CN117258997A - Method for separating collophanite by multi-grade product spiral chute gravity-flotation joint - Google Patents
Method for separating collophanite by multi-grade product spiral chute gravity-flotation joint Download PDFInfo
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- 238000005188 flotation Methods 0.000 title claims abstract description 83
- 238000000034 method Methods 0.000 title claims abstract description 49
- 239000012141 concentrate Substances 0.000 claims abstract description 51
- 230000005484 gravity Effects 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 24
- 238000000227 grinding Methods 0.000 claims abstract description 14
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 40
- 230000008569 process Effects 0.000 claims description 22
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 238000000498 ball milling Methods 0.000 claims description 9
- 230000002000 scavenging effect Effects 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 7
- 238000003756 stirring Methods 0.000 claims description 7
- 229920002472 Starch Polymers 0.000 claims description 6
- 239000008394 flocculating agent Substances 0.000 claims description 6
- 235000019698 starch Nutrition 0.000 claims description 6
- 239000008107 starch Substances 0.000 claims description 6
- 238000010494 dissociation reaction Methods 0.000 claims description 5
- 230000005593 dissociations Effects 0.000 claims description 5
- 229920002261 Corn starch Polymers 0.000 claims description 2
- 239000008120 corn starch Substances 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 239000000126 substance Substances 0.000 claims 1
- 239000010459 dolomite Substances 0.000 abstract description 14
- 229910000514 dolomite Inorganic materials 0.000 abstract description 14
- 239000002367 phosphate rock Substances 0.000 abstract description 11
- OJMIONKXNSYLSR-UHFFFAOYSA-N phosphorous acid Chemical compound OP(O)O OJMIONKXNSYLSR-UHFFFAOYSA-N 0.000 abstract description 11
- 229910052586 apatite Inorganic materials 0.000 abstract description 6
- 229910052500 inorganic mineral Inorganic materials 0.000 abstract description 6
- 239000011707 mineral Substances 0.000 abstract description 6
- VSIIXMUUUJUKCM-UHFFFAOYSA-D pentacalcium;fluoride;triphosphate Chemical compound [F-].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O VSIIXMUUUJUKCM-UHFFFAOYSA-D 0.000 abstract description 6
- 229910019142 PO4 Inorganic materials 0.000 abstract description 5
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 abstract description 5
- 239000010452 phosphate Substances 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 3
- 238000004537 pulping Methods 0.000 abstract description 2
- 238000011084 recovery Methods 0.000 description 13
- 239000011362 coarse particle Substances 0.000 description 7
- 239000002245 particle Substances 0.000 description 7
- 239000002002 slurry Substances 0.000 description 5
- 230000001276 controlling effect Effects 0.000 description 4
- 239000003814 drug Substances 0.000 description 4
- 238000002474 experimental method Methods 0.000 description 4
- 239000008396 flotation agent Substances 0.000 description 4
- 230000008719 thickening Effects 0.000 description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000002516 radical scavenger Substances 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 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
- 239000000178 monomer Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002699 waste material Substances 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
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B9/00—General arrangement of separating plant, e.g. flow sheets
Abstract
The invention provides a method for multi-grade product spiral chute gravity-flotation combined collophanite separation, firstly grinding and pulping collophanite, then carrying out gravity separation and classification, and dividing the products into coarse-grade products, medium-grade products and fine-grade products; wherein the medium-grade product returns to continue grinding, and the coarse-grade product and the fine-grade product are respectively subjected to reverse flotation treatment. According to the invention, a medium-grade product is added on a common double-product gravity separation process, most of the product is the dolomite which is not fully separated, and because the physical difference of the specific gravity of the apatite and the dolomite in the phosphorite is small, the influence of coarse-grain dolomite on the grade of the gravity-separated coarse-grade product is large, the medium-grade product is returned to the ball mill for secondary separation, so that the mineral separation process flow is simple, the operation cost is low, the separation effect is improved, the index of the phosphate concentrate product is optimized, and the reasonable utilization of the phosphorite resource is realized.
Description
Technical Field
The invention belongs to the technical field of phosphorite beneficiation, and particularly relates to a method for multi-grade product spiral chute heavy floatation combined collophanite beneficiation.
Background
Phosphorus is an indispensable element in life, but most of existing phosphorite is sedimentary medium-low grade phosphorite, which cannot be directly and effectively utilized, and is required to be separated by adopting a proper method. There are many kinds of sorting methods for treating phosphate ore at present, and flotation is the most effective and widely used mineral separation process at present, wherein reverse flotation is more applied to separating collophanite and dolomite. However, the demand of all types of phosphorite cannot be met only by single flotation, particularly the problem that coarse and fine-grained particles are mixed after ore grinding is solved, after entering flotation operation, the low-grade fine-grained particles often adsorb a large amount of flotation agents in the flotation process due to the physical characteristics of the low-grade fine-grained particles, and meanwhile, the low-grade fine-grained particles are adsorbed on the surfaces of other ore particles, so that flotation foam is difficult to crack, the flotation efficiency is low, the flotation agent consumption is high, fine-grained apatite is extremely easy to bring into tailings, the tailings grade is higher, the yield and the recovery rate are lower, and the phosphorite resources are greatly wasted. In order to solve the problem, the gravity flotation is combined at the present stage, and a gravity separation method is adopted to enable most of coarse and fine particles to be respectively gathered, so that the independent separation of high-grade coarse-grain-grade materials and low-grade fine-grain-grade materials is realized, and the adverse influence of two materials in flotation ore pulp on flotation is greatly reduced.
CN103240169a discloses a process for separating phosphorite by gravity-flotation combination, which combines a gravity medium beneficiation process and a flotation process, and has the advantages of energy saving and high separation efficiency, but the adopted gravity medium beneficiation process is applicable to a narrower granularity range, and has no universality compared with a spiral chute.
CN105880032a discloses a gravity-flotation combined separation method for medium-low grade collophanite, and also discloses a combined process consisting of spiral chute gravity separation and flotation, wherein after separation equipment is selected, the separation effect is good, and the selected granularity is fine. However, the example data show that the method has the defect of large fluctuation of product quality.
In conclusion, although the existing gravity-flotation combined process can solve the influence of coarse and fine particle mixing on flotation to a certain extent, the gravity-flotation concentrate grade is lower due to the fact that the specific gravity of high-grade apatite and low-grade dolomite is similar by hydraulic classification, and the influence on subsequent flotation is caused.
Disclosure of Invention
The invention provides a method for separating collophanite by multi-grade product spiral chute gravity-flotation coupling, which is characterized in that a medium-grade product is added on the basis of traditional double-product gravity separation, and returned to a mill for dissociation, so that apatite and dolomite are better separated, and the mineral separation effect is improved.
In order to achieve the above object, the present invention adopts the following technical scheme: a method for separating collophanite by multi-grade product spiral chute gravity-flotation combined comprises grinding collophanite, mixing slurry, and then carrying out gravity separation and classification to divide the product into coarse-grade product, medium-grade product and fine-grade product; wherein the medium-grade product returns to continue grinding, and the coarse-grade product and the fine-grade product are respectively subjected to reverse flotation treatment.
Further, during the reselection classification, a spiral chute is adopted for hydraulic classification, wherein the interception points of the coarse-grain product, the medium-grain product and the fine-grain product respectively occupy 3-4 of the length ratio of the chute from inside to outside: 1-2: 5.
further, P in the collophanite raw ore 2 O 5 The grade is 22.84% -23.45%, the MgO content is 1.85% -2.36%, al 2 O 3 3.46% -3.68%.
Further, the medium-grade product is returned to the ore grinding process, and ball milling is carried out by adopting a single mill. The ball milling process conditions are preferably ball milling rotating speed of 300-330 r/min, ball milling time of 12-20min and ball material ratio of 3-5:1.
Further, during the reselection classification, a spiral chute is adopted for hydraulic classification, wherein the interception points of the coarse-grain product, the medium-grain product and the fine-grain product respectively occupy 3-4 of the length ratio of the chute from inside to outside: 1-2: 5.
further, P in the collophanite raw ore 2 O 5 The grade is 22.84% -23.45%, the MgO content is 1.85% -2.36%, al 2 O 3 3.46% -3.68%.
Further, the operation method comprises the following specific steps:
s1, grinding raw ore, adding water, and pulping until the concentration of ore pulp is 20-30wt%;
s2, feeding ore pulp into a spiral chute, and dividing the ore pulp into a coarse-grain product, a medium-grain product and a fine-grain product after hydraulic classification, wherein the medium-grain product returns to a mill for secondary dissociation;
s3, adding water into the coarse-fraction product obtained in the S2, stirring, adding phosphoric acid to adjust the pH value, then adding an anti-floatation collector to perform a coarse-scavenging operation, wherein the roughing concentrate is the final concentrate of the coarse-fraction product, and the scavenging concentrate is used as middlings and returned to a roughing system;
and S4, adding starch into the fine-fraction product obtained in the S2 as a flocculating agent to carry out concentration, adding phosphoric acid to adjust the pH, then adding an anti-floatation collector to carry out a rough-fine two-sweep operation, concentrating concentrate to obtain a final concentrate of the fine-fraction product, combining the concentrate tailings with the first-time scavenging concentrate to obtain a second-time scavenging raw ore, and returning the second-time scavenging concentrate to a rough-concentration system.
S5, mixing the coarse fraction product final concentrate and the fine fraction product final concentrate in the S3 and the S4 to obtain the final concentrate.
Further, after grinding in S1, the-0.074 mm ratio is more than 70%.
Further, the concentration of the ore pulp after being added with water and stirred in the S3 is 20 to 30 weight percent, and the pH value is adjusted to 4.5 to 4.8.
Further, the dosage of the reverse flotation collector for one-coarse one-sweep operation in S3 is 1.0-1.1kg/t and 0.4-0.5kg/t respectively.
Further, the flocculant in S3 is industrial corn starch, the dosage is 1.0-1.2 kg/t, the pulp concentration is 20-25wt%, and the pH is adjusted to 4.5-4.8.
Further, the operation of one coarse and one fine in S3 is only to add medicines in the course separation and the first scavenging, and the dosage of the reverse flotation collector is respectively 0.7-0.8 kg/t and 0.2-0.3 kg/t.
The invention has the following beneficial effects:
in the process of carrying out chute reselection on phosphorite, the grade of the phosphorite is V-shaped at the outlet of the chute, namely the grade of the phosphorite is firstly reduced and then increased from inside to outside on the chute. The inventor has further verified that the lowest grade part is mainly dolomite; the dolomite is easy to grind, the dissociation degree of the ground dolomite monomer is high, most of the dolomite is fine-sized particles, but coarse particles which are not completely dissociated are still partially present, and the physical difference of the specific gravity of the apatite (3.1-3.2) and the dolomite (2.85-2.9) in the phosphate ore is small, and the separation strip of the dolomite and the apatite with similar granularity is not obvious in the separation process by utilizing a spiral chute, so that the invention increases the medium-sized product during reselection and returns the product to the grinding machine for dissociation. The method is equivalent to removing part of low-grade coarse particles, reducing the influence of coarse-particle dolomite which is not completely dissociated in coarse-particle products, improving the grade of coarse-particle products before entering flotation, saving the consumption of flotation agents and realizing the efficient separation of collophanite.
Aiming at the fact that coarse-grained dolomite which is not completely dissociated is completely dissociated after regrinding, the original useless tailings become a part of fine-grained products, the yield and recovery rate of final concentrate are improved, meanwhile, the process flow is simplified, the types and the quantity of flotation agents are reduced, the production cost is reduced, and phosphorus resources are effectively recycled.
By adopting the beneficiation process, the phosphate concentrate P 2 O 5 The grade is more than or equal to 32 percent, and the recovery rate of the phosphate concentrate is more than or equal to 78 percent.
Drawings
Fig. 1 is a process flow diagram of example 1 of the present invention.
Detailed Description
Embodiments of the present invention will be described in detail below with reference to examples, but it will be understood by those skilled in the art that the following examples are only for illustrating the present invention and should not be construed as limiting the scope of the present invention.
The following examples are not specifically described, but the reagents used are commercially available chemical reagents or industrial products.
Example 1
A method for separating collophanite by multi-grade product spiral chute gravity-flotation joint is shown in figure 1.
1) The samples used in this example were derived from Yichang collophanite, P 2 O 5 The grade is 23.07%, the MgO content is 2.02%, al 2 O 3 The content is 3.56 percent, the fineness of the ground ore is 70 percent of the ore particles with the size of-0.074 mm,water is added to prepare ore pulp with the concentration of 25 weight percent, so that the phosphorus-containing mineral is separated from gangue materials, and the main gangue minerals are magnesium-containing compounds and sesquioxides.
2) Adding the regulated ore pulp into a spiral chute with the diameter of 1.2 m and the moment-diameter ratio of 0.8, wherein the interception points of the coarse-grain product, the medium-grain product and the fine-grain product respectively account for 3.5 of the length ratio of the chute from inside to outside: 1.5:5, respectively taking coarse-grain products, medium-grain products and fine-grain products in the interval ranges of 0-210mm,210-300mm and 300-600mm from inside to outside of the chute, wherein the medium-grain products return to regrinding.
3) The coarse fraction product is classified into a coarse and a sweep operation.
Coarse fraction product flotation stage: adding water into the obtained coarse-fraction product to adjust the slurry to 25% of the concentration, adding phosphoric acid to adjust the pH, and then adding a reverse flotation collector to perform reverse flotation operation, wherein the dosage of the phosphoric acid is 11.0kg/t, and the dosage of the reverse flotation collector is 1.0kg/t.
4) The fine fraction product is classified into a coarse and fine two-sweep operation.
Fine fraction product flotation stage: adding starch into the obtained fine-fraction product as a flocculating agent to carry out thickening, controlling the concentration of ore pulp to be 25%, adding phosphoric acid, stirring and adjusting, then adding an anti-flotation collector to carry out one-coarse one-fine two-sweep operation, and only adding the collector in the coarse flotation and the first-sweep operation, wherein the consumption of the phosphoric acid is 15.0kg/t, and the consumption of the anti-flotation collector is 0.7kg/t and 0.2kg/t respectively.
And finally mixing the coarse fraction product final concentrate and the fine fraction product final concentrate to obtain final concentrate. X1 is coarse fraction product scavenger tailings, and X2 and X3 are fine fraction product scavenger tailings.
Through the above experiments, the final concentrates of the coarse fraction and fine fraction products were obtained, respectively, see in particular table 1.
Table 1 (unit is%)
Flotation concentrate P obtained by a gravity flotation joint process in this example 2 O 5 The grade is 32.29%, the yield is 57.02%, and the recovery rate is 79.82%.
Example 2
A method for separating collophanite by multi-grade product spiral chute gravity flotation. The sample properties described in this example are the same as in example 1, and the intermediate grade product is not returned to regrind and directly enters the coarse grade product. In the spiral chute, the interception points of coarse fraction products and fine fraction products respectively occupy the length ratio of 5:5, the dosage of the rest medicaments is unchanged.
The coarse fraction product is classified into a coarse and a sweep operation.
Coarse fraction product flotation stage: adding water into the obtained coarse-fraction product to adjust the slurry to 25% of the concentration, adding phosphoric acid to adjust the pH, and then adding a reverse flotation collector to perform reverse flotation operation, wherein the dosage of the phosphoric acid is 11.0kg/t, and the dosage of the reverse flotation collector is 1.0kg/t.
The fine fraction product is classified into a coarse and fine two-sweep operation.
Fine fraction product flotation stage: adding starch into the obtained fine-fraction product as a flocculating agent to carry out thickening, controlling the concentration of ore pulp to be 25%, adding phosphoric acid, stirring and adjusting, then adding an anti-flotation collector to carry out one-coarse one-fine two-sweep operation, and only adding the collector in the coarse flotation and the first-sweep operation, wherein the consumption of the phosphoric acid is 15.0kg/t, and the consumption of the anti-flotation collector is 0.7kg/t and 0.2kg/t respectively.
And finally mixing the coarse fraction product final concentrate and the fine fraction product final concentrate to obtain final concentrate.
Through the above experiments, the final concentrates of the coarse fraction and fine fraction products were obtained, respectively, see in particular table 2.
Table 2 (unit is%)
Flotation concentrate P obtained by a gravity flotation combined process 2 O 5 The grade is 31.87%, the yield is 52.96%, and the recovery rate is 73.15%.
Example 3
A method for separating collophanite by multi-grade product spiral chute gravity flotation. The sample properties described in this example are the same as in example 1, and the intermediate grade product (P) obtained in example 1 was reselected 2 O 5 Grade 16.84), without regrinding, with the remainder being as in example 1.
The coarse fraction product is classified into a coarse and a sweep operation.
Coarse fraction product flotation stage: adding water into the obtained coarse-fraction product to adjust the slurry to 25% of the concentration, adding phosphoric acid to adjust the pH, and then adding a reverse flotation collector to perform reverse flotation operation, wherein the dosage of the phosphoric acid is 11.0kg/t, and the dosage of the reverse flotation collector is 1.0kg/t.
The fine fraction product is classified into a coarse and fine two-sweep operation.
Fine fraction product flotation stage: adding starch into the obtained fine-fraction product as a flocculating agent to carry out thickening, controlling the concentration of ore pulp to be 25%, adding phosphoric acid, stirring and adjusting, then adding an anti-flotation collector to carry out one-coarse one-fine two-sweep operation, and only adding the collector in the coarse flotation and the first-sweep operation, wherein the consumption of the phosphoric acid is 15.0kg/t, and the consumption of the anti-flotation collector is 0.7kg/t and 0.2kg/t respectively.
And finally mixing the coarse fraction product final concentrate and the fine fraction product final concentrate to obtain final concentrate.
Through the above experiments, the final concentrates of the coarse fraction and fine fraction products were obtained, respectively, see in particular table 3.
Table 3 (unit is%)
Flotation concentrate P obtained by a gravity flotation combined process 2 O 5 The grade is 33.25%, the yield is 47.89%, and the recovery rate is 66.14%.
Example 4
A method for separating collophanite by multi-grade product spiral chute gravity flotation. The sample properties in this example are the same as those in example 1, and the length ratio of the points of interception of the coarse-grain product, the medium-grain product and the fine-grain product, which are respectively taken up from inside to outside, to the chute is changed to 4:2:4, the rest of the procedure is unchanged, and the addition amount of the medicament is the same as that of the example 1.
The coarse fraction product is classified into a coarse and a sweep operation.
Coarse fraction product flotation stage: adding water into the obtained coarse-fraction product to adjust the slurry to 25% of the concentration, adding phosphoric acid to adjust the pH, and then adding a reverse flotation collector to perform reverse flotation operation, wherein the dosage of the phosphoric acid is 11.0kg/t, and the dosage of the reverse flotation collector is 1.0kg/t.
The fine fraction product is classified into a coarse and fine two-sweep operation.
Fine fraction product flotation stage: adding starch into the obtained fine-fraction product as a flocculating agent to carry out thickening, controlling the concentration of ore pulp to be 25%, adding phosphoric acid, stirring and adjusting, then adding an anti-flotation collector to carry out one-coarse one-fine two-sweep operation, and only adding the collector in the coarse flotation and the first-sweep operation, wherein the consumption of the phosphoric acid is 15.0kg/t, and the consumption of the anti-flotation collector is 0.7kg/t and 0.2kg/t respectively.
And finally mixing the coarse fraction product final concentrate and the fine fraction product final concentrate to obtain final concentrate.
Through the above experiments, the final concentrates of the coarse fraction and fine fraction products were obtained, respectively, see in particular table 4.
Table 4 (unit is%)
Flotation concentrate P obtained by a gravity flotation combined process 2 O 5 The grade is 31.14/%, the yield is 51.37 percent, and the recovery rate is 69.34 percent
Comparing example 1 with example 2, regrinding the medium grade product and mixing with the direct and coarse grade products, the final concentrate P obtained by the process under the condition of unchanged addition of the medicament 2 O 5 Although the grade is only improved by 0.5 percent, the yield and the recovery rate are both improved by 5 percent. Example 1 in comparison with example 3, the low grade medium grade product was discarded directly, although P was obtained 2 O 5 Higher grade but significantly reduced recovery, resulting inA great deal of waste of effective minerals; in comparison of example 1 with example 4, the selection range of the medium-grade product was adjusted for regrinding, resulting in a result P 2 O 5 The grade, the yield and the recovery rate are all greatly different.
Example 5
Based on example 1, the difference is only that the medium-sized product is ground by a mill alone, the ball milling speed is 300r/min, the ball milling time is 15min, and the ball-material ratio is 4:1.
Flotation concentrate P obtained by a gravity flotation combined process 2 O 5 Grade 32.54%, yield 60.27% and recovery 82.62%.
Example 6
Based on example 1, the difference is only 2) that in the spiral chute, the interception points of the coarse-grain product, the medium-grain product and the fine-grain product respectively occupy the length ratio of 3:2:5.
flotation concentrate P obtained by a gravity flotation combined process 2 O 5 Grade 32.02%, yield 55.27%, recovery 78.32%.
Example 7
Based on example 1, the difference is only 2) that in the spiral chute, the interception points of the coarse-grain product, the medium-grain product and the fine-grain product respectively occupy the length ratio of 5:2:3.
flotation concentrate P obtained by a gravity flotation combined process 2 O 5 Grade 29.14%, yield 64.12% and recovery 75.15%.
It should be noted that the above embodiments are only for illustrating the technical solution of the present invention, and are not limiting; while the invention has been described in detail with reference to the foregoing embodiments, it will be appreciated by those skilled in the art that variations may be made in the techniques described in the foregoing embodiments, or equivalents may be substituted for in part or in whole; such modifications and substitutions do not depart from the spirit of the invention.
Claims (10)
1. A method for separating collophanite by multi-grade product spiral chute gravity-flotation connection is characterized in that the collophanite is subjected to ore grinding and pulp mixing, and then the collophanite is subjected to gravity separation and classification, and the products are divided into coarse-grade products, medium-grade products and fine-grade products; wherein the medium-grade product returns to continue grinding, and the coarse-grade product and the fine-grade product are respectively subjected to reverse flotation treatment.
2. The method according to claim 1, characterized in that: during gravity separation and classification, a spiral chute is adopted for hydraulic classification, wherein the intercepting points of coarse-grain products, medium-grain products and fine-grain products respectively occupy the length ratio of 3-4: 1-2: 5.
3. the method according to claim 1, characterized in that: p in collophanite raw ore 2 O 5 The grade is 22.84% -23.45%, the MgO content is 1.85% -2.36%, and the Al content is 2 O 3 3.46% -3.68%.
4. The method according to claim 1, characterized in that: the medium-grade product returns to the ore grinding process, and is subjected to ball milling by adopting an independent mill; ball milling rotating speed is 300-330 r/min, ball milling time is 12-20min, and ball-material ratio is 3-5:1.
5. The method according to any one of claims 1 to 4, characterized by comprising the specific steps of:
s1, grinding raw ores, and adding water to pulp until the concentration of ore pulp is 20-30wt%;
s2, feeding ore pulp into a spiral chute, and dividing the ore pulp into a coarse-grain product, a medium-grain product and a fine-grain product after hydraulic classification, wherein the medium-grain product returns to a mill for secondary dissociation;
s3, adding water into the coarse-fraction product obtained in the S2, stirring, adding phosphoric acid to adjust the pH value, then adding an anti-floatation collector to perform a coarse-scavenging operation, wherein the roughing concentrate is the final concentrate of the coarse-fraction product, and the scavenging concentrate is used as middlings and returned to a roughing system;
s4, adding starch into the fine fraction product obtained in the S2 as a flocculating agent to carry out concentration, adding phosphoric acid to adjust the pH, then adding an anti-flotation collector to carry out a rough-fine two-sweep operation, concentrating concentrate to obtain a final concentrate of the fine fraction product, combining the concentrate tailings with the first-time scavenging concentrate to obtain a second-time scavenging raw ore, and returning the second-time scavenging concentrate to a rough-concentration system;
s5, mixing the coarse fraction product final concentrate and the fine fraction product final concentrate in the S3 and the S4 to obtain the final concentrate.
6. The method according to claim 5, wherein: after grinding in S1, the-0.074 mm ratio is more than 70%.
7. The method according to claim 5, wherein: and S3, adding water, stirring to obtain pulp with the concentration of 20-30wt% and the pH value of 4.5-4.8.
8. The method according to claim 7, wherein: the dosage of the reverse flotation collector for the operation of one coarse and one sweep in the S3 is respectively 1.0 to 1.1kg/t and 0.4 to 0.5kg/t.
9. The method according to claim 5, wherein: and S3, the flocculant is industrial corn starch, the dosage is 1.0-1.2 kg/t, the concentration of ore pulp is 20-25wt%, and the pH is regulated to 4.5-4.8.
10. The method according to claim 9, wherein: and S3, performing rough-fine two-pass operation only in rough separation and first-pass chemical adding, wherein the dosage of the reverse flotation collector is 0.7-0.8 kg/t and 0.2-0.3 kg/t respectively.
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| CN202311019901.0A CN117258997A (en) | 2023-08-14 | 2023-08-14 | Method for separating collophanite by multi-grade product spiral chute gravity-flotation joint |
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| CN202311019901.0A CN117258997A (en) | 2023-08-14 | 2023-08-14 | Method for separating collophanite by multi-grade product spiral chute gravity-flotation joint |
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