CN109225653B - Beneficiation method for removing phosphorus from high-phosphorus hematite - Google Patents

Beneficiation method for removing phosphorus from high-phosphorus hematite Download PDF

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CN109225653B
CN109225653B CN201810795423.5A CN201810795423A CN109225653B CN 109225653 B CN109225653 B CN 109225653B CN 201810795423 A CN201810795423 A CN 201810795423A CN 109225653 B CN109225653 B CN 109225653B
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CN109225653A (en
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柏少军
文书明
丁湛
吴猛
付翔宇
李春龙
吴丹丹
白旭
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Kunming University of Science and Technology
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    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/02—Froth-flotation processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/001—Flotation agents
    • B03D1/004—Organic compounds
    • B03D1/01—Organic compounds containing nitrogen
    • 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
    • B03D1/004—Organic compounds
    • B03D1/012—Organic compounds containing sulfur
    • 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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    • 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
    • B03D2203/00—Specified materials treated by the flotation agents; specified applications
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Abstract

The invention relates to a beneficiation method for removing phosphorus from high-phosphorus limonite ore, belonging to the technical field of mineral processing engineering. Crushing and grinding the high-phosphorus hematite and limonite raw materials to obtain ground ore products; mixing the obtained ore grinding product, adding sodium carbonate, then adding sodium silicate, a novel combined inhibitor and a mixed collector MG, performing rough concentration, inflating and scraping for 4-8 min to obtain rough concentration high-phosphorus foam and rough concentration bottom flow; adding sodium carbonate into the obtained underflow after rough concentration, then adding sodium silicate, a novel combined inhibitor and a mixed collecting agent MG, carrying out scavenging, and carrying out air inflation and foam scraping for 5-8 min to obtain scavenged high-phosphorus foam and first scavenging underflow; and adding sodium carbonate into the obtained first scavenging underflow, then adding sodium silicate, a novel combined inhibitor and a mixed collecting agent MG, carrying out secondary scavenging, inflating and scraping for 3-6 min, and obtaining secondary scavenging foam and a product in the tank. The method has low cost and convenient and simple operation, and realizes effective removal of the phosphorus-containing minerals.

Description

Beneficiation method for removing phosphorus from high-phosphorus hematite
Technical Field
The invention relates to a beneficiation method for removing phosphorus from high-phosphorus limonite ore, belonging to the technical field of mineral processing engineering.
Background
The high-phosphorus limonite ore mainly takes sedimentary iron ore, and phosphorus in the iron ore is densely symbiotic with other minerals mainly in the form of apatite or carbon fluorapatite. Since the apatite agglomerates are very fine in size and partly in the form of a homogeneous and very fine mechanical inclusion in the limonite carrier mineral, this poses difficulties in the dephosphorization of mineral concentrates. Phosphorus removal of high-phosphorus hematite is always a hot problem which is not fundamentally solved in the field of mineral separation.
The sedimentary hematite and limonite ore has the characteristics of high phosphorus, high silicon, low sulfur and low iron content. The ore generally contains 35-55 wt% of iron, 0.5-0.9 wt% of phosphorus, and part of phosphorus is more than 1.0 wt%. Phosphorus is one of the most main harmful impurity elements in iron ore, high-phosphorus iron ore can be directly used as an iron-making raw material without dephosphorization, and pig iron can not be used as a qualified steel-making raw material due to high cold brittleness caused by the high phosphorus content. Because of the above-mentioned hazards of the phosphorus component, the content of the phosphorus component in the smelting raw materials should be reduced as much as possible during the steel smelting process. After the hematite and the limonite are subjected to mineral dressing and reduction roasting, the obtained product mainly contains sintered materials containing metallic iron, magnetite and phosphorus-rich slag, wherein the metallic iron and the magnetite can be used as iron-making raw materials. However, the high-phosphorus limonite ore has not been developed and utilized effectively because of the lack of reasonably feasible phosphorus removal technology.
The known red-brown iron ore dephosphorization technology comprises a physical method, a chemical method, a metallurgical method and a microbiological method. The most common of these is physical. This often requires fine grinding of the ore until the iron minerals are fully dissociated and then separated by magnetic separation or flotation. The dephosphorization by the magnetic separation method generally has the problems of low dephosphorization rate, low iron recovery rate and the like, and the problem is particularly obvious for finely ground fine particle fraction sorted materials. Dephosphorization by a flotation method usually realizes removal of phosphorus-containing minerals by using a fatty acid collecting agent under an alkaline condition. In order to enhance the selectivity of dephosphorization by reverse flotation, sodium silicate, sodium hexametaphosphate, carboxymethyl cellulose and other agents are generally added into the ore pulp solution to serve as a dispersing agent, and starch is added to serve as an inhibitor of iron minerals. However, the traditional fatty acid collecting agent generally has the problems of poor solubility, poor selectivity and the like. In addition, the amount of starch used is large, and the solubility of starch in water at normal temperature is not high. Therefore, the traditional physical beneficiation method is difficult to achieve satisfactory effects. The chemical dephosphorization is to perform acid leaching on the ore by nitric acid, sulfuric acid or hydrochloric acid, has high dephosphorization rate and low requirement on the iron mineral cleavage degree, but has high acid consumption and high cost by the chemical method, and causes the loss of iron by dissolving some soluble iron minerals. Dephosphorization by a microbial method mainly reduces the pH value of a system by producing acid through microbial metabolism so as to dissolve phosphate ores, and metabolic acid forms a complex with Ca, Mg, Al and other ions so as to promote the dissolution of phosphorus minerals. However, for some reasons of technical economy, the research results are not common in industrial production.
Application No. 200610019950.4 a production method of dephosphorization and iron extraction of high phosphorus oolitic hematite, carry out direct reduction to high phosphorus oolitic hematite and obtain metallic iron and phosphorus-rich sediment, obtain qualified iron ore concentrate after the low intensity magnetic separation, the good or bad of low intensity magnetic separation index depends on the degree of iron and sediment separation in the direct reduction operation, therefore has strict restriction to the nature of the raw materials of entering the stove, and high temperature operation makes the processing cost higher simultaneously.
The application number is 200810163393.2 oolitic high phosphorus hematite's iron lifting phosphorus reduction method, application number is 200810058801.8 a high phosphorus hematite red brown iron ore magnetic roasting-leaching phosphorus reduction method, reduce the calcination to high phosphorus red brown iron ore to change the occurrence state of iron promptly, make the gathering of iron mineral crystal certain degree grow greatly, adopt weak magnetic separation to dephosphorize in advance and carry out the iron-extracting, carry out the acid leaching phosphorus reduction to the magnetic separation concentrate again and obtain qualified iron concentrate, the method flow is complicated, the treatment cost is high, acid consumption is big in the acid leaching operation, metal loss is also more serious when the phosphorus desorption.
Based on the above technical situation, the utilization rate of the high-phosphorus limonite ore is extremely low, and the resource cannot be effectively utilized because an ideal phosphorus reduction method is not developed. In recent years, the market price of iron ore is in a rising trend, serious impact is brought to iron and steel enterprises in China, and if an effective ore dressing method is adopted, the content of phosphorus in the hematite and the limonite can be greatly reduced, so that a low-phosphorus iron-making raw material is obtained, and good economic benefit and environmental benefit are generated.
Disclosure of Invention
Aiming at the problems and the defects in the prior art, the invention provides a beneficiation method for removing phosphorus from high-phosphorus limonite ore. The method has low cost and convenient and simple operation, and realizes effective removal of the phosphorus-containing minerals. The invention is realized by the following technical scheme.
A beneficiation method for removing phosphorus from high-phosphorus hematite ore comprises the following specific steps:
step 1, crushing and grinding a high-phosphorus limonite raw material until the content of mineral aggregate with the particle size of-74 mu m accounts for 75-95% to obtain a ground ore product, wherein the ground ore mass concentration is 55-65 wt%;
step 2, mixing the ore grinding product obtained in the step 1 until the solid mass concentration is 25-35 wt%, adding sodium carbonate to control the pH value of an ore pulp solution to be 8-10, stirring for 4-8 min, then adding sodium silicate 1000-1600 g/t, stirring for 4-8 min, adding a combined inhibitor 100-300 g/t, stirring for 5-15 min, adding a mixed collecting agent MG 200-400 g/t, stirring for 5-15 min, performing rough separation, and performing air-inflation foam scraping for 4-8 min to obtain rough-separated high-phosphorus foam and underflow after rough separation;
step 3, adding sodium carbonate into the roughly selected underflow obtained in the step 2 to control the pH value of the ore pulp solution to be 8-10, stirring for 3-6 min, adding 500-800 g/t of sodium silicate and 100-200 g/t of a combined inhibitor, stirring for 5-15 min, mixing 100-200 g/t of a collecting agent MG, stirring for 5-15 min, scavenging, and carrying out air-inflation foam scraping for 5-8 min to obtain scavenged high-phosphorus foam and first scavenging underflow;
step 4, adding sodium carbonate into the primary scavenging underflow obtained in the step 3 to control the pH value of the ore pulp solution to be 8-10, stirring for 4-8 min, adding 200-400 g/t of sodium silicate, stirring for 4-8 min, adding 50-100 g/t of combined inhibitor, stirring for 5-15 min, mixing collecting agent MG 50-100 g/t, stirring for 5-15 min, then performing secondary scavenging, and performing air-inflation foam scraping for 3-6 min to obtain secondary scavenging foam and products in the tank; combining the rough concentration high-phosphorus foam obtained in the step 2, the scavenging high-phosphorus foam obtained in the step 3 and the secondary scavenging foam obtained in the step 4 to obtain high-phosphorus foam, wherein the obtained in-tank product is the final iron ore material;
the combined inhibitor in the steps 2, 3 and 4 is a mixture of sodium lignosulfonate and 3, 4-dihydroxybenzylamine in a molar ratio of 3-5: 1; in the steps 2, 3 and 4, the mixed collecting agent MG is a mixture of oleamide and linolenic acid in a molar ratio of 5: 1.
The g/t refers to the grams of the reagent added to each ton of the high-phosphorus hematite ore raw material.
The invention has the beneficial effects that:
1. compared with the traditional iron mineral inhibitor, the combined inhibitor has less dosage and good solubility, and the sodium lignosulfonate and the 3, 4-dihydroxy benzylamine contain amino and a plurality of hydroxyl groups, so that the iron oxide mineral can be effectively inhibited.
2. The solubility and the selectivity of the mixed collector MG are better, compared with a single fatty acid collector, the effective removal of the phosphorus-containing minerals can be realized by adding a small amount of the mixed collector MG, and the problems of high iron loss rate, low dephosphorization rate and the like in the dephosphorization by a flotation method are solved.
3. The method has the advantages of short flow, low cost, simple operation and higher popularization value, and has certain guiding significance for the full utilization of other refractory high-phosphorus iron ore resources.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The invention is further described with reference to the following drawings and detailed description.
Example 1
As shown in fig. 1, the beneficiation method for removing phosphorus from high-phosphorus limonite ore comprises the following specific steps:
1, crushing and grinding a high-phosphorus hematite raw material (the raw material is from an iron ore in Yunnan, the phosphorus content of an oxidized ore in the area is higher, and the main chemical element analysis and iron phase analysis results of the raw ore are respectively shown in tables 1 and 2) until the content of mineral aggregate with the particle size of-74 mu m accounts for 75 percent to obtain a ground ore product, wherein the ground ore mass concentration is 60 percent by weight;
TABLE 1 analysis of main chemical elements of raw ore and
element(s) TFe P S SiO2 Al2O3
Content/% 34.75 0.65 0.16 29.93 8.43
TABLE 2 analysis results of the crude iron phases
Figure DEST_PATH_IMAGE002
Step 2, mixing the ore grinding product obtained in the step 1 until the solid mass concentration is 25wt%, adding sodium carbonate to control the pH value of the ore pulp solution to be 8, stirring for 4min, then adding 1600g/t of sodium silicate, stirring for 6min, adding 200g/t of combined inhibitor, stirring for 8min, adding 200g/t of mixed collector MG200g/t, stirring for 8min, performing roughing, and performing air-charging foam scraping for 6min to obtain roughing high-phosphorus foam and roughing underflow;
step 3, adding sodium carbonate into the underflow obtained after rough concentration in the step 2 to control the pH value of the ore pulp solution to be 8, stirring for 3min, adding 800g/t of sodium silicate and 100g/t of a combined inhibitor, stirring for 6min, mixing a collector MG100g/t, stirring for 6min, then scavenging, aerating and scraping for 5min to obtain scavenged high-phosphorus foam and a first scavenging underflow;
step 4, adding sodium carbonate into the first scavenging underflow obtained in the step 3 to control the pH value of the ore pulp solution to be 8, stirring for 4min, adding 400g/t of sodium silicate, stirring for 4min, adding 50g/t of a combined inhibitor, stirring for 5min, mixing a collecting agent MG50g/t, stirring for 5min, then carrying out secondary scavenging, and carrying out air inflation and foam scraping for 4min to obtain secondary scavenging foam and products in the tank; combining the rough concentration high-phosphorus foam obtained in the step 2, the scavenging high-phosphorus foam obtained in the step 3 and the secondary scavenging foam obtained in the step 4 to obtain high-phosphorus foam, wherein the obtained in-tank product is the final iron ore material;
in the steps 2, 3 and 4, the combined inhibitor is a mixture of sodium lignosulfonate and 3, 4-dihydroxybenzylamine in a molar ratio of 3: 1; in the steps 2, 3 and 4, the mixed collecting agent MG is a mixture of oleamide and linolenic acid in a molar ratio of 5: 1.
The iron grade in the final iron mineral material is 37.57wt%, the phosphorus content is 0.16wt%, the iron recovery rate is 76.85%, and the dephosphorization rate is 82.5%.
Comparative example 1
Replacing the combined inhibitor and mixed collector MG of example 1 with a conventional starch inhibitor and a conventional sodium oleate collector; in the step 2, the adding amount of the conventional starch inhibitor is 600g/t, and the adding amount of the conventional sodium oleate is 400 g/t; the adding amount of the conventional starch inhibitor in the step 3 is 300g/t, and the adding amount of the conventional sodium oleate collecting agent is 200 g/t; the adding amount of the conventional starch inhibitor in the step 4 is 100g/t, the adding amount of the conventional sodium oleate collecting agent is 100g/t, and other parameters are unchanged. In the final iron mineral material obtained in comparative example 1, the iron grade was 38.17wt%, phosphorus content was 0.25wt%, the iron recovery rate was 74.12%, and the dephosphorization rate was 74.05%.
From this example 1 and comparative example 1, it can be seen that the combined inhibitor and mixed collector MG used in the present invention are less, the mixed collector MG added in the present invention can effectively remove the phosphorus-containing minerals, and the iron recovery rate and the dephosphorization rate are higher than those in comparative example 1. The production cost of the invention is reduced by 12 yuan/ton of raw ore.
Example 2
As shown in fig. 1, the beneficiation method for removing phosphorus from high-phosphorus limonite ore comprises the following specific steps:
step 1, crushing and grinding a high-phosphorus limonite raw material (the main chemical element analysis and iron phase analysis results of the raw material raw ore are respectively shown in tables 3 and 4) until the content of mineral aggregate with the particle size of-74 mu m accounts for 85 percent to obtain a ground ore product, wherein the ground ore mass concentration is 65wt percent;
TABLE 3 analysis of main chemical elements of raw ore and
element(s) TFe P S SiO2 Al2O3
Content/% 44.28 0.85 0.077 22.54 5.73
TABLE 4 analysis results of the crude iron phases
Name of the photo Magnetic iron Iron carbonate Silicates of acid or alkali Sulfide compound Hematite and others Total up to
Iron content 4.56 1.26 7.73 ＜0.5 30.23 44.28
Occupancy/%) 10.30 2.85 17.46 ＜1.13 68.26 100
Step 2, mixing the ore grinding product obtained in the step 1 until the solid mass concentration is 30wt%, adding sodium carbonate to control the pH value of the ore pulp solution to be 10, stirring for 6min, then adding 1400g/t of sodium silicate, stirring for 8min, adding 300g/t of combined inhibitor, stirring for 15min, adding 300g/t of mixed collecting agent, stirring for 15min, performing roughing, and performing air-charging foam scraping for 8min to obtain roughing high-phosphorus foam and roughing underflow;
step 3, adding sodium carbonate into the underflow obtained after rough concentration in the step 2 to control the pH value of the ore pulp solution to be 9, stirring for 4min, adding 600g/t of sodium silicate and 200g/t of a combined inhibitor, stirring for 15min, mixing a collector MG150g/t, stirring for 15min, then scavenging, aerating and scraping for 8min to obtain scavenging high-phosphorus foam and first scavenging underflow;
step 4, adding sodium carbonate into the first scavenging underflow obtained in the step 3 to control the pH value of the ore pulp solution to be 9, stirring for 6min, adding 300g/t of sodium silicate, stirring for 8min, adding 100g/t of combined inhibitor, stirring for 15min, mixing the collecting agent MG100g/t, stirring for 15min, then performing secondary scavenging, and aerating and scraping for 3min to obtain secondary scavenging foam and products in the tank; combining the rough concentration high-phosphorus foam obtained in the step 2, the scavenging high-phosphorus foam obtained in the step 3 and the secondary scavenging foam obtained in the step 4 to obtain high-phosphorus foam, wherein the obtained in-tank product is the final iron ore material;
in the steps 2, 3 and 4, the combined inhibitor is a mixture of sodium lignosulfonate and 3, 4-dihydroxybenzylamine in a molar ratio of 5: 1; in the steps 2, 3 and 4, the mixed collecting agent MG is a mixture of oleamide and linolenic acid in a molar ratio of 5: 1.
The iron grade in the final iron mineral material is 47.17wt%, the phosphorus content is 0.24wt%, the iron recovery rate is 78.75%, and the dephosphorization rate is 79.12%.
Comparative example 2
Replacing the combined inhibitor and mixed collector MG of example 2 with a conventional starch inhibitor and a conventional oxidized paraffin soap collector; in the step 2, the adding amount of the conventional starch inhibitor is 800g/t, and the adding amount of the conventional oxidized paraffin soap collecting agent is 800 g/t; the adding amount of the conventional starch inhibitor in the step 3 is 400g/t, and the adding amount of the conventional oxidized paraffin soap collecting agent is 400 g/t; the adding amount of the conventional starch inhibitor in the step 4 is 200g/t, the adding amount of the conventional oxidized paraffin soap collecting agent is 200g/t, and other parameters are unchanged. In the final iron mineral material obtained in comparative example 2, the iron grade was 48.23wt%, the phosphorus content was 0.36wt%, the iron recovery rate was 75.18%, and the dephosphorization rate was 70.77%.
From this example 2 and comparative example 2, it can be seen that the combined inhibitor and mixed collector MG used in the present invention are less, the mixed collector MG added in the present invention can effectively remove the phosphorus-containing minerals, and the iron recovery rate and the dephosphorization rate are higher than those in comparative example 2. The production cost of the invention is reduced by 15 yuan per ton of raw ore.
Example 3
As shown in fig. 1, the beneficiation method for removing phosphorus from high-phosphorus limonite ore comprises the following specific steps:
step 1, crushing and grinding a high-phosphorus limonite raw material (the main chemical element analysis and iron phase analysis results of the raw material raw ore are respectively shown in tables 5 and 6) until the content of mineral aggregate with the particle size of-74 mu m accounts for 95 percent to obtain a ground ore product, wherein the ground ore mass concentration is 55 weight percent;
TABLE 5 analysis of main chemical elements of raw ore and
element(s) TFe P S SiO2 Al2O3
Content/% 48.63 1.02 0.09 18.54 4.23
TABLE 6 analysis results of the crude iron phases
Name of the photo Magnetic iron Iron carbonate Silicates of acid or alkali Sulfide compound Red brown iron and others TFe
Iron content 4.12 1.08 5.42 ＜0.5 37.51 48.63
Occupancy/%) 8.47 2.22 11.15 ＜1.03 77.13 100
Step 2, mixing the ore grinding product obtained in the step 1 until the solid mass concentration is 35wt%, adding sodium carbonate to control the pH value of an ore pulp solution to be 9, stirring for 8min, then adding 1000g/t of sodium silicate, stirring for 4min, adding 100g/t of a combined inhibitor, stirring for 5min, adding a mixed collector MG400g/t, stirring for 5min, performing roughing, and performing air-charging foam scraping for 4min to obtain roughing high-phosphorus foam and roughing underflow;
step 3, adding sodium carbonate into the underflow obtained after rough concentration in the step 2 to control the pH value of the ore pulp solution to be 10, stirring for 6min, adding 500g/t of sodium silicate and 150g/t of combined inhibitor, stirring for 5min, mixing with a collector MG200g/t, stirring for 5min, scavenging, aerating and scraping for 6min to obtain scavenging high-phosphorus foam and first scavenging underflow;
step 4, adding sodium carbonate into the first scavenging underflow obtained in the step 3 to control the pH value of the ore pulp solution to be 10, stirring for 8min, adding 200g/t of sodium silicate, stirring for 6min, adding 80g/t of a combined inhibitor, stirring for 10min, mixing a collecting agent MG80g/t, stirring for 10min, then carrying out secondary scavenging, and carrying out air inflation and foam scraping for 6min to obtain secondary scavenging foam and products in the tank; combining the rough concentration high-phosphorus foam obtained in the step 2, the scavenging high-phosphorus foam obtained in the step 3 and the secondary scavenging foam obtained in the step 4 to obtain high-phosphorus foam, wherein the obtained in-tank product is the final iron ore material;
in the steps 2, 3 and 4, the combined inhibitor is a mixture of sodium lignosulfonate and 3, 4-dihydroxybenzylamine in a molar ratio of 4: 1; in the steps 2, 3 and 4, the mixed collecting agent MG is a mixture of oleamide and linolenic acid in a molar ratio of 5: 1.
The iron grade in the final iron mineral material is 50.12wt%, the phosphorus content is 0.30wt%, the iron recovery rate is 80.45%, and the dephosphorization rate is 75.61%.
Comparative example 3
Replacing the combined inhibitor and mixed collector MG of example 3 with a conventional starch inhibitor and conventional tall oil; in the step 2, the adding amount of the conventional starch inhibitor is 800g/t, and the adding amount of the conventional tall oil collecting agent is 800 g/t; the adding amount of the conventional starch inhibitor in the step 3 is 400g/t, and the adding amount of the conventional tall oil collecting agent is 400 g/t; the adding amount of the conventional starch inhibitor in the step 4 is 200g/t, the adding amount of the conventional tall oil collector is 200g/t, and other parameters are unchanged. In the final iron mineral material obtained in comparative example 3, the iron grade was 49.52wt%, the phosphorus content was 0.40wt%, the iron recovery rate was 77.56%, and the dephosphorization rate was 70.13%.
From this example 3 and comparative example 3, it can be seen that the combined inhibitor and mixed collector MG used in the present invention are less, the mixed collector MG added in the present invention can effectively remove the phosphorus-containing minerals, and both the iron recovery rate and the dephosphorization rate are higher than those in comparative example 3. The production cost of the invention is reduced by 13 yuan/ton of raw ore.
While the present invention has been described in detail with reference to the embodiments shown in the drawings, the present invention is not limited to the embodiments, and various changes can be made without departing from the spirit and scope of the present invention.

Claims (1)

1. A beneficiation method for removing phosphorus from high-phosphorus hematite ore is characterized by comprising the following specific steps:
step 1, crushing and grinding a high-phosphorus limonite raw material until the content of mineral aggregate with the particle size of-74 mu m accounts for 75-95% to obtain a ground ore product, wherein the ground ore mass concentration is 55-65 wt%;
step 2, mixing the ore grinding product obtained in the step 1 until the solid mass concentration is 25-35 wt%, adding sodium carbonate to control the pH value of an ore pulp solution to be 8-10, stirring for 4-8 min, then adding sodium silicate 1000-1600 g/t, stirring for 4-8 min, adding a combined inhibitor 100-300 g/t, stirring for 5-15 min, adding a mixed collecting agent MG 200-400 g/t, stirring for 5-15 min, performing rough separation, and performing air-inflation foam scraping for 4-8 min to obtain rough-separated high-phosphorus foam and underflow after rough separation;
step 3, adding sodium carbonate into the roughly selected underflow obtained in the step 2 to control the pH value of the ore pulp solution to be 8-10, stirring for 3-6 min, adding 500-800 g/t of sodium silicate and 100-200 g/t of a combined inhibitor, stirring for 5-15 min, mixing 100-200 g/t of a collecting agent MG, stirring for 5-15 min, scavenging, and carrying out air-inflation foam scraping for 5-8 min to obtain scavenged high-phosphorus foam and first scavenging underflow;
step 4, adding sodium carbonate into the primary scavenging underflow obtained in the step 3 to control the pH value of the ore pulp solution to be 8-10, stirring for 4-8 min, adding 200-400 g/t of sodium silicate, stirring for 4-8 min, adding 50-100 g/t of combined inhibitor, stirring for 5-15 min, mixing collecting agent MG 50-100 g/t, stirring for 5-15 min, then performing secondary scavenging, and performing air-inflation foam scraping for 3-6 min to obtain secondary scavenging foam and products in the tank; combining the rough concentration high-phosphorus foam obtained in the step 2, the scavenging high-phosphorus foam obtained in the step 3 and the secondary scavenging foam obtained in the step 4 to obtain high-phosphorus foam, wherein the obtained in-tank product is the final iron ore material;
the combined inhibitor in the steps 2, 3 and 4 is a mixture of sodium lignosulfonate and 3, 4-dihydroxybenzylamine in a molar ratio of 3-5: 1; in the steps 2, 3 and 4, the mixed collecting agent MG is a mixture of oleamide and linolenic acid in a molar ratio of 5: 1.
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