CN114653478B - Method for recycling phosphate concentrate from collophanite low-phosphate tailings - Google Patents
Method for recycling phosphate concentrate from collophanite low-phosphate tailings Download PDFInfo
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- CN114653478B CN114653478B CN202210351345.6A CN202210351345A CN114653478B CN 114653478 B CN114653478 B CN 114653478B CN 202210351345 A CN202210351345 A CN 202210351345A CN 114653478 B CN114653478 B CN 114653478B
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- collophanite
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- 229910019142 PO4 Inorganic materials 0.000 title claims abstract description 72
- 239000010452 phosphate Substances 0.000 title claims abstract description 72
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 title claims abstract description 62
- 239000012141 concentrate Substances 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 42
- 238000004064 recycling Methods 0.000 title claims abstract description 13
- 238000005188 flotation Methods 0.000 claims abstract description 103
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims abstract description 38
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 38
- 239000006260 foam Substances 0.000 claims abstract description 20
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims abstract description 19
- 239000003153 chemical reaction reagent Substances 0.000 claims abstract description 5
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 12
- 239000000194 fatty acid Substances 0.000 claims description 12
- 229930195729 fatty acid Natural products 0.000 claims description 12
- 150000004665 fatty acids Chemical class 0.000 claims description 12
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 4
- 238000005273 aeration Methods 0.000 claims description 2
- 239000002367 phosphate rock Substances 0.000 abstract description 8
- OJMIONKXNSYLSR-UHFFFAOYSA-N phosphorous acid Chemical compound OP(O)O OJMIONKXNSYLSR-UHFFFAOYSA-N 0.000 abstract description 7
- 239000011574 phosphorus Substances 0.000 abstract description 7
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 7
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 5
- 239000003795 chemical substances by application Substances 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 238000003756 stirring Methods 0.000 description 18
- 229910052500 inorganic mineral Inorganic materials 0.000 description 7
- 239000011707 mineral Substances 0.000 description 7
- 238000002474 experimental method Methods 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 230000007123 defense Effects 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
- 238000007667 floating Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000002686 phosphate fertilizer Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
Classifications
-
- 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
-
- 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
- B03B1/00—Conditioning for facilitating separation by altering physical properties of the matter to be treated
-
- 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
- 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
- B03D2203/00—Specified materials treated by the flotation agents; specified applications
- B03D2203/02—Ores
- B03D2203/04—Non-sulfide ores
- B03D2203/06—Phosphate ores
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- Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The application discloses a method for recycling phosphate concentrate from collophanite low-phosphorus tailings, and relates to the technical field of tailings recycling. Adding collophanite tailings into a flotation machine for pre-flotation, wherein no reagent is added in the flotation process, flotation foam is used as pre-selected tailings, and ore pulp in a flotation tank is used as pre-selected concentrate; concentrating the pre-selected concentrate, merging overflow into the pre-selected tailings, grinding concentrated underflow for one time, sequentially adding sulfuric acid, phosphoric acid and a fat collector, and performing reverse flotation; the primary flotation foam returns to the preliminary flotation, secondary grinding is carried out on primary flotation ore pulp in a tank, sulfuric acid, phosphoric acid and a fat collecting agent are sequentially added, and reverse flotation is carried out; the secondary flotation foam returns to the primary flotation, and the secondary flotation pulp in the tank is a phosphate concentrate product; p in collophanite tailings 2 O 5 The content is 6.00% -9.00%. Through multi-element grinding and floatation, the content of phosphorus in tailings is reduced, phosphate concentrate is effectively recovered, the utilization rate of phosphorus resources is improved, and the comprehensive production cost of a phosphorite floatation plant is reduced.
Description
Technical Field
The application relates to the technical field of tailing recycling, in particular to a method for recycling phosphate concentrate from collophanite low-phosphorus tailings.
Background
Phosphate rock is an important chemical raw material and can be used in industries such as phosphate fertilizer, medicine, food, new energy batteries, national defense and the like. Along with the development of national economy, the demand of phosphate ores is larger and larger, high-grade and high-quality phosphate ore resources are smaller and smaller, and phosphate ores mainly take medium and low grades as main materials, so that the phosphorus in the ores needs to be enriched through flotation and other processes for facilitating the use of the phosphorus. The raw ore quantity treated by a phosphate ore floatation plant in Yunnan in one year is 450 ten thousand tons, the tailing yield is about 40.0 percent, the phosphate tailing quantity produced in one year is about 186 ten thousand tons, the phosphate tailing (P 2 O 5 The content is 9% -16%), and the yield of the phosphate tailings is approximately 1860 ten thousand tons after ten years of production. By adopting the method for reducing P in tailings 2 O 5 Content technology process for P in tailings 2 O 5 The content is controlled to be about 7.0 percent, but the P in the tailings is continuously recovered 2 O 5 It is difficult.
Chinese patent CN111135947a discloses a collophanite flotation tailing treatment process, discloses a P-phosphate tailing treatment method 2 O 5 The treatment process with the grade of 8.0-13.0% has better indexes of the obtained concentrate, but the range of the treated phosphate tailings is only 8.0-13.0%, and the tailings with the grade of less than 8.0% are difficult to treat.
Literature (research on the recleaning of phosphate tailings in some flotation plant in Yunnan, li Relan and the like) reports a utilization process of the research on the recleaning of the phosphate tailings in some flotation plant in Yunnan, wherein the process adopts a reverse flotation one-coarse one-fine one-sweep closed process flow, and tailings P 2 O 5 The grade is reduced from 9.35% to 7.21%. However, the literature does not address phosphate tailings P 2 O 5 Less than 9.0% of treatment process has low adaptability.
Therefore, development of a tailing treatment process for P is highly demanded 2 O 5 The recovery of the phosphate concentrate in the tailings with the content of 6.0-9.0 percent improves the utilization rate of the phosphate resource.
Disclosure of Invention
The application aims to provide a method for recycling phosphate concentrate from collophanite low-phosphate tailings, which solves the problem that the prior tailings treatment process is difficult to recycle P 2 O 5 The content of phosphate concentrate in tailings is 6.0-9.0%.
In order to solve the technical problems, the application adopts the following technical scheme: the method for recycling the phosphate concentrate from the collophanite low-phosphate tailings is characterized by comprising the following steps of:
s1, adding collophanite tailings with the concentration of 16.0% -25.0% into a flotation machine for pre-flotation, wherein no reagent is added in the flotation process, flotation foam is used as pre-selected tailings, and ore pulp in a flotation tank is used as pre-selected concentrate;
s2, adding the pre-selected concentrate into a cyclone for concentration, overflowing and merging the concentrate into pre-selected tailings, and carrying out primary grinding on the underflow with the concentration of 30% -50%, so that the concentration of the underflow is between 27% -30.0% after grinding, the fraction ratio of-0.038 mm is between 60.0% -70.0%, carrying out primary grinding on undissociated phosphorite, further improving the monomer dissociation degree of the phosphorite, and fully separating useful minerals from gangue minerals and improving the sorting property of the ore;
s3, adding ore pulp subjected to primary ore grinding into a flotation machine, sequentially adding sulfuric acid, phosphoric acid and a fat collector, and performing reverse flotation; the primary flotation foam returns to the step S1 to carry out pre-flotation together with collophanite tailings, secondary ore grinding is carried out on primary flotation pulp in a tank, after secondary ore grinding, the concentration range after ore grinding is between 27% and 30.0%, the fraction ratio of-0.038 mm is between 70% and 80%, and the undissociated part of the primary ore grinding is further dissociated;
s4, adding ore pulp subjected to secondary ore grinding into a flotation machine, sequentially adding sulfuric acid, phosphoric acid and a fat collector, and performing reverse flotation; the secondary flotation foam returns to the step S3 to carry out primary flotation together with ore pulp after primary ore grinding, and the secondary flotation ore pulp in the tank is a phosphate concentrate product;
wherein, the chemical composition P in the collophanite tailings 2 O 5 6.00-9.00% of MgO, 9.00-17.00% of SiO 2 3.00% -10.00% of sesquioxide R 2 O 3 1.00 to 3.00 percent of CaO and 25.00 to 40.00 percent of CaO.
In the step S3, 15.00kg/t of sulfuric acid is added and stirred for 0.50-1.00 min, 1.00kg/t of phosphoric acid is added and stirred for 1.00min, and 2.00kg/t of fatty acid collector is added and stirred for 2.00-5.00 min.
In the step S4, 15.00kg/t of sulfuric acid is added and stirred for 0.50-1.00 min, 1.00kg/t of phosphoric acid is added and stirred for 1.00min, and 2.00kg/t of fatty acid collector is added and stirred for 2.00-5.00 min.
The further technical proposal is that the flotation aeration amount in the step S1 is controlled to be 3.33-6.67 m 3 /m 2 And (3) min, wherein the floatation time is 3.0-5.0 min, and the foam thickness is kept at 2.0-6.0 cm in the floatation process.
The further technical proposal is that the mass concentration of the sulfuric acid is 40 percent and the mass concentration of the phosphoric acid is 5 percent.
A further technical proposal is that the chemical composition P of the tailings is preselected in the step S1 2 O 5 4.00-6.00% of MgO, 14.00-17.00% of SiO 2 3.00% -6.00% of sesquioxide R 2 O 3 1.00 to 3.00 percent of CaO and 23.00 to 40.0 percent of CaO0％。
Further technical proposal is that the chemical composition P of the phosphate concentrate product 2 O 5 26.00-30.00% of MgO, 1.00-2.00% of SiO 2 8.00% -15.00% of sesquioxide R 2 O 3 1.00-2.00% of CaO and 25.00-30.00% of CaO.
Compared with the prior art, the application has the beneficial effects that:
the technology can more efficiently decompose collophanite and gangue minerals through a two-time ore grinding and reverse flotation combined process, and can not only decompose phosphate tailings P 2 O 5 The grade is reduced to 4.0 to 6.0 percent, and meanwhile, the qualified phosphate concentrate for the acid process can be obtained, thereby solving the problem of phosphate tailing P in the prior art 2 O 5 The grade is reduced to 6.0 percent, and the bottleneck of the qualified phosphorite by the acid method can not be obtained.
The pH value of the ore pulp is regulated by sulfuric acid to be suitable for floating magnesium gangue minerals, and the phosphoric acid activates the phosphorite, so that the phosphorite is more hydrophilic and is not easy to float upwards, the collecting agent is used for collecting the gangue minerals, and the three agents are combined together, so that the phosphorite and the gangue minerals can be separated efficiently. The adding amount of the three agents can ensure that the flotation PH of the tailings is between 4.0 and 4.5, and the collecting agent can efficiently collect most gangue minerals in the phosphate tailings, so that the qualified phosphate concentrate for the acid process is obtained.
Drawings
FIG. 1 is a process flow diagram of the present application.
Detailed Description
In order to make the objects, technical solutions and advantages of the present application more apparent, the present application will be further described in detail with reference to the accompanying drawings and examples. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the application.
Example 1
Experiments are carried out by using tailings of a flotation plant in Yunnan, and phosphate tailings P of the tailings 2 O 5 The content is 7.12%, the tailings are added into a flotation machine for pre-flotation, no medicament is added in the flotation process, the flotation foam is used as the pre-selected tailings, and the flotation tank is filled with the flotation foamThe pulp serves as a pre-concentrate. Concentrating the pre-selected concentrate in a cyclone of concentrating equipment, merging overflow into pre-selected tailings, concentrating the underflow with the concentration of 30-50% into a mill, and grinding for one time. The fineness of the primary grinding is controlled to be more than or equal to 60.00 percent with the granularity of-400 meshes, and ore pulp is added into a flotation machine after the primary grinding is performed to the target fineness. Firstly adding 15.00kg/t of sulfuric acid, stirring for 0.50-1.00 min, then adding 1.00kg/t of phosphoric acid, stirring for 1.00min, then adding 6-62.00kg/t of fatty acid collector YP, stirring for 2.00-5.00 min, performing primary flotation, returning primary flotation foam to pre-flotation, enabling ore pulp in a primary flotation tank to enter secondary ore grinding, controlling the ore grinding fineness of the secondary ore grinding to be more than or equal to 70.00% of-400 meshes, and adding the ore pulp into a flotation machine after grinding to the target fineness. Firstly adding 15.00kg/t of sulfuric acid and stirring for 0.50-1.00 min, then adding 1.00kg/t of phosphoric acid and stirring for 1.00min, then adding 2.00kg/t of fatty acid collector and stirring for 2.00-5.00 min to perform secondary flotation, returning secondary flotation foam to primary flotation, and obtaining the phosphate concentrate product as ore pulp in the secondary tank. The various indexes in the experiment are shown in table 1.
TABLE 1
| Name of the name | P 2 O 5 ％ | MgO％ | Fe 2 O 3 ％ | Al 2 O 3 ％ | SiO 2 ％ |
| Collophanite tailing | 7.10 | 14.32 | 0.91 | 1.13 | 8.51 |
| Phosphate concentrate product | 27.23 | 1.50 | 1.48 | 1.30 | 20.12 |
| Final tailings | 4.98 | 17.61 | 0.77 | 0.67 | 7.08 |
| Recovery rate of phosphate tailing resource | 36.54 |
As can be seen from Table 1, after the phosphate tailings are subjected to multi-component grinding and flotation, the phosphate tailings P 2 O 5 From 7.12% to 4.98%, concentrate P 2 O 5 The content is 27.50%, the recovery rate of the phosphorus resource is improved by 36.54%, and the amount of the phosphate tailings is reduced.
Example 2
Experiments are carried out by using phosphate tailings of Yunnan flotation plant, and raw ore thereofP 2 O 5 The content is 9.00%, the tailings are added into a flotation machine for pre-flotation, no reagent is added in the flotation process, the flotation foam is used as pre-selected tailings, and the ore pulp in the flotation tank is used as pre-selected concentrate. Concentrating the pre-selected concentrate in a cyclone of concentrating equipment, merging overflow into pre-selected tailings, concentrating the underflow with the concentration of 30-50% into a mill, and grinding for one time. The fineness of the primary grinding is controlled to be more than or equal to 60.00 percent with the granularity of-400 meshes, and ore pulp is added into a flotation machine after the primary grinding is performed to the target fineness. Firstly adding 15.00kg/t of sulfuric acid, stirring for 0.50-1.00 min, then adding 1.00kg/t of phosphoric acid, stirring for 1.00min, then adding 6-62.00kg/t of fatty acid collector YP, stirring for 2.00-5.00 min, performing primary flotation, returning primary flotation foam to pre-flotation, enabling ore pulp in a primary flotation tank to enter secondary ore grinding, controlling the ore grinding fineness of the secondary ore grinding to be more than or equal to 70.00% of-400 meshes, and adding the ore pulp into a flotation machine after grinding to the target fineness. Firstly adding 15.00kg/t of sulfuric acid and stirring for 0.50-1.00 min, then adding 1.00kg/t of phosphoric acid and stirring for 1.00min, then adding 2.00kg/t of fatty acid collector and stirring for 2.00-5.00 min to perform secondary flotation, returning secondary flotation foam to primary flotation, and obtaining the phosphate concentrate product as ore pulp in the secondary tank. The various indices in the experiment are shown in table 2.
TABLE 2
| Name of the name | P 2 O 5 ％ | MgO％ | Fe 2 O 3 ％ | Al 2 O 3 ％ | SiO 2 ％ |
| Collophanite tailing | 9.00 | 12.58 | 1.05 | 1.00 | 10.42 |
| Phosphate concentrate product | 28.01 | 1.30 | 1.23 | 1.12 | 17.22 |
| Final tailings | 6.00 | 15.17 | 0.82 | 0.67 | 6.80 |
| Recovery rate of phosphate tailing resource | 42.42 |
As can be seen from Table 2, after the phosphate tailings are subjected to multi-component grinding and flotation, the phosphate tailings P 2 O 5 From 9.00% to 6.00%, concentrate P 2 O 5 The content is 28.01%, and the phosphate tailing resource returnsThe yield is 42.42 percent, and the amount of the phosphate tailings is reduced.
Example 3
Experiments are carried out by using phosphate tailings of Yunnan flotation plant, and raw ore P 2 O 5 The content is 6.00%, the tailings are added into a flotation machine for pre-flotation, no reagent is added in the flotation process, the flotation foam is used as pre-selected tailings, and the ore pulp in the flotation tank is used as pre-selected concentrate. Concentrating the pre-selected concentrate in a cyclone of concentrating equipment, merging overflow into pre-selected tailings, concentrating the underflow with the concentration of 30-50% into a mill, and grinding for one time. The fineness of the primary grinding is controlled to be more than or equal to 60.00 percent with the granularity of-400 meshes, and ore pulp is added into a flotation machine after the primary grinding is performed to the target fineness. Firstly adding 15.00kg/t of sulfuric acid, stirring for 0.50-1.00 min, then adding 1.00kg/t of phosphoric acid, stirring for 1.00min, then adding 2.00kg/t of fatty acid collector, stirring for 2.00-5.00 min, performing primary flotation, returning primary flotation foam to perform preliminary flotation, enabling ore pulp in a primary flotation tank to enter secondary ore grinding, controlling the ore grinding fineness of the secondary ore grinding to be more than or equal to 70.00% below-400 meshes, and adding the ore pulp into a flotation machine after grinding to the target fineness. Firstly adding 15.00kg/t of sulfuric acid and stirring for 0.50-1.00 min, then adding 1.00kg/t of phosphoric acid and stirring for 1.00min, then adding 2.00kg/t of fatty acid collector and stirring for 2.00-5.00 min to perform secondary flotation, returning secondary flotation foam to primary flotation, and obtaining the phosphate concentrate product as ore pulp in the secondary tank. The various indices in the experiment are shown in table 3.
TABLE 3 Table 3
| Name of the name | P 2 O 5 ％ | MgO％ | Fe 2 O 3 ％ | Al 2 O 3 ％ | SiO 2 ％ |
| Collophanite tailing | 6.00 | 15.58 | 1.05 | 1.00 | 10.42 |
| Phosphate concentrate product | 26.00 | 1.80 | 1.23 | 1.12 | 17.22 |
| Final tailings | 4.00 | 17.17 | 0.82 | 0.67 | 6.80 |
| Recovery rate of phosphate tailing resource | 39.39 |
As can be seen from Table 3, the phosphate tailingsAfter multi-element grinding and flotation, the phosphate tailing P 2 O 5 From 6.0% to 4.0%, concentrate P 2 O 5 The content is 26.00%, the phosphate tailing resource is recovered by 39.39%, and the phosphate tailing amount is reduced.
From the results of examples 1 to 3, it can be seen that: the process is used for treating the collophanite phosphate tailings with the grade of 6.00-9.00%, so that good economic benefit is obtained, and the process has demonstration significance for the application of the phosphate tailings.
Although the application has been described herein with reference to a number of illustrative embodiments thereof, it should be understood that numerous other modifications and embodiments can be devised by those skilled in the art that will fall within the scope and spirit of the principles of this disclosure. More specifically, various variations and modifications may be made to the component parts or arrangements of the subject combination arrangement within the scope of the present disclosure, the drawings and the claims. In addition to variations and modifications in the component parts or arrangements, other uses will be apparent to those skilled in the art.
Claims (5)
1. The method for recycling the phosphate concentrate from the collophanite low-phosphate tailings is characterized by comprising the following steps of:
s1, adding collophanite tailings with the concentration of 16.0% -25.0% into a flotation machine for pre-flotation, wherein no reagent is added in the flotation process, flotation foam is used as pre-selected tailings, and ore pulp in a flotation tank is used as pre-selected concentrate;
s2, adding the pre-selected concentrate into a cyclone for concentration, merging overflow into pre-selected tailings, and carrying out primary grinding on the underflow which is concentrated to 30% -50% of concentration, wherein the concentration is between 27% -30.0% after grinding, and the fraction ratio of-0.038 mm is between 60% -70%;
s3, adding ore pulp subjected to primary ore grinding into a flotation machine, sequentially adding sulfuric acid, phosphoric acid and fatty acid collectors, and performing reverse flotation; the primary flotation foam returns to the step S1 to carry out pre-flotation together with collophanite tailings, secondary ore grinding is carried out on the primary flotation pulp in a tank, the concentration range after ore grinding is between 27% and 30.0%, and the fraction ratio of-0.038 mm is between 70% and 80%;
wherein, in the step S3, 20.00kg/t of sulfuric acid is firstly added and stirred for 0.50-1.00 min, then 1.00kg/t of phosphoric acid is added and stirred for 1.00min, and then 2.00kg/t of fatty acid collector is added and stirred for 2.00-5.00 min; the mass concentration of the sulfuric acid is 40%, and the mass concentration of the phosphoric acid is 5%;
s4, adding ore pulp subjected to secondary ore grinding into a flotation machine, sequentially adding sulfuric acid, phosphoric acid and fatty acid collectors, and performing reverse flotation; the secondary flotation foam returns to the step S3 to carry out primary flotation together with ore pulp after primary ore grinding, and the secondary flotation ore pulp in the tank is a phosphate concentrate product;
wherein, the chemical composition P in the collophanite tailings 2 O 5 6.00-9.00% of MgO, 9.00-17.00% of SiO 2 3.00% -10.00% of sesquioxide R 2 O 3 1.00 to 3.00 percent of CaO and 25.00 to 40.00 percent of CaO.
2. The method for recycling phosphate concentrate from collophanite low-phosphate tailings according to claim 1, wherein the method comprises the following steps: in the step S4, 15.00kg/t of sulfuric acid is added and stirred for 0.50-1.00 min, 1.00kg/t of phosphoric acid is added and stirred for 1.00min, and 2.00kg/t of fatty acid collector is added and stirred for 2.00-5.00 min.
3. The method for recycling phosphate concentrate from collophanite low-phosphate tailings according to claim 1, wherein the method comprises the following steps: the flotation aeration amount in the step S1 is controlled to be 3.33-6.67 m 3 /(m 2 Min), flotation time is 3.0-5.0 min, and the foam thickness is kept to be 2.0-6.0 cm in the flotation process.
4. The method for recycling phosphate concentrate from collophanite low-phosphate tailings according to claim 1, wherein the method comprises the following steps: the chemical composition P of the tailings is preselected in the step S1 2 O 5 4.00-6.00% of MgO, 14.00-17.00% of SiO 2 3.00% -6.00% of sesquioxide R 2 O 3 1.00 to 3.00 percent of CaO and 23.00 to 40.00 percent of CaO.
5. The method for recycling phosphate concentrate from collophanite low-phosphate tailings according to claim 1, wherein the method comprises the following steps: the phosphate concentrate is acid phosphate concentrate with chemical composition P 2 O 5 26.00-30.00% of MgO, 1.00-2.00% of SiO 2 8.00% -15.00% of sesquioxide R 2 O 3 1.00-2.00% of CaO and 25.00-30.00% of CaO.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202210351345.6A CN114653478B (en) | 2022-04-02 | 2022-04-02 | Method for recycling phosphate concentrate from collophanite low-phosphate tailings |
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| CN202210351345.6A CN114653478B (en) | 2022-04-02 | 2022-04-02 | Method for recycling phosphate concentrate from collophanite low-phosphate tailings |
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| CN114653478A CN114653478A (en) | 2022-06-24 |
| CN114653478B true CN114653478B (en) | 2023-11-17 |
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