CN104826741A - Flotation and backwater method aiming at collophanite double-back flotation process - Google Patents
Flotation and backwater method aiming at collophanite double-back flotation process Download PDFInfo
- Publication number
- CN104826741A CN104826741A CN201510234815.0A CN201510234815A CN104826741A CN 104826741 A CN104826741 A CN 104826741A CN 201510234815 A CN201510234815 A CN 201510234815A CN 104826741 A CN104826741 A CN 104826741A
- Authority
- CN
- China
- Prior art keywords
- magging
- desiliconization
- backwater
- flotation
- roughly
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Abstract
A method adopting separate backwater in a double-back flotation process aiming at collophanite comprises ore grinding operation; de-magging roughing operation; de-magging roughing foam recleaning operation; product fine selection operation in a de-magging roughing slot; returning of filtrate back to a de-magging backwater pool after filtering of a product in a de-magging fine selection slot; returning of overflow of the de-magging operation and the filtrate back to the de-magging backwater pool; feeding of a filter cake of the de-magging concentrate and replenished water, which are mixed, into a surge tank A, overflowing of the surge tank A to a surge tank B, feeding of the surge tank B for reverse flotation desiliconization roughing operation, wherein the replenished water is selected from backwater in a desiliconization backwater pool; reverse flotation desiliconization roughing operation; foam recleaning operation of the desiliconization operation; returning of the product in a desiliconization recleaning operation slot back to the desiliconization roughing operation, and returning of backwater back to the desiliconization backwater pool after dehydration of a foam product. Separate backwater is adopted, the influence of the backwater on the reverse flotation de-magging operation and the reverse flotation desiliconization operation is effectively avoided, stable operation of a double-reverse flotation process in actual production is facilitated, efficiency is improved and drug usage is reduced.
Description
Technical field
The invention belongs to technical field of mineral processing, particularly a kind of method for adopting independent backwater in collophane bi-anti-symmetric matrix technique.
Background technology
China's phosphate rock resource is very abundant, and resource base reserves occupy the second in the world, but major part is middle-low grade calcium siliceous phosphorite, and this kind of ore must deviate from carbonate gangue and silicate gangue simultaneously, could meet the requirement of phosphorus ore following process.Current high-grade phosphorus ore is fewer and feweri, and how rational exploitation and utilization mid low grade phosphate rock has become the important problem that we face.At present for low-grade calcium-silicon phosphate rock, mainly contain direct reverse floatation process, direct-reverse flotation technique, trans-direct floatation process, these three kinds of floatation process of bi-anti-symmetric matrix technique, there is the higher problem of concentrate silicon content in direct flotation technique, and there is raw ore mog compared with the defect thin, sodium carbonate amount is large, collector dosage is many in direct-reverse flotation technique and trans-direct floatation process, and bi-anti-symmetric matrix technique just in time meets the flotation principle of " floating few easily many ", have dosing low, concentrate is easy to the advantages such as dehydration.
The backwater of bi-anti-symmetric matrix technique traditional is at present the mixing backwater of de-magging operation and desiliconization operation, the pH value of mixing backwater is faintly acid, existing anionic polar group in backwater, also cationic polar group is had, when carrying out the flotation of reverse flotation de-magging, the cation group of enrichment in backwater can bring adverse influence to de-magging operation, causes de-magging deleterious; When carrying out Counterfloatating desiliconization operation, anionic group residual in backwater can cause tailings grade higher, in addition, cation-collecting agent is generally when neutrality or alkalescent, collecting ability is the strongest, and the pH value due to backwater is faintly acid, needs to add adjusting agent, pH values of pulp is adjusted to neutral or alkalescent, causes beneficiation cost to raise.
Summary of the invention
Technical problem to be solved by this invention is for the deficiencies in the prior art, provide a kind of new method design rationally, improve yield, the flotation for collophane bi-anti-symmetric matrix technique of saving floating agent and water return method.
Technical problem to be solved by this invention is realized by following technical scheme.The present invention is a kind of method for adopting independent backwater in collophane bi-anti-symmetric matrix technique, is characterized in, comprises the steps:
(1) phosphorite is milled to the mog that flotation operation needs;
(2) ore pulp of milled adds inhibitor acid, anionic collector carries out de-magging and roughly select operation;
(3) de-magging is roughly selected foam and is added inhibitor acid and carry out de-magging and roughly select operation and be elected to be industry more at least one times;
(4) in de-magging initial separatory cell, product adds inhibitor acid, anionic collector carries out primary cleaning operation;
(5) foam of the selected operation of de-magging converge with product in the groove once selected again together with return de-magging and roughly select operation;
(6) in the groove that de-magging is selected, product after filtering, and filtrate returns de-magging back pool;
(7) de-magging operation mine tailing through dense, filter after, overflow and filtrate return de-magging back pool;
(8) filter cake feeds surge tank A through dosing equipment with adding after water mixes, surge tank A overflow is to surge tank B, surge tank B is given to Counterfloatating desiliconization and roughly selects operation, dosing equipment installs belt conveyer scale, add water and control valve is installed, the water yield and belt conveyer scale displayed quantity regulate according to desiliconization operation floatation concentration, and dosing equipment electric machine frequency, according to the displayed quantity frequency control of belt conveyer scale, adds backwater in wet concentration desiliconization back pool;
(9) Counterfloatating desiliconization is roughly selected in operation and is added cation-collecting agent;
(10) foam of desiliconization operation is once elected to be industry again;
(11) desiliconization scan operation groove in product return desiliconization and roughly select operation, froth pulp is after filtration or after dense dewatering operation, backwater returns desiliconization back pool;
(12) desiliconization roughly selects the concentrate of operation after dewatering operation, and filtrate is back to desiliconization back pool;
(13) backwater of de-magging back pool is back to ore grinding and reverse flotation de-magging flow process, and the backwater in desiliconization back pool is back to in Counterfloatating desiliconization technological process.
In the above-mentioned flotation that the present invention is directed to collophane bi-anti-symmetric matrix technique and water return method, if no special instructions, relevant method for floating and parameter can be conventional method and the parameter of collophane bi-anti-symmetric matrix technique in present technology.
In flotation for collophane bi-anti-symmetric matrix technique of the present invention and water return method: described anionic collector is preferably C
12-
20alkyl fatty acid or fatty acid sodium salt or fatty acid potassium salt; Cation-collecting agent is preferably C
12-18primary amine hydrochloride or primary amine acetate or acid amides acetate or ether amine acetate; Described inhibitor acid is preferably phosphoric acid or sulfuric acid or both mixtures.
Flotation for collophane bi-anti-symmetric matrix technique of the present invention and water return method, further: in step (3), de-magging is roughly selected foam and is added inhibitor acid and carry out de-magging and roughly select operation and preferably carry out being elected to be industry again twice.
In the inventive method, preferred apatite raw ore main component is by weight percentage containing P
2o
518.0 ~ 26.0%, MgO1.5 ~ 6.0%, SiO
210.0 ~ 33.0%, all the other are impurity.
Compared with prior art, the advantage of the inventive method is mainly reflected in:
1. the inventive method is reasonable in design, and it uses the independent backwater flow process of bi-anti-symmetric matrix, and Counterfloatating desiliconization dosing can reduce 10% ~ 18%, and the rate of recovery of final phosphorus concentrate can improve 1% ~ 3%.The apatite concentrate grade P that the inventive method obtains
2o
5be 30.0 ~ 32.5%, the apatite concentrate rate of recovery of acquisition is 70.0 ~ 93.0% by weight percentage.
2. the present invention adopts de-magging operation and the independent backwater of desiliconization operation, efficiently avoid the impact of backwater on the operation of reverse flotation de-magging and Counterfloatating desiliconization operation, is conducive to the stable operation of bi-anti-symmetric matrix flow process in actual production.
Accompanying drawing explanation
Fig. 1 is a kind of process flow diagram of the present invention.
Detailed description of the invention
Referring to accompanying drawing, further describe concrete technical scheme of the present invention, so that those skilled in the art understands the present invention further, and do not form the restriction to its right.
Embodiment 1, a kind of flotation for collophane bi-anti-symmetric matrix technique and water return method, its step is as follows:
(1) apatite raw ore is milled to the mog that flotation operation needs;
(2) ore pulp of milled adds inhibitor acid, anionic collector carries out de-magging and roughly select operation;
(3) de-magging is roughly selected foam and is added inhibitor acid and carry out de-magging and roughly select operation and be elected to be industry more at least one times;
(4) in de-magging initial separatory cell, product adds inhibitor acid, anionic collector carries out primary cleaning operation;
(5) foam of the selected operation of de-magging converge with product in the groove once selected again together with return de-magging and roughly select operation;
(6) in the groove that de-magging is selected, product after filtering, and filtrate returns de-magging back pool;
(7) de-magging operation mine tailing through dense, filter after, overflow and filtrate return de-magging back pool;
(8) filter cake feeds surge tank A through dosing equipment with adding after water mixes, surge tank A overflow is to surge tank B, surge tank B is given to Counterfloatating desiliconization and roughly selects operation, dosing equipment installs belt conveyer scale, add water and control valve is installed, the water yield and belt conveyer scale displayed quantity regulate according to desiliconization operation floatation concentration, and dosing equipment electric machine frequency, according to the displayed quantity frequency control of belt conveyer scale, adds backwater in wet concentration desiliconization back pool;
(9) Counterfloatating desiliconization is roughly selected in operation and is added cation-collecting agent;
(10) foam of desiliconization operation is once elected to be industry again;
(11) desiliconization scan operation groove in product return desiliconization and roughly select operation, froth pulp is after filtration or after dense dewatering operation, backwater returns desiliconization back pool;
(12) desiliconization roughly selects the concentrate of operation after dewatering operation, and filtrate is back to desiliconization back pool;
(13) backwater of de-magging back pool is back to ore grinding and reverse flotation de-magging flow process, and the backwater in desiliconization back pool is back to in Counterfloatating desiliconization technological process.
Embodiment 2, in the flotation for collophane bi-anti-symmetric matrix technique described in embodiment 1 and water return method: described anionic collector is C
12-
20alkyl fatty acid or fatty acid sodium salt or fatty acid potassium salt; Cation-collecting agent is C
12-18primary amine hydrochloride or primary amine acetate or acid amides acetate or ether amine acetate; Described inhibitor acid is phosphoric acid or sulfuric acid or both mixtures.
Embodiment 3, the flotation for collophane bi-anti-symmetric matrix technique described in embodiment 1 or 2 and water return method, in step (3), de-magging is roughly selected foam and is added inhibitor acid and carry out de-magging and roughly select operation and carry out being elected to be industry again twice.All the other are all identical with embodiment 1 or 2.
Embodiment 4, the flotation for collophane bi-anti-symmetric matrix technique described in embodiment 1 or 2 or 3 and water return method: described apatite raw ore main component is by weight percentage: containing P
2o
518.0 ~ 26.0%, MgO1.5 ~ 6.0%, SiO
210.0 ~ 33.0%, all the other are impurity.
The low grade phosphorite selected in following embodiment is somewhere mineral products, mainly contains and uses mineral rubber phosphorus ore, and gangue mineral is dolomite, quartz and feldspar.
Embodiment 5, a kind of flotation for collophane bi-anti-symmetric matrix technique and water return method test one:
The phosphorite main component selected is by weight percentage containing P
2o
521.0%, MgO 1.9%, SiO
230.80%, all the other are impurity;
(1) phosphorite is milled to mog-200 order 75.00%,
(2) ore pulp of milled adds inhibitor acid 8kg/t, anionic collector 0.8kg/t and carries out de-magging and roughly select operation;
(3) de-magging is roughly selected foam and is added inhibitor acid 2kg/t and carry out de-magging and roughly select operation and carry out being elected to be industry again twice;
(4) in de-magging initial separatory cell, product adds inhibitor acid 2kg/t, and anionic collector 0.5kg/t carries out primary cleaning operation;
(5) foam of the selected operation of de-magging converge with product in the groove once selected again together with return de-magging and roughly select operation;
(6) in the groove that de-magging is selected product through dense, filter after, concentrator overflow, filter filtrate return de-magging back pool;
(7) mine tailing of de-magging operation after filtering, and filtrate returns de-magging back pool;
(8) filter cake feeds surge tank A through belt feeder with adding after water mixes, surge tank A overflow is to surge tank B, surge tank B is given to Counterfloatating desiliconization and roughly selects operation, belt feeder installs belt conveyer scale, add water water and control valve is installed, the water yield and belt conveyer scale displayed quantity regulate according to desiliconization operation floatation concentration, and belt feeder electric machine frequency, according to the displayed quantity frequency control of belt conveyer scale, adds backwater in wet concentration desiliconization back pool;
(9) Counterfloatating desiliconization is roughly selected in operation and is added cation-collecting agent 0.3kg/t;
(10) foam of desiliconization operation is once elected to be industry again;
(11) desiliconization scan operation groove in product return desiliconization and roughly select operation, froth pulp is after filtration after operation, and backwater returns desiliconization back pool;
(12) desiliconization roughly selects the concentrate of operation after dewatering operation, and filtrate is back to desiliconization back pool;
(13) backwater of de-magging back pool is back to ore grinding and reverse flotation de-magging flow process, and the backwater in desiliconization back pool is back to in Counterfloatating desiliconization technological process.
The apatite concentrate grade P obtained in said method
2o
5be 30.05%, the apatite concentrate rate of recovery obtained in said method is 81.6% by weight percentage.
Embodiment 6, a kind of flotation for collophane bi-anti-symmetric matrix technique and water return method test two:
The phosphorite main component selected is by weight percentage containing P
2o
521.9%, MgO 2.5%, SiO
227.0%, all the other are impurity;
(1) phosphorite is milled to mog-200 order 78.00%;
(2) ore pulp of milled adds inhibitor acid 10kg/t, anionic collector 1.2kg/t and carries out de-magging and roughly select operation;
(3) de-magging is roughly selected foam and is added inhibitor acid 3.5kg/t and carry out de-magging and roughly select operation and carry out scanning operation twice;
(4) in de-magging initial separatory cell product add inhibitor acid 3.0kg/t, anionic collector 0.6kg/t carry out primary cleaning operation;
(5) foam of the selected operation of de-magging converge with product in the groove once selected again together with return de-magging and roughly select operation;
(6) in the groove that de-magging is selected, product after filtering, and filter filtrate returns de-magging back pool;
(7) mine tailing of de-magging operation after filtering, and filtrate returns de-magging back pool;
(8) filter cake feeds surge tank A through belt feeder with adding after water mixes, surge tank A overflow is to surge tank B, surge tank B is given to Counterfloatating desiliconization and roughly selects operation, belt feeder installs belt conveyer scale, add water water and control valve is installed, the water yield and belt conveyer scale displayed quantity regulate according to desiliconization operation floatation concentration, and belt feeder electric machine frequency, according to the displayed quantity frequency control of belt conveyer scale, adds backwater in wet concentration desiliconization back pool;
(9) Counterfloatating desiliconization is roughly selected in operation and is added cation-collecting agent 0.35kg/t;
(10) foam of desiliconization operation carries out once purging selection operation;
(11) desiliconization scan operation groove in product return desiliconization and roughly select operation, froth pulp is after filtration after operation, and backwater returns desiliconization back pool;
(12) desiliconization roughly selects the concentrate of operation after dewatering operation, and filtrate is back to desiliconization back pool;
(13) backwater of de-magging back pool is back to ore grinding and reverse flotation de-magging flow process, and the backwater in desiliconization back pool is back to in Counterfloatating desiliconization technological process.
The apatite concentrate grade P obtained in said method
2o
5be 30.8%, the apatite concentrate rate of recovery obtained in said method is 82.6% by weight percentage.
Embodiment 7, a kind of flotation for collophane bi-anti-symmetric matrix technique and water return method test three:
The phosphorite main component selected is by weight percentage containing P
2o
521.8%, MgO 2.6%, SiO
226.6.0%, all the other are impurity;
(1) phosphorite is milled to mog-200 order 85.00%,
(2) ore pulp of milled adds inhibitor acid 10kg/t, anionic collector 1.5kg/t and carries out de-magging and roughly select operation;
(3) de-magging is roughly selected foam and is added inhibitor acid 2kg/t and carry out de-magging and roughly select operation and carry out being elected to be industry again twice;
(4) in de-magging initial separatory cell product add inhibitor acid 4kg/t, anionic collector 0.3kg/t carry out primary cleaning operation;
(5) foam of the selected operation of de-magging converge with product in the groove once selected again together with return de-magging and roughly select operation;
(6) in the groove that de-magging is selected product through dense, filter after, concentrator overflow, filter filtrate return de-magging back pool;
(7) de-magging operation mine tailing through dense and filter after, concentrator overflow and filter filtrate return de-magging back pool;
(8) filter cake feeds surge tank A through belt feeder with adding after water mixes, surge tank A overflow is to surge tank B, surge tank B is given to Counterfloatating desiliconization and roughly selects operation, belt feeder installs belt conveyer scale, add water water and control valve is installed, the water yield and belt conveyer scale displayed quantity regulate according to desiliconization operation floatation concentration, and belt feeder electric machine frequency, according to the displayed quantity frequency control of belt conveyer scale, adds backwater in wet concentration desiliconization back pool;
(9) Counterfloatating desiliconization is roughly selected in operation and is added cation-collecting agent 0.25kg/t;
(10) foam of desiliconization operation carries out once purging selection operation;
(11) desiliconization scan operation groove in product return desiliconization and roughly select operation, froth pulp is after filtration after operation, and backwater returns desiliconization back pool;
(12) desiliconization roughly selects the concentrate of operation after dewatering operation, and filtrate is back to desiliconization back pool;
(13) backwater of de-magging back pool is back to ore grinding and reverse flotation de-magging flow process, and the backwater in desiliconization back pool is back to in Counterfloatating desiliconization technological process.
The apatite concentrate grade P obtained in said method
2o
5be 31.1%, the apatite concentrate rate of recovery obtained in said method is 85.6% by weight percentage.
Claims (4)
1., for flotation and the water return method of collophane bi-anti-symmetric matrix technique, it is characterized in that, comprise the steps:
(1) apatite raw ore is milled to the mog that flotation operation needs;
(2) ore pulp of milled adds inhibitor acid, anionic collector carries out de-magging and roughly select operation;
(3) de-magging is roughly selected foam and is added inhibitor acid and carry out de-magging and roughly select operation and be elected to be industry more at least one times;
(4) in de-magging initial separatory cell, product adds inhibitor acid, anionic collector carries out primary cleaning operation;
(5) foam of the selected operation of de-magging converge with product in the groove once selected again together with return de-magging and roughly select operation;
(6) in the groove that de-magging is selected, product after filtering, and filtrate returns de-magging back pool;
(7) de-magging operation mine tailing through dense, filter after, overflow and filtrate return de-magging back pool;
(8) filter cake feeds surge tank A through dosing equipment with adding after water mixes, surge tank A overflow is to surge tank B, surge tank B is given to Counterfloatating desiliconization and roughly selects operation, dosing equipment installs belt conveyer scale, add water and control valve is installed, the water yield and belt conveyer scale displayed quantity regulate according to desiliconization operation floatation concentration, and dosing equipment electric machine frequency, according to the displayed quantity frequency control of belt conveyer scale, adds backwater in wet concentration desiliconization back pool;
(9) Counterfloatating desiliconization is roughly selected in operation and is added cation-collecting agent;
(10) foam of desiliconization operation is once elected to be industry again;
(11) desiliconization scan operation groove in product return desiliconization and roughly select operation, froth pulp is after filtration or after dense dewatering operation, backwater returns desiliconization back pool;
(12) desiliconization roughly selects the concentrate of operation after dewatering operation, and filtrate is back to desiliconization back pool;
(13) backwater of de-magging back pool is back to ore grinding and reverse flotation de-magging flow process, and the backwater in desiliconization back pool is back to in Counterfloatating desiliconization technological process.
2. the flotation for collophane bi-anti-symmetric matrix technique according to claim 1 and water return method, is characterized in that: described anionic collector is C
12-
20alkyl fatty acid or fatty acid sodium salt or fatty acid potassium salt; Cation-collecting agent is C
12-18primary amine hydrochloride or primary amine acetate or acid amides acetate or ether amine acetate; Described inhibitor acid is phosphoric acid or sulfuric acid or both mixtures.
3. the flotation for collophane bi-anti-symmetric matrix technique according to claim 1 and 2 and water return method, is characterized in that: in step (3), and de-magging is roughly selected foam and added inhibitor acid and carry out de-magging and roughly select operation and carry out being elected to be industry again twice.
4. the flotation for collophane bi-anti-symmetric matrix technique according to claim 1 and 2 and water return method, is characterized in that: described apatite raw ore main component is by weight percentage: containing P
2o
518.0 ~ 26.0%, MgO1.5 ~ 6.0%, SiO
210.0 ~ 33.0%, all the other are impurity.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510234815.0A CN104826741B (en) | 2015-05-08 | 2015-05-08 | A kind of flotation and water return method for collophane bi-anti-symmetric matrix technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510234815.0A CN104826741B (en) | 2015-05-08 | 2015-05-08 | A kind of flotation and water return method for collophane bi-anti-symmetric matrix technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104826741A true CN104826741A (en) | 2015-08-12 |
| CN104826741B CN104826741B (en) | 2017-05-31 |
Family
ID=53805147
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510234815.0A Active CN104826741B (en) | 2015-05-08 | 2015-05-08 | A kind of flotation and water return method for collophane bi-anti-symmetric matrix technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104826741B (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105689149A (en) * | 2016-04-27 | 2016-06-22 | 中蓝连海设计研究院 | Double-reverse flotation method applicable to silico-calcium phosphorite |
| CN106242109A (en) * | 2016-08-11 | 2016-12-21 | 中蓝连海设计研究院 | A kind of phosphorus ore direct reverse flotation produces waste water segmentation and utilizes technique |
| 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 |
| CN107252736A (en) * | 2017-06-21 | 2017-10-17 | 远安县燎原矿业有限责任公司 | A kind of appositional pattern silicon calcium quality ore bi-anti-symmetric matrix technique |
| CN109174471A (en) * | 2018-08-28 | 2019-01-11 | 北京矿冶科技集团有限公司 | A kind of automatically cleaning return water processing method |
| CN109453891A (en) * | 2018-10-23 | 2019-03-12 | 宜都兴发化工有限公司 | A kind of high sesquialter collophane spiral chute floats process integration again |
| CN109954579A (en) * | 2019-03-29 | 2019-07-02 | 中冶北方（大连）工程技术有限公司 | Two product ore-dressing technique of apatite ilmenite |
| CN110076004A (en) * | 2019-05-08 | 2019-08-02 | 武汉工程大学 | A kind of novel Counterfloatating desiliconization cationic collecting agent and its preparation method and application |
| CN110124870A (en) * | 2019-05-31 | 2019-08-16 | 北京矿冶科技集团有限公司 | A kind of ore dressing impurity-removing method of the carbon containing high sesquichloride collophane containing magnesium |
| CN111617885A (en) * | 2020-05-18 | 2020-09-04 | 宜都兴发化工有限公司 | Synchronous reverse flotation process for low-magnesium high-sesqui collophanite |
| CN112007759A (en) * | 2019-07-23 | 2020-12-01 | 中蓝连海设计研究院有限公司 | Double-reverse middling direct flotation method for treating low-magnesium high-iron aluminum silicon calcium collophanite |
| CN112237993A (en) * | 2020-09-17 | 2021-01-19 | 宜都兴发化工有限公司 | Method for recycling wastewater in collophanite double-reverse flotation process according to quality |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101972710A (en) * | 2010-10-18 | 2011-02-16 | 中蓝连海设计研究院 | Double reverse flotation process of middle-low grade phosphorite |
| CN102441498A (en) * | 2011-10-31 | 2012-05-09 | 中蓝连海设计研究院 | Phosphorite double-reverse flotation process |
| CN103212484A (en) * | 2013-04-18 | 2013-07-24 | 武汉工程大学 | Phosphorite reverse flotation process |
| CN104437885A (en) * | 2014-11-12 | 2015-03-25 | 中蓝连海设计研究院 | Collophanite classification reverse flotation desilication method |
| CN104549762A (en) * | 2014-11-14 | 2015-04-29 | 云南磷化集团有限公司 | Grinding-flotation closed circuit technology for refractory high-magnesium collophanite |
-
2015
- 2015-05-08 CN CN201510234815.0A patent/CN104826741B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101972710A (en) * | 2010-10-18 | 2011-02-16 | 中蓝连海设计研究院 | Double reverse flotation process of middle-low grade phosphorite |
| CN102441498A (en) * | 2011-10-31 | 2012-05-09 | 中蓝连海设计研究院 | Phosphorite double-reverse flotation process |
| CN103212484A (en) * | 2013-04-18 | 2013-07-24 | 武汉工程大学 | Phosphorite reverse flotation process |
| CN104437885A (en) * | 2014-11-12 | 2015-03-25 | 中蓝连海设计研究院 | Collophanite classification reverse flotation desilication method |
| CN104549762A (en) * | 2014-11-14 | 2015-04-29 | 云南磷化集团有限公司 | Grinding-flotation closed circuit technology for refractory high-magnesium collophanite |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105689149B (en) * | 2016-04-27 | 2018-03-06 | 中蓝连海设计研究院 | A kind of bi-anti-symmetric matrix method of suitable silicon calcium quality ore |
| CN105689149A (en) * | 2016-04-27 | 2016-06-22 | 中蓝连海设计研究院 | Double-reverse flotation method applicable to silico-calcium phosphorite |
| CN106242109A (en) * | 2016-08-11 | 2016-12-21 | 中蓝连海设计研究院 | A kind of phosphorus ore direct reverse flotation produces waste water segmentation and utilizes technique |
| CN106242109B (en) * | 2016-08-11 | 2020-03-24 | 中蓝连海设计研究院有限公司 | Process for utilizing waste water generated in phosphorite direct and reverse flotation production in sections |
| CN106423584B (en) * | 2016-12-21 | 2019-07-12 | 中蓝连海设计研究院有限公司 | A kind of collophane direct reverse flotation technique that floatation process water recycles respectively |
| 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 |
| CN107252736A (en) * | 2017-06-21 | 2017-10-17 | 远安县燎原矿业有限责任公司 | A kind of appositional pattern silicon calcium quality ore bi-anti-symmetric matrix technique |
| CN109174471A (en) * | 2018-08-28 | 2019-01-11 | 北京矿冶科技集团有限公司 | A kind of automatically cleaning return water processing method |
| CN109453891A (en) * | 2018-10-23 | 2019-03-12 | 宜都兴发化工有限公司 | A kind of high sesquialter collophane spiral chute floats process integration again |
| CN109453891B (en) * | 2018-10-23 | 2021-06-18 | 宜都兴发化工有限公司 | High sesqui-collophanite spiral chute re-floating combined process |
| CN109954579A (en) * | 2019-03-29 | 2019-07-02 | 中冶北方（大连）工程技术有限公司 | Two product ore-dressing technique of apatite ilmenite |
| CN110076004A (en) * | 2019-05-08 | 2019-08-02 | 武汉工程大学 | A kind of novel Counterfloatating desiliconization cationic collecting agent and its preparation method and application |
| CN110124870A (en) * | 2019-05-31 | 2019-08-16 | 北京矿冶科技集团有限公司 | A kind of ore dressing impurity-removing method of the carbon containing high sesquichloride collophane containing magnesium |
| CN112007759A (en) * | 2019-07-23 | 2020-12-01 | 中蓝连海设计研究院有限公司 | Double-reverse middling direct flotation method for treating low-magnesium high-iron aluminum silicon calcium collophanite |
| CN111617885A (en) * | 2020-05-18 | 2020-09-04 | 宜都兴发化工有限公司 | Synchronous reverse flotation process for low-magnesium high-sesqui collophanite |
| CN111617885B (en) * | 2020-05-18 | 2022-09-16 | 宜都兴发化工有限公司 | Synchronous reverse flotation process for low-magnesium high-sesqui collophanite |
| CN112237993A (en) * | 2020-09-17 | 2021-01-19 | 宜都兴发化工有限公司 | Method for recycling wastewater in collophanite double-reverse flotation process according to quality |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104826741B (en) | 2017-05-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104826741A (en) | Flotation and backwater method aiming at collophanite double-back flotation process | |
| CN102744152A (en) | Reverse/direct flotation technology of collophanite | |
| CN102744151B (en) | Branch flotation technology for silicon calcium collophanite | |
| US10434520B2 (en) | Collector for beneficiating carbonaceous phosphate ores | |
| CN105689149B (en) | A kind of bi-anti-symmetric matrix method of suitable silicon calcium quality ore | |
| CN104907183B (en) | A kind of silico-calcium matter low grade collophanite direct reverse flotation technique | |
| CN101972710B (en) | Double reverse flotation process of middle-low grade phosphorite | |
| CN101099946A (en) | Collophanite floatation method | |
| CN101856634B (en) | Iron-increasing and silicon-reduction mineral separation method for iron ores | |
| CN102284351B (en) | Beneficiation method for separating potassium feldspar concentrates from BayanObo potassium-rich slates | |
| CN106423536B (en) | A kind of substep ore grinding floatation process anyway handling silicon calcium collophanite | |
| CN103301949B (en) | Foaming agent for rare earth ore dressing and normal-temperature ore dressing process of low-grade refractory rare earth ore | |
| CN105268560A (en) | Method for simultaneous anti-flotation of carbonate and silicate in phosphorus ore | |
| CN104801418B (en) | A kind of coarse grain reverse flotation de-magging method for phosphorus ore | |
| CN104607321A (en) | Collophanite froth flotation collecting agent and preparation method thereof | |
| CN110152889A (en) | A kind of silicon calcium quality ore Counterfloatating desiliconization removal of impurities combined capturing and collecting agent and its preparation method and application | |
| CN110142145A (en) | The technique of sesquichloride and magnesium addition in a kind of flotation removing silicon calcium collophanite | |
| CN104174504A (en) | Direct-flotation branching floatation method of low-and-medium-grade mixed type refractory collophane | |
| CN106269265A (en) | A kind of classification stepped-flotation separation technique processing high alumina high ferro silicon calcium collophanite | |
| CN112058503A (en) | Silico-calcium collophanite double-reverse flotation process | |
| CN103386365B (en) | Dual obverse and reverse floatation method for silicon calcium phosphorite | |
| CN107309075A (en) | Collophane beneficiation method | |
| CN112474061B (en) | Ester-group-containing quaternary ammonium salt cationic collector and preparation method and application thereof | |
| CN103950911B (en) | Slag acid and yellow phosphorus furnace slag is utilized to prepare the method for calcium hydrophosphate fodder coproduction water glass | |
| CN106076607A (en) | A kind of two step desliming reverse floatation process processing high alumina-silica collophane |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| EXSB | Decision made by sipo to initiate substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |