CN102698873A - Beneficiation method for desorbing silicate impurities in collophanite through direct flotation - Google Patents
Beneficiation method for desorbing silicate impurities in collophanite through direct flotation Download PDFInfo
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- CN102698873A CN102698873A CN2011103846846A CN201110384684A CN102698873A CN 102698873 A CN102698873 A CN 102698873A CN 2011103846846 A CN2011103846846 A CN 2011103846846A CN 201110384684 A CN201110384684 A CN 201110384684A CN 102698873 A CN102698873 A CN 102698873A
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Abstract
The invention discloses a beneficiation method for desorbing silicate impurities in collophanite through direct flotation, and relates to a beneficiation method, in particular to a beneficiation method for removing impurities from ores through direct-reverse flotation. The method comprises the following steps of: (a), fully dissolving siliceous collophanite raw ores containing the silicate impurities, and controlling the size mixing concentration to form 30 to 35 weight percent ore pulp; (b), introducing the ore pulp into a mineralization stirring tank of a flotation machine, adding a collophanite flotation reagent and a composite inhibitor for pneumatic flotation, and adding a small number of composite inhibitors for fine selection to obtain direct flotation concentrate in a foam tank, wherein a product in the tank is the silicate impurities; and (c), adding the direct flotation concentrate into a flotation tank, adding a reverse flotation regulator, adding a carbonate collecting agent, and performing select flotation, wherein a foam product is carbonate impurities, and a product in the tank is a high-grade phosphate concentrate product. By the method, impurities such as clay aluminosilicate are effectively reduced, the quality of phosphate concentrate is improved, and the difficulty in production and purification of phosphoric acid is reduced.
Description
Technical field
The present invention relates to a kind of first ore deposit method, particularly employing just-reverse flotation carries out the beneficiation method of ore removal of impurities.
Background technology
Along with the high speed development of phosphate fertilizer industry, the exploitation of phosphorus ore and consumption also sharply rise, and the overall grade of phosphorus ore descends day by day; Cause in the phosphoric acid impurity component to become more complicated with more, exploitation mid low grade phosphate rock stone has become the task of top priority, in, the low-grade phosphate ore major impurity is silicate and carbonate impurity; Through tackling key problem for many years; The removing process of carbonate is ripe, because the silicate dopant species is complicated, disseminated grain size differs, is difficult to remove.The silicate dopant species is complicated, disseminated grain size differs, is difficult to deviate from, clay class silicate impurity especially wherein, it is micro-size fraction, and if this part particulate ore deposit does not remove, the grade of phosphorus concentrate is difficult to enrichment and gets on.Its drawback in ore dressing: adopt the collocation of traditional silicate inhibitor waterglass and collecting agent to use, removal efficiency is low; Because its fine size, specific area is big, consume too much collecting agent, concentrate sinking speed slow, consume too much flocculant; And this part particulate ore deposit also influences the production of postorder chemical industry acid system operation, and it is restive to cause foaming in the acid technological process.Get from the size sieves analysis result, clay class silicate impurity can be removed major part through desliming.Because its granularity very carefully (0.025mm), does not have suitable efficient desliming device that raw ore is carried out classification at present, is prone to cause a large amount of phosphorus ore thing direct losses simultaneously.And causing technological process complicated, production cost is higher, is difficult to control.Adopted the direct floatation process flow process in the past, and reach the purpose that removes fine fraction clay class silicate impurity, and must adopt long flow process and big medicament, to such an extent as to former flotation process is complicated, dosing is big, and cost is high, and commercial production is restive.
Summary of the invention
The object of the invention is intended to overcome the defective of prior art, provides a kind of technological process simple, and production cost is low, and the direct flotation of processing ease removes the beneficiation method of collophane mesosilicic acid salt impurity.
Direct flotation of the present invention removes the beneficiation method of collophane mesosilicic acid salt impurity, and step is following:
A. will contain the siliceous collophane stone crushing raw ore, levigate for particle diameter 0.074mm >=98% of silicate impurity, phosphorus ore thing and silicate mineral are fully dissociated, controlling the concentration of sizing mixing is the ore pulp of 30～35wt%;
B. ore pulp is introduced in the flotation device mineralising tank diameter; Add Collophanite flotation medicament and the composite inhibitor be used to remove collophane mesosilicic acid salt impurity and carry out air flotation; In foam tank, obtain to roughly select the phosphorus concentrate, roughly select concentrate and introduce flotation device, add a small amount of composite inhibitor and carry out selected; In foam tank, obtain the direct flotation concentrate, product is a silicate impurity in the groove;
C. the direct flotation phosphorus concentrate that obtains in the above-mentioned foam tank is added in the flotation cell; Add reverse flotation adjustment agent and make pH values of pulp be controlled at 4.0～5.0, add the carbonate collecting agent, carry out air flotation; Froth pulp is a carbonate impurity, and product is high grade phosphorus concentrate product in the groove.
Described direct flotation removes the beneficiation method of collophane mesosilicic acid salt impurity; The inhibitor of traditional silicate impurity all is to adopt waterglass as inhibitor; Waterglass generally suppresses easy repressed silicate impurity such as quartz sand, for the clay class aluminum silicate inhibition effect relative mistake of micro-size fraction; Described composite inhibitor is waterglass and aluminium chelate salt.Can reach the purpose of " catching a little less than pressure is arranged by force ", thereby reach effective elimination silicate impurity, simplify the purpose of technological process.
Described composite inhibitor is by amphoteric metal salt aluminum sulfate Al
2(SO
4)
3.XH
2O and polyalcohol HO--CH
2CH
2CH
2-OH combines, and the ratio 1.5:1 of two kinds of medicaments～2.0:1 is diluted to 1.0%～2.0%) the concentration interpolation.The mechanism of action of inhibitor: main Al
2(SO
4)
3.XH
2O has double action, presses down the silicon synergist and is mainly amphoteric metal salt aluminum sulfate Al
2(SO
4)
3.XH
2O is based on Al
2(SO
4)
3.XH
2O has flocculation and common-ion effect, makes fine-particle minerals coacervating large particle mineral, Al
2(SO
4)
3.XH
2O sticks to aluminosilicate impurity surface, forms one deck hydrophilic membrane; Next HO--CH
2CH
2CH
2Ca in-OH and the ore pulp
2+, Mg
2+Generate chelate, attached to silicate impurity surface, form the cover cap layer, dual hydrophilic membrane effectively avoids silicate impurity to contact with collecting agent, thereby reaches repressed purpose.
In the described direct flotation air flotation of step b, the aeration quantity of air flotation is 0.04～0.09m
3/ h, flotation time 3 ~ 6min.Because clay class microfine silicate impurity has been suppressed, flotation speed has improved, and the flowability of flotation froth also improves.
Described to siliceous collophane just adopting-during the floating phosphorus technology of reverse flotation; Direct flotation adjustment agent is sodium carbonate, waterglass, composite inhibitor; The collecting agent of direct flotation is aliphatic acid and soap class thereof, and reverse flotation adjustment agent is a sulfuric acid, and collecting agent in reverse floatation is aliphatic acid and soap class thereof.
The consumption of collecting agent, reverse flotation adjustment agent and the collecting agent in reverse floatation of described direct flotation adjustment agent, direct flotation is that raw ore per ton uses: sodium carbonate 2.0 ~ 5.0Kg, waterglass 3.5 ~ 5.0Kg, composite inhibitor 0.4 ~ 0.8Kg, direct flotation collecting agent 1.5 ~ 3.0 Kg; Sulfuric acid 6.0 ~ 9.0 Kg, collecting agent in reverse floatation 1.0 ~ 1.5g.
Direct flotation of the present invention removes the beneficiation method of collophane mesosilicic acid salt impurity; Realized removing the beneficiation method of the fine fraction silicate impurity in the phosphorus concentrate at floatation process; Reduce the silicate impurity content in the phosphorus concentrate, simplified purification process and reduction production and operation cost in the downstream relieving haperacidity enterprise production.In the direct flotation operation, adopt composite inhibitor targetedly, clay class aluminosilicate impurity is selectively suppressed and the inhibition of flocculating, reduced reagent consumption, improved the flowability of flotation froth, be convenient to the industrialization operation.Added composite inhibitor, adopted the mode of " catching a little less than suppressing ", improved the removal efficiency of silicate impurity in the direct flotation operation, simplified flotation process, the direct floatation process flow process is reduced to a thick Seiko process flow from one thick two original single-minded sweeping.Can reduce the construction investment expense of suitability for industrialized production significantly and cut operating costs.Removing of the clay class aluminosilicate impurity of microfine can be reduced the influence of fine level mineral to the concentrate slurry sinking speed, and the sinking speed of concentrate slurry significantly improves, and has reduced the consumption of flocculant, reduces the consumption of assistant medicament.The present invention reduces silicate impurity targetedly in the Collophanite flotation process; Especially the beneficiation method of clay class aluminosilicate; Obtain the low high grade phosphorus concentrate of impurity content, alleviated shortcomings such as dosing is big in the direct flotation process, flotation froth is clamminess, technological process is grown; Effectively reduce impurity such as clay class aluminosilicate, improved the quality of phosphorus concentrate, reduce the difficulty of phosphoric acid production and purification, simplify the beneficiation method of phosphoric acid purification flow process and operation cost expense.
Description of drawings
Fig. 1 is a flow chart of the present invention.
The specific embodiment
Below in conjunction with embodiment the present invention is further described, but is not limited to embodiment.In an embodiment, removing has special instruction, and all percentage compositions are mass percent.
Embodiment 1
Sample ore is chosen in certain mining area, raw ore P
2O
5Content 19.88wt%, MgO content 1.25wt%, SiO
2Content 36.87wt%, Al
2O
3Content 2.58wt% according to the above-mentioned process program of the present invention, takes off the joint process of MgO at normal temperature condition through the rich desiliconization enriched phosphorus+reverse flotation of direct flotation, obtains phosphorus concentrate yield 52.75%, P
2O
5Content 30.70wt%, MgO content 0.35wt%, SiO
2Content 18.00wt%, Al
2O
3Content 1.00wt%, wherein SiO
2Elimination factor reaches 74.16wt%, Al
2O
3Elimination factor reaches: 79.55wt%.CaO/?P
2O
5＝1.44、MgO/?P
2O
5=1.14wt%、Al
2O
3/?P
2O
5＝3.25wt%；
Two kinds of technology direct flotation conditions: the waterglass inhibitor is adopted in (1); The operation of top-uping is twice selected operation of one roughing once purging selection; The direct flotation dosing: sodium carbonate 2.0Kg/t, waterglass by quantity of goods produced count 8.0Kg/t, collecting agent is YP2-1, consumption is 3.5 Kg/t; Open circuit result: concentrate product 48.85%, P
2O
528.10 %, SiO
218.80, the rate of recovery is 69.05%.(2) adopting waterglass and composite inhibitor to mix uses; The operation of top-uping is the operation of one roughing primary cleaning; The direct flotation dosing: it is YP2-1 that sodium carbonate 2.0Kg/t, waterglass count 4.5Kg/t, composite inhibitor 0.6Kg/t, collecting agent by quantity of goods produced, and consumption is 2.6Kg/t; The open circuit result: concentrate yield is 50.15%, P
2O
528.45%, SiO
217.85%, the rate of recovery is 71.76%.
Embodiment 2
Certain mining area sample ore, raw ore P
2O
5Content 22.71wt%, MgO content 3.21wt%, SiO
2Content 22.17wt%, Al
2O
3Content 2.00wt% according to the above-mentioned process program of the present invention, takes off the joint process of MgO at normal temperature condition through direct-flotation desiliconisation enriched phosphorus+reverse flotation, obtains phosphorus concentrate yield 63.99%, P
2O
5Content 31.17wt%, MgO content 0.69wt%, SiO
2Content 13.31wt%, Al
2O
3Content 1.00wt%, wherein SiO
2Elimination factor reaches 61.58wt%, Al
2O
3Elimination factor reaches: 68.01wt%.CaO/?P
2O
5＝1.38、MgO/?P
2O
5=2.21wt%、Al
2O
3/?P
2O
5＝3.21wt%；
Two kinds of technology direct flotation conditions: the waterglass inhibitor is adopted in (1); The operation of top-uping is two operations of one roughing once purging selection; The direct flotation dosing: sodium carbonate 2.5Kg/t, waterglass by quantity of goods produced count 5.0Kg/t, collecting agent is YP2-1, consumption in kind is 3.0 Kg/t amounts; Open circuit result: concentrate product 62.05%, P
2O
527.10%, SiO
211.72%, the rate of recovery is 74.04%.(2) adopting waterglass and composite inhibitor to mix uses; The operation of top-uping is two operations of one roughing once purging selection; The direct flotation dosing: it is YP2-1 that sodium carbonate 3.0Kg/t, waterglass count 3.2Kg/t, composite inhibitor 0.3Kg/t, collecting agent by quantity of goods produced, and consumption is 2.45Kg/t; The open circuit result: concentrate yield is 60.25%, P
2O
526.85%, SiO
212.85%, the rate of recovery is 71.23%.
Embodiment 3
Certain mining area sample ore, raw ore P
2O
5Content 23.17wt%, MgO content 1.43wt%, SiO
2Content 25.23wt%, Al
2O
3Content 2.19wt% according to the above-mentioned process program of the present invention, takes off the joint process of MgO at normal temperature condition through direct-flotation desiliconisation enriched phosphorus+reverse flotation, obtains phosphorus concentrate yield 63.49%, P
2O
5Content 30.24wt%, MgO content 0.52wt%, SiO
2Content 15.75wt%, Al
2O
3Content 1.01wt%, wherein SiO
2Elimination factor reaches 60.37wt%, Al
2O
3Elimination factor reaches: 70.72wt%.CaO/?P
2O
5＝1.23、MgO/?P
2O
5=1.72wt%、Al
2O
3/?P
2O
5＝3.34wt%；
Two kinds of technology direct flotation conditions: the waterglass inhibitor is adopted in (1); The operation of top-uping is two operations of one roughing once purging selection; The direct flotation dosing: sodium carbonate 3.1Kg/t, waterglass by quantity of goods produced count 4.5Kg/t, collecting agent is YP2-1, consumption in kind is 2.6 Kg/t; Open circuit result: concentrate product 53.10%, P
2O
526.65%, SiO
216.72, the rate of recovery is 61.08%.(2) adopting waterglass and composite inhibitor to mix uses; The operation of top-uping is two operations of one roughing once purging selection; The direct flotation dosing: it is YP2-1 that sodium carbonate 3.1Kg/t, waterglass count 3.0Kg/t, composite inhibitor 0.45Kg/t, collecting agent by quantity of goods produced, and consumption is 2.30Kg/t; The open circuit result: concentrate yield is 55.32%, P
2O
527.06%, SiO
215.50%, the rate of recovery is 64.61%.
In 3 embodiment, the phosphorus concentrate index that is obtained all reaches national phosphoric acid by wet process with ore deposit Grade A I class standard, its impurity SiO
2, Al
2O
3, MgO content uses the ore deposit standard well below phosphoric acid by wet process with ore deposit high-class product I class.Wherein direct flotation operation interpolation composite inhibitor uses waterglass to compare as inhibitor with direct use, and dosing reduces, and the productive rate and the rate of recovery raise, and the direct-flotation desiliconisation rate improves.
Claims (6)
1. a direct flotation removes the beneficiation method of collophane mesosilicic acid salt impurity, it is characterized in that step is following:
A. will contain the siliceous collophane stone crushing raw ore, levigate for particle diameter 0.074mm >=98% of silicate impurity, phosphorus ore thing and silicate mineral are fully dissociated, controlling the concentration of sizing mixing is the ore pulp of 30～35wt%;
B. ore pulp is introduced in the flotation device mineralising tank diameter; Add Collophanite flotation medicament and the composite inhibitor be used to remove collophane mesosilicic acid salt impurity and carry out air flotation; In foam tank, obtain to roughly select the phosphorus concentrate, roughly select concentrate and introduce flotation device, add a small amount of composite inhibitor and carry out selected; In foam tank, obtain the direct flotation concentrate, product is a silicate impurity in the groove;
C. the direct flotation phosphorus concentrate that obtains in the above-mentioned foam tank is added in the flotation cell; Add reverse flotation adjustment agent and make pH values of pulp be controlled at 4.0～5.0, add the carbonate collecting agent, carry out air flotation; Froth pulp is a carbonate impurity, and product is high grade phosphorus concentrate product in the groove.
2. direct flotation according to claim 1 removes the beneficiation method of collophane mesosilicic acid salt impurity, it is characterized in that, composite inhibitor is by amphoteric metal salt aluminum sulfate Al
2(SO
4)
3.
3.XH
2O and polyalcohol HO--CH
2CH
2CH
2-OH combines, and the ratio 1.5:1 of two kinds of medicaments～2.0:1 is diluted to 1.0～2.0% concentration.
4. direct flotation according to claim 1 removes the beneficiation method of collophane mesosilicic acid salt impurity, it is characterized in that, in the described direct flotation air flotation of step b, the aeration quantity of air flotation is 0.04～0.09m
3/ h, flotation time 3 ~ 6min.
5. direct flotation according to claim 1 removes the beneficiation method of collophane mesosilicic acid salt impurity; It is characterized in that; To siliceous collophane just adopting-during the floating phosphorus technology of reverse flotation, direct flotation adjustment agent is sodium carbonate, waterglass, composite inhibitor, the collecting agent of direct flotation is aliphatic acid and soap class thereof; Reverse flotation adjustment agent is a sulfuric acid, and collecting agent in reverse floatation is aliphatic acid and soap class thereof.
6. direct flotation according to claim 4 removes the beneficiation method of collophane mesosilicic acid salt impurity; It is characterized in that; The consumption of the collecting agent of direct flotation adjustment agent, direct flotation, reverse flotation adjustment agent and collecting agent in reverse floatation is that raw ore per ton uses: sodium carbonate 2.0 ~ 5.0Kg, waterglass 3.5 ~ 5.0Kg, composite inhibitor 0.4 ~ 0.8Kg, direct flotation collecting agent 1.5 ~ 3.0 Kg; Sulfuric acid 6.0 ~ 9.0 Kg, collecting agent in reverse floatation 1.0 ~ 1.5g.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103934114A (en) * | 2014-04-22 | 2014-07-23 | 甘肃瓮福化工有限责任公司 | Beneficiation method for medium-low-grade phosphate ores |
| CN104959239A (en) * | 2015-06-26 | 2015-10-07 | 中国地质科学院矿产综合利用研究所 | Low-grade refractory weathered collophanite segmented desliming flotation process |
| CN106076607A (en) * | 2016-08-18 | 2016-11-09 | 中蓝连海设计研究院 | A kind of two step desliming reverse floatation process processing high alumina-silica collophane |
| CN106269265A (en) * | 2016-08-18 | 2017-01-04 | 中蓝连海设计研究院 | A kind of classification stepped-flotation separation technique processing high alumina high ferro silicon calcium collophanite |
| CN106423582A (en) * | 2016-12-07 | 2017-02-22 | 广西大学 | Preparation method of potassium feldspar inhibitor |
| CN110369121A (en) * | 2019-07-25 | 2019-10-25 | 宜都兴发化工有限公司 | Screening-gravity separation technology is added before phosphorus ore direct flotation operation |
| CN110455781A (en) * | 2019-08-26 | 2019-11-15 | 云南磷化集团有限公司 | For the LIBS on-line detecting system of flotation of phosphate rock system and its application |
| CN112547314A (en) * | 2020-11-18 | 2021-03-26 | 云南磷化集团有限公司 | Full-quantity resource production method of siliceous and silicate refractory collophanite |
| WO2024040893A1 (en) * | 2022-08-26 | 2024-02-29 | 广东邦普循环科技有限公司 | Method for purifying and whitening phosphogypsum |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103934114A (en) * | 2014-04-22 | 2014-07-23 | 甘肃瓮福化工有限责任公司 | Beneficiation method for medium-low-grade phosphate ores |
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| CN106269265A (en) * | 2016-08-18 | 2017-01-04 | 中蓝连海设计研究院 | A kind of classification stepped-flotation separation technique processing high alumina high ferro silicon calcium collophanite |
| CN106076607B (en) * | 2016-08-18 | 2019-02-26 | 中蓝连海设计研究院有限公司 | A kind of two step desliming reverse floatation process handling high alumina-silica collophane |
| CN106423582A (en) * | 2016-12-07 | 2017-02-22 | 广西大学 | Preparation method of potassium feldspar inhibitor |
| CN106423582B (en) * | 2016-12-07 | 2018-08-17 | 广西大学 | A kind of preparation method of potassium feldspar inhibitor |
| CN110369121A (en) * | 2019-07-25 | 2019-10-25 | 宜都兴发化工有限公司 | Screening-gravity separation technology is added before phosphorus ore direct flotation operation |
| CN110369121B (en) * | 2019-07-25 | 2021-08-10 | 宜都兴发化工有限公司 | Screening-gravity separation process added before phosphorite direct flotation operation |
| CN110455781A (en) * | 2019-08-26 | 2019-11-15 | 云南磷化集团有限公司 | For the LIBS on-line detecting system of flotation of phosphate rock system and its application |
| CN112547314A (en) * | 2020-11-18 | 2021-03-26 | 云南磷化集团有限公司 | Full-quantity resource production method of siliceous and silicate refractory collophanite |
| WO2024040893A1 (en) * | 2022-08-26 | 2024-02-29 | 广东邦普循环科技有限公司 | Method for purifying and whitening phosphogypsum |
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Application publication date: 20121003 |