that of existing processes, significantly reducing reagent consumption and saving reagent costs. The present process has the advantages of a simple process, low reagent consumption, high economic benefits, environmental friendliness, and high practicality. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 The figure is a schematic flow chart of the positive flotation process of high-magnesium and high-silicon collophosphate ore according to the present invention. DETAILED DESCRIPTION

[0028] In order to make the objectives, technical solutions and advantages of the present invention more clear, the present invention is described in detail below with reference to the accompanying drawings and specific embodiments.

[0029] It should also be noted here that, in order to avoid obscuring the present invention due to unnecessary details, only structures and / or processing steps closely related to the solutions of the present invention are shown in the drawings, while other details that are not closely related to the present invention are omitted.

[0030] In addition, it should be noted that the terms "comprises", "includes" or any other variations thereof are intended to cover non-exclusive inclusion, so that a process, method, article or apparatus that includes a series of elements includes not only those elements, but also includes other elements not explicitly listed, or also includes elements inherent to such process, method, article or apparatus.

[0031] See also Figure 1 As shown, a positive flotation process for high-magnesium and high-silicon collophosphate ore comprises the following steps:

[0032] S1. Crushing the high-magnesium and high-silicon collophosphate ore to be selected, and wet grinding it to a certain fineness. The mass of the ore powder with a grinding fineness of -0.074mm accounts for 90% to 92% of the total mass of the ore powder; adding water to the slurry concentration is 30% to 35%;

[0033] S2, adding a roughing agent to the ore pulp of step S1 to perform roughing to obtain a roughing concentrate and a roughing tailing; the roughing agent includes water glass, an inhibitor DP and sodium tetradecyl fatty acid;

[0034] S3, the rougher concentrate obtained in step S2 is subjected to two-stage concentrating to obtain phosphate concentrate, and the selected middlings obtained in the two stages of concentrating are combined and further subjected to two-stage middling reselection; wherein the reselected concentrate from the first stage of middling reselection is returned to the rougher process in step S2, and the reselected concentrate from the second stage of middling reselection is returned to the first stage of middling reselection, and the reselected tailings from the second stage of middling reselection are the final tailings II;

[0035] The reagents for the two-stage selection include the inhibitor DP, the reagents for the first-stage middling reselection include the inhibitor DP and sodium tetradecyl fatty acid, and the reagents for the second-stage middling reselection include sodium tetradecyl fatty acid;

[0036] S4, the roughing tailings obtained in step S2 are subjected to two-stage scavenging to obtain final tailings I, and the scavenged tailings obtained by scavenging are returned to the previous operation in sequence; the scavenging agent includes sodium tetradecyl fatty acid;

[0037] Specifically, in steps S2 and S3, the inhibitor DP comprises aluminum sulfate, citric acid, tannic acid, and hydroxypropyl cellulose. The components of the inhibitor DP, by mass percentage, are: 45%-55% aluminum sulfate, 15%-25% citric acid, 7%-12% tannic acid, and 7%-12% hydroxypropyl cellulose. As a novel, independently developed, combined inhibitor, the aluminum sulfate and citric acid in the inhibitor DP dissolve magnesium ions on the dolomite surface without reacting with the collophanite. The tannic acid and hydroxypropyl cellulose selectively adsorb on the dissolved dolomite surface, imparting a negative charge to the surface and preventing it from interacting with the collector, sodium tetradecyl fatty acid. The collophanite, on the other hand, chemically adsorbs onto the collector, sodium tetradecyl fatty acid, causing it to float upwards and enter the phosphate concentrate, effectively separating the collophanite from the dolomite.

[0038] It should be noted that the acid-free direct flotation process of the present invention achieves efficient separation of collophanite from dolomite and quartz, thereby improving the concentrate grade and recovery rate of the collophanite. The successful implementation of this process is inseparable from the coordinated cooperation of various reagents, especially the role of the new inhibitor DP. Under the combined action of the effective inhibitor DP and the collector, the total chemical consumption of the entire process is only 30% of that of the existing process, which greatly reduces chemical consumption and saves chemical costs.

[0039] In some specific embodiments, the components of the inhibitor DP include, by mass percentage, 50% aluminum sulfate, 20% citric acid, 10% tannic acid, and 10% hydroxypropyl cellulose.

[0040] Specifically, in step S2, the mass ratio of water glass, depressant DP, and collector sodium tetradecyl fatty acid in the roughing reagent is 15:8:3.6. In step S3, the mass ratio of depressant DP to sodium tetradecyl fatty acid in the reagent for reselection of the first-stage middlings is (1.1-1.3):1. In step S3, in the two-stage concentrating process, the amount of depressant DP added in the second stage is 0.5-1.0 times the amount added in the first stage. By limiting the additive components and amounts of the reagents in each process step, the separation of collophanite from dolomite and quartz is achieved in a simple acid-free direct flotation process, eliminating the need for separate steps or different slurry environments. This shortens the process flow and reduces the flotation cost of high-magnesium, high-silica collophanite.

[0041] Specifically, the composition of the high-magnesium, high-silica collophosphate ore, by mass percentage, includes: 17%-19.5% P2O5, 5.5%-8% MgO, 18%-40% SiO2, and 34%-37% CaO. During the roughing of this high-magnesium, high-silica collophosphate ore, the addition amount of water glass is 1000-2000g / t, the addition amount of DP inhibitor is 700-1000g / t, and the addition amount of sodium tetradecyl fatty acid is 300-500g / t. In the two-stage concentration process, the amount of inhibitor DP added in the first stage of concentration is 100~300g / t, and the amount of inhibitor DP added in the second stage of concentration is 100~300g / t; in the first stage of middling reselection, the amount of inhibitor DP added is 100~200g / t, and the amount of sodium tetradecyl fatty acid added is 80~160g / t; in the second stage of middling reselection, the amount of sodium tetradecyl fatty acid added is 60~120g / t; in both stages of sweeping and selection, the amount of sodium tetradecyl fatty acid added is 80~160g / t.

[0042] In some specific embodiments, the amount of reagent added can be adjusted according to the different components of the high-magnesium and high-silicon collophosphate ore.

[0043] Example 1

[0044] This embodiment provides a positive flotation process for high-magnesium and high-silicon collophosphate ore. The components of the high-magnesium and high-silicon collophosphate ore include, by mass percentage, 18.25% P2O5, 6.12% MgO, 20.03% SiO2, and 36.67% CaO. The process specifically includes the following steps:

[0045] S1. Crushing the high-magnesium and high-silicon collophosphate ore to be selected to -2mm, and then wet grinding, the mass of the ore powder with a grinding fineness of -0.074mm accounts for 90.50% of the total mass of the ore powder; adding water to the slurry concentration of 30%;

[0046] S2. Adding a roughing agent to the ore pulp of step S1 to perform roughing to obtain a roughing concentrate and a roughing tailing; the roughing agent includes 1500 g / t of water glass, 800 g / t of inhibitor DP (the mass ratio of each component is aluminum sulfate: citric acid: tannic acid: hydroxypropyl cellulose = 5:2:1:1), and 360 g / t of sodium tetradecyl fatty acid;

[0047] S3, the rougher concentrate obtained in step S2 is subjected to two-stage concentrating to obtain phosphate concentrate, and the selected middlings obtained in the two stages of concentrating are combined and further subjected to two-stage middling reselection; wherein the reselected concentrate from the first stage of middling reselection is returned to the rougher process in step S2, and the reselected concentrate from the second stage of middling reselection is returned to the first stage of middling reselection, and the reselected tailings from the second stage of middling reselection are the final tailings II;

[0048] The amount of inhibitor DP added in the first stage of concentration is 200 g / t, and the amount of inhibitor DP added in the second stage of concentration is 100 g / t; the reagents for reselection of the middlings in the first stage include 120 g / t of inhibitor DP and 100 g / t of sodium tetradecyl fatty acid, and the reagents for reselection of the middlings in the second stage include 80 g / t of sodium tetradecyl fatty acid;

[0049] S4. The roughing tailings obtained in step S2 are subjected to two-stage scavenging to obtain final tailings I. The scavenged tailings obtained by scavenging are returned to the previous operation step by step; the scavenging reagent includes 100 g / t of sodium tetradecyl fatty acid.

[0050] The phosphate concentrate obtained in Example 1 and the flotation results were tested, and the results showed that the P2O5 content of the phosphate concentrate was 32.25%, the recovery rate was 78.85%, the MgO content in the phosphate concentrate was 0.91%, and the SiO2 content was 9.98%.

[0051] Example 2

[0052] This embodiment provides a positive flotation process for high-magnesium and high-silicon collophosphate ore. Compared with Example 1, the difference is that the components of the high-magnesium and high-silicon collophosphate ore include, by mass percentage, 19.16% P2O5, 7.44% MgO, 23.48% SiO2, and 34.98% CaO. The rest are roughly the same as in Example 1 and will not be repeated here.

[0053] Comparative Example 1

[0054] Comparative Example 1 provides a positive flotation process for high-magnesium and high-silicon collophosphate. Compared with Example 1, the difference is that sodium hexametaphosphate inhibitor is used instead of inhibitor DP. The rest is roughly the same as Example 1 and will not be repeated here.

[0055] Comparative Example 2

[0056] Comparative Example 2 provides a positive flotation process for high-magnesium and high-silicon collophosphate. Compared with Example 1, the difference is that the inhibitor DP does not contain aluminum sulfate, and the mass ratio of the components is citric acid: tannic acid: hydroxypropyl cellulose = 2:1:1. The rest is roughly the same as Example 1 and will not be repeated here.

[0057] Comparative Example 3

[0058] Comparative Example 3 provides a positive flotation process for high-magnesium and high-silicon collophosphate. Compared with Example 1, the difference is that the inhibitor DP does not contain citric acid, and the mass ratio of the components is aluminum sulfate: tannic acid: hydroxypropyl cellulose = 5:1:1. The rest is roughly the same as Example 1 and will not be repeated here.

[0059] Comparative Example 4

[0060] Comparative Example 4 provides a positive flotation process for high-magnesium and high-silica collophosphate. Compared with Example 1, the difference is that the inhibitor DP does not contain tannic acid, and the mass ratio of the components is aluminum sulfate: citric acid: hydroxypropyl cellulose = 5:2:1. The rest is roughly the same as Example 1 and will not be repeated here.

[0061] Comparative Example 5

[0062] Comparative Example 5 provides a positive flotation process for high-magnesium and high-silicon collophosphate. Compared with Example 1, the difference is that the inhibitor DP does not contain hydroxypropyl cellulose, and the mass ratio of each component is aluminum sulfate: citric acid: hydroxypropyl cellulose = 5:2:1. The rest is roughly the same as Example 1 and will not be repeated here.

[0063] The phosphate concentrates obtained in Examples 1-2 and Comparative Examples 1-5 and the flotation results were tested, and the results obtained are shown in the following table.

[0064] Table 1 Correlation test results of Examples 1-2 and Comparative Examples 1-5

[0065]

[0066] As shown in Table 1, in Comparative Example 1, conventional sodium hexametaphosphate inhibitor was used instead of the novel inhibitor DP of the present invention in the process of the present invention. Compared with Example 1, the recovered phosphate concentrate had a lower P2O5 content and higher MgO and SiO2 contents, indicating poor removal of dolomite and quartz during flotation. Comparative Examples 2-5 demonstrate that the components of the inhibitor DP (aluminum sulfate: citric acid: tannic acid: hydroxypropyl cellulose = 5:2:1:1) exhibit a synergistic inhibitory effect; lacking any of these components, the flotation performance of the high-magnesium, high-silica collophosphate ore of Examples 1 and 2 cannot be achieved.

[0067] In summary, the present invention provides a positive flotation process for high-magnesium and high-silicon collophanite. First, the raw ore is crushed and wet-ground, and water is added to prepare a pulp. The pulp is then subjected to roughing to obtain a roughing concentrate and a roughing tailing. The roughing concentrate is then subjected to two-stage selection to obtain a phosphate concentrate. The selected middlings obtained from the two stages of selection are combined and then subjected to two-stage middling reselection. The reselected tailings from the second stage of middling reselection are the final tailings II. The roughing tailings are subjected to two-stage scavenging to obtain the final tailings I. The present invention adopts an acid-free positive flotation process. With the coordinated cooperation of the process and the reagent, the efficient separation of collophanite from dolomite and quartz is achieved, and the concentrate grade and recovery rate of the collophanite are improved. Moreover, with the combined action of the effective inhibitor DP and the collector, the total drug consumption is only 30% of that of the existing process, which greatly reduces the drug consumption and saves the cost of the reagent. The process of the present invention has the advantages of simple process, low reagent consumption, high economic benefit, environmental friendliness, and high practicality. The present invention flots collophanite in a neutral slurry environment, achieving acid-free direct flotation of high-magnesium, high-silicon collophanite. This effectively avoids corrosion to equipment and environmental impacts caused by strongly acidic slurries, avoids excessive foam viscosity in alkaline direct flotation processes, and ensures the stability of the production process. Compared with existing combined direct and reverse flotation or reverse flotation processes, the present process is simpler, eliminates the need for separate desiliconization and dephosphorization steps, and is carried out entirely in a neutral slurry. This avoids the problem of excessive acid or alkali consumption caused by the exchange of strongly acidic and strongly alkaline slurries, resulting in higher economic benefits.

[0068] The above embodiments are only used to illustrate the technical solutions of the present invention and are not intended to limit the present invention. Although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solutions of the present invention may be modified or replaced by equivalents without departing from the spirit and scope of the technical solutions of the present invention.

Claims

1. A positive flotation process for high-magnesium and high-silicon collophosphate, characterized in that: The process is implemented in a neutral slurry environment and includes the following steps: S1. Crushing the high-magnesium and high-silicon collophosphate ore to be selected, and wet grinding it to a certain fineness, and adding water to the pulp concentration of 30% to 35%; S2, adding a roughing agent to the slurry of step S1 to perform roughing to obtain a roughing concentrate and a roughing tailing; the roughing agent comprises water glass, an inhibitor DP and sodium tetradecyl fatty acid; S3, the rougher concentrate obtained in step S2 is subjected to two-stage concentrating to obtain phosphate concentrate, and the selected middlings obtained in the two stages of concentrating are combined and further subjected to two-stage middling reselection; wherein the reselected concentrate from the first stage of middling reselection is returned to the rougher process in step S2, and the reselected concentrate from the second stage of middling reselection is returned to the first stage of middling reselection, and the reselected tailings from the second stage of middling reselection are the final tailings II; The reagents for the two-stage selection include the inhibitor DP, the reagents for the first-stage middling reselection include the inhibitor DP and sodium tetradecyl fatty acid, and the reagents for the second-stage middling reselection include sodium tetradecyl fatty acid; S4, the roughing tailings obtained in step S2 are subjected to two-stage scavenging to obtain final tailings I, and the scavenged tailings obtained by scavenging are returned to the previous operation step by step; the scavenging agent includes sodium tetradecyl fatty acid; In step S2 and step S3, the components of the inhibitor DP include aluminum sulfate, citric acid, tannic acid and hydroxypropyl cellulose; The components of the inhibitor DP include, by mass percentage, 45% to 55% of aluminum sulfate, 15% to 25% of citric acid, 7% to 12% of tannic acid, and 7% to 12% of hydroxypropyl cellulose.

2. The positive flotation process of high-magnesium and high-silicon collophosphate according to claim 1, characterized in that: The components of the inhibitor DP include, by mass percentage, 50% aluminum sulfate, 20% citric acid, 10% tannic acid, and 10% hydroxypropyl cellulose.

3. The positive flotation process of high-magnesium and high-silicon collophosphate according to claim 1, characterized in that: In step S2, the mass ratio of the water glass, the inhibitor DP and the sodium tetradecyl fatty acid in the roughing agent is 15:8:3.

6.

4. The positive flotation process of high-magnesium and high-silicon collophosphate according to claim 1, characterized in that: In step S3, in the reagent for reselection of the first-stage middlings, the mass ratio of the inhibitor DP to sodium tetradecyl fatty acid is (1.1-1.3):

1.

5. The positive flotation process of high-magnesium and high-silicon collophosphate according to claim 1, characterized in that: In step S1, after the raw ore is wet-ground, the mass of the ore powder with a grinding fineness of -0.074 mm accounts for 90% to 92% of the total mass of the ore powder.

6. The positive flotation process of high-magnesium and high-silicon collophosphate according to claim 1, characterized in that: In step S3, in the two-stage concentrating process, the amount of inhibitor DP added in the second stage of concentrating is 0.5 to 1.0 times the amount of inhibitor DP added in the first stage of concentrating.

7. The positive flotation process of high-magnesium and high-silicon collophosphate according to claim 1, characterized in that: The components of the high-magnesium and high-silicon collophosphate ore include, by mass percentage, 17% to 19.5% of P2O5, 5.5% to 8% of MgO, 18% to 40% of SiO2, and 34% to 37% of CaO.

8. The direct flotation process of high-magnesium and high-silicon collophosphate according to claim 7, characterized in that: In the rough selection, the amount of water glass added is 1000-2000 g / t, the amount of inhibitor DP added is 700-1000 g / t, and the amount of sodium tetradecyl fatty acid added is 300-500 g / t.

9. The direct flotation process of high-magnesium and high-silicon collophosphate according to claim 8, characterized in that: In the two-stage concentration process, the amount of inhibitor DP added in the first stage of concentration is 100~300g / t, and the amount of inhibitor DP added in the second stage of concentration is 100~300g / t; in the first stage of middling reselection, the amount of inhibitor DP added is 100~200g / t, and the amount of sodium tetradecyl fatty acid added is 80~160g / t; in the second stage of middling reselection, the amount of sodium tetradecyl fatty acid added is 60~120g / t; in both stages of sweeping and selection, the amount of sodium tetradecyl fatty acid added is 80~160g / t.

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