CN114682386B - Fractional step flotation method for treating medium-low grade silicon-calcium collophanite - Google Patents
Fractional step flotation method for treating medium-low grade silicon-calcium collophanite Download PDFInfo
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- CN114682386B CN114682386B CN202011568758.7A CN202011568758A CN114682386B CN 114682386 B CN114682386 B CN 114682386B CN 202011568758 A CN202011568758 A CN 202011568758A CN 114682386 B CN114682386 B CN 114682386B
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- 238000005188 flotation Methods 0.000 title claims abstract description 236
- 238000000034 method Methods 0.000 title claims abstract description 73
- OSMSIOKMMFKNIL-UHFFFAOYSA-N calcium;silicon Chemical compound [Ca]=[Si] OSMSIOKMMFKNIL-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 239000012141 concentrate Substances 0.000 claims abstract description 89
- 239000000463 material Substances 0.000 claims abstract description 35
- 238000000227 grinding Methods 0.000 claims abstract description 30
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000012216 screening Methods 0.000 claims abstract description 18
- 229910052500 inorganic mineral Inorganic materials 0.000 claims abstract description 15
- 239000011707 mineral Substances 0.000 claims abstract description 15
- 230000002441 reversible effect Effects 0.000 claims abstract description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 7
- -1 aluminum silicon-calcium Chemical compound 0.000 claims abstract description 5
- 229910052742 iron Inorganic materials 0.000 claims abstract description 5
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims abstract description 3
- 239000006260 foam Substances 0.000 claims description 28
- 229910019142 PO4 Inorganic materials 0.000 claims description 26
- 239000010452 phosphate Substances 0.000 claims description 26
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 26
- 238000003756 stirring Methods 0.000 claims description 26
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 claims description 18
- 239000011734 sodium Substances 0.000 claims description 16
- 239000003795 chemical substances by application Substances 0.000 claims description 14
- 239000002253 acid Substances 0.000 claims description 12
- 238000007873 sieving Methods 0.000 claims description 12
- 239000004115 Sodium Silicate Substances 0.000 claims description 10
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 10
- 239000000194 fatty acid Substances 0.000 claims description 10
- 229930195729 fatty acid Natural products 0.000 claims description 10
- 229910052911 sodium silicate Inorganic materials 0.000 claims description 10
- 150000004676 glycans Chemical class 0.000 claims description 9
- 229920000620 organic polymer Polymers 0.000 claims description 9
- 150000008442 polyphenolic compounds Chemical class 0.000 claims description 9
- 235000013824 polyphenols Nutrition 0.000 claims description 9
- 229920001282 polysaccharide Polymers 0.000 claims description 9
- 239000005017 polysaccharide Substances 0.000 claims description 9
- 150000004665 fatty acids Chemical class 0.000 claims description 8
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 7
- 239000000292 calcium oxide Substances 0.000 claims description 7
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 6
- 239000000344 soap Substances 0.000 claims description 6
- 229920001353 Dextrin Polymers 0.000 claims description 4
- 239000004375 Dextrin Substances 0.000 claims description 4
- 235000019425 dextrin Nutrition 0.000 claims description 4
- 239000003112 inhibitor Substances 0.000 claims description 4
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 3
- 150000007522 mineralic acids Chemical class 0.000 claims description 3
- 229920002472 Starch Polymers 0.000 claims description 2
- 239000001913 cellulose Substances 0.000 claims description 2
- 229920002678 cellulose Polymers 0.000 claims description 2
- 235000010980 cellulose Nutrition 0.000 claims description 2
- 229920001277 pectin Polymers 0.000 claims description 2
- 239000001814 pectin Substances 0.000 claims description 2
- 235000010987 pectin Nutrition 0.000 claims description 2
- 230000002000 scavenging effect Effects 0.000 claims description 2
- 239000008107 starch Substances 0.000 claims description 2
- 235000019698 starch Nutrition 0.000 claims description 2
- 229920001864 tannin Polymers 0.000 claims description 2
- 239000001648 tannin Substances 0.000 claims description 2
- 235000018553 tannin Nutrition 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 14
- 230000008901 benefit Effects 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 4
- 238000000926 separation method Methods 0.000 abstract description 4
- 230000002829 reductive effect Effects 0.000 abstract description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052782 aluminium Inorganic materials 0.000 abstract description 2
- 239000011362 coarse particle Substances 0.000 abstract 1
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000010419 fine particle Substances 0.000 abstract 1
- 235000019353 potassium silicate Nutrition 0.000 description 8
- 239000000203 mixture Substances 0.000 description 5
- 239000002367 phosphate rock Substances 0.000 description 5
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- OJMIONKXNSYLSR-UHFFFAOYSA-N phosphorous acid Chemical compound OP(O)O OJMIONKXNSYLSR-UHFFFAOYSA-N 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 230000007547 defect Effects 0.000 description 3
- 229920002261 Corn starch Polymers 0.000 description 2
- 239000008120 corn starch Substances 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 230000002401 inhibitory effect Effects 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 150000004670 unsaturated fatty acids Chemical class 0.000 description 2
- 235000021122 unsaturated fatty acids Nutrition 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 235000020774 essential nutrients Nutrition 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000002686 phosphate fertilizer Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/001—Flotation agents
- B03D1/018—Mixtures of inorganic and organic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B7/00—Combinations of wet processes or apparatus with other processes or apparatus, e.g. for dressing ores or garbage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B9/00—General arrangement of separating plant, e.g. flow sheets
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/007—Modifying reagents for adjusting pH or conductivity
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/02—Collectors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/06—Depressants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2203/00—Specified materials treated by the flotation agents; specified applications
- B03D2203/02—Ores
- B03D2203/04—Non-sulfide ores
- B03D2203/06—Phosphate ores
Abstract
The invention relates to a grading step-by-step flotation method for treating low-grade silicon-calcium collophanite, which adopts a grading step-by-step flotation process, firstly, raw ore is subjected to crushing operation and then is subjected to screening operation, and the raw ore is screened into coarse and fine particle fractions; and then removing silicate gangue minerals in the fine-fraction materials by adopting forward flotation, performing forward flotation on the obtained forward flotation concentrate and the coarse-fraction materials again to remove silicate gangue minerals, and finally removing carbonate gangue minerals in the obtained forward flotation concentrate by adopting reverse flotation. The process is not only suitable for the high-iron aluminum silicon-calcium collophanite, but also suitable for the weathered silicon-calcium collophanite. Compared with the conventional forward-reverse flotation process, the undersize fine fraction materials are separated step by step for a plurality of times, so that the separation property of the fine fraction materials is greatly improved, and the recovery rate loss caused by fine fraction mechanical entrainment in the flotation operation is reduced; in addition, the process reduces the energy consumption of ore grinding, thereby reducing the ore dressing cost. The process has the advantages of stable mineral separation process flow, good separation effect, high concentrate recovery rate, low iron and aluminum half oxides in concentrate products and the like.
Description
Technical Field
The invention belongs to the technical field of mineral processing, and particularly relates to a grading step-by-step flotation method for treating medium-low grade silicon-calcium collophanite.
Background
Phosphate fertilizers are essential nutrients for agricultural production. Phosphate ore is used as the main raw material of phosphate fertilizer. No material is found in the world to replace it. As the world population grows, so does the demand for phosphate fertilizers. In China, phosphorite resources are mainly concentrated in Yun Guichuan Hunan jaw places and the like, sedimentary phosphorite is mainly used, medium-grade and low-grade collophanite is mainly used, and qualified phosphate concentrate can be produced for a phosphate chemical industry through beneficiation enrichment of the medium-grade and low-grade phosphorite. Due to processing and engineering problems, the utilization rate of the resource is low.
At present, the conventional process flow aiming at the middle-low grade silicon-calcium collophanite is a forward-reverse flotation process flow and a pre-desliming-double reverse flotation process flow, and the forward-reverse flotation process has the defects of finer grinding fineness, finer granularity of concentrate products, difficult concentrate conveying and dewatering operation, higher concentrate dressing cost and the like. The prior desliming-double reverse flotation process flow has the defects of poor reagent selectivity, large influence on the flow by mineral mud, serious loss of desliming operation P 2O5 and low recovery rate of final concentrate P 2O5. The conventional process flow has the technical problems of difficult concentration and difficult defoaming, has poor comprehensive technical and economic indexes, and cannot guarantee stable production.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a beneficiation method for the middle-low grade silicon-calcium collophanite, which has more reasonable process, high efficiency and high sortability.
The technical problems to be solved by the invention are realized by the following technical proposal. The invention relates to a grading step-by-step flotation method for treating medium-low grade silicon-calcium collophanite, which is characterized by comprising the following steps of: the method comprises the steps of adopting a grading step-by-step flotation process, crushing raw ore, then feeding the crushed raw ore into screening operation, and screening the crushed raw ore into coarse and fine grain fractions; and then removing silicate gangue minerals in the fine-fraction materials by adopting forward flotation, performing forward flotation on the obtained forward flotation concentrate and the coarse-fraction materials again to remove silicate gangue minerals, and finally removing carbonate gangue minerals in the obtained forward flotation concentrate by adopting reverse flotation.
The invention relates to a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which has the further preferable technical scheme that: the ore type of the medium-low grade silicon-calcium collophanite is high-iron aluminum silicon-calcium collophanite or weathered silicon-calcium collophanite.
The invention relates to a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which has the further preferable technical scheme that: the medium-low grade silicon-calcium collophanite ore comprises the following components: the grade of P 2O5 is 16.2% -24%, the mass content of MgO is 1.0% -5.9%, and the mass content of SiO 2 is 12% -39%.
The invention relates to a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which has the further preferable technical scheme that: the method is characterized by comprising the following specific steps:
(1) Crushing raw ore, sieving with concentration of 30.00-50.00%, and grading with granularity of 0.074mm, 0.063mm or 0.045 mm;
(2) Adding undersize fine-fraction materials obtained by screening operation into a forward flotation stirring tank 1, sequentially adding an adjusting agent Na 2CO3 to adjust pH, adding polysaccharides and polyphenol organic polymer adjusting agents with the addition of 20-50g/t, adding sodium silicate to inhibit silicate with the addition of 200-5000 g/t, adding a forward flotation collecting agent with the addition of 500-2500 g/t, and then carrying out forward flotation operation 1, wherein a foam product is forward flotation concentrate 1, and a product in the tank is forward flotation tailings 1;
(3) The coarse-grain-grade material on the screen obtained by screening operation enters the ore grinding operation, the grinding fineness is 70-90% of-0.074 mm, and the material after ore grinding and the positive flotation concentrate 1 are mixed and fed into a positive flotation stirring tank 2; sequentially adding Na 2CO3 to adjust the pH, wherein the adding amount is 1000-2000g/t, adding sodium silicate to inhibit silicate, the adding amount is 100-4000 g/t, then adding a positive flotation collector, the adding amount is 500-2500 g/t, then carrying out positive flotation operation 2, wherein the foam product is positive flotation concentrate 2, and the product in the tank is positive flotation tailings 2;
(4) The direct flotation concentrate 2 is fed into a direct flotation magnesium-removing stirring tank, acid is firstly added to adjust the pH, the addition amount is 4000-8000g/t, then a direct flotation collector is added, the addition amount is 100-500 g/t, then the direct flotation operation is carried out, the foam product is magnesium-removing direct flotation tailings, and the product in the tank is magnesium-removing direct flotation concentrate, namely the final phosphate concentrate.
The invention relates to a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which has the further preferable technical scheme that: the method comprises the following specific steps:
(1) Crushing raw ore, sieving with concentration of 35.00-45.00%, and grading with granularity of 0.074mm, 0.063mm or 0.045 mm;
(2) Adding undersize fine-fraction materials obtained by screening operation into a forward flotation stirring tank 1, sequentially adding an adjusting agent Na 2CO3 to adjust the pH, wherein the adding amount is 2000-2500g/t, adding a polysaccharide and polyphenol organic polymer adjusting agent, the adding amount is 30-45g/t, adding sodium silicate to inhibit silicate, the adding amount is 1000-4000 g/t, then adding a forward flotation collecting agent, the adding amount is 1000-1500 g/t, then carrying out forward flotation operation 1, wherein a foam product is forward flotation concentrate 1, and a product in the tank is forward flotation tailings 1;
(3) The coarse-grain-grade material on the screen obtained by screening operation enters the ore grinding operation, the grinding fineness is 75-85% of-0.074 mm, and the material after ore grinding and the positive flotation concentrate 1 are mixed and fed into a positive flotation stirring tank 2; sequentially adding Na 2CO3 to adjust the pH, wherein the adding amount is 1500-2000g/t, adding sodium silicate to inhibit silicate, the adding amount is 1000-3000 g/t, then adding a positive flotation collector, the adding amount is 500-1500 g/t, then carrying out positive flotation operation 2, wherein the foam product is positive flotation concentrate 2, and the product in the tank is positive flotation tailings 2;
(4) The direct flotation concentrate 2 is fed into a direct flotation magnesium-removing stirring tank, acid is firstly added to adjust the pH, the addition amount is 4000-6000g/t, then a direct flotation collector is added, the addition amount is 200-300 g/t, then the direct flotation operation is carried out, the foam product is magnesium-removing direct flotation tailings, and the product in the tank is magnesium-removing direct flotation concentrate, namely the final phosphate concentrate.
The invention relates to a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which has the further preferable technical scheme that: the regulator polysaccharide and polyphenol organic polymer selected in the step (2) is selected from starch, cellulose, dextrin, tannin and pectin, and the collector is C 12-C20 higher fatty acid or fatty acid sodium salt.
The invention relates to a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which has the further preferable technical scheme that: in the step (2), the collecting agent in the positive flotation operation 2 is selected from fatty acid soap organic matters.
The invention relates to a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which has the further preferable technical scheme that: in the reverse flotation, the inhibitor is inorganic acid, the inorganic acid is sulfuric acid, phosphoric acid or a mixed acid of the sulfuric acid and the phosphoric acid, and the collector is fatty acid soap organic matters.
The invention relates to a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which has the further preferable technical scheme that: the flow structure of the forward flotation and reverse flotation is roughing operation or is formed by arbitrary combination of roughing operation and carefully selecting operation and scavenging operation.
The invention relates to a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which has the further preferable technical scheme that: the composition of the silicon-calcium collophanite ore is 17.5-22.5% of P 2O5 grade, the mass content of MgO is 1.5-3.0%, and the mass content of SiO 2 is 22.0-38.5%.
The invention combines the classification of phosphate rock with a multi-step flotation process, and provides a classification step-by-step flotation method for medium-low grade silicon-calcium collophanite, which has the following three advantages compared with the traditional process:
(1) Mineral separation cost is reduced: the phosphorite which is dissociated by the monomer is screened out in advance through classification operation, if a direct flotation process is adopted, ore grinding operation is needed to be added before flotation, and the classification cost is at least half lower than the ore grinding cost for the ore which is dissociated by the monomer.
(2) The particle size of the undersize fine-fraction minerals is controlled within a narrower range through classification operation, so that adverse effects of the mud formation of the weathered phosphate ores on flotation can be effectively solved. The classifying multi-step floatation of fine fraction mineral greatly improves the classifying property, and has the advantages of high comprehensive concentrate recovery rate and low iron and aluminum half oxides in concentrate products.
(3) The flotation operation adopts polysaccharides and polyphenols organic polymers as regulators, so that the fine fraction flotation environment can be effectively improved, and the recovery rate loss caused by fine fraction mechanical entrainment in the flotation operation is reduced.
The grade of the obtained comprehensive phosphate concentrate P 2O5 is 28.0% -31.5%, the mass content of MgO is 0.3% -1.5%, and the recovery rate of the phosphate concentrate P 2O5 is 75.0% -85.0%.
Detailed Description
Specific embodiments of the invention are described further below by way of example, so that those skilled in the art will further understand the invention without limiting the scope of the claims.
Embodiment 1, a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which specifically comprises the following steps:
(1) Crushing raw ore, sieving with concentration of 38.00% and granularity of 0.074 mm;
(2) Adding the fine-fraction material with the size of-0.074 mm obtained by sieving operation into a forward flotation stirring tank 1, sequentially adding a regulator Na 2CO3 to regulate the pH, wherein the addition amount is 2000g/t, adding a regulator dextrin to improve the fine-fraction flotation environment, the addition amount is 30g/t, water glass inhibits silicate, the addition amount is 2500g/t, then adding a forward flotation collector, the addition amount is 1100g/t, then carrying out forward flotation operation 1, wherein a foam product is forward flotation concentrate 1, and a product in the tank is forward flotation tailings 1;
(3) The coarse-grain-grade material on the screen obtained by screening operation enters the ore grinding operation, the grinding fineness is-0.074 mm and accounts for 78%, and the material after ore grinding and the positive flotation concentrate 1 are mixed and fed into a positive flotation stirring tank 2; sequentially adding Na 2CO3 to adjust pH, wherein the adding amount is 1500g/t, the adding amount of water glass is 1500g/t, then adding a positive flotation collector, the adding amount is 1300g/t, then carrying out positive flotation operation 2, wherein the foam product is positive flotation concentrate 2, and the product in the tank is positive flotation tailings 2;
(4) The direct flotation concentrate 2 is fed into a direct flotation magnesium-removing stirring tank, acid is firstly added to adjust the pH, the adding amount is 4000g/t, then a direct flotation collector is added, the adding amount is 220g/t, then the direct flotation operation is carried out, the foam product is magnesium-removing direct flotation tailings, and the product in the tank is magnesium-removing direct flotation concentrate, namely the final phosphate concentrate.
In the method, the ore composition of the silicon-calcium collophanite is 18.5 percent of P 2O5 percent, the mass content of MgO is 2.0 percent, and the mass content of SiO 2 is 35 percent;
The P 2O5 grade in the integrated phosphate concentrate obtained by the method is 29.3 percent, the MgO mass content is 0.55 percent, and the recovery rate of the integrated phosphate concentrate P 2O5 is 85.5 percent.
Embodiment 2, a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which specifically comprises the following steps:
(1) Crushing raw ore, sieving with concentration of 40.00% and granularity of 0.074 mm;
(2) Adding the fine-fraction material with the size of-0.074 mm obtained by sieving operation into a forward flotation stirring tank 1, sequentially adding a regulator Na 2CO3 to regulate the pH, wherein the addition amount is 2000g/t, adding a regulator corn starch to improve the fine-fraction flotation environment, the addition amount is 35g/t, water glass is used for inhibiting silicate, the addition amount is 2000g/t, then adding a forward flotation collector, the addition amount is 1000g/t, then carrying out forward flotation operation 1, wherein a foam product is forward flotation concentrate 1, and a product in the tank is forward flotation tailings 1;
(3) The coarse-grain-grade material on the screen obtained by screening operation enters the ore grinding operation, the grinding fineness is-0.074 mm accounting for 85 percent, and the material after ore grinding and the positive flotation concentrate 1 are mixed and fed into a positive flotation stirring tank 2; sequentially adding Na 2CO3 to adjust pH, wherein the adding amount is 1500g/t, the adding amount of water glass is 1500g/t, then adding a positive flotation collector, the adding amount is 1100g/t, then carrying out positive flotation operation 2, wherein the foam product is positive flotation concentrate 2, and the product in the tank is positive flotation tailings 2;
(4) The direct flotation concentrate 2 is fed into a direct flotation magnesium-removing stirring tank, acid is firstly added to adjust the pH, the adding amount is 4000g/t, then a direct flotation collector is added, the adding amount is 150g/t, then the direct flotation operation is carried out, the foam product is magnesium-removing direct flotation tailings, and the product in the tank is magnesium-removing direct flotation concentrate, namely the final phosphate concentrate.
In the method, the ore composition of the silicon-calcium collophanite is 19.5 percent of P 2O5 grade, the mass content of MgO is 1.8 percent, and the mass content of SiO 2 is 34.5 percent;
The P 2O5 grade in the integrated phosphate concentrate obtained by the method is 29.0%, the MgO mass content is 0.48%, and the recovery rate of the integrated phosphate concentrate P 2O5 is 77.3%.
Embodiment 3, a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which specifically comprises the following steps:
(1) Crushing raw ore, sieving with concentration of 35.00% and granularity of 0.063 mm;
(2) Adding the fine-fraction material of-0.063 mm obtained by sieving operation into a forward flotation stirring tank 1, sequentially adding a regulator Na 2CO3 to regulate the pH, wherein the addition amount is 2000g/t, adding a regulator dextrin to improve the fine-fraction flotation environment, the addition amount is 35g/t, the silicate is inhibited by water glass, the addition amount is 2200g/t, then adding a forward flotation collector, the addition amount is 1000g/t, then carrying out forward flotation operation 1, the foam product is forward flotation concentrate 1, and the product in the tank is forward flotation tailings 1;
(3) The coarse-grain-grade material on the screen obtained by screening operation enters the ore grinding operation, the grinding fineness is-0.074 mm and accounts for 78%, and the material after ore grinding and the positive flotation concentrate 1 are mixed and fed into a positive flotation stirring tank 2; sequentially adding Na 2CO3 to adjust pH, wherein the adding amount is 1500g/t, the adding amount of water glass is 1500g/t, then adding a positive flotation collector, the adding amount is 1300g/t, then carrying out positive flotation operation 2, wherein the foam product is positive flotation concentrate 2, and the product in the tank is positive flotation tailings 2;
(4) The direct flotation concentrate 2 is fed into a direct flotation magnesium-removing stirring tank, acid is firstly added to adjust the pH, the adding amount is 4000g/t, then a direct flotation collector is added, the adding amount is 220g/t, then the direct flotation operation is carried out, the foam product is magnesium-removing direct flotation tailings, and the product in the tank is magnesium-removing direct flotation concentrate, namely the final phosphate concentrate.
In the method, the ore composition of the silicon-calcium collophanite is 18.5 percent of P 2O5 percent, the mass content of MgO is 2.0 percent, and the mass content of SiO 2 is 35.0 percent;
The P 2O5 grade in the integrated phosphate concentrate obtained by the method is 29.2%, the MgO mass content is 0.54%, and the recovery rate of the integrated phosphate concentrate P 2O5 is 83.8%.
Embodiment 4, a fractional step flotation method for treating medium-low grade silicon-calcium collophanite, which specifically comprises the following steps:
(1) Crushing raw ore, sieving with concentration of 40.00% and granularity of 0.045 mm;
(2) Adding the fine-fraction material with the size of-0.045 mm obtained by sieving operation into a forward flotation stirring tank 1, sequentially adding a regulator Na 2CO3 to regulate the pH value, wherein the addition amount is 2000g/t, adding a regulator corn starch to improve the fine-fraction flotation environment, the addition amount is 32g/t, water glass is used for inhibiting silicate, the addition amount is 2000g/t, then adding a forward flotation collector, the addition amount is 1000g/t, then carrying out forward flotation operation 1, wherein a foam product is forward flotation concentrate 1, and a product in the tank is forward flotation tailings 1;
(3) The coarse-grain-grade material on the screen obtained by screening operation enters the ore grinding operation, the grinding fineness is-0.074 mm accounting for 85 percent, and the material after ore grinding and the positive flotation concentrate 1 are mixed and fed into a positive flotation stirring tank 2; sequentially adding Na 2CO3 to adjust pH, wherein the adding amount is 1500g/t, the adding amount of water glass is 1500g/t, then adding a positive flotation collector, the adding amount is 1100g/t, then carrying out positive flotation operation 2, wherein the foam product is positive flotation concentrate 2, and the product in the tank is positive flotation tailings 2;
(4) The direct flotation concentrate 2 is fed into a direct flotation magnesium-removing stirring tank, acid is firstly added to adjust the pH, the adding amount is 4000g/t, then a direct flotation collector is added, the adding amount is 150g/t, then the direct flotation operation is carried out, the foam product is magnesium-removing direct flotation tailings, and the product in the tank is magnesium-removing direct flotation concentrate, namely the final phosphate concentrate.
In the method, the ore composition of the silicon-calcium collophanite is 19.5 percent of P 2O5 grade, the mass content of MgO is 1.8 percent, and the mass content of SiO 2 is 34.5 percent;
The P 2O5 grade in the integrated phosphate concentrate obtained by the method is 29.1 percent, the MgO mass content is 0.45 percent, and the recovery rate of the integrated phosphate concentrate P 2O5 is 76.7 percent.
Example 5, a fractional step flotation method for treating low-and-medium grade silica-calcia collophanite, which is compared with the effect of the conventional direct and reverse flotation process, has the data shown in Table I:
(1) Conventional positive and negative processes: the grinding fineness is-0.074 mm and the grain size is 90%; the pH value in the positive flotation process is 9.5, the dosage of the pH regulator sodium carbonate is 3000g/t, and the dosage of the inhibitor sodium silicate is 2500kg/t; the amount of the collector C18 unsaturated fatty acid saponified material is 2000kg/t. And (3) after pulp mixing, the pulp enters a positive flotation tank to carry out positive flotation operation, the foam product is positive flotation concentrate, and the product in the tank is positive flotation tailings. The direct flotation concentrate is fed into a direct flotation magnesium-removing stirring tank, acid is firstly added to adjust the pH, the adding amount is 4000g/t, then a direct flotation collector is added, the adding amount is 250g/t, then the direct flotation operation is carried out, the foam product is magnesium-removing direct flotation tailings, and the product in the tank is magnesium-removing direct flotation concentrate, namely the final phosphate concentrate.
(2) The result was that the grade of the raw ore P 2O5 was 18.5%, the grade of the concentrate P 2O5 after flotation was 27.5%, and the recovery rate of the concentrate P 2O5 after flotation was 71.8%.
Table one comparative test results
The comparative test can be seen: by using the process provided by the invention, the grade of the concentrate P2O5 can be improved by about 2%, the recovery rate of the concentrate P2O5 can be improved by more than 13%, and the economic benefit is very remarkable.
Example 6, a fractional step flotation method for treating low-and-medium grade silicon-calcium collophanite, which is compared with the effect of the conventional direct-reverse flotation process, has the data shown in Table II:
(1) Conventional positive and negative processes: the grinding fineness is-0.074 mm and the grain size is 85%; the pH value in the positive flotation process is 9.5, the dosage of the pH regulator sodium carbonate is 3000g/t, and the dosage of the inhibitor sodium silicate is 4500g/t; the amount of the collector C18 unsaturated fatty acid saponified material is 2000g/t. And (3) after pulp mixing, the pulp enters a positive flotation tank to carry out positive flotation operation, the foam product is positive flotation concentrate, and the product in the tank is positive flotation tailings. The direct flotation concentrate is fed into a direct flotation magnesium-removing stirring tank, acid is firstly added to adjust the pH, the adding amount is 4000g/t, then a direct flotation collector is added, the adding amount is 150g/t, then the direct flotation operation is carried out, the foam product is magnesium-removing direct flotation tailings, and the product in the tank is magnesium-removing direct flotation concentrate, namely the final phosphate concentrate.
(2) The result was that the grade of the raw ore P 2O5 was 19.5%, the grade of the concentrate P 2O5 after flotation was 28.8%, and the recovery rate of the concentrate P 2O5 after flotation was 71.3%.
Table II shows the results of the comparative tests
The comparative test can be seen: by using the process provided by the invention, the grade of the concentrate P2O5 can be improved by about 0.2%, the recovery rate of the concentrate P2O5 can be improved by about 6%, and the economic benefit is very remarkable.
In the above embodiments: the classifying screening operation adopts a vibrating screen and a high-frequency fine screen, the regulator 2 adopts polysaccharide and polyphenol organic polymers as regulators, and the collector adopts fatty acid soap organic matters.
It will be understood that various changes, modifications, substitutions and alterations can be made to the embodiments without departing from the principles of the present invention, the scope of which is defined in the claims and their equivalents. The regulator 2 is prepared from polysaccharides and polyphenols organic polymers, and the collector is prepared from fatty acid soap organic matters.
Claims (8)
1. A fractional step flotation method for treating medium-low grade silicon-calcium collophanite is characterized by comprising the following steps: the method comprises the steps of adopting a grading step-by-step flotation process, crushing raw ore, then feeding the crushed raw ore into screening operation, and screening the crushed raw ore into coarse and fine grain fractions; then, removing silicate gangue minerals in the fine-fraction materials by adopting forward flotation, performing forward flotation on the obtained forward flotation concentrate and the coarse-fraction materials again to remove the silicate gangue minerals, and finally, removing carbonate gangue minerals in the obtained forward flotation concentrate by adopting reverse flotation;
The method comprises the following specific steps:
(1) Crushing raw ore, sieving with concentration of 30.00-50.00%, and grading with granularity of 0.074mm, 0.063mm or 0.045 mm;
(2) Adding undersize fine-fraction materials obtained by screening operation into a forward flotation stirring tank 1, sequentially adding an adjusting agent Na 2CO3 to adjust pH, adding polysaccharides and polyphenol organic polymer adjusting agents with the addition of 20-50g/t, adding sodium silicate to inhibit silicate with the addition of 200-5000 g/t, adding a forward flotation collecting agent with the addition of 500-2500 g/t, and then carrying out forward flotation operation 1, wherein a foam product is forward flotation concentrate 1, and a product in the tank is forward flotation tailings 1;
(3) The coarse-grain-grade material on the screen obtained by screening operation enters the ore grinding operation, the grinding fineness is 70-90% of-0.074 mm, and the material after ore grinding and the positive flotation concentrate 1 are mixed and fed into a positive flotation stirring tank 2; sequentially adding Na 2CO3 to adjust the pH, wherein the adding amount is 1000-2000g/t, adding sodium silicate to inhibit silicate, the adding amount is 100-4000 g/t, then adding a positive flotation collector, the adding amount is 500-2500 g/t, then carrying out positive flotation operation 2, wherein the foam product is positive flotation concentrate 2, and the product in the tank is positive flotation tailings 2;
(4) The direct flotation concentrate 2 is fed into a direct flotation magnesium-removing stirring tank, acid is firstly added to adjust the pH, the addition amount is 4000-8000g/t, then a direct flotation collector is added, the addition amount is 100-500 g/t, then the direct flotation operation is carried out, the foam product is magnesium-removing direct flotation tailings, and the product in the tank is magnesium-removing direct flotation concentrate, namely the final phosphate concentrate.
2. The fractional step flotation method for treating low-grade silica-calcia collophanite according to claim 1, wherein the method comprises the following steps: the ore type of the medium-low grade silicon-calcium collophanite is high-iron aluminum silicon-calcium collophanite or weathered silicon-calcium collophanite.
3. The fractional step flotation method for treating low-grade silica-calcia collophanite according to claim 2, wherein the method comprises the steps of: the medium-low grade silicon-calcium collophanite ore comprises the following components: the grade of P 2O5 is 16.2% -24%, the mass content of MgO is 1.0% -5.9%, and the mass content of SiO 2 is 12% -39%.
4. The fractional step flotation method for treating low-grade silica-calcia collophanite according to claim 1, which is characterized by comprising the following specific steps:
(1) Crushing raw ore, sieving with concentration of 35.00-45.00%, and grading with granularity of 0.074mm, 0.063mm or 0.045 mm;
(2) Adding undersize fine-fraction materials obtained by screening operation into a forward flotation stirring tank 1, sequentially adding an adjusting agent Na 2CO3 to adjust the pH, wherein the adding amount is 2000-2500g/t, adding a polysaccharide and polyphenol organic polymer adjusting agent, the adding amount is 30-45g/t, adding sodium silicate to inhibit silicate, the adding amount is 1000-4000 g/t, then adding a forward flotation collecting agent, the adding amount is 1000-1500 g/t, then carrying out forward flotation operation 1, wherein a foam product is forward flotation concentrate 1, and a product in the tank is forward flotation tailings 1;
(3) The coarse-grain-grade material on the screen obtained by screening operation enters the ore grinding operation, the grinding fineness is 75-85% of-0.074 mm, and the material after ore grinding and the positive flotation concentrate 1 are mixed and fed into a positive flotation stirring tank 2; sequentially adding Na 2CO3 to adjust the pH, wherein the adding amount is 1500-2000g/t, adding sodium silicate to inhibit silicate, the adding amount is 1000-3000 g/t, then adding a positive flotation collector, the adding amount is 500-1500 g/t, then carrying out positive flotation operation 2, wherein the foam product is positive flotation concentrate 2, and the product in the tank is positive flotation tailings 2;
(4) The direct flotation concentrate 2 is fed into a direct flotation magnesium-removing stirring tank, acid is firstly added to adjust the pH, the addition amount is 4000-6000g/t, then a direct flotation collector is added, the addition amount is 200-300 g/t, then the direct flotation operation is carried out, the foam product is magnesium-removing direct flotation tailings, and the product in the tank is magnesium-removing direct flotation concentrate, namely the final phosphate concentrate.
5. The fractional step flotation method for treating low-grade silica-calcia collophanite according to claim 1, wherein the method comprises the following steps: the regulator polysaccharide and polyphenol organic polymer selected in the step (2) is selected from starch, cellulose, dextrin, tannin and pectin, and the collector is C12-C20 higher fatty acid or fatty acid sodium salt.
6. The fractional step flotation method for treating low-grade silica-calcia collophanite according to claim 1, wherein the method comprises the following steps: in the step (2), the collecting agent in the positive flotation operation 2 is selected from fatty acid soap organic matters.
7. The fractional step flotation method for treating low-grade silicon-calcium collophanite according to claim 1, wherein in the reverse flotation, inorganic acid is selected as an inhibitor, sulfuric acid, phosphoric acid or a mixed acid of the two, and fatty acid soap organic matters are selected as a collector.
8. The fractional step flotation method for treating low-grade silica-calcia collophanite according to claim 1, wherein the method comprises the following steps: the flow structure of the forward flotation and reverse flotation is roughing operation or is formed by arbitrary combination of roughing operation and carefully selecting operation and scavenging operation.
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| US4317715A (en) * | 1977-11-22 | 1982-03-02 | Outokumpu Oy | Process for the selective froth-flotation of phosphate and carbonate minerals from finely-divided phosphate-carbonate-silicate ores or concentrates |
| CN103949318A (en) * | 2014-04-25 | 2014-07-30 | 中蓝连海设计研究院 | Method for performing fine sieving, regrinding and bulk flotation on low-level silicon calcium collophanite |
| CN106269265A (en) * | 2016-08-18 | 2017-01-04 | 中蓝连海设计研究院 | A kind of classification stepped-flotation separation technique processing high alumina high ferro silicon calcium collophanite |
| CN112007760A (en) * | 2019-07-23 | 2020-12-01 | 中蓝连海设计研究院有限公司 | Beneficiation method for treating high sesquioxide collophanite |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4317715A (en) * | 1977-11-22 | 1982-03-02 | Outokumpu Oy | Process for the selective froth-flotation of phosphate and carbonate minerals from finely-divided phosphate-carbonate-silicate ores or concentrates |
| CN103949318A (en) * | 2014-04-25 | 2014-07-30 | 中蓝连海设计研究院 | Method for performing fine sieving, regrinding and bulk flotation on low-level silicon calcium collophanite |
| CN106269265A (en) * | 2016-08-18 | 2017-01-04 | 中蓝连海设计研究院 | A kind of classification stepped-flotation separation technique processing high alumina high ferro silicon calcium collophanite |
| CN112007760A (en) * | 2019-07-23 | 2020-12-01 | 中蓝连海设计研究院有限公司 | Beneficiation method for treating high sesquioxide collophanite |
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