Recovery process of titanium resource in vanadium-titanium-iron concentrate

Abstract

The invention discloses a process for recovering titanium resources in vanadium-titanium-iron concentrate, and relates to the technical field of mineral processing. The recycling process comprises a selective dissociation stage, a cascade separation stage and a flotation stage, and based on the innovative process of selective dissociation-cascade separation-collaborative separation, the technical index that the recycling rate of the micro-fine-particle ilmenite (-0.045 mm) breaks through 85% is achieved by optimizing an ore grinding system, conducting composite force field separation and combining novel agents. Compared with a traditional agent, the novel agent is small in dosage and high in recovery rate, and the recovery cost of titanium resources is greatly saved; a closed cycle system enables the wastewater circulation rate to reach 100%; and the obtained titanium concentrate is high in quality, and a flotation reagent is environmentally friendly.

Description

Technical Field

[0001] The present invention relates to the technical field of mineral processing, in particular to a process for recovering titanium resources from vanadium-titanium iron concentrate. Background Art

[0002] Vanadium-titanium magnetite is an important polymetallic mineral resource in my country, rich in various metallic elements, including iron, titanium, and vanadium. In existing mineral processing techniques, staged grinding and weak magnetic separation are typically used to recover iron concentrate. However, the iron concentrate still contains a large amount of titanium resources, primarily ilmenite. This is due to the complex symbiotic relationship between titanium and iron in vanadium-titanium magnetite. On the one hand, approximately 40% of the titanium, in the form of micron-sized ilmenite flakes (0.01mm-0.03mm), is embedded in the interstices between magnetite particles and easily enters the product with the iron concentrate during weak magnetic separation. On the other hand, approximately 10% of the titanium exists as a solid solution in the titanomagnetite lattice. This lattice substitution phenomenon makes it difficult to completely separate iron and titanium using physical separation methods.

[0003] The current ilmenite recovery technology in vanadium-titanium iron concentrate faces multiple technical bottlenecks: First, the embedded particle size of ilmenite is extremely fine (-0.038mm particle size accounts for more than 60%), and traditional gravity separation and magnetic separation equipment have low recovery efficiency, with operating recovery rates generally below 38%; second, although the flotation process can partially solve the problem, it requires the consumption of a large amount of inhibitors (such as water glass) and collectors (such as fatty acids), which not only has high reagent costs but also causes serious water pollution; third, fine-grained minerals are prone to non-selective agglomeration due to their high surface energy, resulting in an inversion of concentrate grade and recovery rate (TiO2 recovery rate <40%); in addition, ilmenite and major gangue minerals (such as pyroxene and hornblende) are extremely similar in physical and chemical properties, further reducing the sorting efficiency.

[0004] Existing patent technologies, such as Chinese patent CN115254397A, disclose a method for producing high-grade iron concentrate and titanium middlings from vanadium-titanium magnetite concentrate. The method uses alkali fusion-magnetic separation to treat vanadium-titanium magnetite concentrate. Although low-titanium iron concentrate and TiO2-rich titanium material can be obtained, the final product is only titanium middlings and it is difficult to further improve the grade. Chinese patent CN114054204A discloses a method for improving the quality of Panxi titanium magnetite concentrate, reducing titanium and sulfur. The method prepares the iron concentrate obtained from the second-stage grinding-magnetic separation in Panxi into a slurry; the slurry is transported to a grinding equipment (stirred mill) for grinding; the finely ground iron concentrate is subjected to a "one coarse, one fine, one sweep" magnetic separation process for iron separation to obtain a selected iron concentrate, but the titanium and sulfur content is reduced, and the separated ilmenite is not effectively recovered. The above technologies fail to simultaneously solve the three core problems of low grade, low recovery rate, and high cost in the recovery process of titanium resources in vanadium-titanium iron concentrate.

[0005] In view of this, the present invention is proposed. Summary of the Invention

[0006] The purpose of the present invention is to provide a process for recovering titanium resources from vanadium-titanium iron concentrate to solve the above technical problems.

[0007] The present invention is achieved in that: In a first aspect, an embodiment of the present invention provides a process for recovering titanium resources from vanadium-titanium iron concentrate, the recovery process comprising a selective dissociation stage, a cascade separation stage, and a flotation stage; Among them, in the selective dissociation stage, the -0.045mm particle size accounts for 80%-95%, and the -0.019mm particle size accounts for 45%-60%; In the step separation stage, the magnetic field strength is 0.1T-1.4T, and the separation concentration is 20%-30%; In the flotation stage, 550g / t-650g / t of modified collector and 750g / t-850g / t of combined depressant are used.

[0008] The present invention has the following beneficial effects: The titanium resource recovery process from vanadium-titanium iron concentrate provided by the present invention is based on an innovative process of "selective dissociation-cascade separation-coordinated sorting." By optimizing the grinding system, composite force field sorting, and combining novel reagents, the process achieves a recovery rate exceeding 80% for fine-grained ilmenite (-0.045 mm) in vanadium-titanium iron concentrate. Compared to traditional reagents, the novel reagent requires less, significantly reducing titanium resource recovery costs. The closed-loop system achieves a 100% wastewater recycling rate, resulting in superior titanium concentrate quality. Furthermore, the flotation reagents are environmentally friendly. BRIEF DESCRIPTION OF THE DRAWINGS

[0009] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for use in the embodiments. It should be understood that the following drawings only illustrate certain embodiments of the present invention and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other relevant drawings can be obtained based on these drawings without paying any creative work.

[0010] Figure 1 This is a schematic diagram of the process for recovering titanium resources from vanadium-titanium iron concentrate. DETAILED DESCRIPTION

[0011] To make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention are described clearly and completely below. Where specific conditions are not specified in the embodiments, conventional conditions or conditions recommended by the manufacturer are used. Where the manufacturer of the reagents or instruments is not specified, all are conventional products that can be purchased commercially.

[0012] In a first aspect, an embodiment of the present invention provides a process for recovering titanium resources from vanadium-titanium iron concentrate, the recovery process comprising a selective dissociation stage, a cascade separation stage, and a flotation stage; Among them, in the selective dissociation stage, the -0.045mm particle size accounts for 80%-95%, and the -0.019mm particle size accounts for 45%-60%; In the step separation stage, the magnetic field strength is 0.1T-0.35T, and the separation concentration is 20%-30%; In the flotation stage, 550g / t-650g / t of modified collector and 750g / t-850g / t of combined depressant are used.

[0013] It should be noted that the recovery process of titanium resources in vanadium-titanium iron concentrate provided in the embodiment of the present invention is based on the innovative process of "selective dissociation-cascade separation-coordinated sorting". By optimizing the grinding system, composite force field sorting and new reagent combination, it achieves the technical indicator of exceeding 80% recovery rate of fine-grained ilmenite (-0.045mm); the TiO2 recovery rate is increased from 38% of the traditional process to 81.2%; the amount of collector is reduced by 45%, and the amount of inhibitor is reduced by 30%; the final titanium concentrate TiO2 grade is ≥47%, and the silicate impurity content is ≤4.5%; the wastewater recycling rate reaches 100%.

[0014] The selective dissociation stage includes selective dissociation enhancement technology based on particle size characteristic regulation, multi-stage classification and regrinding coordinated dissociation to achieve differentiated dissociation of ilmenite and gangue minerals, and the monomer dissociation degree is increased from 78% of the traditional process to more than 94%.

[0015] Specifically, this embodiment uses a hydrocyclone to pre-separate the slurry to a particle size of greater than 80% of the -0.045mm fraction. Specifically, in this embodiment, the -0.045mm fraction accounts for 80%-95%. This is then combined with a vertical mill (using Ø3mm zirconia balls) for selective regrinding. Through real-time monitoring, the -0.019mm fraction is controlled at 45%-60%, thereby achieving selective dissociation of the ore. In other embodiments of the present invention, the specifications of the sorting equipment, grinding equipment, and media size can be appropriately selected based on actual needs.

[0016] In an optional embodiment, the recovery process also includes a raw material pretreatment stage, wherein the -0.074 mm particle size accounts for >70%, the inorganic dispersant is 20g / t-30g / t, and the pulp concentration is 60%-70%.

[0017] In an optional embodiment, the inorganic dispersant is selected from at least one of sodium hexametaphosphate, sodium tripolyphosphate, sodium pyrophosphate and silicate.

[0018] It should be noted that, in the embodiment of the present invention, adding an inorganic dispersant before grinding, combined with mechanical stirring (e.g., 1200 rpm×5 min), is beneficial to destroying the surface charge agglomeration of fine-grained ilmenite, adjusting the zeta potential of the ore pulp from -25 mV to -38 mV, and significantly improving the subsequent sorting efficiency.

[0019] In the optimal embodiment, the inorganic dispersant is sodium hexametaphosphate, which dissociates a large number of negatively charged phosphate groups, adsorbs on the surface of the particles, forms a double layer, increases the electrostatic repulsion between particles, thereby inhibiting agglomeration and achieving dispersion.

[0020] In an optional embodiment, the selective dissociation stage further comprises a media filling rate of 35%-45%, a grinding concentration of 60%-70%, and a mill speed of 15 Hz-25 Hz.

[0021] It should be noted that by adjusting the mill speed through frequency conversion, over-crushing can be suppressed, the target mineral dissociation degree can be increased by 14 percentage points, and the generation of -5μm fine mud can be reduced by 30%.

[0022] In an optional embodiment, the cascade separation stage includes primary separation, secondary separation, tertiary separation, and quaternary separation.

[0023] Among them, the magnetic field strength of the first-stage separation and the second-stage separation is independently 0.3T-0.35T; the magnetic field strength of the third-stage separation is 0.15T-0.2T; and the magnetic field strength of the fourth-stage separation is 0.2T-0.3T.

[0024] It should be noted that the equipment used in the cascade separation stage can be reasonably selected according to actual needs, and the present invention does not make any special restrictions. Specifically in this embodiment, the first-stage separation and the second-stage separation are high-gradient magnetic separation: a SLon magnetic separator (background field strength 0.2T, stroke 15mm) is used to preferentially release ilmenite particles with a better degree of dissociation, and the pre-enrichment ratio reaches 3.2-3.5. The third-stage separation and the fourth-stage separation are high-frequency harmonic magnetic separation: the dual forces of high-frequency harmonic alternating magnetic field and mineral rotation are used to release the magnetically encapsulated ultrafine-grained ilmenite. After the Panxi iron ore concentrate passes through the fourth stage separation, the released ultrafine-grained ilmenite is recovered by flotation, wherein a microporous ceramic foamer (wherein the bubble size is 10μm-50μm) is used for enhanced mineralization treatment, which increases the recovery rate of fine-grained ilmenite by 22 percentage points.

[0025] The present invention uses magnetic-gravity-flotation composite force field separation in the cascade separation stage, and the total recovery rate of ilmenite is increased by 28% compared with the single flotation process, and the TiO2 grade of the concentrate is stabilized at more than 47%.

[0026] In an optional embodiment, after cascade separation, the TiO2 grade of the ilmenite is 14%-26%.

[0027] In an optional embodiment, the modified collector is selected from at least one of modified oleic acid, stearic acid, oxidized paraffin soap, tall oil fatty acid, and fatty acid methyl ester.

[0028] In the most preferred embodiment, the modified collector is modified oleic acid.

[0029] It should be noted that the traditional oleic acid is sulfonated and modified with hydroxyl oxime (introducing -SO3H and -C(OH)=NOH‌ groups) to improve the selective adsorption capacity of ilmenite in weakly acidic media (pH=3.5-5.0), reducing the collector dosage from 1200g / t to 600g / t, and the adsorption rate of pyroxene and hornblende to more than 85%.

[0030] In an alternative embodiment, the combined inhibitor comprises an organic dispersant and a polysaccharide in a mass ratio of (2.5-3.5):(0.5-1.5).

[0031] In an optional embodiment, the organic dispersant is selected from at least one of sodium humate, sodium polyaspartate, sodium gluconate, tannic acid, oxalic acid and urea; the polysaccharide is selected from at least one of maltodextrin, cyclodextrin, oligofructose, oligogalactose, chitosan oligosaccharide, soluble starch, cellulose, pectin, xanthan gum, hyaluronic acid, carboxymethyl cellulose, hydroxypropyl methylcellulose and hydroxyethyl cellulose.

[0032] Compared with traditional agents, the use of new agents reduces the amount of collectors by 45% and the amount of inhibitors by 30%, greatly reducing the cost of using agents and saving the cost of recovering titanium resources.

[0033] In the optimal embodiment, the organic dispersant is sodium humate and the polysaccharide is carboxymethyl cellulose. The dosage of the two can be selected from any one of 2.5:0.5, 3:1, 3.2:1.3, 3.5:1.2 and 3.5:1.5, or other values ​​within the range of (2.5-3.5): (0.5-1.5).

[0034] The combined inhibitor formed by sodium humate and carboxymethyl cellulose reduces the floatability of silicate gangue minerals by 40% and the total amount of inhibitor used by 30% through the dual effects of steric hindrance and electrostatic repulsion.

[0035] In an optional embodiment, the flotation stage adopts a "one roughing, three fines, and three scavenging" closed-circuit operation process; specifically, it includes one roughing, three fines, and three scavenging processes, see Figure 1 Schematic diagram of the process for recovering titanium resources from vanadium-titanium iron concentrate.

[0036] In an optional embodiment, the pH in the roughing stage is 3.5-5.0; 15g / t-25g / t of a foaming agent is added in the cleaning stage; and the foaming agent is selected from at least one of MIBC, pine oil, methyl isobutyl carbinol, sodium lauryl sulfate and acetone.

[0037] In an optional embodiment, the flotation roughing stage uses microbubble flotation technology with a bubble size of 10 μm-50 μm.

[0038] It should be noted that the slurry flow state is regulated during the flotation stage. Specifically, guide plates and flow stabilizers are installed in the flotation tank to reduce the slurry flow rate from 0.8m / s to 0.5m / s, prolonging the contact time between fine mineral particles and bubbles to 12s-15s, and increasing the mineralization probability by 35%. In addition, microbubble flotation technology is used, using a 0.1mm diameter microporous ceramic bubbler, and using the bubble-particle collision probability model based on the Stokes equation and DLVO theory to optimize the microbubble generator parameters (gas flow rate 0.3m 3 / h, pressure 0.15MPa), the mineralization efficiency of -0.01mm ilmenite reaches 58% (the traditional process is only 36%).

[0039] In an optional embodiment, the recovery process further includes a tail water treatment stage, wherein the tail water is treated with ozone, polyaluminum chloride, and a flocculant.

[0040] In an optional embodiment, after the tail water is treated, the degradation rate of organic pollutants is >90%, and the solid content is less than 200 mg / L.

[0041] It should be noted that the tail water treatment in the present invention adopts a closed-loop circulation and pollution control treatment system. After the flotation wastewater is catalytically oxidized by ozone to degrade organic matter, 80% of it is reused for grinding operations, and 20% is added with flocculants for precipitation treatment and discharged after meeting the standards. Specifically, in the ozone catalytic oxidation treatment, the flotation tail water is treated with ozone (dosage 50mg / L) and Fe 20 Nano-catalyst synergistic treatment achieves an organic pollutant degradation rate of >90%, and the recycled water quality meets the first-level standard of GB 8978-1996.

[0042] Modified polyaluminium chloride is used to achieve targeted removal of clay and colloidal substances, reducing the solid content of the return water to less than 200 mg / L.

[0043] The features and performance of the present invention are further described in detail below with reference to the embodiments.

[0044] Example 1 This embodiment provides a process for recovering titanium resources from vanadium-titanium iron concentrate. Figure 1 Processing flow: Raw material pretreatment stage: The dispersant used in grinding is sodium hexametaphosphate.

[0045] Selective dissociation stage: An iron concentrate from Panzhihua area (TFe 55.14%, -0.045mm particle size 82%) was taken, and the equipment was a hydrocyclone.

[0046] Cascade separation stage: After four-stage separation and enrichment, the crude titanium concentrate with a TiO2 grade of 21.3% was obtained, and the recovery rate of vanadium-titanium-iron concentrate was 58.7%; among them, the magnetic field strength of the first separation was 0.3T, the magnetic field strength of the second separation was 0.32T, the magnetic field strength of the third separation was 0.2T, and the magnetic field strength of the fourth separation was 0.3T. The equipment was a SLon magnetic separator.

[0047] Flotation stage: The collector used was modified oleic acid 580g / t and combined depressant 820g / t (the mass ratio of sodium humate to carboxymethyl cellulose was 3.5:1.2).

[0048] The final concentrate TiO2 grade is 47.20%, and the operating recovery rate is 87.50%; the processing cost per ton of ore is reduced by 18.6% compared with the traditional process.

[0049] Example 2 This embodiment provides a process for recovering titanium resources from vanadium-titanium iron concentrate. The difference between this recovery process and that of Example 1 is that: Raw material pretreatment stage: The dispersant used in grinding is sodium tripolyphosphate.

[0050] Cascade separation stage: After four-stage separation and enrichment, the crude titanium concentrate with a TiO2 grade of 20.98% was obtained, and the recovery rate of vanadium-titanium iron concentrate was 57.69%.

[0051] Flotation stage: The collector used was modified oleic acid 600g / t and combined depressant 800g / t (the mass ratio of sodium humate to carboxymethyl cellulose was 3.5:1.2).

[0052] The final concentrate TiO2 grade is 47.16%, and the operating recovery rate is 86.27%.

[0053] Example 3 This embodiment provides a process for recovering titanium resources from vanadium-titanium iron concentrate. The difference between this recovery process and that of Example 1 is that: Flotation stage: combined depressant (sodium humate and carboxymethyl cellulose mass ratio of 3:1).

[0054] The final concentrate TiO2 grade is 47.23%, and the operating recovery rate is 87.06%.

[0055] Comparative Example 1 This comparative example provides a process for recovering titanium resources from vanadium-titanium iron concentrate, which differs from Example 1 only in that: Cascade separation stage: Four-stage magnetic separation uses a conventional drum magnetic separator. After four-stage separation and enrichment, the crude titanium concentrate has a TiO2 grade of 13.3% and a vanadium-titanium-iron concentrate recovery rate of 18.7%.

[0056] The final concentrate TiO2 grade is 46.80%, and the operating recovery rate is 67.50%.

[0057] The four-stage magnetic separation equipment provided by the present invention is an effective equipment for separating fine-grained and ultrafine-grained ilmenite. If a traditional magnetic separator is used, the separation effect is poor.

[0058] Comparative Example 2 This comparative example provides a process for recovering titanium resources from vanadium-titanium iron concentrate, and the specific process is as follows: Selective dissociation stage: An iron concentrate from Panzhihua area (-0.074mm particle size accounts for 65%) was taken and ground using a ball mill (-0.038mm particle size accounts for 95%).

[0059] Cascade separation stage: The iron concentrate is separated by magnetic separation using a traditional semi-countercurrent drum magnetic separator. The ilmenite separated from the tailings has a dissociation degree of 84.30%, but it suffers from over-grinding (the -0.019mm particle size accounts for more than 85%).

[0060] Flotation stage: Use traditional flotation machine and traditional oleic acid collector for flotation.

[0061] The final titanium concentrate TiO2 grade is 44.80%, and the operating recovery rate is only 55.90%.

[0062] Comparative Example 3 This embodiment provides a process for recovering titanium resources from vanadium-titanium iron concentrate, which differs from embodiment 1 only in that: Raw material pretreatment stage: No dispersant was added during the grinding process.

[0063] Cascade separation stage: After four-stage separation and enrichment, the crude titanium concentrate has a TiO2 grade of 13.53% and a recovery rate of vanadium-titanium iron concentrate of 49.16%.

[0064] The final concentrate TiO2 grade is 45.92%, and the operating recovery rate is 73.18%.

[0065] The main reason is that no dispersant is added during the grinding process, resulting in over-grinding of the minerals, which increases the difficulty of subsequent flotation recovery by the magnetic separator, thereby reducing the recovery rate and grade.

[0066] Comparative Example 4 This embodiment provides a process for recovering titanium resources from vanadium-titanium iron concentrate, which differs from embodiment 1 only in that: Cascade separation stage: The four-stage magnetic separation was replaced with a three-stage magnetic separation, eliminating the fourth stage. The parameters for the first through third stages remained unchanged. The magnetic tailings were concentrated and then fed to flotation. After three-stage separation and enrichment, the crude titanium concentrate had a TiO2 grade of 18.56% and a vanadium-titanium-iron concentrate recovery rate of 61.23%.

[0067] The final concentrate TiO2 grade is 45.13%, and the operating recovery rate is 60.17%.

[0068] The reason for the poor recovery effect is that the three-stage magnetic separation results in some magnetite not being effectively recovered and entering the flotation operation, resulting in the TiO2 grade entering the flotation being lower than that of the four-stage magnetic separation, and the concentrate grade obtained in the flotation operation is low.

[0069] Comparative Example 5 This embodiment provides a process for recovering titanium resources from vanadium-titanium iron concentrate, which differs from embodiment 1 only in that: Cascade separation stage: After four-stage separation and enrichment, the crude titanium concentrate has a TiO2 grade of 21.3% and a recovery rate of vanadium-titanium iron concentrate of 58.7%.

[0070] Flotation stage: The collector used in the flotation stage is MOH 600g / t.

[0071] The final concentrate TiO2 grade is 44.12%, and the operating recovery rate is 70.18%.

[0072] The reason for the poor recovery effect is that MOH as a collector is difficult to effectively recover fine-grained ilmenite, so the concentrate grade and recovery rate are low.

[0073] Comparative Example 6 This embodiment provides a process for recovering titanium resources from vanadium-titanium iron concentrate, which differs from embodiment 1 only in that: Flotation stage: The inhibitor is water glass.

[0074] The final concentrate TiO2 grade is 43.09% and the operating recovery rate is 72.19%.

[0075] The reason for the poor recovery effect is that water glass as an inhibitor is difficult to effectively inhibit the gangue minerals in the fine-grained ilmenite, so the concentrate grade and recovery rate are low.

[0076] In summary, the process for recovering titanium resources in vanadium-titanium iron concentrate provided by the present invention is based on the innovative process of "selective dissociation-cascade separation-coordinated sorting". By optimizing the grinding system, composite force field sorting and new reagent combination, the technical indicator of the recovery rate of fine-grained ilmenite (-0.045mm) exceeds 80%; specifically: the titanium recovery rate is improved: the TiO2 recovery rate is increased from 38% of the traditional process to 81.2%; the reagent cost is reduced: the amount of collector is reduced by 45%, and the amount of inhibitor is reduced by 30%; the concentrate quality is optimized: the final titanium concentrate TiO2 grade is ≥47%; environmentally friendly: the wastewater reuse rate reaches 100%.

[0077] The foregoing description is merely a preferred embodiment of the present invention and is not intended to limit the present invention. Those skilled in the art will readily appreciate that various modifications and variations of the present invention are possible. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of the present invention are intended to be within the scope of protection of the present invention.

Claims

1. A process for recovering titanium resources from vanadium-titanium iron concentrate, characterized in that: The recovery process includes a selective dissociation stage, a cascade separation stage and a flotation stage; In the selective dissociation stage, the -0.045mm particle size accounts for 80%-95%, and the -0.019mm particle size accounts for 45%-60%; In the step separation stage, the magnetic field strength is 0.1T-0.35T, and the separation concentration is 20%-30%; In the flotation stage, 550g / t-650g / t of modified collector and 750g / t-850g / t of combined depressant are used.

2. The recycling process according to claim 1, characterized in that The selective dissociation stage also includes a media filling rate of 35%-45%, a grinding concentration of 60%-70%, and a mill speed of 15Hz-25Hz.

3. The recycling process according to claim 1, characterized in that The cascade separation stage includes primary separation, secondary separation, tertiary separation and quaternary separation; Among them, the magnetic field strength of the first-stage separation and the second-stage separation is independently 0.3T-0.35T; the magnetic field strength of the third-stage separation is 0.15T-0.2T; the magnetic field strength of the fourth-stage separation is 0.2T-0.3T; Preferably, after cascade separation, the TiO2 grade of the ilmenite is 14%-26%.

4. The recycling process according to claim 1, characterized in that The modified collector is selected from at least one of modified oleic acid, stearic acid, oxidized paraffin soap, tall oil fatty acid and fatty acid methyl ester.

5. The recycling process according to claim 1, characterized in that The combined inhibitor comprises an organic dispersant and a polysaccharide in a mass ratio of (2.5-3.5): (0.5-1.5); Preferably, the organic dispersant is selected from at least one of sodium humate, sodium polyaspartate, sodium gluconate, tannic acid, oxalic acid and urea; Preferably, the polysaccharide is selected from at least one of maltodextrin, cyclodextrin, fructooligosaccharide, galacto-oligosaccharide, chitosan oligosaccharide, soluble starch, cellulose, pectin, xanthan gum, hyaluronic acid, carboxymethyl cellulose, hydroxypropyl methylcellulose and hydroxyethyl cellulose.

6. The recycling process according to claim 1, characterized in that The flotation stage adopts a closed-circuit process of "one roughing, three fines, and three sweeping"; Preferably, the pH in the roughing stage is 3.5-5.0; Preferably, 15 g / t to 25 g / t of a foaming agent is added in the beneficiation stage; the foaming agent is selected from at least one of MIBC, pine oil, methyl isobutyl carbinol, sodium lauryl sulfate and acetone.

7. The recycling process according to claim 6, characterized in that Microbubble flotation technology is used in the roughing stage of flotation, with bubble size ranging from 10μm to 50μm.

8. The recycling process according to claim 1, characterized in that The recycling process also includes a raw material pretreatment stage, wherein the -0.074mm particle size accounts for >70%, an inorganic dispersant of 20g / t-30g / t, and a slurry concentration of 60%-70%; Preferably, the inorganic dispersant is selected from at least one of sodium hexametaphosphate, sodium tripolyphosphate, sodium pyrophosphate and silicate.

9. The recycling process according to claim 1, characterized in that The recovery process also includes a tail water treatment and recycling stage, in which the tail water is treated with at least one of ozone, polyaluminium chloride and flocculant.

10. The recycling process according to claim 9, characterized in that After tail water treatment, the degradation rate of organic pollutants is >90% and the solid content is less than 200 mg / L.

Images