CN114011580A - Impurity removal method for low-grade micro-fine particle phosphate ore - Google Patents
Impurity removal method for low-grade micro-fine particle phosphate ore Download PDFInfo
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- CN114011580A CN114011580A CN202111274193.6A CN202111274193A CN114011580A CN 114011580 A CN114011580 A CN 114011580A CN 202111274193 A CN202111274193 A CN 202111274193A CN 114011580 A CN114011580 A CN 114011580A
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- flotation
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- 238000000034 method Methods 0.000 title claims abstract description 44
- 239000010419 fine particle Substances 0.000 title claims abstract description 34
- 239000012535 impurity Substances 0.000 title claims abstract description 18
- 229910019142 PO4 Inorganic materials 0.000 title claims description 21
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 title claims description 21
- 239000010452 phosphate Substances 0.000 title claims description 21
- 238000005188 flotation Methods 0.000 claims abstract description 195
- 230000002441 reversible effect Effects 0.000 claims abstract description 69
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 46
- 239000012141 concentrate Substances 0.000 claims abstract description 43
- 239000006260 foam Substances 0.000 claims abstract description 38
- 239000002367 phosphate rock Substances 0.000 claims abstract description 27
- OJMIONKXNSYLSR-UHFFFAOYSA-N phosphorous acid Chemical compound OP(O)O OJMIONKXNSYLSR-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000011777 magnesium Substances 0.000 claims abstract description 11
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 11
- 230000001360 synchronised effect Effects 0.000 claims abstract description 11
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims abstract description 10
- 230000002378 acidificating effect Effects 0.000 claims abstract description 5
- 238000003756 stirring Methods 0.000 claims description 31
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical group OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 22
- 239000000395 magnesium oxide Substances 0.000 claims description 18
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 18
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 18
- 229920002401 polyacrylamide Polymers 0.000 claims description 15
- 239000002253 acid Substances 0.000 claims description 11
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 11
- GNHOJBNSNUXZQA-UHFFFAOYSA-J potassium aluminium sulfate dodecahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.O.O.[Al+3].[K+].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O GNHOJBNSNUXZQA-UHFFFAOYSA-J 0.000 claims description 11
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 10
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 9
- 239000011707 mineral Substances 0.000 claims description 9
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 8
- 239000000194 fatty acid Substances 0.000 claims description 8
- 229930195729 fatty acid Natural products 0.000 claims description 8
- 150000004665 fatty acids Chemical class 0.000 claims description 7
- 230000002000 scavenging effect Effects 0.000 claims description 7
- GCLGEJMYGQKIIW-UHFFFAOYSA-H sodium hexametaphosphate Chemical compound [Na]OP1(=O)OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])O1 GCLGEJMYGQKIIW-UHFFFAOYSA-H 0.000 claims description 7
- 235000019982 sodium hexametaphosphate Nutrition 0.000 claims description 7
- 239000001577 tetrasodium phosphonato phosphate Substances 0.000 claims description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 6
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 4
- 150000001412 amines Chemical group 0.000 claims description 3
- -1 ether amine Chemical class 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims description 2
- 229910052593 corundum Inorganic materials 0.000 claims description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 claims description 2
- 229920000768 polyamine Polymers 0.000 claims description 2
- 238000007127 saponification reaction Methods 0.000 claims description 2
- 150000004670 unsaturated fatty acids Chemical class 0.000 claims description 2
- 235000021122 unsaturated fatty acids Nutrition 0.000 claims description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 11
- 229910001748 carbonate mineral Inorganic materials 0.000 abstract description 7
- 229910052604 silicate mineral Inorganic materials 0.000 abstract description 4
- 238000005273 aeration Methods 0.000 description 26
- 230000005484 gravity Effects 0.000 description 17
- 238000011084 recovery Methods 0.000 description 12
- 238000000926 separation method Methods 0.000 description 8
- OSMSIOKMMFKNIL-UHFFFAOYSA-N calcium;silicon Chemical compound [Ca]=[Si] OSMSIOKMMFKNIL-UHFFFAOYSA-N 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 238000011161 development Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003607 modifier Substances 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010494 dissociation reaction Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 235000019353 potassium silicate Nutrition 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000002829 reductive effect Effects 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
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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
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/02—Froth-flotation processes
-
- 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
- B03D1/08—Subsequent treatment of concentrated product
-
- 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
- B03D1/14—Flotation machines
-
- 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
- B03D1/14—Flotation machines
- B03D1/1443—Feed or discharge mechanisms for flotation tanks
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- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Biotechnology (AREA)
- Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Dispersion Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention belongs to the technical field of phosphorite beneficiation, and relates to a method for removing impurities from low-grade micro-fine particle phosphorite. The method comprises the following specific steps: (1) reverse flotation magnesium removal; (2) synchronous demagging and desiliconizing by reverse flotation: adding a flotation regulator, and simultaneously adding a demagging collecting agent and a dealumination collecting agent to synchronously remove carbonate minerals and silicate minerals; (3) reverse flotation desilication: adding a dealuminization collecting agent to perform desiliconization roughing under an acidic condition, wherein a product in the cell is final concentrate, and a product in the cell after the foam product is subjected to secondary flotation is returned to desiliconization roughing as middling. Compared with the existing forward and reverse treatment process, the method well avoids the problem of poor flotation effect of the forward and reverse flotation process under the low-temperature condition, and the reverse flotation magnesium removal and desilication can well obtain good flotation indexes at the low temperature. The flotation regulator is added to optimize the foam phenomenon during desilication reverse flotation, increase the mobility of the foam and improve the feasibility of industrial application.
Description
Technical Field
The invention belongs to the technical field of phosphorite beneficiation, and particularly relates to a method for removing impurities from low-grade micro-fine particle phosphorite.
Background
The phosphorite is an essential basic raw material for producing phosphate fertilizers and phosphorus chemical products, the reserves of phosphorite resources in China are rich, but the reserves of high-grade phosphorite are less, the proportion is low, and the low-grade silicon-calcium collophanite is mainly used, so that the low-grade silicon-calcium collophanite is poor in fine impurities. Collophanite has the problems of fine disseminated particle size and poor dissociation property, and the development and utilization of collophanite are worldwide problems because of high content of silicate minerals and carbonate minerals. At present, most ore dressing plants adopt a single reverse flotation method to treat phosphorite, and a fatty acid collecting agent is used for floating magnesium-containing carbonate minerals under an acidic condition, so that the grade is improved, and the process flow is simple and is suitable for treating high-magnesium low-silicon phosphorite. For silicon-calcium collophanite, the selection is mainly carried out by adopting positive and negative flotation and double-reverse flotation at present, the positive and negative flotation process has poor flotation effect at low temperature, the process is complex and has high cost, and the application is very few at present; the desilication process of the double reverse flotation process needs to use an amine cationic collector for flotation, and due to the characteristics of the amine cationic collector, the problems of sticky flotation foam, poor foam fluidity, difficult defoaming, sensitivity to slime and the like exist, so that the industrial application is difficult. In recent years, researchers adopt the gravity flotation to process the silicon-calcium collophanite, namely, the spiral chute is used for pre-sorting the phosphorite to obtain a high-grade phosphorite product and a low-grade phosphorite product, the high-grade phosphorite product has larger granularity, and a double reverse flotation process is adopted for sorting; the low-grade phosphorite product has fine granularity, and is sorted by adopting a direct-reverse flotation process, but the problem of poor flotation effect under the low-temperature condition of the direct-reverse flotation still exists. Along with continuous exploitation of phosphorite resources, high-grade phosphorite is consumed, and low-grade collophanite with finer embedded particle size needs finer grinding fineness when being selected, so that the development of the low-temperature-resistant micro-fine particle phosphorite treatment technology has great significance for comprehensive utilization of the low-grade silico-calcium collophanite by combining the current situation of the development of the current mineral separation technology.
Disclosure of Invention
The invention provides a method for removing impurities from low-grade micro-fine particle phosphate ore, which has high efficiency and low temperature resistance, and the process flow is simple and easy to industrialize.
The working principle of the invention is as follows:
(1) reverse flotation demagging: preparing the micro-fine particle phosphorite into ore pulp with the concentration of 18-22%, feeding the obtained ore pulp into a reverse flotation stirring tank, and adding an acidic regulator for size mixing to ensure that the pH value of the ore pulp is between 4 and 5; adding a demagging collecting agent into the pulp after size mixing, and feeding the pulp into a flotation tank for reverse flotation demagging; the flotation foam is the demagnetised tailings, and the flotation tank is the demagnetised concentrate.
(2) Synchronous demagging and desiliconizing by reverse flotation: adding a flotation regulator into the demagging concentrate obtained in the step (1) to perform size mixing and stirring; adding a demagging collecting agent and a desiliconization collecting agent in sequence to perform reverse flotation and synchronous demagging and desiliconization; the flotation foam is the demagging desiliconized tailings, and the flotation tank is the demagging desiliconized concentrate.
(3) Reverse flotation desilication: adding an acid regulator into the demagging and desiliconizing concentrate obtained in the step (2) for size mixing to enable the pH value of ore pulp to be between 4 and 5; adding desiliconized collecting agent into the ore pulp after adjustment and feeding the ore pulp into a flotation tank for reverse flotation desiliconization roughing; and final concentrate is obtained in the flotation tank, flotation foam enters the flotation tank again for desilication scavenging, the flotation foam is reverse flotation desilication tailings, desilication middlings are obtained in the flotation tank, and the desilication middlings are returned to the reverse flotation desilication roughing flow.
According to the scheme, in the step (1), the low-grade micro-fine particle phosphorite is the tailings separated by the spiral chute, the main gangue minerals of the low-grade micro-fine particle phosphorite are magnesium-containing compounds and sesquioxide, and P of the gangue minerals is P2O5Grade (L) of a material<22wt%, magnesium oxide content 2.0-4.0wt%, sesquioxide R2O3（Fe2O3+ Al2O3) The content of the fine particle phosphorite is 4.0 to 10.0 weight percent, and the fine particle phosphorite is prepared into ore pulp with the concentration of 18 to 22 percent.
According to the scheme, the mineral particle fineness of-0.074 mm in the micro-fine phosphorite accounts for 85-95% by mass.
Preferably, the acid regulator is phosphoric acid, the dosage of the acid regulator is 7-10kg/t relative to raw ore in the step (1), and the dosage of the acid regulator is 2-5kg/t relative to raw ore in the step (3), and the acid regulator is adjusted to ensure that the pH value of the ore pulp is between 4 and 5.
Further preferably, the flotation regulator consists of the following components in percentage by mass: 30-60% of aluminum potassium sulfate dodecahydrate, 10-40% of polyacrylamide, 5-15% of sodium hexametaphosphate and 15-30% of polyaluminum chloride, wherein the sum of the mass percentages of the components is 100%, and the dosage of the flotation regulator relative to the raw ore is 7-9 kg/t. The flotation process can be optimized by adding the flotation regulator, so that the demagging anion collecting agent and the desiliconization cation collecting agent can be added together for flotation, and the flotation phenomenon is optimized.
Preferably, the demagging collector is a saponified product of mixed fatty acid obtained by mixing short-carbon-chain (C8-C12) fatty acid and unsaturated fatty acid according to a certain proportion, wherein the mass ratio of the mixed fatty acid to a sodium hydroxide solution is 1: (0.5-3) saponification reaction at 70-80 ℃. The use of short carbon chain fatty acids increases low temperature flexibility.
Further preferably, the amount of the demagging collector used in step (1) is 0.6-1.0kg/t and the amount used in step (2) is 0.1-0.4 kg/t.
Preferably, the dealumination collector is an amine collector, the main components of the dealumination collector are ether amine and ether polyamine, and the dosage of the dealumination collector in the step (2) is 0.1-0.3kg/t, and the dosage of the dealumination collector in the step (3) is 0.3-0.5 kg/t.
The invention has the following beneficial effects:
1. the raw ore is low-grade gravity separation raw ore with high sesquioxide content and fine granularity, and the direct and reverse flotation is generally adopted for treating the low-grade fine-granularity minerals, but the low-temperature adaptability is extremely poor. By adopting double reverse flotation and flotation, fine mud in micro-fine particles influences the flotation effect, and flotation foam is difficult to control and cannot be industrialized. The invention can solve the problem of poor low-temperature adaptability of the forward and reverse flotation, and can eliminate the influence of the double reverse fine mud. The method comprises the steps of carrying out flotation on low-grade micro-fine particle phosphate ores in three steps, wherein in the first step, a magnesium-removing collecting agent is adopted to remove part of magnesium-containing carbonate minerals in advance in an acid environment, and because the carbonate minerals have lower hardness in the collophanite and have finer fineness compared with other minerals, the content of fine particles in the selected phosphate ores can be reduced by removing the carbonate minerals in advance, and the subsequent flotation environment is optimized; and in the second step, a flotation regulator with surface activity, inhibiting effect and flocculating effect is adopted, a demagging collecting agent and a dealumination collecting agent are added to synchronously remove residual carbonate minerals and partial silicate minerals, and the flotation regulator and the dealumination collecting agent are added, so that the foam phenomenon of the dealumination collecting agent in flotation can be effectively improved, and the mobility of foam is improved. And the third step is to remove the residual silicate minerals by using a dealumination collecting agent in an acid environment, and the flotation froth phenomenon is improved because part of fine-grained gangue minerals are removed in the first two steps and the flocculation effect of the flotation regulator in the first step is achieved. Compared with positive and negative flotation, the low-temperature adaptability of the whole process is improved.
2. The invention has the advantages of solving the problem of low flotation efficiency of low-grade micro-fine particle phosphate ore in the forward and reverse flotation at low temperature, and obtaining good flotation indexes at low temperature by adopting reverse flotation, magnesium removal and desilication. The flotation regulator is added to optimize the foam phenomenon during desilication reverse flotation, increase the mobility of the foam and improve the feasibility of industrial application.
Drawings
FIG. 1 is a process flow diagram of the method for removing impurities from low-grade micro-fine particle phosphate ore.
Detailed Description
The technical solution of the present invention is further explained by the following embodiments. It should be understood by those skilled in the art that the examples are only for the understanding of the present invention and should not be construed as the specific limitations of the present invention.
Example 1
A method for removing impurities from low-grade micro-fine particle phosphate ore comprises the following specific steps:
(1) reverse flotation demagging: taking 150g of gravity tailings (the grade is 21.63%, the fineness is 87.6%, the content of magnesium oxide is 2.61, and the content of sesquioxide is 6.05) obtained by gravity separation of a spiral chute, modulating the gravity tailings into ore pulp with the concentration of 20%, transferring the obtained ore pulp into a flotation tank under the condition that the temperature is 10 ℃, adding 8kg/t phosphoric acid (10%), and stirring for 1 minute to adjust the pH value of the ore pulp; then adding 0.85kg/t of a demagging collecting agent into the ore pulp, stirring for 2 minutes, turning on an aeration switch of a flotation machine, adjusting the aeration quantity to 150L/h, and performing reverse flotation demagging; the flotation foam is the demagnetised tailings, and the flotation tank is the demagnetised concentrate.
(2) Synchronous demagging and desiliconizing by reverse flotation: adding 8kg/t of flotation regulator (50% of aluminum potassium sulfate dodecahydrate, 10% of polyacrylamide, 10% of sodium hexametaphosphate and 30% of polyaluminium chloride) into the demagging concentrate obtained in the step (1), mixing and stirring for 1 minute; then sequentially adding 0.2kg/t of demagging collecting agent and 0.15kg/t of desiliconization collecting agent, continuing stirring for 3 minutes, turning on an aeration switch of the flotation machine, adjusting the aeration quantity to 150L/h, and performing reverse flotation and synchronous demagging and desiliconization; the flotation foam is the demagging desiliconized tailings, and the flotation tank is the demagging desiliconized concentrate.
(3) Reverse flotation desilication: adding 4kg/t phosphoric acid into the demagging and desiliconizing concentrate obtained in the step (2), and stirring for 1 minute to adjust the pH value of the ore pulp to be between 4 and 5; adding 0.4kg/t desiliconization collecting agent into the pulp after size mixing, stirring for 2 minutes, turning on an aeration switch of a flotation machine, adjusting the aeration quantity to be 150L/h, and performing reverse flotation desiliconization roughing; and final concentrate is obtained in the flotation tank, flotation foam enters the flotation tank again for desilication scavenging, the flotation foam is reverse flotation desilication tailings, desilication middlings are obtained in the flotation tank, and the desilication middlings are returned to the reverse flotation desilication roughing flow.
Through the process, the grade of the final concentrate can reach 31.45%, the recovery rate is 64.17%, the content of magnesium oxide is 0.59%, and the content of sesquioxide is 2.29%.
Example 2
A method for removing impurities from low-grade micro-fine particle phosphate ore comprises the following specific steps:
(1) reverse flotation demagging: taking 150g of gravity tailings (the grade is 21.63%, the fineness is 87.6%, the content of magnesium oxide is 2.61, and the content of sesquioxide is 6.05) obtained by gravity separation of a spiral chute, modulating the gravity tailings into ore pulp with the concentration of 20%, transferring the obtained ore pulp into a flotation tank under the condition that the temperature is 5 ℃, adding 8kg/t phosphoric acid (10%), and stirring for 1 minute to adjust the pH value of the ore pulp; then adding 0.85kg/t of a demagging collecting agent into the ore pulp, stirring for 2 minutes, turning on an aeration switch of a flotation machine, adjusting the aeration quantity to 150L/h, and performing reverse flotation demagging; the flotation foam is the demagnetised tailings, and the flotation tank is the demagnetised concentrate.
(2) Synchronous demagging and desiliconizing by reverse flotation: adding 8kg/t of flotation regulator (50% of aluminum potassium sulfate dodecahydrate, 10% of polyacrylamide, 10% of sodium hexametaphosphate and 30% of polyaluminium chloride) into the demagging concentrate obtained in the step (1), mixing and stirring for 1 minute; then sequentially adding 0.2kg/t of demagging collecting agent and 0.15kg/t of desiliconization collecting agent, continuing stirring for 3 minutes, turning on an aeration switch of the flotation machine, adjusting the aeration quantity to 150L/h, and performing reverse flotation and synchronous demagging and desiliconization; the flotation foam is the demagging desiliconized tailings, and the flotation tank is the demagging desiliconized concentrate.
(3) Reverse flotation desilication: adding 4kg/t phosphoric acid into the demagging and desiliconizing concentrate obtained in the step (2), and stirring for 1 minute to adjust the pH value of the ore pulp to be between 4 and 5; adding 0.4kg/t desiliconization collecting agent into the pulp after size mixing, stirring for 2 minutes, turning on an aeration switch of a flotation machine, adjusting the aeration quantity to be 150L/h, and performing reverse flotation desiliconization roughing; and final concentrate is obtained in the flotation tank, flotation foam enters the flotation tank again for desilication scavenging, the flotation foam is reverse flotation desilication tailings, desilication middlings are obtained in the flotation tank, and the desilication middlings are returned to the reverse flotation desilication roughing flow.
Through the process, the grade of the final concentrate can reach 31.20%, the recovery rate is 60.45%, the content of magnesium oxide is 0.67%, and the content of sesquioxide is 2.41%.
Example 3
A method for removing impurities from low-grade micro-fine particle phosphate ore comprises the following specific steps:
(1) reverse flotation demagging: taking 150g of gravity tailings (the grade is 19.13%, the fineness is 92.3%, the content of magnesium oxide is 3.35 and the content of sesquioxide is 6.87) obtained by gravity separation of a spiral chute, modulating the gravity tailings into ore pulp with the concentration of 20%, transferring the obtained ore pulp into a flotation tank under the condition that the temperature is 5 ℃, adding 8kg/t phosphoric acid (10%), stirring for 1 minute, and adjusting the pH value of the ore pulp; then adding 0.9kg/t of demagging collecting agent into the ore pulp, stirring for 2 minutes, turning on an aeration switch of a flotation machine, adjusting aeration quantity to 150L/h, and performing reverse flotation demagging; the flotation foam is the demagnetised tailings, and the flotation tank is the demagnetised concentrate.
(2) Synchronous demagging and desiliconizing by reverse flotation: adding 8kg/t of flotation regulator (50% of aluminum potassium sulfate dodecahydrate, 10% of polyacrylamide, 10% of sodium hexametaphosphate and 30% of polyaluminium chloride) into the demagging concentrate obtained in the step (1), mixing and stirring for 1 minute; then sequentially adding 0.2kg/t of demagging collecting agent and 0.2kg/t of desiliconization collecting agent, continuing stirring for 3 minutes, turning on an aeration switch of the flotation machine, adjusting the aeration quantity to 150L/h, and performing reverse flotation and synchronous demagging and desiliconization; the flotation foam is the demagging desiliconized tailings, and the flotation tank is the demagging desiliconized concentrate.
(3) Reverse flotation desilication: adding 4kg/t phosphoric acid into the demagging and desiliconizing concentrate obtained in the step (2), and stirring for 1 minute to adjust the pH value of the ore pulp to be between 4 and 5; adding 0.5kg/t desiliconization collecting agent into the pulp after size mixing, stirring for 2 minutes, turning on an aeration switch of a flotation machine, adjusting the aeration quantity to be 150L/h, and performing reverse flotation desiliconization roughing; and final concentrate is obtained in the flotation tank, flotation foam enters the flotation tank again for desilication scavenging, the flotation foam is reverse flotation desilication tailings, desilication middlings are obtained in the flotation tank, and the desilication middlings are returned to the reverse flotation desilication roughing flow.
Through the process, the grade of the final concentrate can reach 30.06%, the recovery rate is 58.77%, the content of magnesium oxide is 0.77%, and the content of sesquioxide is 2.47%.
Comparative example 1
The procedure shown in example 2 was followed, without the addition of a flotation modifier in step 2. And (3) the mobility of the flotation foam tailings obtained in the step 2 is poor. The grade of the final concentrate is only 27.93%, the recovery rate is 61.38%, the content of magnesium oxide is 1.12, and the content of sesquioxide is 3.24%.
Comparative example 2
The procedure shown in example 2 was used, except for the flotation modifier. Scheme 1) polyacrylamide is added in the step 2, the dosage is 0-8kg/t, and multiple groups of tests are carried out, wherein the dosage of polyacrylamide under the best effect can reach 28.12% at most, the recovery rate is 58.26%, the content of magnesium oxide is 1.11%, and the content of sesquioxide is 3.07%. Scheme 2) the steps shown in example 2 are repeated, polyacrylamide is added in step 2, under the above best effect of polyacrylamide, aluminum potassium sulfate dodecahydrate is continuously added, the using amount is 0-8kg/t, multiple groups of experiments are carried out, under the best effect, the concentrate grade can reach 28.73% at most, the recovery rate is 59.79%, the content of magnesium oxide is 1.1, and the content of sesquioxide is 3.02%. Scheme 3) the steps shown in example 2 are repeated, polyacrylamide and aluminum potassium sulfate dodecahydrate are added in step 2, and then polyaluminium chloride with the dosage of 0-8kg/t is added, and multiple experiments are carried out, so that the grade of the concentrate of the polyaluminium chloride can reach 30.03% at most, the recovery rate is 60.17%, the content of magnesium oxide is 0.98, and the content of sesquioxide is 2.68%. Scheme 4) the steps shown in example 2 are repeated, polyacrylamide, aluminum potassium sulfate dodecahydrate and polyaluminium chloride are added in step 2, the dosage is the dosage under the optimal effect, then sodium hexametaphosphate is added continuously, the dosage is 0-8kg/t, multiple groups of experiments are carried out, the concentrate grade can reach 31.20%, the recovery rate is 60.45%, the content of magnesium oxide is 0.67, and the content of sesquioxide is 2.41.
The optimized formula of the scheme 1 is as follows: the dosage of polyacrylamide is 0.8 kg/t;
scheme 2 formula after optimization: the dosage of polyacrylamide is 0.8kg/t, and the dosage of aluminum potassium sulfate dodecahydrate is 4 kg/t;
scheme 3 optimized formula: the dosage of polyacrylamide is 0.8kg/t, the dosage of aluminum potassium sulfate dodecahydrate is 4kg/t, and the dosage of polyaluminium chloride is 2.4 kg/t;
scheme 4 formula after optimization: the dosage of polyacrylamide is 0.8kg/t, the dosage of aluminum potassium sulfate dodecahydrate is 4kg/t, the dosage of polyaluminium chloride is 2.4kg/t, and the dosage of sodium hexametaphosphate is 0.8 kg/t;
through the process, the grade of the final concentrate can reach 31.20%, the recovery rate is 60.45%, the content of magnesium oxide is 0.67%, and the content of sesquioxide is 2.41%.
According to the data, the addition of the reagent can effectively improve the micro-fine particle flotation environment and improve the flotation effect. The concentrate grade and the recovery rate are improved.
Comparative example 3
The raw ore with the same properties as in example 2 is used, the demagging collecting agent and the dealumination collecting agent used in example 2 are adopted, and the separation is carried out by adopting a double reverse flow process, and the specific steps are as follows:
(1) reverse flotation demagging: taking 150g of gravity tailings (the grade is 21.63%, the fineness is 87.6%, the content of magnesium oxide is 2.61, and the content of sesquioxide is 6.05) obtained by gravity separation of a spiral chute, modulating the gravity tailings into ore pulp with the concentration of 20%, transferring the obtained ore pulp into a flotation tank under the condition that the temperature is 5 ℃, adding 8kg/t phosphoric acid (10%), and stirring for 1 minute to adjust the pH value of the ore pulp; then adding 0.85kg/t of a demagging collecting agent into the ore pulp, stirring for 2 minutes, turning on an aeration switch of a flotation machine, adjusting the aeration quantity to 150L/h, and performing reverse flotation demagging; the flotation foam is the demagnetised tailings, and the flotation tank is the demagnetised concentrate.
(2) Reverse flotation desilication: adding 4kg/t phosphoric acid into the demagging concentrate obtained in the step (1), and stirring for 1 minute to adjust the pH value of the ore pulp to be between 4 and 5; adding 0.4kg/t desiliconization collecting agent into the pulp after size mixing, stirring for 2 minutes, turning on an aeration switch of a flotation machine, adjusting the aeration quantity to be 150L/h, and performing reverse flotation desiliconization roughing; and final concentrate is obtained in the flotation tank, flotation foam enters the flotation tank again for desilication scavenging, the flotation foam is reverse flotation desilication tailings, desilication middlings are obtained in the flotation tank, and the desilication middlings are returned to the reverse flotation desilication roughing flow.
The concentrate grade can only reach 27.9 percent, the recovery rate is 61.43 percent, the content of magnesium oxide is 1.15 percent, the content of sesquioxide is 3.26 percent, and the fluidity of a foam product in the flotation process is extremely poor.
Comparative example 4
The same properties of the raw ore in example 2 were used, and the conventional forward and reverse flow was used for sorting, the specific steps were as follows:
(1) direct flotation desilicication: taking 150g of gravity tailings (the grade is 21.63%, the fineness is 87.6%, the content of magnesium oxide is 2.61, and the content of sesquioxide is 6.05) obtained by gravity separation of a spiral chute, modulating the gravity tailings into ore pulp with the concentration of 20%, transferring the obtained ore pulp into a flotation tank under the condition that the temperature is 5 ℃, adding sodium carbonate, stirring for 1 minute, and adjusting the pH value of the ore pulp to 10; then adding 3.5kg/t water glass into the ore pulp, stirring for 1 minute, then adding a proper amount of positive flotation collecting agent into the ore pulp, stirring for 2 minutes, turning on an aeration switch of a flotation machine, adjusting the aeration quantity to 150L/h, and carrying out positive flotation desiliconization; the flotation foam is desiliconized concentrate, desiliconized tailings are arranged in the flotation tank, the desiliconized tailings are continuously added with a positive flotation collector for scavenging, the foam product returns to the previous operation, and the product in the tank is the final desiliconized tailings.
(2) Reverse flotation demagging: adding a proper amount of phosphoric acid (10%) into the desiliconized concentrate obtained in the step (1), stirring for 1 minute, and adjusting the pH value of the ore pulp to 4.5; then adding 0.85kg/t of a demagging collecting agent into the ore pulp, stirring for 2 minutes, turning on an aeration switch of a flotation machine, adjusting the aeration quantity to 150L/h, and performing reverse flotation demagging; the flotation foam is the demagnetised tailings, and the flotation tank is the demagnetised concentrate.
The concentrate grade can only reach 26.13%, the recovery rate is 62.85%, the content of magnesium oxide is 1.35%, and the content of sesquioxide is 3.42%.
The technical solutions of the present invention are explained by the above embodiments, but the present invention is not limited to the above embodiments, that is, it is not meant that the present invention must depend on the above specific embodiments to be implemented. Any modification of the invention or equivalent substitution of the materials for the invention chosen by the skilled person is within the scope of protection of the patent.
Claims (8)
1. A method for removing impurities from low-grade micro-fine particle phosphate ore is characterized by comprising the following steps: the method comprises the following steps:
(1) reverse flotation demagging: preparing ore pulp from the micro-fine particle phosphorite, feeding the obtained ore pulp into a reverse flotation stirring tank, and adding an acidic regulator for size mixing; adding a demagging collecting agent into the pulp after size mixing, and feeding the pulp into a flotation tank for reverse flotation demagging; the flotation foam is demagging tailings, and demagging concentrate is in the flotation tank;
(2) synchronous demagging and desiliconizing by reverse flotation: adding a flotation regulator into the demagging concentrate obtained in the step (1) to perform size mixing and stirring; adding a demagging collecting agent and a desiliconization collecting agent in sequence to perform reverse flotation and synchronous demagging and desiliconization; the flotation foam is the demagging desiliconized tailings, and the flotation tank is the demagging desiliconized concentrate;
(3) reverse flotation desilication: adding an acidic regulator into the demagging and desiliconizing concentrate obtained in the step (2) to carry out size mixing; adding desiliconized collecting agent into the ore pulp after adjustment and feeding the ore pulp into a flotation tank for reverse flotation desiliconization roughing; and final concentrate is obtained in the flotation tank, flotation foam enters the flotation tank again for desilication scavenging, the flotation foam is reverse flotation desilication tailings, desilication middlings are obtained in the flotation tank, and the desilication middlings are returned to the reverse flotation desilication roughing flow.
2. The method for removing impurities from low-grade micro-fine particle phosphate ore according to claim 1, characterized in that: in the step (1), the low-grade micro-fine particle phosphate ore is the tailings separated by the spiral chute, the main gangue minerals of the low-grade micro-fine particle phosphate ore are magnesium-containing compounds and sesquioxide, and P is P2O5Grade (L) of a material<22wt%, magnesium oxide content 2.0-4.0wt%, sesquioxide R2O3（Fe2O3+ Al2O3) The content of the fine particle phosphorite is 4.0 to 10.0 weight percent, and the fine particle phosphorite is prepared into ore pulp with the concentration of 18 to 22 percent.
3. The method for removing impurities from low-grade micro-fine particle phosphate ore according to claim 2, characterized in that: the mineral particle fineness of-0.074 mm in the micro-fine particle phosphorite accounts for 85-95% by mass.
4. The method for removing impurities from low-grade micro-fine particle phosphate ore according to claim 3, characterized in that: the acid regulator is phosphoric acid, the dosage of the acid regulator is 7-10kg/t relative to raw ore in the step (1), the dosage of the acid regulator is 2-5kg/t relative to raw ore in the step (3), and the pH value of the ore pulp is adjusted to be between 4 and 5 by the acid regulator.
5. The method for removing impurities from low-grade micro-fine particle phosphate ore according to claim 1, characterized in that: the flotation regulator comprises the following components in percentage by mass: 30-60% of aluminum potassium sulfate dodecahydrate, 10-40% of polyacrylamide, 5-15% of sodium hexametaphosphate and 15-30% of polyaluminum chloride, wherein the sum of the mass percentages of the components is 100%, and the dosage of the flotation regulator relative to the raw ore is 7-9 kg/t.
6. The method for removing impurities from low-grade micro-fine particle phosphate ore according to claim 1, characterized in that: the magnesium removal collecting agent is a saponified product of mixed fatty acid obtained by mixing short-carbon-chain (C8-C12) fatty acid and unsaturated fatty acid according to a certain proportion, and the mixed fatty acid and sodium hydroxide solution are mixed according to a mass ratio of 1: (0.5-3) saponification reaction at 70-80 ℃.
7. The method for removing impurities from low-grade micro-fine particle phosphate ore according to claim 6, characterized in that: the dosage of the magnesium removal collecting agent in the step (1) is 0.6-1.0kg/t, and the dosage of the magnesium removal collecting agent in the step (2) is 0.1-0.4 kg/t.
8. The method for removing impurities from low-grade micro-fine particle phosphate ore according to claim 1, wherein the dealumination collecting agent is an amine collecting agent, the main components of the amine collecting agent are ether amine and ether polyamine, the dosage of the dealumination collecting agent in the step (2) is 0.1-0.3kg/t, and the dosage of the dealumination collecting agent in the step (3) is 0.3-0.5 kg/t.
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| CN114653480A (en) * | 2022-03-29 | 2022-06-24 | 武汉工程大学 | Reverse flotation process for synchronously removing silicon and magnesium impurities from collophanite and collecting agent thereof |
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