CN111229393B - Magnesite beneficiation process with short flow and over-grinding prevention - Google Patents
Magnesite beneficiation process with short flow and over-grinding prevention Download PDFInfo
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- CN111229393B CN111229393B CN202010057012.3A CN202010057012A CN111229393B CN 111229393 B CN111229393 B CN 111229393B CN 202010057012 A CN202010057012 A CN 202010057012A CN 111229393 B CN111229393 B CN 111229393B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
- B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
- B02C21/00—Disintegrating plant with or without drying of the material
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
- B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
- B02C17/00—Disintegrating by tumbling mills, i.e. mills having a container charged with the material to be disintegrated with or without special disintegrating members such as pebbles or balls
- B02C17/10—Disintegrating by tumbling mills, i.e. mills having a container charged with the material to be disintegrated with or without special disintegrating members such as pebbles or balls with one or a few disintegrating members arranged in the container
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
- B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
- B02C17/00—Disintegrating by tumbling mills, i.e. mills having a container charged with the material to be disintegrated with or without special disintegrating members such as pebbles or balls
- B02C17/18—Details
- B02C17/20—Disintegrating members
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/001—Flotation agents
- B03D1/018—Mixtures of inorganic and organic compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/02—Froth-flotation processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/02—Collectors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2203/00—Specified materials treated by the flotation agents; specified applications
- B03D2203/02—Ores
- B03D2203/04—Non-sulfide ores
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Abstract
The invention relates to a magnesite beneficiation process with short flow and over-grinding prevention, which comprises the following steps: 1) grinding raw ore by adding water for the first time and then feeding the raw ore into the first grading; 2) reverse flotation; 3) direct flotation; 4) feeding the primary positive flotation scavenging foam products, the primary positive flotation concentration bottom flow products and the secondary positive flotation concentration bottom flow products into a classifier for three-time classification, and feeding the three-time classification sand setting into a ball mill; and (4) combining ore discharge of the ball mill and tertiary grading overflow and returning to the direct flotation roughing. The method adopts a mode of combining stage grinding, stage sorting and positive and negative flotation, and produces the final qualified concentrate and tailings after sorting; the problems of large consumption of flotation reagents, difficulty in flotation and the like caused by excessive grinding of magnesite are avoided, efficient recovery of magnesite is realized, the recovery rate of magnesite is greatly improved, and the energy consumption for grinding the magnesite is reduced; the novel reagent is adopted to realize the reverse flotation and the rough concentration at one time, so that the silicon can be basically and completely removed, the normal-temperature flotation is realized, the mineral separation process is shortened, the heat energy consumption is greatly reduced, and the environmental pollution can be effectively reduced.
Description
Technical Field
The invention relates to the technical field of mineral separation, in particular to a magnesite mineral separation process which is short in flow and capable of avoiding over-grinding.
Background
Although natural magnesite resources in China are quite rich, after being mined for decades, commercial-grade magnesite is less and less, particularly high-grade magnesite cannot meet production requirements, low-grade magnesite cannot be directly used for producing high-grade products, and particularly a large amount of extra-grade magnesite cannot be utilized, so that magnesite resources are wasted.
At present, most of the magnesite used for mining is first-grade magnesite, and according to statistics, in the ascertained total reserves, ores above the first-grade product only account for 20% of the total reserves, and powder ores (granularity is less than 40mm) generated in the mining process account for less than 30% of mined ores, and because the existing light-burning kiln cannot calcine small-sized ores, only a part of the mined small-sized ores are used as raw materials of fused magnesia, and the rest of the small-sized ores cannot be used. Therefore, the amount of ore above the available first grade accounts for only 5-10% of the total reserves. Therefore, more than 70% of magnesium resources are in a place with low utilization value or are abandoned.
Along with the development of the mineral separation technology, the mineral separation research of magnesite is mainly concentrated on a flotation reagent, the mineral separation technology mainly adopts one-section or two-section continuous grinding until the content of-200 meshes accounts for about 70%, and then adopts the technological processes of reverse flotation for removing silicon and direct flotation for removing calcium.
The Chinese patent with publication number CN101773868B discloses a magnesite purifying process, which adopts the process flows of closed circuit grinding, grinding of more than 70 percent of ore with a 200-mesh, two-stage reverse flotation and two-stage direct flotation. Chinese patent application publication No. CN109225613A discloses a magnesite beneficiation process, which comprises two-stage continuous closed circuit grinding of magnesite, and magnetic separation-reverse flotation-direct flotation process flow to obtain 5 beneficiation products. The above process flow has the following disadvantages: firstly, the adoption of a continuous grinding process leads to the overgrinding of magnesite, increases energy consumption, increases ore dressing cost and reduces the recovery rate of the magnesite; secondly, reverse flotation adopts multistage, causes the flow overlength, and the ore dressing technology is complicated.
Disclosure of Invention
The invention provides a magnesite beneficiation process which is short in flow and avoids over-grinding, and by adopting a mode of combining stage grinding, stage sorting and positive and negative flotation, final qualified concentrate and tailings are produced after sorting; the problems of large consumption of flotation reagents, difficulty in flotation and the like caused by excessive grinding of magnesite are avoided, efficient recovery of magnesite is realized, the recovery rate of magnesite is greatly improved, and the energy consumption for grinding the magnesite is reduced; the novel agent KD-J1 is adopted to realize reverse flotation and one-time rough concentration, so that the silicon can be basically and completely removed, normal-temperature flotation is realized, the mineral separation process is shortened, the heat energy consumption is greatly reduced, and the environmental pollution can be effectively reduced.
In order to achieve the purpose, the invention adopts the following technical scheme:
the magnesite beneficiation process with short flow and over-grinding avoidance specifically comprises the following steps:
1) crushing raw ore, feeding the crushed raw ore into a ball mill for primary ore grinding, and adding water into the ball mill while feeding the raw ore to dissociate magnesite and gangue minerals; under the action of water power, discharging ore through a ball mill to a classifier for primary classification, returning settled sand subjected to primary classification to the ball mill, wherein the granularity of a primary classification overflow product is 45-50% of that of a primary classification overflow product of-200 meshes;
2) the primary grading overflow product enters reverse flotation, the bottom flow product of the reverse flotation is fed into forward flotation roughing, the foam product of the reverse flotation is fed into secondary grading, the settled sand of the secondary grading returns to ball milling, and the overflow of the secondary grading is final tailings;
3) the bottom flow of the forward flotation roughing is fed into primary scavenging, the foam product of the forward flotation roughing is fed into primary forward flotation concentration, the foam of the primary forward flotation concentration is fed into secondary forward flotation concentration, and the foam product of the secondary forward flotation concentration is the final concentrate; the underflow product of the primary direct flotation scavenging is the final tailings;
4) feeding the primary positive flotation scavenging foam products, the primary positive flotation concentration bottom flow products and the secondary positive flotation concentration bottom flow products into a classifier for three-time classification, and feeding the three-time classification sand setting into a ball mill; and (4) combining ore discharge of the ball mill and tertiary grading overflow and returning to the direct flotation roughing.
The ore grinding concentration in the primary ore grinding in the step 1) is 75-80%; the ball medium filling rate of the ball mill is 40-45%.
The chemical system in the reverse flotation in the step 2) is as follows: the using amount of sodium carbonate is 1100-1300 g/t, the using amount of sodium hexametaphosphate is 30-50 g/t, and the flotation collecting agent is ether amine and N-tallow-1, 3-propylenediamine according to the mass ratio of 1: (0.1-10) the amount of the mixed mixture is 150-200 g/t; the concentration of the flotation ore pulp is 35-45%, and the pH value is 9-10.
The pH value of the ore pulp in the step 3) is 10.5-11.5 during the positive flotation, and the concentration of the flotation operation is 30% -35%; the direct flotation roughing agent and the dosage are as follows: the flotation collector is prepared from a fatty acid compound and a hydrocarbon compound according to a mass ratio of 1: (0.5-1.5) the amount of the mixed mixture is 300-350 g/t; the positive flotation concentration reagent and the dosage are as follows: the dosage of the water glass is 900-1100 g/t, and the dosage of the sodium hexametaphosphate is 15-25 g/t.
Compared with the prior art, the invention has the beneficial effects that:
1) the invention fully utilizes the hardness difference between gangue minerals and magnesite and the characteristic of uneven magnesite monomer crystal size, adopts the process flow of stage grinding and stage sorting, greatly improves the utilization rate of the ball mill, and realizes energy conservation and consumption reduction;
2) by adopting stage grinding and stage sorting, the problems of large consumption of flotation reagents, difficulty in sorting and the like caused by magnesite over-grinding are avoided;
3) the efficient recovery of magnesite is realized, and the recovery rate of magnesite is greatly improved while the grade is improved;
4) by adopting a new reagent KD-J1, silicon can be substantially removed by one-time rough concentration of reverse flotation, normal-temperature flotation is realized, the mineral separation process is shortened, the heat energy consumption is greatly reduced, and the environmental pollution is effectively reduced;
5) the method realizes low-cost and high-efficiency utilization of magnesite resources, brings considerable economic benefits to magnesite enterprises and brings huge environmental benefits to society.
Drawings
Fig. 1 is a flow chart of a magnesite beneficiation process with short flow and over-grinding prevention according to the present invention.
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in fig. 1, the magnesite beneficiation process with short flow and over-grinding prevention provided by the invention specifically comprises the following steps:
1) crushing raw ore, feeding the crushed raw ore into a ball mill for primary ore grinding, and adding water into the ball mill while feeding the raw ore to dissociate magnesite and gangue minerals; under the action of water power, discharging ore through a ball mill to a classifier for primary classification, returning settled sand subjected to primary classification to the ball mill, wherein the granularity of a primary classification overflow product is 45-50% of that of a primary classification overflow product of-200 meshes;
2) the primary grading overflow product enters reverse flotation, the bottom flow product of the reverse flotation is fed into forward flotation roughing, the foam product of the reverse flotation is fed into secondary grading, the settled sand of the secondary grading returns to ball milling, and the overflow of the secondary grading is final tailings;
3) the bottom flow of the forward flotation roughing is fed into primary scavenging, the foam product of the forward flotation roughing is fed into primary forward flotation concentration, the foam of the primary forward flotation concentration is fed into secondary forward flotation concentration, and the foam product of the secondary forward flotation concentration is the final concentrate; the underflow product of the primary direct flotation scavenging is the final tailings;
4) feeding the primary positive flotation scavenging foam products, the primary positive flotation concentration bottom flow products and the secondary positive flotation concentration bottom flow products into a classifier for three-time classification, and feeding the three-time classification sand setting into a ball mill; and (4) combining ore discharge of the ball mill and tertiary grading overflow and returning to the direct flotation roughing.
The ore grinding concentration in the primary ore grinding in the step 1) is 75-80%; the ball medium filling rate of the ball mill is 40-45%.
The chemical system in the reverse flotation in the step 2) is as follows: the using amount of sodium carbonate is 1100-1300 g/t, the using amount of sodium hexametaphosphate is 30-50 g/t, and the flotation collecting agent is ether amine and N-tallow-1, 3-propylenediamine according to the mass ratio of 1: (0.1-10) the amount of the mixed mixture is 150-200 g/t; the concentration of the flotation ore pulp is 35-45%, and the pH value is 9-10.
The pH value of the ore pulp in the step 3) is 10.5-11.5 during the positive flotation, and the concentration of the flotation operation is 30% -35%; the direct flotation roughing agent and the dosage are as follows: the flotation collector is prepared from a fatty acid compound and a hydrocarbon compound according to a mass ratio of 1: (0.5-1.5) the amount of the mixed mixture is 300-350 g/t; the positive flotation concentration reagent and the dosage are as follows: the dosage of the water glass is 900-1100 g/t, and the dosage of the sodium hexametaphosphate is 15-25 g/t.
The following examples are carried out on the premise of the technical scheme of the invention, and detailed embodiments and specific operation processes are given, but the scope of the invention is not limited to the following examples. The methods used in the following examples are conventional methods unless otherwise specified.
[ example 1 ]
In the embodiment, the magnesite beneficiation process which is short in flow and avoids over-grinding is implemented by adopting a mode of combining stage grinding, stage sorting, reverse flotation and direct flotation, and finally qualified concentrate and tailings are obtained after sorting.
1) Crushing raw magnesite ore to a granularity of-12 mm or more than 90%, sieving, feeding the crushed raw magnesite ore into a primary ball mill by a belt conveyor to grind the raw magnesite, and feeding the ground raw magnesite into a primary classifier after grinding, wherein the overflow granularity of the primary classifier is 45-50% of the content of-200 meshes; the settled sand of the primary classifier returns to the primary ball mill, and the primary classifier and the primary ball mill form a closed circuit ore grinding system.
The concentration of the grinding ore in the primary ball mill is 75-80%, namely the mass ratio of the raw ore to the (raw ore + water) is 75-80%.
The ball medium filling rate of the primary ball mill is 45%.
2) The overflow of the primary classifier is fed into a reverse flotation roughing flotation machine, the bottom flow product of the reverse flotation roughing flotation machine is fed into a positive flotation roughing flotation machine, and the foam product of the reverse flotation roughing flotation machine is fed into a secondary classifier. The overflow of the secondary classifier is the final tailings, and the settled sand (particles which do not reach the monomer dissociation) of the secondary classifier returns to the primary ball mill for regrinding.
During reverse flotation, the using amount of sodium carbonate is 1220g/t, the using amount of sodium hexametaphosphate is 37g/t, and the flotation collecting agent is ether amine and N-tallow-1, 3-propylenediamine according to the mass ratio of 1: 5 the mixed mixture, the dosage is 182g/t, the concentration of flotation pulp is 42 percent, and the pH value of the pulp is 9.5.
3) The bottom flow of the reverse flotation roughing is fed into the forward flotation roughing, the foam of the forward flotation roughing is fed into the forward flotation concentrating, the foam of the forward flotation concentrating is fed into the forward flotation concentrating, and the foam of the forward flotation concentrating is the final concentrate.
And (4) feeding the underflow of the forward flotation roughing into forward flotation scavenging, wherein the underflow product of the forward flotation scavenging is final tailings.
The foam swept by the positive flotation, the underflow of the positive flotation concentration and the underflow of the positive flotation concentration are fed into a tertiary classifier, and the settled sand of the tertiary classifier is fed into a secondary ball mill. And the ore discharge of the secondary ball mill and the overflow of the tertiary classifier are combined and returned to the direct flotation roughing.
During direct flotation, the pH value of ore pulp is 11, the concentration of flotation operation is 32%, and the direct flotation roughing agent and the dosage are as follows: the flotation collector is prepared from alpha chlorinated fatty acid and polycyclic aromatic hydrocarbon according to the mass ratio of 1: 1, the amount of the mixed mixture is 328 g/t; the positive flotation concentration reagent and the dosage are as follows: the dosage of the water glass is 1050g/t, and the dosage of the sodium hexametaphosphate is 18 g/t.
In the embodiment, staged grinding and staged sorting are adopted, namely middlings are reground and then sorted, reverse flotation middlings are returned to primary ball milling, and direct flotation middlings are subjected to secondary ball milling, reground respectively and then sorted respectively; thereby improving the recovery rate of magnesite. Compared with the prior art, the recovery rate of the magnesite is improved by more than 5 percent.
The collecting agents used by the reverse flotation and the forward flotation are normal-temperature collecting agents, the reverse flotation primary desilicification is realized by modifying the conventional collecting agents, the silicon content of the underflow product is basically 0, the concentrate grade is improved, and the energy conservation and the consumption reduction are realized.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (2)
1. A short-flow and avoid the magnesite ore dressing process of the over-grinding, characterized by that, adopt the way that stage grinding, stage sorting and positive and negative flotation combine together, produce the final qualified concentrate and tailings after sorting; the method specifically comprises the following steps:
1) crushing raw ore, feeding the crushed raw ore into a ball mill for primary ore grinding, and adding water into the crushed raw ore into the ball mill to dissociate magnesite and gangue minerals; under the action of water power, discharging ore through a ball mill to a classifier for primary classification, returning settled sand subjected to primary classification to the ball mill, wherein the granularity of overflow products subjected to primary classification is 45-50% of that of-200 meshes;
2) the overflow product of the primary grading enters into reverse flotation, the underflow product of the reverse flotation is fed into the roughing of the positive flotation, the foam product of the reverse flotation is fed into the secondary grading, the settled sand of the secondary grading returns to the ball mill, the overflow product of the secondary grading is the final tailings;
3) the bottom flow product of the forward flotation roughing is fed into a primary forward flotation scavenging, the foam product of the forward flotation roughing is fed into a primary forward flotation concentration, the foam product of the primary forward flotation concentration is fed into a secondary forward flotation concentration, and the foam product of the secondary forward flotation concentration is the final concentrate; the underflow product of the primary direct flotation scavenging is the final tailings;
4) feeding the foam product scavenged by the primary positive flotation, the underflow product carefully selected by the primary positive flotation and the underflow product carefully selected by the secondary positive flotation into a classifier for three-time classification, and feeding the settled sand subjected to the three-time classification into a ball mill; the ore discharge of the ball mill and the overflow products of the third grading are combined together and returned to the direct flotation roughing;
the reagents and the dosage in the reverse flotation in the step 2) are as follows: the using amount of sodium carbonate is 1100-1300 g/t, the using amount of sodium hexametaphosphate is 30-50 g/t, and the flotation collecting agent is ether amine and N-tallow-1, 3-propylenediamine according to the mass ratio of 1: (0.1-10) the amount of the mixed mixture is 150-200 g/t; the concentration of the flotation ore pulp is 35-45%, and the pH value is 9-10;
the pH value of the ore pulp in the step 3) is 10.5-11.5 during the positive flotation, and the concentration of the flotation operation is 30% -35%; the direct flotation roughing agent and the dosage are as follows: the flotation collector is prepared from a fatty acid compound and a hydrocarbon compound according to a mass ratio of 1: (0.5-1.5) the amount of the mixed mixture is 300-350 g/t; the positive flotation concentration reagent and the dosage are as follows: the dosage of the water glass is 900-1100 g/t, and the dosage of the sodium hexametaphosphate is 15-25 g/t.
2. The magnesite beneficiation process which is short in flow and avoids over grinding as claimed in claim 1, wherein the grinding concentration in the primary grinding in the step 1) is 75% -80%; the ball medium filling rate of the ball mill is 40-45%.
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| CN101773868A (en) * | 2009-01-08 | 2010-07-14 | 鞍钢集团矿业公司 | Novel process for purifying magnesite |
| CN101890398A (en) * | 2010-07-12 | 2010-11-24 | 南通北极光自动控制技术有限公司 | Multifunctional ore dressing chemical, synthesis method thereof and using method thereof |
| CN102600982A (en) * | 2012-03-26 | 2012-07-25 | 武汉理工大学 | Fluoride-free low-acid zwitterion quartz sand reverse flotation process |
| CN102744151A (en) * | 2012-07-06 | 2012-10-24 | 中蓝连海设计研究院 | Branch flotation technology for silicon calcium collophanite |
| CN103252285A (en) * | 2012-02-15 | 2013-08-21 | 沈阳铝镁设计研究院有限公司 | Ore grinding technology for magnesite |
| WO2014179134A1 (en) * | 2013-04-30 | 2014-11-06 | Newmont Usa Limited | Method for processing mineral material containing acid-consuming carbonate and precious metal in sulfide minerals |
| CN109225613A (en) * | 2018-09-27 | 2019-01-18 | 辽宁科技大学 | A kind of magnesite ore-dressing technique |
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Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101773868A (en) * | 2009-01-08 | 2010-07-14 | 鞍钢集团矿业公司 | Novel process for purifying magnesite |
| CN101890398A (en) * | 2010-07-12 | 2010-11-24 | 南通北极光自动控制技术有限公司 | Multifunctional ore dressing chemical, synthesis method thereof and using method thereof |
| CN103252285A (en) * | 2012-02-15 | 2013-08-21 | 沈阳铝镁设计研究院有限公司 | Ore grinding technology for magnesite |
| CN102600982A (en) * | 2012-03-26 | 2012-07-25 | 武汉理工大学 | Fluoride-free low-acid zwitterion quartz sand reverse flotation process |
| CN102744151A (en) * | 2012-07-06 | 2012-10-24 | 中蓝连海设计研究院 | Branch flotation technology for silicon calcium collophanite |
| WO2014179134A1 (en) * | 2013-04-30 | 2014-11-06 | Newmont Usa Limited | Method for processing mineral material containing acid-consuming carbonate and precious metal in sulfide minerals |
| CN109225613A (en) * | 2018-09-27 | 2019-01-18 | 辽宁科技大学 | A kind of magnesite ore-dressing technique |
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