CN106315530B - A kind of processing method of phosphorite tailings - Google Patents
A kind of processing method of phosphorite tailings Download PDFInfo
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- CN106315530B CN106315530B CN201510374405.6A CN201510374405A CN106315530B CN 106315530 B CN106315530 B CN 106315530B CN 201510374405 A CN201510374405 A CN 201510374405A CN 106315530 B CN106315530 B CN 106315530B
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Abstract
The present invention relates to a kind of processing methods of phosphorite tailings, and the phosphorite tailings generated after sulfur acid pretreatment are first carried out calcining digestion, and the processing mode for then recycling two steps to leach, the magnesium elements being sufficiently separated in phosphorus tailing improve phosphorus tailing quality；And waste liquid, the waste gas recovery generated in the process, treated, and solvent recycles, filtrate after acquisition high-quality phosphorus ore is subjected to subsequent processing, make the calcium obtained, magnesium products can be with further progress application, effective recycling not only has been carried out to calcium magnesium element, waste liquid, the discharge of exhaust gas and the accumulation of tailing are also avoided, the improvement of ecological environment is conducive to.
Description
Technical field
The present invention relates to phosphate ore processing processing technology field more particularly to a kind of processing methods of phosphorite tailings.
Technical background
Phosphorus ore reserves huge but mined phosphorus ore grade in China's is lower, and mineral grain is thin, embedding cloth is close, association magnesium
Equal impurity are higher.The phosphorus ore after exploitation is pre-processed in tradition, then carries out the production of next step product, is come with this
The content of the impurity such as magnesium in phosphorus ore is reduced, and then achievees the purpose that purify phosphorus ore, improves the quality of phosphorus ore, reduces subsequent to phosphorus ore
Or phosphoric acid by wet process utilizes the difficulty and energy consumption of phosphorus ore；The ore dressing of China's phosphorus ore mainly uses the methods of flotation, reverse flotation at present,
But the content of MgO is difficult to drop to 1% hereinafter, and P2O5Loss it is higher.Therefore, not only phosphorus loss is big for conventional beneficiation method,
And its tailing overwhelming majority heap is stored in Tailings Dam, and there are larger environmental risks.
Since the composition of various regions phosphorus ore is different, the composition difference of phosphorite tailings is also larger, therefore for the comprehensive of phosphorite tailings
Close utilization ways it is also not the same, such as with making cement, air entrained concrete, devitrified glass product raw material, to siliceous high phosphorus
Ingredient of the mine tailing for calcium magnesium phosphate or kiln-process phosphoric acid.The composition of Guizhou phosphorus ore mainly has dolomite and a small amount of apatite, existing
Have in technology, calcium superphosphate (magnesium) fertilizer is produced using the method that Mixed phosphoric acid and sulfuric acid decomposes tailing, although can be to a certain extent
The Utilizing question of phosphorite tailings is solved, but a large amount of sulfuric acid of consumption, phosphoric acid go processing to be equivalent to the tailing of dolomite and obtain phosphorus magnesium
Fertilizer does not conform to convention, and normal superphosphate physical property is poor currently on the market, and quality need to be wait further increase.In addition at sulfuric acid
A large amount of ardealite will be generated after reason, and ardealite discharge will will cause the serious pollution of environment, and magnesium in the natural environment
Equal elements do not reach in tailing to be efficiently separated, and then the quality for resulting in the tailing after sulfur acid pretreatment does not improve, and reaches
Less than screening concentrate, the purpose of comprehensive utilization；And in treatment process, after forming micro-soluble material due to calcium sulfate, keep sulfuric acid difficult
It is recycled with return, the cost in turn resulted in progress tailing preprocessing process is larger.CN85107209 is disclosed
A kind of method of chemical sepn, by after phosphorus ore radiation roasting in such a way that ammonium chloride and ammonium nitrate mix leaching
Separating magnesium utilizes to improve quality and the by-product recovery of low-grade phosphate ore and provides a kind of processing mode, but in engineering
In, due in ammonium chloride chloride ion and nitrate anion stainless steel equipment can be corroded, be difficult carry out largely and hold
The processing of continuous property so having particular requirement to the material of equipment, and cannot be applied in practical mass production with economic extensively.
For this purpose, this researcher passes through to form and content etc. existing for phosphorus pentoxide in phosphorite tailings, calcium, magnesium elements
Analysis and discussion is carried out, and traditional tailing processing technology is adjusted, is combined into using nitric acid and ammonium nitrate solution
After combined processing liquid, then phosphorite tailings are pre-processed, improves P in tailing2O5Content, then further use ammonium sulfate
The method of leaching leaches magnesium elements sufficiently, so as to improve the quality of tailing；Finally to the ammonium salt leaching liquid after separation
It is handled, obtains calcium, magnesium products.At present for using nitric acid and ammonium nitrate to process phosphorite tailings, and effectively return
The processing method for receiving calcium and magnesium yet there are no document report.
Summary of the invention
The present invention provides a kind of processing of phosphorite tailings, and step of preparation process is simple, and process flow is short, the processing of consumption
Liquid can recycle, the discharge of no exhaust gas, waste liquid, waste residue, and can be improved the quality and quality of low-grade phosphorus tailing, reach
The purpose utilized to resource of tailings, and calcium, magnesium products can be obtained, improve the added value of technique.
Specific technical solution is as follows:
A kind of processing method of phosphorite tailings, which comprises the following steps:
(1) phosphorus ore after exploitation is subjected at 1000-1200 DEG C calcining 45-75min, then uses 60-100 DEG C of hot water
It is digested；
(2) nitre of ammonium nitrate solution and 50%-75% that concentration is 30%-50% is added in the tailing for completing digestion process
Acid solution, stir process 60-80min under room temperature；
(3) by step (2) leaching, treated that slurry is filtered, washs, and obtains leached mud and leachate；
(4) the leached mud ammonium sulfate of 20-30% is leached into 60-80min in 70-90 DEG C of at a temperature of stirring；Leaching
Mixed liquor after taking is filtered, washed, and obtains filter residue and ammonium sulfate leaching liquid；Filter residue is dried at 100 DEG C or more, obtains phosphorus essence
Mine；
(5) ammonia generated in the carbon dioxide and step (2), (4) leaching process of step (1) calcining generation is passed into
It in absorption tower, is handled using water absorption, obtains sal volatile；
(6) the sal volatile adjustment concentration obtained step (5) is 20-35%, the sulfuric acid then obtained with step (4)
The mixing of ammonium leaching liquid, 50-70 DEG C at a temperature of be stirred to react 40-60min, reaction solution is filtered, washed, and filtrate and cleaning solution are mixed
It returns after conjunction and is recycled in sulphur ammonium leaching step；Calcining is after filter cake drying to get magnesia；
(7) sal volatile that concentration is 20-35% is added in the leachate for obtaining step (3), in 50-70 DEG C of temperature
Under be stirred to react 40-60min；Mixed liquor after reaction is filtered, washed, and returns to leaching step after ammonium nitrate filtrate and cleaning solution mixing
Middle recycling；Filter cake after leaching is dried to get calcium carbonate.
The dosage of ammonium nitrate is that 1.0-1.5kg is added according to every 1kg phosphorus tailing in the step (2), and nitric acid solution adds
Entering amount is that 100-120g is added according to every 1kg phosphorus tailing.
Ammonium sulfate dosage is that 1.0-1.2kg is added according to every 1kg phosphorus tailing in the step (4).
The dosage of ammonium carbonate is that 0.8-1.2kg is added according to every 1kg phosphorus tailing in the step (6).
The dosage of ammonium carbonate is that 1.2-1.5kg is added according to every 1kg phosphorus tailing in the step (7).
The dosage of water is that every 1kg phosphorus tailing uses 1.0-1.2L water in water digestion process in the step (1).
The step (2), (4), (6), the stirring in (7) are to be suspended in treated substance sufficiently in treatment fluid.
In the above-mentioned scheme using the compound leaching processing tailing of ammonium nitrate solution and nitric acid solution, it can take ammonium nitrate
Solution is charged first in tailing, then nitric acid solution is added in tailing；Or nitric acid solution and ammonium nitrate solution are mixed
It closes and then adds it in tailing and leached.
Compared with prior art, the invention has the following beneficial effects:
(1) present invention by calcining digestion process, accelerate the decomposable process of calcium carbonate and magnesium carbonate, in conjunction with ammonium nitrate solution with
The combined-circulation leaching mode of nitric acid solution and the further leaching processing of ammonium sulfate, so that magnesium elements are adequately soaked
It takes, makes P2O5Content improve to 32% or more, content of magnesium is reduced to≤1.5%, improves tailing quality, fills resource
Divide and utilizes；
(2) ammonia of output in the exhaust gas and leaching process generated in calcination process is absorbed and utilized in the present invention,
In addition ammonium bicarbonate treated filtrate and cleaning solution are recycled, have prevented the discharge of waste liquid, exhaust gas, has greatly protected
Environment adapts to the development need of ecological environment from now on；
(3) two steps are leached into the filter residue after obtaining high-quality phosphorus ore or filtrate carry out subsequent processing, obtain calcium carbonate and
Magnesia has not only carried out effective recycling to calcium magnesium element, make obtain calcium and magnesium product can with further progress application,
The accumulation that phosphorite tailings can also be greatly reduced not only improves resource regeneration, improves value-added content of product, and is conducive to environment guarantor
Shield；
(4) the process step of the invention is simple, and process cycle is short, and low energy consumption in treatment process, and raw material especially leaches
Agent can be partially recovered and recycle, and reduce pretreated cost；And there is no exhaust gas, waste liquid, waste residue in treatment process
Discharge, improve the added value of product of entire technique；
(5) present invention substitutes traditional sulfuric acid treating processes using the compound leaching of ammonium nitrate and nitric acid, reduces ardealite
Discharge amount, avoid ardealite it is a large amount of stockpiling give environment bring pollution, have the significant value of environmental protection and economic benefit.
Technical solution of the present invention is further elaborated using test below, to prove effect of the invention.
It selects the phosphorite tailings in Guizhou Wanshan Mountain area as experimental raw, and every ingredient in phosphorus tailing is examined
It surveys, obtains raw material composition as shown in Table 1:
Table 1
| Ingredient | P2O5 | CaO | MgO | Fe2O3 | Al2O3 | F | AI | It burns and loses |
| % | 7.05 | 34.16 | 18.47 | 0.25 | 0.26 | 0.81 | 3.53 | 38.4 |
1 technical study of test example
1.1 calcining digestion
By the calcining of phosphorus mine tailing, digestion, following reaction occurs:
CaCO3·MgCO3→CaO+MgO+2CO2
CaO+MgO+2H2O→Ca(OH)2+Mg(OH)2
45-75min is handled in 1000-1200 DEG C of temperature lower calcination, guarantees abundant decomposition, the abjection of calcium carbonate and magnesium carbonate.
The compound leaching of 1.2 ammonium nitrate, nitric acid
Take calcining digestion process after phosphorus tailing, investigate respectively different ammonium nitrate dosages (0.8kg, 1kg, 1.2kg,
1.5kg), concentration (20%, 30%, 40%, 50%, 60%), leaching temperature (room temperature, 65-75 DEG C, 85-90 DEG C), leaching time
(50min, 60min, 70min, 80min, 90min), concentration of nitric acid (40%, 50%, 60%, 75%, 85%), dosage (80g,
100g, 120g, 150g) etc. factors to P2O5The influence of content, investigate the result shows that, select the dosage of ammonium nitrate for according to every 1kg
1.0-1.5kg, concentration 30%-50% is added in phosphorus tailing, and the additional amount of nitric acid solution is that 100- is added according to every 1kg phosphorus tailing
120kg, concentration 50%-75% leach 60-80min, and leaching temperature is room temperature, P2O5Content is improved to 33.58%.It is preferred that nitric acid
The dosage of ammonium is that 100g, concentration 30% are added according to every 1kg phosphorus tailing, and the additional amount of nitric acid solution is according to every 1kg phosphorus tailing
120g, concentration 65% is added, leaches 60min.
Reaction equation is as follows:
Ca(OH)2+NH4NO3+HNO3→Ca(NO3)2+NH3+2H2O
1.3 ammonium sulfate leach magnesium
Leached mud after taking the compound leaching of ammonium nitrate, nitric acid, then leach magnesium with ammonium sulfate, ammonium sulfate dosage is respectively 0.9,
1.0,1.1,1.2,1.3kg is tested, the results showed that, calcium leaching rate influences less, but the leaching rate of magnesium dramatically increases, preferably
Ammonium sulfate dosage is 1.0-1.2kg, and for the total leaching rate of magnesium up to 89.2-99.3%, more preferable dosage is 1.2kg.
Reaction equation is as follows:
Mg(OH)2+(NH4)2SO4→MgSO4+2NH3+2H2O
2 process certification of test example
Phosphorus tailing 1kg is taken respectively, is handled according to the method for 1-3 of the embodiment of the present invention, then to five oxygen in phosphorus concentrate
The content of the content and magnesia of changing two phosphorus is detected, and is obtained: the content of phosphorus pentoxide is 33.1-34.7%, magnesia
Content be 1.15-1.34%；As it can be seen that the technical solution of the invention enables to the content of the phosphorus pentoxide in phosphorus tailing
It improves to 32% or more, content of magnesium in phosphorus tailing can be reduced to≤1.5%；Achieve the purpose that recycling, reduces phosphorus
The waste residue saturation of mine advanced treating, reduces environmental pollution.
Also, calcium carbonate content is 91.6% in subsequent heavy calcium, magnesium sinking treated residue, and content of magnesia is
94.5%, subsequent processing can be carried out to it, further obtain the products such as calcium and magnesium compound fertilizer, produced after improving phosphorus ore pretreatment
The added value of product.
In addition, carrying out the work under laboratory condition by the phosphorite tailings to other areas such as Fuquan area, Kaiyang Region
Skill verifying, technical solution of the present invention is equally applicable to the processing and utilization of above-mentioned regional phosphorite tailings as the result is shown, can be obtained five
Phosphorus concentrate of two phosphorus contents 32% or more is aoxidized, and calcium, magnesium are recycled, the production such as calcium and magnesium compound fertilizer can further be made
Product, while also resource is sufficiently recycled, there is no the discharge of exhaust gas, waste liquid, waste residue in treatment process, improves entire technique
Added value of product.
Specific embodiment:
It is limited below with reference to specific embodiment technical solution of the present invention is further, but claimed
Range is not only limited to made description.
Embodiment 1
A kind of processing method of phosphorite tailings, which comprises the following steps:
(1) phosphorus ore after exploitation is subjected at 1000 DEG C calcining 75min, is then digested with 60 DEG C of hot water；
(2) concentration is added for 30% ammonium nitrate solution and 50% nitric acid solution, often in the tailing for completing digestion process
The lower stir process 80min of temperature；
(3) by step (2) leaching, treated that slurry is filtered, washs, and obtains leached mud and leachate；
(4) 20% ammonium sulfate of leached mud is leached into 60min in 90 DEG C of at a temperature of stirring；Mixing after leaching
Liquid is filtered, washed, and obtains filter residue and ammonium sulfate leaching liquid；Filter residue is dried at 100 DEG C or more, obtains phosphorus concentrate；
(5) ammonia generated in the carbon dioxide and step (2), (4) leaching process of step (1) calcining generation is passed into
It in absorption tower, is handled using water absorption, obtains sal volatile；
(6) the sal volatile adjustment concentration obtained step (5) is 20%, the ammonium sulfate then obtained with step (4)
Leaching liquid mixing, 50 DEG C at a temperature of be stirred to react 60min, reaction solution is filtered, washed, filtrate and cleaning solution mixing after return
It is recycled in sulphur ammonium leaching step；Calcining is after filter cake drying to get magnesia；
(7) by step (3) obtain leachate be added concentration be 20% sal volatile, 50 DEG C at a temperature of stir
React 60min；Mixed liquor after reaction is filtered, washed, and returning to recycle in leaching step after ammonium nitrate filtrate and cleaning solution mixing makes
With；Filter cake after leaching is dried to get calcium carbonate.
The dosage of ammonium nitrate is that 1.0kg, the additional amount of nitric acid solution is added according to every 1kg phosphorus tailing in the step (2)
For 100g is added according to every 1kg phosphorus tailing.
Ammonium sulfate dosage is that 1.0kg is added according to every 1kg phosphorus tailing in the step (4).
The dosage of ammonium carbonate is that 0.8kg is added according to every 1kg phosphorus tailing in the step (6).
The dosage of ammonium carbonate is that 1.2kg is added according to every 1kg phosphorus tailing in the step (7).
The dosage of water is that every 1kg phosphorus tailing uses 1.0L water in water digestion process in the step (1).
The step (2), (4), (6), the stirring in (7) are to be suspended in treated substance sufficiently in treatment fluid.
Processing result: P in phosphorus concentrate2O5Content 33.1%, content of magnesium 1.34%；Calcium carbonate content 92.3%；Magnesia
Content 94.7%.
Embodiment 2
A kind of processing method of phosphorite tailings, which comprises the following steps:
(1) phosphorus ore after exploitation is subjected at 1100 DEG C calcining 60min, is then digested with 80 DEG C of hot water；
(2) concentration is added for 40% ammonium nitrate solution and 65% nitric acid solution, often in the tailing for completing digestion process
The lower stir process 70min of temperature；
(3) by step (2) leaching, treated that slurry is filtered, washs, and obtains leached mud and leachate；
(4) 30% ammonium sulfate of leached mud is leached into 70min in 80 DEG C of at a temperature of stirring；Mixing after leaching
Liquid is filtered, washed, and obtains filter residue and ammonium sulfate leaching liquid；Filter residue is dried at 100 DEG C or more, obtains phosphorus concentrate；
(5) ammonia generated in the carbon dioxide and step (2), (4) leaching process of step (1) calcining generation is passed into
It in absorption tower, is handled using water absorption, obtains sal volatile；
(6) the sal volatile adjustment concentration obtained step (5) is 30%, the ammonium sulfate then obtained with step (4)
Leaching liquid mixing, 60 DEG C at a temperature of be stirred to react 50min, reaction solution is filtered, washed, filtrate and cleaning solution mixing after return
It is recycled in sulphur ammonium leaching step；Calcining is after filter cake drying to get magnesia；
(7) by step (3) obtain leachate be added concentration be 30% sal volatile, 60 DEG C at a temperature of stir
React 50min；Mixed liquor after reaction is filtered, washed, and returning to recycle in leaching step after ammonium nitrate filtrate and cleaning solution mixing makes
With；Filter cake after leaching is dried to get calcium carbonate.
The dosage of ammonium nitrate is that 1.2kg, the additional amount of nitric acid solution is added according to every 1kg phosphorus tailing in the step (2)
For 120g is added according to every 1kg phosphorus tailing.
Ammonium sulfate dosage is that 1.2kg is added according to every 1kg phosphorus tailing in the step (4).
The dosage of ammonium carbonate is that 1.0kg is added according to every 1kg phosphorus tailing in the step (6).
The dosage of ammonium carbonate is that 1.2kg is added according to every 1kg phosphorus tailing in the step (7).
The dosage of water is that every 1kg phosphorus tailing uses 1.2L water in water digestion process in the step (1).
The step (2), (4), (6), the stirring in (7) are to be suspended in treated substance sufficiently in treatment fluid.
Processing result: P in phosphorus concentrate2O5Content 34.7%, content of magnesium 1.15%；Calcium carbonate content 91.7%；Magnesia
Content 94.4%.
Embodiment 3
A kind of processing method of phosphorite tailings, which comprises the following steps:
(1) phosphorus ore after exploitation is subjected at 1200 DEG C calcining 45min, is then digested with 100 DEG C of hot water；
(2) concentration is added for 50% ammonium nitrate solution and 75% nitric acid solution, often in the tailing for completing digestion process
The lower stir process 60min of temperature；
(3) by step (2) leaching, treated that slurry is filtered, washs, and obtains leached mud and leachate；
(4) 30% ammonium sulfate of leached mud is leached into 80min in 70 DEG C of at a temperature of stirring；Mixing after leaching
Liquid is filtered, washed, and obtains filter residue and ammonium sulfate leaching liquid；Filter residue is dried at 100 DEG C or more, obtains phosphorus concentrate；
(5) ammonia generated in the carbon dioxide and step (2), (4) leaching process of step (1) calcining generation is passed into
It in absorption tower, is handled using water absorption, obtains sal volatile；
(6) the sal volatile adjustment concentration obtained step (5) is 35%, the ammonium sulfate then obtained with step (4)
Leaching liquid mixing, 50 DEG C at a temperature of be stirred to react 40min, reaction solution is filtered, washed, filtrate and cleaning solution mixing after return
It is recycled in sulphur ammonium leaching step；Calcining is after filter cake drying to get magnesia；
(7) by step (3) obtain leachate be added concentration be 35% sal volatile, 50 DEG C at a temperature of stir
React 60min；Mixed liquor after reaction is filtered, washed, and returning to recycle in leaching step after ammonium nitrate filtrate and cleaning solution mixing makes
With；Filter cake after leaching is dried to get calcium carbonate.
The dosage of ammonium nitrate is that 1.5kg, the additional amount of nitric acid solution is added according to every 1kg phosphorus tailing in the step (2)
For 120g is added according to every 1kg phosphorus tailing.
Ammonium sulfate dosage is that 1.2kg is added according to every 1kg phosphorus tailing in the step (4).
The dosage of ammonium carbonate is that 1.2kg is added according to every 1kg phosphorus tailing in the step (6).
The dosage of ammonium carbonate is that 1.5kg is added according to every 1kg phosphorus tailing in the step (7).
The dosage of water is that every 1kg phosphorus tailing uses 1.2L water in water digestion process in the step (1).
The step (2), (4), (6), the stirring in (7) are to be suspended in treated substance sufficiently in treatment fluid.
Processing result: P in phosphorus concentrate2O5Content 33.7%, content of magnesium 1.22%；Calcium carbonate content 92.0%；Magnesia
Content 94.5%.
Claims (2)
1. a kind of processing method of phosphorite tailings, which comprises the following steps:
(1) phosphorus ore after exploitation is subjected at 1000-1200 DEG C calcining 45-75min, is then carried out with 60-100 DEG C of hot water
Digestion；The dosage of the hot water is that every 1kg phosphorus tailing uses 1.0-1.2L water；
(2) it is molten for the ammonium nitrate solution of 30%-50% and the nitric acid of 50%-75% that concentration is added in the tailing for completing digestion process
Liquid, stir process 60-80min under room temperature；The dosage of the ammonium nitrate is that 1.0-1.5kg, nitric acid is added according to every 1kg phosphorus tailing
The additional amount of solution is that 100-120g is added according to every 1kg phosphorus tailing；
(3) by step (2) leaching, treated that slurry is filtered, washs, and obtains leached mud and leachate；
(4) the leached mud ammonium sulfate of 20-30% is leached into 60-80min in 70-90 DEG C of at a temperature of stirring；After leaching
Mixed liquor be filtered, washed, obtain filter residue and ammonium sulfate leaching liquid；Filter residue is dried at 100 DEG C or more, obtains phosphorus concentrate；
The ammonium sulfate dosage is that 1.0-1.2kg is added according to every 1kg phosphorus tailing；
(5) ammonia generated in the carbon dioxide of step (1) calcining generation and step (2), (4) leaching process is passed into absorption
It in tower, is handled using water absorption, obtains sal volatile；
(6) the sal volatile adjustment concentration obtained step (5) is 20-35%, and the ammonium sulfate then obtained with step (4) soaks
Take liquid to mix, 50-70 DEG C at a temperature of be stirred to react 40-60min, reaction solution is filtered, washed, filtrate and cleaning solution mixing after
It returns and is recycled in sulphur ammonium leaching step；Calcining is after filter cake drying to get magnesia；The dosage of the ammonium carbonate is according to every
0.8-1.2kg is added in 1kg phosphorus tailing；
(7) by step (3) obtain leachate be added concentration be 20-35% sal volatile, 50-70 DEG C at a temperature of stir
Mix reaction 40-60min；Mixed liquor after reaction is filtered, washed, and is returned after ammonium nitrate filtrate and cleaning solution mixing and is followed in leaching step
Ring uses；Filter cake after leaching is dried to get calcium carbonate；The dosage of the ammonium carbonate is that 1.2- is added according to every 1kg phosphorus tailing
1.5kg。
2. the processing method of phosphorite tailings as described in claim 1, it is characterised in that: the step (2), (4), (6), (7)
In stirring be to be suspended in treated substance sufficiently in treatment fluid.
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| CN109336072A (en) * | 2018-09-30 | 2019-02-15 | 贵州芭田生态工程有限公司 | Phosphorus ore calcines utilization method and phosphorus concentrate of exhaust gas washing water and preparation method thereof |
| CN109351481B (en) * | 2018-11-29 | 2020-10-16 | 长沙矿冶研究院有限责任公司 | Phosphorite calcining-digesting-reverse flotation separation process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85107209A (en) * | 1985-09-24 | 1986-05-10 | 陕西省化学肥料工业公司 | The low grade calcareous phosphorous ore fractionation |
| CN102557086A (en) * | 2012-02-18 | 2012-07-11 | 贵州大学 | Method for recovering phosphorus from phosphorite tailings and preparing light magnesium oxide |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3635669A (en) * | 1968-12-26 | 1972-01-18 | B D Bohna & Co Inc | Method of producing concentrated phosphoric acid compounds from phosphate rock |
| CN85100187B (en) * | 1985-04-01 | 1985-09-10 | 陕西省化学肥料工业公司 | Process for chemcial separation of phosphate ore |
| US5500193A (en) * | 1993-06-14 | 1996-03-19 | University Of South Florida | Method for ION exchange based leaching of the carbonates of calcium and magnesium from phosphate rock |
| CN101624196A (en) * | 2008-07-10 | 2010-01-13 | 朱作远 | Hydrochloric acid-ammonium salt circulation method phosphorite comprehensive utilization clean production technology |
| CN102320872A (en) * | 2011-07-18 | 2012-01-18 | 贵州省化工研究院 | Method for producing high-water-solubility nitric phosphate fertilizer by decomposing phosphate ores with nitric acid and circulating ammonium sulfate |
-
2015
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85107209A (en) * | 1985-09-24 | 1986-05-10 | 陕西省化学肥料工业公司 | The low grade calcareous phosphorous ore fractionation |
| CN102557086A (en) * | 2012-02-18 | 2012-07-11 | 贵州大学 | Method for recovering phosphorus from phosphorite tailings and preparing light magnesium oxide |
Non-Patent Citations (1)
| Title |
|---|
| "磷矿浮选尾矿煅烧铵盐法实验研究";黄芳等;《化工矿物与加工》;20100115(第1期);第11-12页 * |
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