CN105750089A - Magnesian collophanite separation method - Google Patents
Magnesian collophanite separation method Download PDFInfo
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- CN105750089A CN105750089A CN201610299996.XA CN201610299996A CN105750089A CN 105750089 A CN105750089 A CN 105750089A CN 201610299996 A CN201610299996 A CN 201610299996A CN 105750089 A CN105750089 A CN 105750089A
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- collophane
- ore
- collophanite
- magnesia
- concentrate
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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
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Abstract
The invention relates to a magnesian collophanite separation method. According to the technical scheme, the method comprises the following steps: crushing and finely grinding the magnesian collophanite until the content of grains with the granularity less than 0.074 mm is 40 to 95 weight percent, performing classification to obtain coarse-grained ore pulp and fine-grained ore pulp, and performing dehydration to obtain corresponding coarse-grained collophanite and fine-grained collophanite respectively; regulating the coarse-grained collophanite to be ore pulp, adding sodium dodecyl sulfate, and performing reverse rough flotation operation to obtain concentrates I and middlings; mixing the fine-grained collophanite and the middlings to obtain mixed ores, regulating the mixed ores to be ore pulp, sequentially adding a regulator and a fatty acid collector, and performing reverse fine flotation operation to obtain concentrates II and tailings; mixing the concentrates I and II to obtain a phosphate concentrate product. The method has the characteristics of high ore adaptability, low flotation agent consumption, low separation cost and less environmental pollution.
Description
Technical field
The invention belongs to collophane sorting technology field.It is specifically related to a kind of magnesia collophane method for separating.
Background technology
China's phosphate rock resource world rankings the 3rd, but grade is generally on the low side, and major part is mid-low grade collophanite ore, and objectionable impurities content is high, it is necessary to just can be used effectively after enrichment remove impurity.In mid-low grade collophanite ore, account for the overwhelming majority with the refractory cellophane that content of MgO is high again.At present, magnesia Collophanite de-magging is generally adopted floatation process, next to that chemical method and Roasting-slaking method.Current widely used method is reverse floatation process, the general inhibitor using mineral acid (sulphuric acid or phosphoric acid and derivant) thereof as slurry pH regulator and Phosphate minerals, with fatty-acid collector emersion dolomite in weak acidic medium, Phosphate minerals is enriched in groove.Though this technique is simple, carbonate separation efficiency is high and achieves normal temperature flotation, but still suffers from the problem that floating agent consumption is big, beneficiation cost is high and environmental pollution is serious.Therefore, magnesia collophane reverse floatation process is optimized it is significant.
It is reported, adopt sodium lauryl sulphate as the collecting agent of dolomite, be about 50wt% and P to containing dolomite2O5Grade is the Yichang phosphate rock of 19.25%, when being not added with other any medicament, through roughly selecting, selected and scan operation, it is possible to obtain P2O5Grade is 30.7% and phosphorus concentrate that the response rate is 82.86%.But this technique is difficult to sorting, and disseminated grain size is thin, the magnesia collophane of tight symbiosis, there is the problem that foam is tacky simultaneously.
The patented technology of " a kind of coarse grain reverse flotation de-magging method for phosphorus ore " (CN104801418A), by optimizing reverse flotation work and regime of agent, on high concentration pulping basis, adopt reverse flotation hybrid collector to reach the effect of coarse grain de-magging, reduce phosphorus concentrate content of magnesium.Though this technique can improve phosphorus concentrate quality, but is only applicable to process coarse grain phosphorus ore, Ore adaptability is not strong, and acid consumption is bigger.
The patented technology of " one sorts calcium collophanite post groove process integration " (CN102886306A), achieve new technology, commercial application that new equipment sorts in calcium collophanite, roughly select, selected operation realizes self-flowing pastefill, the purpose saved energy and reduce the cost can be reached, and be conducive to improving flotation effect.But, this technique can consume a large amount of phosphoric acid and sulphuric acid, and then causes that beneficiation cost rising and environmental pollution increase the weight of.
In sum, although existing reverse floatation process separating effect is better, but still suffer from the problem that Ore adaptability is not strong, floating agent consumption is big, beneficiation cost is high and environmental pollution is serious.
Summary of the invention
It is contemplated that overcome prior art defect, it is therefore intended that provide a kind of Ore strong adaptability, floating agent consumption is little, beneficiation cost is low and environmental pollution is little magnesia collophane method for separating.
For achieving the above object, the comprising the concrete steps that of the technical solution used in the present invention:
(1) magnesia collophane is crushed, it is finely ground to granularity for account for 40 ~ 95wt% less than 0.074mm, classification, obtain the granularity coarse fraction ore pulp more than 0.038mm and the granularity fine fraction ore pulp less than 0.038mm, dehydration respectively, obtains corresponding coarse fraction collophane and fine fraction collophane.
(2) described coarse fraction collophane being adjusted to the ore pulp that concentration is 25 ~ 40wt%, send into agitator tank I, then add sodium lauryl sulphate to agitator tank I, the addition of the sodium lauryl sulphate in coarse fraction collophane per ton is 0.1 ~ 1.5kg；Carrying out reverse flotation and roughly select operation, obtain product I and froth pulp I in groove, in groove, product I is concentrate I, is chats after froth pulp I dehydration.
(3) by described fine fraction collophane: the mass ratio of described chats is (2 ~ 8): 1 joins ore deposit, obtain composite ore, described composite ore is adjusted to the ore pulp that concentration is 20 ~ 35wt%, send into agitator tank II, be sequentially added into regulator and fatty-acid collector again to agitator tank II, regulator and the addition of fatty-acid collector in composite ore per ton are correspondingly 3 ~ 11kg and 0.3 ~ 1.5kg；Carrying out the selected operation of reverse flotation, obtain product II and froth pulp II in groove, in groove, product II is concentrate II, and froth pulp II is mine tailing.
(4) described concentrate I and described concentrate II are merged, obtain phosphorus concentrate product.
The P of described magnesia collophane2O5Grade is 20 ~ 30%, and MgO grade is 1 ~ 8%.
Described regulator is one or both in sulphuric acid and phosphoric acid.
Owing to adopting technique scheme, the present invention compared with prior art, has the positive effect that:
1, the present invention is applicable to P2O5The magnesia collophane that grade is 20 ~ 30%, MgO grade is 1 ~ 8%, Ore strong adaptability.
2, coarse fraction collophane is adopted sodium lauryl sulphate to make collecting agent reverse flotation and roughly select dolomite by the present invention, it is not necessary to add any regulator, has that reagent consumption is little and the obvious advantage of separating effect.
3, the present invention adopts graded operation and reverse flotation to roughly select operation, and energy Pre-sorting goes out the phosphorus concentrate of 30 ~ 70%, greatly reduces the treating capacity of the selected operation of follow-up reverse flotation, decreases the consumption of floating agent, reduces beneficiation cost and protect environment.
4, the phosphorus concentrate product P that the present invention obtains2O5Grade more than 30% and MgO grade less than 1%, P2O5The response rate is more than 80%.
Therefore, the feature that the present invention has Ore strong adaptability, floating agent consumption is little, beneficiation cost is low and environmental pollution is little.
Detailed description of the invention
In order to be more fully understood that the present invention, below in conjunction with embodiment, present disclosure is described further, but present disclosure is not limited solely to the following examples.All any simple modification made according to the flesh and blood of the present invention and equivalent structure transformation or modification, all should be encompassed within protection scope of the present invention.
Embodiment 1
A kind of magnesia collophane method for separating.The P of magnesia collophane described in the present embodiment2O5Grade is 20 ~ 25%, and MgO grade is 4 ~ 8%.Comprising the concrete steps that of described magnesia collophane method for separating:
(1) magnesia collophane is crushed, it is finely ground to granularity for account for 70 ~ 95wt% less than 0.074mm, classification, obtain the granularity coarse fraction ore pulp more than 0.038mm and the granularity fine fraction ore pulp less than 0.038mm, dehydration respectively, obtains corresponding coarse fraction collophane and fine fraction collophane.
(2) described coarse fraction collophane being adjusted to the ore pulp that concentration is 25 ~ 30wt%, send into agitator tank I, then add sodium lauryl sulphate to agitator tank I, the addition of the sodium lauryl sulphate in coarse fraction collophane per ton is 0.1 ~ 1.0kg；Carrying out reverse flotation and roughly select operation, obtain product I and froth pulp I in groove, in groove, product I is concentrate I, is chats after froth pulp I dehydration.
(3) by described fine fraction collophane: the mass ratio of described chats is (5 ~ 8): 1 joins ore deposit, obtain composite ore, described composite ore is adjusted to the ore pulp that concentration is 20 ~ 30wt%, send into agitator tank II, be sequentially added into regulator and fatty-acid collector again to agitator tank II, regulator and the addition of fatty-acid collector in composite ore per ton are correspondingly 7 ~ 11kg and 0.5 ~ 1.2kg；Carrying out the selected operation of reverse flotation, obtain product II and froth pulp II in groove, in groove, product II is concentrate II, and froth pulp II is mine tailing.
(4) described concentrate I and described concentrate II are merged, obtain phosphorus concentrate product.
Regulator described in the present embodiment is sulphuric acid.
The present embodiment adopts graded operation and reverse flotation to roughly select operation, and energy Pre-sorting goes out the phosphorus concentrate of 30 ~ 50%；The phosphorus concentrate product P obtained2O5Grade more than 30% and MgO grade less than 1%, P2O5The response rate is more than 80%.
Embodiment 2
A kind of magnesia collophane method for separating.The P of magnesia collophane described in the present embodiment2O5Grade is 25 ~ 30%, and MgO grade is 1 ~ 4%.Comprising the concrete steps that of described magnesia collophane method for separating:
(1) magnesia collophane is crushed, it is finely ground to granularity for account for 40 ~ 60wt% less than 0.074mm, classification, obtain the granularity coarse fraction ore pulp more than 0.038mm and the granularity fine fraction ore pulp less than 0.038mm, dehydration respectively, obtains corresponding coarse fraction collophane and fine fraction collophane.
(2) described coarse fraction collophane being adjusted to the ore pulp that concentration is 35 ~ 40wt%, send into agitator tank I, then add sodium lauryl sulphate to agitator tank I, the addition of the sodium lauryl sulphate in coarse fraction collophane per ton is 0.8 ~ 1.5kg；Carrying out reverse flotation and roughly select operation, obtain product I and froth pulp I in groove, in groove, product I is concentrate I, is chats after froth pulp I dehydration.
(3) by described fine fraction collophane: the mass ratio of described chats is (2 ~ 5): 1 joins ore deposit, obtain composite ore, described composite ore is adjusted to the ore pulp that concentration is 25 ~ 35wt%, send into agitator tank II, be sequentially added into regulator and fatty-acid collector again to agitator tank II, regulator and the addition of fatty-acid collector in composite ore per ton are correspondingly 3 ~ 6kg and 0.3 ~ 1.0kg；Carrying out the selected operation of reverse flotation, obtain product II and froth pulp II in groove, in groove, product II is concentrate II, and froth pulp II is mine tailing.
(4) described concentrate I and described concentrate II are merged, obtain phosphorus concentrate product.
Regulator described in the present embodiment is phosphoric acid.
The present embodiment adopts graded operation and reverse flotation to roughly select operation, and energy Pre-sorting goes out the phosphorus concentrate of 40 ~ 70%；The phosphorus concentrate product P obtained2O5Grade more than 30% and MgO grade less than 1%, P2O5The response rate is more than 92%.
Embodiment 3
A kind of magnesia collophane method for separating.The P of magnesia collophane described in the present embodiment2O5Grade is 22 ~ 28%, and MgO grade is 2 ~ 6%.Comprising the concrete steps that of described magnesia collophane method for separating:
(1) magnesia collophane is crushed, it is finely ground to granularity for account for 60 ~ 85wt% less than 0.074mm, classification, obtain the granularity coarse fraction ore pulp more than 0.038mm and the granularity fine fraction ore pulp less than 0.038mm, dehydration respectively, obtains corresponding coarse fraction collophane and fine fraction collophane.
(2) described coarse fraction collophane being adjusted to the ore pulp that concentration is 30 ~ 35wt%, send into agitator tank I, then add sodium lauryl sulphate to agitator tank I, the addition of the sodium lauryl sulphate in coarse fraction collophane per ton is 0.3 ~ 1.2kg；Carrying out reverse flotation and roughly select operation, obtain product I and froth pulp I in groove, in groove, product I is concentrate I, is chats after froth pulp I dehydration.
(3) by described fine fraction collophane: the mass ratio of described chats is (3 ~ 6): 1 joins ore deposit, obtain composite ore, described composite ore is adjusted to the ore pulp that concentration is 25 ~ 35wt%, send into agitator tank II, be sequentially added into regulator and fatty-acid collector again to agitator tank II, regulator and the addition of fatty-acid collector in composite ore per ton are correspondingly 4 ~ 8kg and 1.0 ~ 1.5kg；Carrying out the selected operation of reverse flotation, obtain product II and froth pulp II in groove, in groove, product II is concentrate II, and froth pulp II is mine tailing.
(4) described concentrate I and described concentrate II are merged, obtain phosphorus concentrate product.
Regulator described in the present embodiment is the mixture of sulphuric acid and phosphoric acid.
The present embodiment adopts graded operation and reverse flotation to roughly select operation, and energy Pre-sorting goes out the phosphorus concentrate of 30 ~ 60%；The phosphorus concentrate product P obtained2O5Grade more than 30% and MgO grade less than 1%, P2O5The response rate is more than 85%.
This detailed description of the invention compared with prior art, has the positive effect that:
1, this detailed description of the invention is applicable to P2O5The magnesia collophane that grade is 20 ~ 30%, MgO grade is 1 ~ 8%, Ore strong adaptability.
2, coarse fraction collophane is adopted sodium lauryl sulphate to make collecting agent reverse flotation and roughly select dolomite by this detailed description of the invention, it is not necessary to add any regulator, has that reagent consumption is little and the obvious advantage of separating effect.
3, this detailed description of the invention adopts graded operation and reverse flotation to roughly select operation, and energy Pre-sorting goes out the phosphorus concentrate of 30 ~ 70%, greatly reduces the treating capacity of the selected operation of follow-up reverse flotation, decreases the consumption of floating agent, reduces beneficiation cost and protect environment.
4, the phosphorus concentrate product P that this detailed description of the invention obtains2O5Grade more than 30% and MgO grade less than 1%, P2O5The response rate is more than 80%.
Therefore, the feature that this detailed description of the invention has Ore strong adaptability, floating agent consumption is little, beneficiation cost is low and environmental pollution is little.
Claims (3)
1. a magnesia collophane method for separating, it is characterised in that comprising the concrete steps that of described method:
(1) magnesia collophane is crushed, it is finely ground to granularity for account for 40～95wt% less than 0.074mm, classification, obtain the granularity coarse fraction ore pulp more than 0.038mm and the granularity fine fraction ore pulp less than 0.038mm, dehydration respectively, obtains corresponding coarse fraction collophane and fine fraction collophane；
(2) described coarse fraction collophane being adjusted to the ore pulp that concentration is 25～40wt%, send into agitator tank I, then add sodium lauryl sulphate to agitator tank I, the addition of the sodium lauryl sulphate in coarse fraction collophane per ton is 0.1～1.5kg；Carrying out reverse flotation and roughly select operation, obtain product I and froth pulp I in groove, in groove, product I is concentrate I, is chats after froth pulp I dehydration；
(3) by described fine fraction collophane: the mass ratio of described chats is (2～8): 1 joins ore deposit, obtain composite ore, described composite ore is adjusted to the ore pulp that concentration is 20～35wt%, send into agitator tank II, be sequentially added into regulator and fatty-acid collector again to agitator tank II, regulator and the addition of fatty-acid collector in composite ore per ton are correspondingly 3～11kg and 0.3～1.5kg；Carrying out the selected operation of reverse flotation, obtain product II and froth pulp II in groove, in groove, product II is concentrate II, and froth pulp II is mine tailing；
(4) described concentrate I and described concentrate II are merged, obtain phosphorus concentrate product.
2. magnesia collophane method for separating according to claim 1, it is characterised in that the P of described magnesia collophane2O5Grade is 20～30%, and MgO grade is 1～8%.
3. magnesia collophane method for separating according to claim 1, it is characterised in that described regulator is one or both in sulphuric acid and phosphoric acid.
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Cited By (5)
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|---|---|---|---|---|
| CN107309075A (en) * | 2017-08-08 | 2017-11-03 | 贵州川恒化工股份有限公司 | Collophane beneficiation method |
| CN112517232A (en) * | 2020-11-18 | 2021-03-19 | 云南磷化集团有限公司 | Flotation method for low-grade collophanite with compact block structure |
| CN112619903A (en) * | 2020-11-10 | 2021-04-09 | 西北矿冶研究院 | Beneficiation method for high-mud high-zinc oxide ore |
| CN113019683A (en) * | 2021-03-11 | 2021-06-25 | 云南磷化集团有限公司 | Treatment method of mixed low-grade collophanite |
| WO2021179862A1 (en) * | 2020-03-10 | 2021-09-16 | 中国地质科学院矿产综合利用研究所 | Mineral separation process for medium-low grade mixed collophanite |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107309075A (en) * | 2017-08-08 | 2017-11-03 | 贵州川恒化工股份有限公司 | Collophane beneficiation method |
| WO2021179862A1 (en) * | 2020-03-10 | 2021-09-16 | 中国地质科学院矿产综合利用研究所 | Mineral separation process for medium-low grade mixed collophanite |
| CN112619903A (en) * | 2020-11-10 | 2021-04-09 | 西北矿冶研究院 | Beneficiation method for high-mud high-zinc oxide ore |
| CN112517232A (en) * | 2020-11-18 | 2021-03-19 | 云南磷化集团有限公司 | Flotation method for low-grade collophanite with compact block structure |
| CN112517232B (en) * | 2020-11-18 | 2022-07-29 | 云南磷化集团有限公司 | Flotation method for low-grade collophanite with compact block structure |
| CN113019683A (en) * | 2021-03-11 | 2021-06-25 | 云南磷化集团有限公司 | Treatment method of mixed low-grade collophanite |
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