CN101099946A - Collophanite floatation method - Google Patents
Collophanite floatation method Download PDFInfo
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- CN101099946A CN101099946A CNA2007100660336A CN200710066033A CN101099946A CN 101099946 A CN101099946 A CN 101099946A CN A2007100660336 A CNA2007100660336 A CN A2007100660336A CN 200710066033 A CN200710066033 A CN 200710066033A CN 101099946 A CN101099946 A CN 101099946A
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Abstract
The present invention discloses one kind of cellophane floating process, which has floatation columns applied for eliminate impurity and includes direct floatation to eliminate silicon and reverse floatation to eliminate magnesium. The cellophane floating process includes crushing crude cellophane, milling and grading to form 20-40 wt% concentration pulp; mixing the pulp with direct floatation reagent, and floatation in direct floatation columns to obtain foamed rough concentrate in the top and direct floated tailings in the bottom; mixing the foamed rough concentrate with reverse floatation reagent in one other mineralizing tank, and floatation in reverse floatation columns to obtain cellophane concentrate in the bottom and foamed reverse floated tailings. The process is simple and stable, and has easy control, high depurating effect, high concentrate quality, less phosphate loss and other advantages.
Description
Technical field
The invention relates to the beneficiation method of phosphorus ore, more particularly, the present invention relates to a kind of method for floating of collophane.
Background technology
The phosphorus ore thing is an important chemical material, along with the social technology expanding economy, the demand of rock phosphate in powder is constantly increased, and the reserves of easily adopting rich ore and Yi Xuan phosphorus ore reduces day by day.Therefore, how the phosphorus ore to poor and difficult choosing is economic effectively again enrichment, has caused the common concern of world's phosphorus ore circle.Particularly the technique of preparing of the calcareous type mid low grade phosphate rock of depositing silicon that reserves are big, the ore dressing difficulty is big is more attracted attention.Deposition phosphorite ore deposit (wherein phosphorus ore containing is mainly collophane) is a topmost rock phosphate in powder in world's phosphate rock resource, accounts for more than 70% of world's phosphorus ore gross reserves, wherein the reserves maximum the most difficult choosing be in low-grade silico-calcium matter collophane.In the ore dressing process of this class rock phosphate in powder, expelling carbonate and silicate impurity could satisfy the requirement of phosphate fertilizer processing simultaneously.
At present the most employing floatation of sorting of this rock phosphate in powder is carried out enrichment both at home and abroad, conventional method for floating has: positive reverse flotation, flotation and two reverse flotations etc. anyway, every kind of technology all has the advantage of self, also there is significantly deficiency simultaneously, mainly selects floatation process for use according to mineralogical character and mineral processing index.The floatation equipment that uses is mainly conventional groove type floatation cell, the adjusting aspect of this class floatation equipment low whipping speed and aeration quantity, mainly rule of thumb regulate, be unfavorable for the popularization of floatation process, and making formed production technology separating effect poor, concentration ratio is low, technological process complexity, reagent consumption height, production cost is higher, and the phosphate rock resource that has limited China's abundant effectively utilizes.
* the applicant once proposed a kind of from rock phosphate in powder, remove the magnesium addition method (application number: 200710065792.0, the applying date: 2007-4-9).This method can satisfy the de-magging requirement of collophane.Use the method, just can satisfy the index request of Wet-process Phosphoric Acid Production behind the middle grade high-magnesium-phosphorus ore de-magging phosphorus ore.But, only remove the magnesia impurity in the raw ore, the requirement that phosphorus concentrate index does not still reach Wet-process Phosphoric Acid Production for silicone content height, middle grade or low-grade collophane that content of magnesium is low.In order to reach Wet-process Phosphoric Acid Production ore deposit index, not only to remove the magnesia impurity in the phosphorus ore, also want desiliconization to improve the phosphorus ore grade.New method---the positive reverse floatation process of collophane post of Collophanite flotation is proposed for this reason.
Summary of the invention
The objective of the invention is provides a kind of good separation effect at the deficiencies in the prior art part, the concentration ratio height, and technology is reasonable, the method for floating of the collophane that reagent consumption is low.
Purpose of the present invention is achieved by the following technical programs.
* except as otherwise noted, percentage of the present invention is percetage by weight.
The invention provides a kind of method for floating of collophane, this method adopts following steps:
(1) selecting microbubble floatation column is floatation separator;
(2) with the collophane raw ore through broken, ore grinding and classification, mog be-200 orders 〉=80%, makes the mineral composition monomer dissociation, controlling pulp density is 25%～45%;
(3) ore pulp of step (2) is introduced in the mineralising groove, and the conventional direct flotation medicament of adding fully mixes with ore pulp;
(4) gains of step (3) are introduced in the described microbubble floatation column of step (1), carried out the direct-flotation desiliconisation operation;
(5) ore pulp enters flotation column through being positioned at the one or more of flotation column shaft middle and upper part branch to the ore deposit point, and the rising group of the tiny bubble that produces along gas foaming device system is descending, the phosphatic particle that bumps with bubble or adhere to will rise to the top of flotation column, final arrive the interface between ore pulp collecting district and the foam clear area, ore deposit and discharge outside the post, promptly obtain rough concentrate;
(6) particle that drops to flotation column bottom is siliceous mine tailing, is sent to the mine tailing storehouse after discharging flotation column;
(7) the rough concentrate slurry that step (5) is obtained is introduced in another mineralising groove, and the conventional reverse floatation agent of adding fully mixes with ore pulp;
(8) gains of step (7) are introduced in the described microbubble floatation column, carried out the operation of reverse flotation de-magging;
(9) ore pulp is same enters flotation column through being positioned at the one or more of flotation column shaft middle and upper part branch to the ore deposit point, and the rising group of the tiny bubble that produces along gas foaming device system is descending, the particle that contains magnesium that bumps with bubble or adhere to will rise to the top of flotation column, final arrive the interface between ore pulp collecting district and the foam clear area, ore deposit and discharge outside the post, thereby reach the effect of demagging;
(10) particle that drops to flotation column bottom is the phosphorus concentrate, discharges post after concentrate, filter and promptly obtain finished product phosphorus concentrate pulp, as phosphoric acid by wet process and the multiple fertile raw materials for production of phosphorus.
Wherein, P in the described phosphorus ore raw ore
2O
5Grade is 18%～30%, and MgO content is 2%～8%; Described flotation column is a static microbubble floatation column.
The rock phosphate in powder of treated mistake, P
2O
5Grade can improve 3%～10%, and MgO content is 0.5%～1.5%, and phosphorous recovery is 80%～95%.
Selected material is identical with the selected material of conventional flotation in the floatation process of the present invention, and the medicament kind that is adopted is identical with the medicament of conventional floatation process; Flotation collector is selected from a kind of in oxidation paraffin wax soap commonly used, tall oil, aliphatic acid, the soap class or derivatives thereof or their mixture; Adjust agent and be selected from a kind of in sodium carbonate, NaOH, polyphosphate, waterglass, small organic molecule, sulfuric acid or the phosphoric acid or their mixture.
Compared with prior art, the present invention has following beneficial effect:
1. the present invention breaks through traditional method for floating, and to the creative direct-flotation desiliconisation that adopts of collophane, reverse flotation removes the technological process of magnesium addition, forms a kind of brand-new Collophanite flotation method thus.
2. adopting static microbubble floatation column to compare with traditional flotation device has the following advantages: 1. device structure is simple, and disposal ability is big, and floor space is little, and the output investment ratio flotation device is saved more than 20%; 2. installed capacity is little, energy consumption is low, and is easy and simple to handle, and vulnerable part is few, and dosing is economized, and production cost is low, and operating cost can reduce by 30%～50%; 3. flotation efficiency height, operation number of times and circulation ore deposit amount are few, and process simplification is easily realized automation.A pillar detached job can replace 3～5 subjobs of flotation device; 4. have the incomparable selected district of flotation device, the concentration ratio height is adapted to handle the big floatation process of flotation froth amount.
3. flotation column has ore deposit foam purging system.The ore deposit foam cleans the useless mineral that can further remove on the foam of flotation ore deposit.The wash water that adds from the flotation column top filters through ore deposit foam district, the particle of sneaking between the flushable foam.Different with floatation equipment commonly used, flotation column does not adopt mechanical agitation, operation movement-less part.Superseded high degree of agitation can improve selectivity, and helps to reclaim thick particle.The outer charger of post can be regulated aeration quantity arbitrarily, and is easy and simple to handle.
4. the present invention is applied to positive reverse flotation silica removal of phosphorus ore and magnesium with static microbubble floatation column.Because a column-type floatation detached job can replace repeatedly conventional flotation operation.With conventional floatation process ratio, reagent consumption can reduce by 10%～20%, and the water consumption can reduce by 20%～40%, power consumption can reduce by 30%～50%, can make full use of the phosphate rock resource of China's abundant, reduces the flotation production cost, improve the business economic benefit, have the excellent development application prospect.
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
The specific embodiment
, the present invention is described in further detail, but they are not the qualification to protection domain of the present invention with the test example and by specific embodiment below in conjunction with accompanying drawing.
Test example 1
The selection microbubble floatation column is a floatation separator; Through fragmentation, ore grinding and classification, mog is-200 orders 〉=80% with the collophane raw ore, and mineral composition reaches monomer dissociation, and the control pulp density is 32%.Ore pulp is introduced in the mineralising groove, added conventional direct flotation medicament and fully mix with ore pulp; Gains are introduced in the described microbubble floatation column, carried out the direct-flotation desiliconisation operation; Ore pulp enters flotation column through being positioned at the one or more of flotation column shaft middle and upper part branch to the ore deposit point, and the rising group of the tiny bubble that produces along gas foaming device system is descending, the phosphatic particle that bumps with bubble or adhere to will rise to the top of flotation column, final arrive the interface between ore pulp collecting district and the foam clear area, ore deposit and discharge outside the post, promptly obtain rough concentrate; The particle that drops to the flotation column bottom is siliceous mine tailing, is sent to the mine tailing storehouse behind the discharge flotation column; The rough concentrate slurry that obtains is introduced in another mineralising groove, and introduces in the described microbubble floatation column after adding conventional reverse floatation agent and ore pulp fully mixing, and carries out the operation of reverse flotation de-magging; Ore pulp is same to enter flotation column through being positioned at the one or more of flotation column shaft middle and upper part branch to the ore deposit point, and the rising group of the tiny bubble that produces along gas foaming device system is descending, the particle that contains magnesium that bumps with bubble or adhere to will rise to the top of flotation column, final arrive the interface between ore pulp collecting district and the foam clear area, ore deposit and discharge outside the post, thereby reach the effect of demagging.The particle that drops to flotation column bottom is the phosphorus concentrate, discharges post after concentrate, filter and promptly obtain finished product phosphorus concentrate pulp, as phosphoric acid by wet process and the multiple fertile raw materials for production of phosphorus.
Wherein, P in the described phosphorus ore raw ore
2O
5Grade is 22.3%, and MgO content is 2.42%; Described flotation column is a static microbubble floatation column.The rock phosphate in powder of treated mistake, P
2O
5Grade has improved 7.96%, and MgO content is 0.57%, and phosphorous recovery is 89.5 6%.
Test example 2
Repeated test example 1 has following difference: the control pulp density is 30%, P in the described phosphorus ore raw ore
2O
5Grade is 23.01%, and MgO content is 5.12%; The rock phosphate in powder of treated mistake, P
2O
5Grade can improve 8.63%, and MgO content is 0.75%, and phosphorous recovery is 90.75%.
Test example 3
Repeated test example 1 has following difference: the control pulp density is 31%, P in the described phosphorus ore raw ore
2O
5Grade is 21.76%, and MgO content is 4.08%; The rock phosphate in powder of treated mistake, P
2O
5Grade can improve 9.2%, and MgO content is 0.76%, and phosphorous recovery is 88.09%.
Test example 4
Repeated test example 1 has following difference: the control pulp density is 28%, P in the described phosphorus ore raw ore
2O
5Grade is 23.64%, and MgO content is 4.35%; The rock phosphate in powder of treated mistake, P
2O
5Grade can improve 8.17%, and MgO content is 0.74%, and phosphorous recovery is 91.16%.
Embodiment 1
Mining area, Anning sample ore, raw ore P
2O
5Grade 22.30%, MgO content 2.42%.Flow process adopts positive reverse floatation process: mog is-200 orders 94%, and ore milling concentration 32%, flotation temperature are normal temperature.Direct flotation dosing: waterglass 7.0kg/t, collecting agent 3.0kg/t.The direct flotation froth pulp enters the reverse flotation system.Reverse floatation agent consumption: sulfuric acid 7.0kg/t, collecting agent 0.4kg/t.Phosphorus concentrate P behind the reverse flotation
2O
5Grade 29.47%, MgO content 0.68%, P
2O
5The rate of recovery reaches 84.58%, and the MgO elimination factor reaches 82.02%.
Embodiment 2
Mining area, Kunyang, Yunnan sample ore, raw ore P
2O
5Grade 23.01%, MgO content 5.12%.Flow process adopts positive reverse floatation process: mog is-200 orders 90%, and ore milling concentration 30%, flotation temperature are normal temperature, the direct flotation dosing: waterglass 6.0kg/t, collecting agent 3.0kg/t.The direct flotation froth pulp enters the reverse flotation system, the reverse floatation agent consumption: sulfuric acid 7.0kg/t, collecting agent 0.4kg/t.Its P
2O
5Grade 30.22%, MgO content 0.96%, P
2O
5The rate of recovery reaches 86.6 8%, MgO elimination factors 87.6 3%.
Embodiment 3
Mining area, Dongchuan, Yunnan sample ore, raw ore P
2O
5Grade 21.76%, MgO content 4.08%.Flow process adopts positive reverse floatation process: mog is-200 orders 93%, and ore milling concentration 31%, flotation temperature are normal temperature, the direct flotation dosing: waterglass 8.0kg/t, collecting agent 3.2kg//t.The direct flotation foam enters the reverse flotation system, the reverse floatation agent consumption: sulfuric acid 8.0kg/t, collecting agent 0.6kg/t gets phosphorus concentrate, its P behind the reverse flotation
2O
5Grade 29.84%, MgO content 0.89%, P
2O
5The rate of recovery reaches 85.02%, MgO elimination factor 86.48%.
Embodiment 4
Sample ore is with embodiment 3, i.e. raw ore P
2O
5Grade 22.8 3%, MgO content 3.91%.Flow process adopts positive reverse floatation process: mog is-200 orders 92%, and ore milling concentration 30%, flotation temperature are normal temperature, the direct flotation dosing: waterglass 7.0kg/t, collecting agent 2.8kg/t.The direct flotation foam enters the reverse flotation system, the reverse floatation agent consumption: nitration mixture 7.0kg/t, collecting agent 0.4kg/t gets phosphorus concentrate, its P behind the reverse flotation
2O
5Grade 31.14%, MgO content 0.77%, P
2O
5The rate of recovery reaches 90.02%, MgO elimination factor 87.0%.
Embodiment 5
Mining area, Yunnan sample ore, raw ore P
2O
5Grade 23.64%, MgO content 4.35%.Flow process adopts positive and negative technology: mog is-200 orders 90%, and ore milling concentration 28%, flotation temperature are normal temperature, the direct flotation dosing: waterglass 6.0kg/t, collecting agent 2.8kg/t.The direct flotation foam enters the reverse flotation system, the reverse floatation agent consumption: sulfuric acid 7.0kg/t, collecting agent 0.5kg/t gets phosphorus concentrate, its P behind the reverse flotation
2O
5Grade 30.83%, MgO content 0.89%, P
2O
5The rate of recovery reaches 87.38%, MgO elimination factor 86.29%.
Embodiment 6
Mining area, Haikou, Yunnan sample ore, raw ore P
2O
5Grade 20.16%, MgO content 3.18%. flow process adopts positive reverse floatation process: mog is-200 orders 95%, ore milling concentration 33%, flotation temperature are normal temperature, the direct flotation dosing: waterglass 9.0kg/t, collecting agent 3.5kg/t.The direct flotation foam enters the reverse flotation system, the reverse floatation agent consumption: nitration mixture 9.0kg/t, collecting agent 0.7kg/t gets phosphorus concentrate, its P behind the reverse flotation
2O
5Grade 29.82%, MgO content 0.65%, P
2O
5The rate of recovery reaches 86.75%, MgO elimination factor 87.74%.
Claims (4)
1. the method for floating of a collophane is characterized in that this method adopts following steps:
(1) selecting microbubble floatation column is floatation separator;
(2) with the collophane raw ore through broken, ore grinding and classification, mog be-200 orders 〉=80%, makes the mineral composition monomer dissociation, controlling pulp density is 25%～45%;
(3) ore pulp of step (2) is introduced in the mineralising groove, and the conventional direct flotation medicament of adding fully mixes with ore pulp;
(4) gains of step (3) are introduced in the described microbubble floatation column of step (1), carried out the direct-flotation desiliconisation operation;
(5) ore pulp enters flotation column through being positioned at the one or more of flotation column shaft middle and upper part branch to the ore deposit point, and the rising group of the tiny bubble that produces along gas foaming device system is descending, the phosphatic particle that bumps with bubble or adhere to will rise to the top of flotation column, final arrive the interface between ore pulp collecting district and the foam clear area, ore deposit and discharge outside the post, promptly obtain rough concentrate;
(6) particle that drops to flotation column bottom is siliceous mine tailing, is sent to the mine tailing storehouse after discharging flotation column;
(7) the rough concentrate slurry that step (5) is obtained is introduced in another mineralising groove, and the conventional reverse floatation agent of adding fully mixes with ore pulp;
(8) gains of step (7) are introduced in the described microbubble floatation column, carried out the operation of reverse flotation de-magging;
(9) ore pulp is same enters flotation column through being positioned at the one or more of flotation column shaft middle and upper part branch to the ore deposit point, and the rising group of the tiny bubble that produces along gas foaming device system is descending, the particle that contains magnesium that bumps with bubble or adhere to will rise to the top of flotation column, final arrive the interface between ore pulp collecting district and the foam clear area, ore deposit and discharge outside the post, thereby reach the effect of demagging;
(10) particle that drops to flotation column bottom is the phosphorus concentrate, discharges flotation column after concentrate, filter, be drying to obtain required finished product.
2. the method for floating of collophane according to claim 1 is characterized in that consisting of of phosphorus ore ore: P
2O
5Grade 18～30%, MgO content are 2～8%; The rock phosphate in powder of treated mistake, P
2O
5Grade improves 3%～10%, and MgO content is 0.5%～1.5%, and phosphorous recovery is 80%～95%.
3. the method for floating of collophane according to claim 1 is characterized in that described flotation column is a static microbubble floatation column, and aeration quantity is regulated as required easily in the floatation process.
4. the method for floating of collophane according to claim 1 is characterized in that the medicament kind that is adopted is identical with the medicament of conventional floatation process, and promptly the direct-flotation desiliconisation inhibitor is a waterglass; Reverse flotation de-magging inhibitor is sulfuric acid or phosphoric acid, or both mixtures; Collecting agent is selected from a kind of in oxidation paraffin wax soap, tall oil, aliphatic acid and soap class or the derivative or their mixture.
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| CNA2007100660336A CN101099946A (en) | 2007-07-13 | 2007-07-13 | Collophanite floatation method |
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|---|---|---|---|
| CNA2007100660336A CN101099946A (en) | 2007-07-13 | 2007-07-13 | Collophanite floatation method |
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| CN101362118B (en) * | 2008-09-17 | 2012-01-11 | 中南大学 | Flotation column pulp quadric mineralising method |
| CN102319634A (en) * | 2011-10-12 | 2012-01-18 | 湖南省矿产测试利用研究所 | Process for recovering fuel from collophanite |
| CN102327809A (en) * | 2011-10-12 | 2012-01-25 | 湖南省矿产测试利用研究所 | Method for removing magnesium oxide from collophanite |
| CN102698873A (en) * | 2011-11-28 | 2012-10-03 | 云南磷化集团有限公司 | Beneficiation method for desorbing silicate impurities in collophanite through direct flotation |
| CN102744160A (en) * | 2012-07-24 | 2012-10-24 | 中蓝连海设计研究院 | Iso-floatable separation process of siliceous-calcareous collophanite |
| CN102744151A (en) * | 2012-07-06 | 2012-10-24 | 中蓝连海设计研究院 | Branch flotation technology for silicon calcium collophanite |
| CN101670317B (en) * | 2009-09-24 | 2012-10-31 | 昆明理工大学 | Combined flotation regulator of mineral phosphate containing siliceous gangue |
| CN102764699A (en) * | 2012-07-23 | 2012-11-07 | 贵州洋浦恒立化工有限公司 | Cellophane beneficiating method |
| CN102886306A (en) * | 2012-07-18 | 2013-01-23 | 云南磷化集团有限公司 | Column-slot combined technology for grading calcium collophanite |
| CN103817012A (en) * | 2013-12-26 | 2014-05-28 | 武汉工程大学 | Pulp pH combined regulator for phosphorite flotation process |
| CN103819016A (en) * | 2013-12-31 | 2014-05-28 | 云南磷化集团有限公司 | Method for treating backwater from mixed production process of collophanite |
| CN103909017A (en) * | 2014-04-18 | 2014-07-09 | 武汉工程大学 | Flotation process for silicon-calcium mixed collophanite containing organic carbon |
| CN103950908A (en) * | 2014-04-04 | 2014-07-30 | 贵阳中化开磷化肥有限公司 | Method for fluidization removal of magnesium from phosphate ore |
| CN104043534A (en) * | 2014-03-15 | 2014-09-17 | 云南磷化集团有限公司 | Novel efficient collophanite reverse flotation collecting agent |
| CN104174504A (en) * | 2014-07-16 | 2014-12-03 | 云南磷化集团有限公司 | Direct-flotation branching floatation method of low-and-medium-grade mixed type refractory collophane |
| CN104841569A (en) * | 2015-06-12 | 2015-08-19 | 中蓝连海设计研究院 | Flotation technology of middle-low-grade silica-calcia bearing phosphate rock |
| CN104959212A (en) * | 2015-07-07 | 2015-10-07 | 湖南有色金属研究院 | Classified ore dressing method of calcareous and siliceous mixed type stone coal vanadium ore |
| CN105597939A (en) * | 2015-12-25 | 2016-05-25 | 湘西自治州鑫汇金属新材料有限公司 | Process for mineral processing of low-grade silicon calcium collophanite |
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| CN106423584A (en) * | 2016-12-21 | 2017-02-22 | 中蓝连海设计研究院 | Direct-reverse collophanite flotation process respectively recycling flotation process water |
| CN107967379A (en) * | 2017-11-08 | 2018-04-27 | 云南磷化集团有限公司 | Computational methods are amplified in Collophanite flotation engineering design |
| CN111451001A (en) * | 2020-03-10 | 2020-07-28 | 中国地质科学院矿产综合利用研究所 | Medium-low grade mixed collophanite flotation separation reagent system and application thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101362118B (en) * | 2008-09-17 | 2012-01-11 | 中南大学 | Flotation column pulp quadric mineralising method |
| CN101670317B (en) * | 2009-09-24 | 2012-10-31 | 昆明理工大学 | Combined flotation regulator of mineral phosphate containing siliceous gangue |
| CN102319634A (en) * | 2011-10-12 | 2012-01-18 | 湖南省矿产测试利用研究所 | Process for recovering fuel from collophanite |
| CN102327809A (en) * | 2011-10-12 | 2012-01-25 | 湖南省矿产测试利用研究所 | Method for removing magnesium oxide from collophanite |
| CN102327809B (en) * | 2011-10-12 | 2013-05-01 | 湖南省矿产测试利用研究所 | Method for removing magnesium oxide from collophanite |
| CN102698873A (en) * | 2011-11-28 | 2012-10-03 | 云南磷化集团有限公司 | Beneficiation method for desorbing silicate impurities in collophanite through direct flotation |
| CN102744151A (en) * | 2012-07-06 | 2012-10-24 | 中蓝连海设计研究院 | Branch flotation technology for silicon calcium collophanite |
| CN102744151B (en) * | 2012-07-06 | 2013-09-04 | 中蓝连海设计研究院 | Branch flotation technology for silicon calcium collophanite |
| CN102886306B (en) * | 2012-07-18 | 2015-07-15 | 云南磷化集团有限公司 | Column-slot combined technology for grading calcium collophanite |
| CN102886306A (en) * | 2012-07-18 | 2013-01-23 | 云南磷化集团有限公司 | Column-slot combined technology for grading calcium collophanite |
| CN102764699A (en) * | 2012-07-23 | 2012-11-07 | 贵州洋浦恒立化工有限公司 | Cellophane beneficiating method |
| CN102744160A (en) * | 2012-07-24 | 2012-10-24 | 中蓝连海设计研究院 | Iso-floatable separation process of siliceous-calcareous collophanite |
| CN102744160B (en) * | 2012-07-24 | 2013-09-04 | 中蓝连海设计研究院 | Iso-floatable separation process of siliceous-calcareous collophanite |
| CN103817012A (en) * | 2013-12-26 | 2014-05-28 | 武汉工程大学 | Pulp pH combined regulator for phosphorite flotation process |
| CN103819016A (en) * | 2013-12-31 | 2014-05-28 | 云南磷化集团有限公司 | Method for treating backwater from mixed production process of collophanite |
| CN103819016B (en) * | 2013-12-31 | 2015-11-18 | 云南磷化集团有限公司 | A kind of collophanite mixture manufacturing technique backwater treatment process |
| CN104043534A (en) * | 2014-03-15 | 2014-09-17 | 云南磷化集团有限公司 | Novel efficient collophanite reverse flotation collecting agent |
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| CN103950908B (en) * | 2014-04-04 | 2016-07-06 | 贵州开磷集团股份有限公司 | A kind of method of rock phosphate in powder fluidization de-magging |
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