CN110302894B - Desilication method for producing bauxite concentrate by using ultra-low grade raw ore - Google Patents
Desilication method for producing bauxite concentrate by using ultra-low grade raw ore Download PDFInfo
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- 239000012141 concentrate Substances 0.000 title claims abstract description 81
- 229910001570 bauxite Inorganic materials 0.000 title claims abstract description 46
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 21
- 238000005188 flotation Methods 0.000 claims abstract description 32
- 238000004062 sedimentation Methods 0.000 claims abstract description 29
- 208000005156 Dehydration Diseases 0.000 claims abstract description 20
- 230000018044 dehydration Effects 0.000 claims abstract description 20
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 20
- CSDREXVUYHZDNP-UHFFFAOYSA-N alumanylidynesilicon Chemical compound [Al].[Si] CSDREXVUYHZDNP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000010494 dissociation reaction Methods 0.000 claims abstract description 7
- 230000005593 dissociations Effects 0.000 claims abstract description 7
- 239000000178 monomer Substances 0.000 claims abstract description 7
- 229910052500 inorganic mineral Inorganic materials 0.000 claims abstract description 6
- 239000011707 mineral Substances 0.000 claims abstract description 6
- 239000002245 particle Substances 0.000 claims abstract description 6
- 238000000227 grinding Methods 0.000 claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 238000000034 method Methods 0.000 claims description 16
- 239000002002 slurry Substances 0.000 claims description 16
- 230000002000 scavenging effect Effects 0.000 claims description 14
- 239000006260 foam Substances 0.000 claims description 12
- 238000007670 refining Methods 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 8
- 239000000706 filtrate Substances 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 6
- 238000003825 pressing Methods 0.000 claims description 5
- 238000007664 blowing Methods 0.000 claims description 4
- 238000000465 moulding Methods 0.000 claims description 4
- 238000005086 pumping Methods 0.000 claims description 4
- 238000010408 sweeping Methods 0.000 claims description 4
- 239000012065 filter cake Substances 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 239000011449 brick Substances 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims description 2
- 238000009826 distribution Methods 0.000 claims description 2
- 239000003337 fertilizer Substances 0.000 claims description 2
- 238000003860 storage Methods 0.000 claims description 2
- 238000012546 transfer Methods 0.000 claims description 2
- 238000009740 moulding (composite fabrication) Methods 0.000 claims 2
- 230000000694 effects Effects 0.000 abstract description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 239000008396 flotation agent Substances 0.000 abstract description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 9
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- 239000000377 silicon dioxide Substances 0.000 description 5
- 229910052681 coesite Inorganic materials 0.000 description 4
- 229910052906 cristobalite Inorganic materials 0.000 description 4
- 238000002474 experimental method Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 235000012239 silicon dioxide Nutrition 0.000 description 4
- 229910052682 stishovite Inorganic materials 0.000 description 4
- 229910052905 tridymite Inorganic materials 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 2
- 238000004131 Bayer process Methods 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 239000002734 clay mineral Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 229910001919 chlorite Inorganic materials 0.000 description 1
- 229910052619 chlorite group Inorganic materials 0.000 description 1
- QBWCMBCROVPCKQ-UHFFFAOYSA-N chlorous acid Chemical compound OCl=O QBWCMBCROVPCKQ-UHFFFAOYSA-N 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 229910001648 diaspore Inorganic materials 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000265 homogenisation Methods 0.000 description 1
- 229910052900 illite Inorganic materials 0.000 description 1
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
- 229910052622 kaolinite Inorganic materials 0.000 description 1
- VGIBGUSAECPPNB-UHFFFAOYSA-L nonaaluminum;magnesium;tripotassium;1,3-dioxido-2,4,5-trioxa-1,3-disilabicyclo[1.1.1]pentane;iron(2+);oxygen(2-);fluoride;hydroxide Chemical compound [OH-].[O-2].[O-2].[O-2].[O-2].[O-2].[F-].[Mg+2].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[K+].[K+].[K+].[Fe+2].O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2 VGIBGUSAECPPNB-UHFFFAOYSA-L 0.000 description 1
- 229910052903 pyrophyllite Inorganic materials 0.000 description 1
- 210000000582 semen Anatomy 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 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
- B03B7/00—Combinations of wet processes or apparatus with other processes or apparatus, e.g. for dressing ores or garbage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B9/00—General arrangement of separating plant, e.g. flow sheets
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- Manufacture And Refinement Of Metals (AREA)
- Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
Abstract
The application relates to a desilication method for producing bauxite concentrate by using ultra-low grade raw ore, which comprises the following steps of (1) homogenizing and crushing; (2) mineral monomer dissociation; (3) fine ore particle preselection; (4) microbubble flotation; (5) fine pulp selection and desliming; (6) secondary dehydration of the concentrate pulp; (7) secondary dewatering of tailing pulp. The application is novel, unique, scientific, reasonable, easy to operate, high in working efficiency, good in desilication effect, capable of effectively improving the silicon-aluminum ratio, improving the productivity, reducing the consumption of flotation agents, improving the concentrate quality, slowing down the pressure of a tailing sedimentation tank, enabling the production process to normally and continuously run, low in production cost, reducing environmental pollution, and being an innovation in ore dressing, and having huge economic and social benefits.
Description
Technical Field
The application relates to ore dressing, in particular to a desilication method for producing bauxite dressing concentrate by using ultra-low grade raw ore.
Background
The bauxite in China has rich resources and reserves in the fourth place of the world, the ore type mainly comprises medium-low grade diasporite, about 80 percent of the ore is occupied, and the ore cannot be directly produced by an economic and efficient Bayer process alumina process. Along with the development of aluminum industry in recent 20 years in China, bauxite resources are largely mined, the bauxite resources are wasted seriously, the quality of the bauxite resources is obviously reduced, the aluminum-silicon ratio of raw materials in the Bayer process alumina production process is reduced to about 4.8 at present, the production cost is continuously increased, most of alumina factories are in a loss state, and the sustainable development of alumina production enterprises is severely restricted. In order to effectively solve the resource problem, the development and utilization of low-grade bauxite are more and more urgent.
The first bauxite beneficiation production line in China is built in China aluminum industry middle state division company in 1 month in 2004, and the bauxite beneficiation and desilication are rapidly developed in 15 years later, so that a large number of bauxite beneficiation plants are developed in the places of Henan, shanxi, shandong and the like, the bauxite beneficiation technology is subjected to multiple technical innovations, and a new road is opened for bauxite resources. With the depletion of bauxite resources, the bauxite raw material grade is lower and lower, and the aluminum-silicon ratio is reduced to about 2.5 from the initial value of more than 6.0, as shown in the following table.
In the ultra-low grade bauxite, the SiO2 content reaches about 25 percent, and the ultra-low grade bauxite is mainly clay minerals such as kaolinite, pyrophyllite, illite, chlorite and the like, and the clay minerals have low hardness and very low silicon-aluminum ratio, are extremely easy to mud in the grinding process, and form secondary mineral mud. The primary slime and the secondary slime generated in the grinding process enter a flotation system, so that the consumption of medicaments is greatly increased, the quality of concentrate is affected due to serious mechanical entrainment phenomenon in the flotation process, and a large amount of primary and secondary slime is difficult to settle and dewater, so that the process cannot continuously run, and the technical problem that how to desilice, improve the silicon-aluminum ratio and ensure ore dressing production is necessary to be solved is solved.
Disclosure of Invention
Aiming at the situation, the application aims to overcome the defects of the prior art, and aims to provide a desilication method for producing bauxite concentrate by using ultra-low grade raw ore, which can effectively solve the problems of improving the silicon-aluminum ratio of the ultra-low grade bauxite and ensuring the beneficiation quality and continuous production.
The application discloses a desilication method for producing bauxite concentrate by using ultra-low grade raw ore, which comprises the following steps:
1. homogenizing and crushing: homogenizing and crushing ultra-low grade bauxite to ensure that the granularity of the crushed bauxite is less than or equal to 15mm;
2. mineral monomer dissociation: carrying out monomer dissociation, grinding and grading on the raw materials subjected to crushing and homogenization treatment on the ultra-low grade raw ores to obtain an underflow I and an overflow I;
3. fine ore particle preselection: performing primary preselection on the overflow I to obtain coarse and fine I and overflow II, wherein the coarse and fine I enters an original ore pulp tank, the overflow II enters secondary preselection, coarse and fine II and tailing pulp I are obtained after the secondary preselection, the tailing pulp I is sent to a tailing sedimentation tank, the coarse and fine II enters the original ore pulp tank, and water is added into the original ore pulp tank to form original ore pulp;
4. and (3) microbubble flotation: performing micro-bubble flotation on raw ore pulp to obtain roughing foam and roughing wake flow, enabling the roughing foam to enter a selection tank for continuous flotation to obtain refined pulp and refined wake flow, and enabling the refined wake flow to enter the roughing tank again for flotation;
5. fine pulp selection and desliming: centrifuging the concentrate to obtain concentrate slurry and overflow III;
6. secondary dehydration of concentrate pulp: the concentrate pulp is dehydrated for the first time to obtain concentrate underflow, the concentrate underflow is dehydrated and pressed to obtain a concentrate filter cake, namely concentrate is selected, and concentrate filtrate water after the concentrate underflow is subjected to filter pressing enters a circulating water tank for recycling;
7. secondary dehydration of tailing pulp: and (3) carrying out primary dehydration on the tailing pulp to obtain tailing underflow, carrying out secondary dehydration and squeezing on the tailing underflow to obtain tailings, and enabling the tailing filtrate water after the tailing pulp is subjected to filter pressing to enter a circulating water tank for recycling.
The method is novel, unique, scientific, reasonable, easy to operate, high in working efficiency and good in desilication effect, can effectively improve the silicon-aluminum ratio, improve the productivity, reduce the consumption of flotation agents, improve the concentrate quality, slow down the pressure of the tailing sedimentation tank, enable the production process to normally and continuously run, have low production cost and reduce environmental pollution, and are an innovation in ore dressing, thus having huge economic and social benefits.
Drawings
FIG. 1 is a process flow diagram of the present application.
Detailed Description
The following describes the embodiments of the present application in detail with reference to the actual situation and process flow diagrams of the present application.
In specific implementation, the desilication method for producing bauxite concentrate by using ultra-low grade raw ore provided by the application comprises the following steps of:
1. homogenizing and crushing: homogenizing ultra-low-grade bauxite, crushing by a two-stage closed-circuit crushing process, conveying the bauxite into a mixing shed through a transfer belt, and uniformly distributing the bauxite by reciprocating movement of a distribution trolley to ensure that the silicon-aluminum ratio deviation value of the bauxite is within +/-0.2, wherein the granularity of the crushed bauxite is less than or equal to 15mm;
2. mineral monomer dissociation: the raw materials treated in the step 1 are subjected to monomer dissociation through two-stage closed circuit grinding, the first-stage grinding closed circuit equipment adopts a high-pressure roller mill and a circular vibrating screen, and the screen hole size of the vibrating screen is 3mm; the second stage ore grinding closed circuit equipment adopts a spiral chute, a wet ball mill and a hydrocyclone, wherein the spiral chute is used for desliming in advance before ore grinding, fine mud generated in crushing and one stage of ore grinding is removed firstly, the overgrinding phenomenon of the wet ball mill is reduced, coarse grain ore pulp and fine grain ore pulp are obtained after desliming in advance through the spiral chute, the fine grain ore pulp enters a fine grain preselecting overflow groove for primary preselecting, the coarse grain ore pulp enters a ball mill for grinding, and classification is carried out after grinding. The diameter of the type of the hydrocyclone equipment of the classifying equipment is 300-600 mm, the underflow I and the overflow I are obtained after classification, the mass concentration of the overflow I is 22-34%, the 200 meshes are more than 88%, the underflow I returns to the wet ball mill, and the overflow I enters a fine ore particle preselection overflow groove;
3. fine ore particle preselection: the overflow I in the step 2 is conveyed to primary preselection equipment by a pump, the primary preselection equipment is a hydrocyclone, the diameter of the equipment model is 100 mm-300 mm, coarse concentrate I and overflow II are obtained after primary preselection, the mass concentration of the coarse concentrate I is 32% -55%, the mass concentration of the coarse concentrate II is more than 85%, the mass concentration of the overflow II is 12% -20%, the mass concentration of the tailing slurry I is more than 95%, the coarse concentrate I enters an original ore pulp tank, the overflow II enters secondary preselection equipment, the secondary preselection equipment is a hydrocyclone or a horizontal sedimentation centrifuge, the diameter of the hydrocyclone equipment model is 25 mm-100 mm when the hydrocyclone is the hydrocyclone, the diameter of a roller is 550 mm-1000 mm, the length-diameter ratio is 2.5-6.0 when the hydrocyclone is the horizontal sedimentation centrifuge, the mass concentration of the coarse concentrate II and the tailing slurry I is obtained after secondary preselection is 55% -80%, the mass concentration of the coarse concentrate II is more than 90%, the mass concentration of the tailing slurry I is 3% -15%, the fine concentration of the coarse concentrate II is more than 80%, the fine slurry I is more than 15% when the tailing slurry I enters the original ore tank, the primary ore pulp tank, the tailing slurry I is uniformly conveyed to the secondary preselection equipment is 15%, and the primary sedimentation tank is equal to the mass concentration of the primary ore is 35%, and the primary sedimentation tank is equal to the mass concentration of the primary ore is added;
4. and (3) microbubble flotation: pumping the raw ore pulp obtained in the step 3 into a roughing tank of a micro-bubble flotation machine by using a pump to obtain roughing foam and roughing wake; feeding the roughing foam into a selection tank for continuous flotation to obtain refined pulp and a selection wake; the refining slurry enters a refining slurry desliming step to further improve the aluminum-silicon ratio, and the refining wake flows enter a roughing tank again for floatation; the roughing wake flow enters a scavenging I groove to carry out flotation continuously to obtain scavenging I foam and scavenging I wake flow, the scavenging I foam enters the roughing groove again to carry out flotation, and the scavenging I wake flow enters a scavenging II flotation groove to carry out flotation continuously to obtain scavenging II foam and tailing pulp II; the froth II enters a sweeping I tank to continue flotation, and tailing pulp II and tailing pulp I are combined into total tailings;
5. fine pulp selection and desliming: feeding the concentrate obtained in the step 4 into a horizontal sedimentation centrifuge, wherein the diameter of a roller of the horizontal sedimentation centrifuge is 350-800 mm, the length-diameter ratio is 2.5-5.0, so as to obtain concentrate pulp and overflow III, feeding the overflow III into a sweeping II flotation tank for continuous flotation, and feeding the concentrate pulp into a semi-buried concentrate sedimentation tank;
6. secondary dehydration of concentrate pulp: pumping the concentrate slurry obtained in the step 5 into a semi-buried concentrate sedimentation tank for primary dehydration, wherein the specification of the semi-buried concentrate sedimentation tank is phi 14000 multiplied by 13800mm, obtaining concentrate underflow with the volume concentration of 40% -55% after primary dehydration, carrying out press molding on the concentrate underflow through a press filter, blowing, obtaining a concentrate filter cake with the water content of 13% -15% after secondary dehydration and press molding, and recycling concentrate filtrate water after concentrate press molding into a circulating water tank;
7. secondary dehydration of tailing pulp: mixing the tailing pulp I obtained in the step 3 and the tailing pulp II obtained in the step 4 to obtain tailing pulp, feeding the tailing pulp into a tailing sedimentation tank, enabling the tailing sedimentation tank to have the specification of phi 10000 multiplied by 15800mm, dehydrating the tailing sedimentation tank once to obtain tailing underflow with the volume concentration of 35% -45%, pressing the tailing underflow through a press filter to form, blowing the air, dehydrating the tailing twice, pressing the tailing to obtain tailings with the water content of 20% -25%, and transporting the tailings to a tailing storage yard to serve as raw materials for manufacturing baking-free bricks, ceramsite, compound fertilizer and the like, and enabling tailing filtrate water after tailing press filtration to enter a circulating water tank for recycling.
The application has very good effect through field application and test, and the related data are as follows.
The concentration of the raw ore pulp is 15% -35%, the fineness of 200 meshes is more than 85%, and the A/S is increased by more than 0.8 compared with that of ore grinding.
The concentrate slurry separating and desliming step can improve the alumina-silica ratio of the concentrate slurry by more than 1.2, and the concentrate slurry yield reaches more than 80%.
The index of the application is determined as follows:
1. raw materials: al (Al) 2 O 3 Content=46 to 55%, a/s=1.6 to 2.8;
2. concentrate: al (Al) 2 O 3 Content=58 to 65%, a/s=6.0 to 9.5;
3. tailings: al (Al) 2 O 3 Content=34 to 38%, a/s=0.9 to 1.2.
Experiment 1, taking a certain Henan coal mine as an example, carrying out two-stage closed circuit crushing, two-stage closed circuit grinding classification, fine ore grain preselection, microbubble flotation and concentrate separation desliming on ultra-low-grade bauxite to obtain concentrate pulp and tailing pulp, and carrying out secondary dehydration to obtain concentrate and tailing, wherein the specific process conditions are as follows:
1. the average granularity of the crushed bauxite is less than or equal to 10mm;
2. the diameter of the hydrocyclone of the two-stage ore grinding and classifying equipment is 350mm, the concentration of overflow I is 24.72%, and the 200 meshes are 92.08% of the hydrocyclone;
3. the primary preselection equipment adopts a hydraulic cyclone, the diameter of the primary preselection equipment is 100mm, the concentration of overflow II is 18.26%, the concentration of 400 meshes is 98.87%, the concentration of coarse and fine I is 42.18%, and the concentration of 200 meshes is 88.45%;
4. the secondary preselection equipment adopts an LW 720X 1800 horizontal decanter centrifuge, the concentration of tailing pulp I is 8.27%, and the 5 micron size is 89.59%; the concentration of coarse and fine II is 63.47%, and the fineness of 400 meshes is 94.86%;
5. the concentration of the raw ore pulp is 24.48%, and the fineness of 200 meshes is 91.02%;
6. the refining pulp desliming equipment adopts LW 550X 1600 horizontal sedimentation centrifuge, the yield of the refining pulp is 93.62%, and the aluminum-silicon ratio is improved by 1.4.
The beneficiation indicators for example 1 are shown in table 1 below.
| Product name | Al2O3 | SiO2 | A/S | Yield rate |
| Raw ore | 50.83 | 24.92 | 2.04 | 100% |
| Semen selectionOre ore | 61.37 | 9.08 | 6.76 | 56.23% |
| Tailings | 37.29 | 35.86 | 1.04 | 43.77% |
Experiment 2, taking a certain Shanxi coal mine as an example, obtaining concentrate pulp and tailing pulp after carrying out two-stage closed circuit crushing, two-stage closed circuit grinding classification, fine ore grain preselection, microbubble flotation and concentrate separation desliming on ultra-low-grade bauxite, and obtaining concentrate and tailing after carrying out secondary dehydration, wherein the specific process conditions are as follows:
1. the average granularity of the crushed bauxite is less than or equal to 14mm;
2. the diameter of the hydrocyclone of the two-stage ore grinding and classifying equipment is 300mm, the concentration of overflow I is 28.35%, and the 200 meshes of the hydrocyclone are 89.97%;
3. the primary preselection equipment adopts a hydraulic cyclone, the diameter of the primary preselection equipment is 150mm, the concentration of overflow II is 14.28%, the concentration of 400 meshes is 96.49%, the concentration of coarse and fine I is 49.29%, and the concentration of 200 meshes is 86.43%;
4. the secondary preselection equipment adopts a hydrocyclone with the diameter of 25mm, the concentration of tailing pulp I is 6.19 percent, and the fineness of 5 microns is 83.79 percent; the concentration of coarse and fine II is 68.37%, and the fineness of 400 meshes is 92.53%;
5. the concentration of the raw ore pulp is 20.28%, and the fineness of 200 meshes is 90.58%;
6. the refining pulp desliming equipment adopts LW 580X 1800 horizontal sedimentation centrifuge, the yield of the concentrate pulp is 94.89%, and the aluminum-silicon ratio is improved by 1.6.
Example 2 beneficiation indicators are shown in table 2 below.
| Product name | Al 2 O 3 | SiO2 | A/S | Yield rate |
| Raw ore | 52.61 | 22.29 | 2.36 | 100% |
| Concentrate dressing | 62.92 | 8.20 | 7.67 | 61.17% |
| Tailings | 36.37 | 37.11 | 0.98 | 38.83% |
Experiment 3, taking another coal mine in Henan as an example, obtaining concentrate pulp and tailing pulp after carrying out two-stage closed circuit crushing, two-stage closed circuit grinding classification, fine ore grain preselection, microbubble flotation and concentrate separation desliming on ultra-low grade bauxite, and obtaining concentrate and tailing after carrying out secondary dehydration, wherein the specific process conditions are as follows:
1. the average granularity of the crushed bauxite is less than or equal to 8mm;
2. the diameter of the hydrocyclone of the two-stage ore grinding and classifying equipment is 300mm, the concentration of overflow I is 32.49%, and 200 meshes are 94.26% of the hydrocyclone;
3. the primary preselection equipment adopts a hydraulic cyclone, the diameter of the primary preselection equipment is 75mm, the concentration of overflow II is 18.46%, the concentration of 400 meshes is 98.42%, the concentration of coarse and fine I is 36.68%, and the concentration of 200 meshes is 91.39%;
4. the secondary preselection equipment adopts an LW 800X 3400 horizontal decanter centrifuge, the concentration of tailing pulp I is 12.38%, and the 5 micron size is 89.93%; the concentration of coarse and fine II is 58.37%, and the fineness of 400 meshes is 96.12%;
5. the concentration of the raw ore pulp is 16.56%, and the fineness of 200 meshes is 93.49%;
6. the refining pulp desliming equipment adopts an LW 650X 2300 horizontal decanter centrifuge, the yield of the concentrate pulp is 86.27%, and the aluminum-silicon ratio is improved by 1.3.
Example 3 beneficiation indicators are shown in table 3 below.
| Product name | Al 2 O 3 | SiO2 | A/S | Yield rate |
| Raw ore | 48.39 | 25.88 | 1.87 | 100% |
| Concentrate dressing | 59.62 | 9.49 | 6.28 | 51.70% |
| Tailings | 36.37 | 37.11 | 0.98 | 48.30% |
Experiments clearly show that the method of the application is novel, unique, scientific, reasonable and easy to operate, and has the following advantages:
(1) The ultra-low-grade bauxite which cannot be utilized in the original production process is utilized, so that the situation of lack of high-grade bauxite resources required by alumina production is effectively relieved;
(2) The application ensures that the total yield of the ultra-low grade bauxite ore dressing reaches more than 50 percent, and the enrichment ratio of A/S reaches 3.3 from 2.4 of the original process;
(3) The fine ore grain pre-selection operation can improve the A/S of raw ore pulp by more than 0.8, so that the ultra-low-grade bauxite is changed into usable low-grade bauxite;
(4) The refining pulp desliming operation can improve the aluminum-silicon ratio of the refining pulp by more than 1.2, and the A/S of the concentrate product finally reaches more than 6.0 and can reach 9.5 at most;
(5) Practice proves that the dosage of the flotation reagent is saved by 40 percent because the flotation fine mud is reduced;
(6) The pollution of the waste to the environment is reduced, the method is an innovation in mineral separation, and great economic and social benefits are achieved.
Claims (1)
1. The desilication method for producing bauxite concentrate by using ultra-low grade raw ore is characterized by comprising the following steps:
(1) Homogenizing and crushing: homogenizing ultra-low-grade bauxite, crushing by a two-stage closed-circuit crushing process, conveying the bauxite into a mixing shed through a transfer belt, and uniformly distributing the bauxite by reciprocating movement of a distribution trolley to ensure that the silicon-aluminum ratio deviation value of the bauxite is within +/-0.2, wherein the granularity of the crushed bauxite is less than or equal to 15mm;
(2) Mineral monomer dissociation: the raw material treated in the step (1) is subjected to monomer dissociation through two-stage closed circuit grinding, the first-stage grinding closed circuit equipment adopts a high-pressure roller mill and a circular vibrating screen, and the screen hole size of the vibrating screen is 3mm; the second stage of ore grinding closed circuit equipment adopts a spiral chute, a wet ball mill and a hydrocyclone, wherein the spiral chute is used for desliming in advance before ore grinding, fine mud generated in crushing and one stage of ore grinding is removed firstly, the overgrinding phenomenon of the wet ball mill is reduced, coarse grain ore pulp and fine grain ore pulp are obtained after desliming in advance through the spiral chute, the fine grain ore pulp enters a fine grain preselecting overflow groove for primary preselecting, the coarse grain ore pulp enters a ball mill for grinding, and classification is carried out after grinding; the diameter of the type of the hydrocyclone equipment of the classifying equipment is 300-600 mm, the underflow I and the overflow I are obtained after classification, the mass concentration of the overflow I is 22-34%, the 200 meshes are more than 88%, the underflow I returns to the wet ball mill, and the overflow I enters a fine ore particle preselection overflow groove;
(3) Fine ore particle preselection: the overflow I in the step (2) is conveyed to primary preselection equipment by a pump, the primary preselection equipment is a hydrocyclone, the diameter of the equipment model is 100 mm-300 mm, coarse concentrate I and overflow II are obtained after primary preselection, the mass concentration of the coarse concentrate I is 32% -55%, the mass concentration of the coarse concentrate II is more than 85% by 200 meshes, the mass concentration of the overflow II is 12% -20%, the mass concentration of the overflow II is more than 95% by 400 meshes, the coarse concentrate I enters an original ore pulp tank, the overflow II enters secondary preselection equipment, the secondary preselection equipment is a hydrocyclone or a horizontal sedimentation centrifuge, when the equipment model is the hydrocyclone, the diameter of the hydrocyclone equipment model is 25 mm-100 mm, when the equipment model is the horizontal sedimentation centrifuge, the diameter of the hydrocyclone is 550 mm-1000 mm, the length-diameter ratio of the hydrocyclone is 2.5-6.0, the mass concentration of the coarse concentrate II and the tailing pulp I are obtained after secondary preselection, the mass concentration of the coarse concentrate II is 55% -80%, the mass concentration of the coarse concentrate II is more than 90%, the mass concentration of the tailing I is 3% -15% by 400 meshes, the fine concentration of the coarse concentrate II reaches more than 80%, when the fine tailings II enters the original ore pulp tank, the primary ore pulp tank is evenly mixed with the primary ore pulp, the fine concentrate I is conveyed to the primary ore pulp for 15% -15% by the secondary sedimentation tank, and proper amount of the fine ore pulp is evenly, and the primary sedimentation tank is conveyed to the primary ore slurry is equal to the primary sedimentation tank to the appropriate concentration of the fine ore is equal to the mass to the fine ore concentration of 15%;
(4) And (3) microbubble flotation: pumping the raw ore pulp obtained in the step (3) into a roughing tank of a micro-bubble flotation machine by using a pump to obtain roughing foam and roughing wake; feeding the roughing foam into a selection tank for continuous flotation to obtain refined pulp and a selection wake; the refining slurry enters a refining slurry desliming step to further improve the aluminum-silicon ratio, and the refining wake flows enter a roughing tank again for floatation; the roughing wake flow enters a scavenging I groove to carry out flotation continuously to obtain scavenging I foam and scavenging I wake flow, the scavenging I foam enters the roughing groove again to carry out flotation, and the scavenging I wake flow enters a scavenging II flotation groove to carry out flotation continuously to obtain scavenging II foam and tailing pulp II; the froth II enters a sweeping I tank to continue flotation, and tailing pulp II and tailing pulp I are combined into total tailings;
(5) Fine pulp selection and desliming: feeding the concentrate obtained in the step (4) into a horizontal sedimentation centrifuge, wherein the diameter of a drum of the horizontal sedimentation centrifuge is 350-800 mm, the length-diameter ratio is 2.5-5.0, so as to obtain concentrate pulp and overflow III, feeding the overflow III into a sweeping II flotation tank for continuous flotation, and feeding the concentrate pulp into a semi-buried concentrate sedimentation tank;
(6) Secondary dehydration of concentrate pulp: pumping the concentrate pulp obtained in the step (5) into a semi-buried concentrate sedimentation tank for primary dehydration, wherein the specification of the semi-buried concentrate sedimentation tank is phi 14000 multiplied by 13800mm, obtaining concentrate underflow with the volume concentration of 40% -55% after primary dehydration, pressing and forming the concentrate underflow through a press filter, blowing, obtaining a concentrate filter cake with the water content of 13% -15% after secondary dehydration and press forming, and recycling concentrate filtrate water after press filtration in a circulating water tank;
(7) Secondary dehydration of tailing pulp: the tailing pulp I obtained in the step (3) and the tailing pulp II obtained in the step (4) are mixed to obtain tailing pulp, the tailing pulp enters a tailing sedimentation tank, the tailing sedimentation tank is in a specification of phi 10000 multiplied by 15800mm, tailing underflow with the volume concentration of 35% -45% is obtained after primary dehydration, the tailing bottom flows through a press filter to be pressed and molded, air blowing is carried out, the tailing with the water content of 20% -25% is obtained after secondary dehydration and press molding, the tailing is dumped to a tailing storage yard and used as raw materials for manufacturing baking-free bricks, ceramsite and compound fertilizer, and tailing filtrate water after tailing press filtration enters a circulating water tank for recycling.
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