CN100392124C - Method of retrieving magnesium from high magnesium phosphorus ore - Google Patents
Method of retrieving magnesium from high magnesium phosphorus ore Download PDFInfo
- Publication number
- CN100392124C CN100392124C CNB2006100216478A CN200610021647A CN100392124C CN 100392124 C CN100392124 C CN 100392124C CN B2006100216478 A CNB2006100216478 A CN B2006100216478A CN 200610021647 A CN200610021647 A CN 200610021647A CN 100392124 C CN100392124 C CN 100392124C
- Authority
- CN
- China
- Prior art keywords
- magnesium
- phosphorus ore
- magging
- processing method
- slip
- 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.)
- Expired - Fee Related
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Manufacture And Refinement Of Metals (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The invention discloses a recycling method of magnesium from high-magnesium-phosphorus ore, which is characterized by the following: predisposing raw material (phosphorus ore); stripping magnesium of high-magnesium-phosphorus ore through composite demagnesium agent; solving the magnesium; separating slurry to obtain the demagnesium concentrate as raw material of phosphorus material; making liquid phase as demagnesium slurry; entering the next reacting procedure; adding neutralizing sediment agent; adjusting pH value to do sediment reaction; separating to remove liquid in the filter; drying sediment magnesium hydroxide to obtain the magnesium hydroxide; recycling liquid in the main flow path.
Description
Technical field
The present invention relates to technical field of phosphorous chemical industry, more particularly, relate to a kind of in the process of producing phosphorus product, removing and reclaim magnesium resource in the phosphorus ore, reduce the processing method of phosphorus product Mg content.
Background technology:
Be that raw material production prepares in the production process of phosphorus product with the phosphorus ore, when the phosphorus in the phosphorus ore is extracted, if the magnesium component enters the extraction liquid phase in large quantities, to not only can have a strong impact on phosphorus product crystallization and filtration, make to produce and be difficult to carry out, and can reduce phosphorus content in the phosphorus product, influence the phosphorus product quality.Along with the development of phosphorus chemical industry, phosphorus ore raw material consumption is increasing, the dilution gradually of world's phosphorus ore, and the phosphorus ore grade reduces gradually, and magnesium content also raises relatively, belongs to height and contains the magnesium phosphorus ore.On the other hand, also there is a large amount of low-grade phosphorus ores in the world, and as China, low-grade phosphate ore is more than 50%.These low-grade phosphorus ores generally also all belong to height and contain the magnesium phosphorus ore, are called for short high-magnesium-phosphorus ore.In the phosphorous chemical industry field, generally MgO in the Rock Phosphate (72Min BPL) and P
2O
5Ratio classify as high-magnesium-phosphorus ore greater than 10% phosphorus ore.The de-magging of high-magnesium-phosphorus ore all compares difficulty, and particularly high magnesium collophanite because the magnesium-containing mineral disseminated grain size is very thin, is difficult to the magnesium in the phosphorus ore is deviate from conventional beneficiation method, and de-magging is difficulty particularly.Magnesium in the phosphorus ore is serious to the quality influence of the production of phosphorus product and phosphorus product, therefore, how to remove the magnesium in the high-magnesium-phosphorus ore, and high-magnesium-phosphorus ore is treated as concentrate through ore dressing, is the popular research topic that present technique field technology personnel are concerned about always.For the de-magging ore dressing of the easy ore dressing in the high-magnesium-phosphorus ore, the external at present general photoelectricity sorting process method that adopts.This processing method is insufficient to be that investment is big.Domestic general employing reverse floatation process method, the domestic insufficient place of this processing method are that the rate of recovery of phosphorus is not high, and the rate of recovery of phosphorus is the highest to be no more than 80%.For the de-magging ore dressing of high magnesium collophanite, all there are some units this to be done some researchs both at home and abroad, proposed to remove magnesium in the phosphorus ore discharging of in the de-magging liquid and back with weak acid.Taking weak acid de-magging processing method, when the content of calcium in the phosphorus ore is higher, be de-magging weak acid usually with the dilute sulphuric acid, but the vitriolic consumption is big, the production cost height, be difficult to economically by; If with phosphoric acid is de-magging weak acid, utilize phosphoric acid that phosphorus ore is carried out pre-preg, can take off a part of magnesium, though magnesium does not enter extraction and filters workshop section, the production process of phosphorus product is gone on, magnesium can enter product phosphoric acid.The weak acid de-magging processing method of prior art can not reclaim magnesium to greatest extent, effectively, and the phosphoric acid product impurity of being produced is more, and product is difficult to reach the industrial raw material level, and the raw material that only can be used as fertilizer uses.And under many circumstances,, be difficult to handle, so, environment is polluted generally with its discharging because its water content is bigger.Therefore, for the de-magging ore dressing of difficult ore dressing in the high-magnesium-phosphorus ore, prior art is the good method of none also, is still the technical barrier of the field technique personnel solution of band ability.
Content of the present invention:
At the U.S. phosphorus ore de-magging of high the deficiencies in the prior art, purpose of the present invention aims to provide a kind of magnesium that reclaims in the high U.S. phosphorus ore that both can remove, and the loss of phosphorus is low, and demagnesium rate can reach 80%～95%, and the phosphorus loss only is 0.5%～2.6% the processing method that reclaims magnesium from high-magnesium-phosphorus ore.
Basic thought of the present invention is, subtractive process with compound de-magging agent strengthen magnesium, make the magnesium of deviating from be retained in the solution as much as possible, adopting cheap calcium hydroxide neutralization precipitation agent such as (milk of limes) to make magnesium hydroxide separate out the sedimentary while, avoid calcium salt to separate out as much as possible, increase the amount of separating out of magnesium, make magnesium hydroxide products reach the technical grade specification.
Realize the processing method that reclaims magnesium from high-magnesium-phosphorus ore of above-mentioned purpose of the present invention, its concrete technical scheme is as follows:
The processing method that reclaims magnesium from high-magnesium-phosphorus ore mainly comprises following processing step:
1, will contain magnesium phosphorus ore powder and compound de-magging agent and insert the mixing of de-magnesium reaction device, add water and adjust pH to 3～4, react 30～120min under 50～70 ℃ of conditions, remove the magnesium in the phosphorus ore, described compound de-magging agent contains sulfuric acid and is selected from a kind of component in disodium ethylene diamine tetraacetate and the nitric acid at least;
2, de-magnesium reaction carries out solid-liquid separation after finishing, and solid phase is for removing the smart phosphorus ore of magnesium, and liquid phase is the de-magging slip, and the de-magging slip enters next process;
3, precipitin reaction is carried out in de-magging slip adding neutralization precipitation agent adjustment pH to 8～14, and precipitation is separated out magnesium hydroxide, and at 30～60 ℃ of following precipitin reaction 40～90min, precipitation is separated out magnesium hydroxide;
4, the precipitation slip after the precipitin reaction end is carried out solid-liquid separation, solid phase is a magnesium hydroxide, promptly prepares magnesium hydroxide products after drying.
In the above-mentioned processing method that from high-magnesium-phosphorus ore, reclaims magnesium, for the liquid phase of the precipitation slip after the precipitin reaction end through the solid-liquid separation gained, preferably making it turn back to the de-magnesium reaction operation recycles, this both can make compound de-magging agent obtain recycle, reclaim magnesium resource, can avoid again the discharging of separating, washing liquid is polluted environment.
In technique scheme, described compound de-magging agent is except sulfuric acid and be selected from least a kind of in disodium ethylene diamine tetraacetate (EDTA) and the nitric acid, also can contain silicofluoric acid.Wherein the sulfuric acid weight content is 2～5 times of other composition weight content sums, and each component of disodium ethylene diamine tetraacetate, silicofluoric acid and nitric acid shared proportion in compound de-magging agent is not more than 30% of compound de-magging agent gross weight.The selection component can be a kind of component in them, also can be two kinds of components in them, can also select three kinds of components simultaneously.Because the vitriolic price is lower, in order to reduce production costs, in compound de-magging agent, can select more sulfuric acid for use, so being defined as other, the vitriolic weight content respectively selects 2～5 times of composition weight content sum.Based on same reason,,, in compound de-magging agent, can select less disodium ethylene diamine tetraacetate for use in order to reduce production costs because the price of disodium ethylene diamine tetraacetate is higher.Usually the weight content of disodium ethylene diamine tetraacetate can be 2～6% of compound de-magging agent gross weight.
In technique scheme, the neutralization precipitation agent that is used for the de-magging slip is carried out precipitin reaction is selected from milk of lime, sodium hydroxide solution and ammoniacal liquor.The weight concentration of milk of lime is generally 10～20%, and the sodium hydroxide solution weight concentration is generally 5～20%, and ammoniacal liquor is commercially available ammoniacal liquor.The neutralization precipitation agent can be not add with the form of solution yet, and directly adds with the solid form.
In technique scheme, the solid-liquid separation after de-magnesium reaction finishes adopts the mode of vacuum filtration that the smart phosphorus ore of de-magging is carried out solid-liquid separation mutually with the de-magging slip.Can certainly other mode separate, as separating in settled mode.
In technique scheme, after with the neutralization precipitation agent de-magging slip being carried out precipitin reaction and finishes, the precipitation slip is carried out the solid-liquid separation washing in the mode of media filtration, filtered wash solution is turned back to the de-magnesium reaction operation recycle.In like manner also can other mode carry out solid-liquid separation, carry out solid-liquid separation as mode with spiral centrifugal settling.
In technique scheme, contain magnesium phosphorus ore powder and be particle diameter and be not more than 200 purpose ratios and be no less than 85%.
In technique scheme, separating obtained magnesium hydroxide is dry many and 30min under 60～100 ℃ of conditions.
Technical process of the present invention can be divided into de-magging substantially and reclaim two parts of magnesium.Wherein the de-magging mechanism of de-magging part is as follows:
Magnesium in the phosphorus ore mainly exists with the form of rhombspar, phosphorus ore under the effect of compound de-magging agent in the molten dephosphorization ore deposit in the magnesium calcium also be dissolved, wherein precipitate under the effect of sulfuric acid of calcium in compound de-magging agent.The precipitin reaction formula is:
Ca+2+SO42-+2H2O＝CaSO4·2H2O↓
Magnesium ion is wherein stayed in the solution by complexing or combined.Process to the magnesium keying action can simply be expressed as follows,
Mg2++X2-＝XMg
Wherein X is a de-magging agent main body.
High-magnesium-phosphorus ore stone is behind de-magnesium reaction, and from the slip that the de-magnesium reaction groove comes out, separation is removed the remaining solid of liquid and is the de-magging concentrate after filtration, can be used as the usefulness of phosphoric acid extraction.The de-magging slip enters into precipitation tank in term, adds neutralization-precipitation reaction agent adjustment pH and carries out precipitin reaction, and the reaction end separates through filter removes liquid, and solid sediment is magnesium hydroxide, can get finished product after drying.Liquid returns main flow and reuses.High-magnesium-phosphorus ore stone is after the processing method that the present invention discloses is handled, and demagnesium rate can reach 80%～95%, and the phosphorus loss only is about 0.5%～2.6%.
The magnesium products that processing method reclaimed that adopts the present invention to disclose is a magnesium hydroxide, and its magnesium hydroxide content can reach more than 90%, and shape is mainly sheet, micro crystal or smectic must shape.The heat decomposition temperature of magnesium hydroxide is 340～490 ℃, and the deacidification of the pyrolysate MgO of magnesium hydroxide is can force rate Al2O3 strong, can be quickly in and the sour gas that produces in the plastics combustion processes.Its deacidification and press down the cigarette ability and all be better than the very big aluminium hydroxide of sales volume in the market.The crystalline form of magnesium hydroxide is generally hexagonal structure or amorphous granular,, has dispersiveness and consistency preferably in resin, and has strengthening action for well with six square shape sheets and whisker shape.Therefore, the present invention reclaim the magnesium hydroxide products produce can be used as fire-retardant, press down the mixing machine-shaping that additives such as cigarette, resistance drip, filling are used for plastics and rubber, advantage such as have, safety, price are low.
High U.S. phosphorus ore adopts processing method of the present invention to carry out the recovery of magnesium, can obtain good economic benefits.With 10,000 tons of high contents of calcium and magnesium ore deposits of year treatment capacity be example estimate (P2O517% in the phosphorus ore, MgO4% CaO34%), produce 1620 tons of magnesium hydroxides per year, and facility investment is about 800,000, about 2565 yuan of production cost, about 4000 yuan/ton of market price, total profits tax is 2,320,000 yuan.Ore dressing investment and working cost have been saved, simultaneously the smart phosphorus ore of 10,000 tons low magnesium of output.
Description of drawings:
Accompanying drawing 1 is a flow process principle schematic of the present invention
Accompanying drawing 2 is process flow diagrams of one embodiment of the invention.
Embodiment
In following each embodiment, except that specifying, described umber is parts by weight, and described per-cent all is weight percentage.
Embodiment 1
(1) P2O5 about 17%, MgO about 4%, CaO about 34%, particle diameter is not more than 200 purposes and is no less than 100 parts in 85% high-magnesium-phosphorus ore powder, insert in the de-magging groove reactor, add concentration and be 17 parts in 98% sulfuric acid, 4 parts in nitric acid, 0.5 part of EDTA is adjusted to material liquid pH about 3 by adding water, reacts about 40min about 65 ℃ down, magnesium and calcium in the phosphorus ore are dissolved under the effect of compound de-magging agent, wherein precipitate under the effect of sulfuric acid of calcium in compound de-magging agent, magnesium ion by complexing, is retained in the solution under the effect of compound de-magging agent.
(2) slip after de-magnesium reaction finishes carries out solid-liquid separation in the mode of vacuum filtration, makes the smart phosphorus ore and the liquid phase de-magging slip solid-liquid separation that contains magnesium ion of de-magging.
(3) the de-magging slip through vacuum filtration enters precipitation tank in term, adds weight concentration and is about 11% milk of lime, the pH of slip is adjusted most about 13, about 45 ℃ of left and right sides precipitin reaction 60min, makes the resultant of reaction magnesium hydroxide separate out precipitation fully.
(4) the precipitation slip after precipitin reaction finishes carries out solid-liquid separation with strainer, and isolated solid phase washes with water, and separating, washing liquid returns the de-magging groove and recycles.
(5) solid phase behind the filtration washing was descended about 70 ℃ dry about 1 hour, promptly prepared MgOH content and can reach 92% magnesium hydroxide products.
Embodiment 2
(1) P2O5 about 26%, MgO about 5%, CaO about 41%, particle diameter is not more than 200 purposes and is no less than 100 parts in 85% high-magnesium-phosphorus ore powder, insert in the de-magging groove reactor, add concentration and be 12 parts in 98% sulfuric acid, 5 parts of silicofluoric acid, 1.0 parts of EDTA are adjusted to material liquid pH about 3.5 by adding water, the following about 60min of de-magnesium reaction about 60 ℃, magnesium and calcium in the phosphorus ore are dissolved under the effect of compound de-magging agent, wherein precipitate under the effect of sulfuric acid of calcium in compound de-magging agent, magnesium ion by complexing, is stayed in the solution under the effect of compound de-magging agent.
(2) slip after de-magnesium reaction finishes carries out solid-liquid separation in the mode of centrifuging, makes the smart phosphorus ore and the liquid phase de-magging slip solid-liquid separation that contains magnesium ion of de-magging.
(3) the de-magging slip after the centrifuging enters precipitation tank in term, adds weight concentration and is about 20% sodium hydroxide solution, the pH of slip is adjusted most about 14, about 58 ℃ of left and right sides precipitin reaction 70min, makes the resultant of reaction magnesium hydroxide separate out precipitation fully.
(4) the precipitation slip after precipitin reaction finishes carries out solid-liquid separation with strainer, and isolated solid phase washes with water, and separating, washing liquid turns back to the de-magging groove and recycles.
(5) solid phase behind the filtration washing was descended about 60 ℃ dry about 1.5 hours, promptly prepared MgOH content and can reach 98% magnesium hydroxide products.
Embodiment 3
(1) P2O5 about 20%, MgO about 4.5%, CaO about 40%, particle diameter is not more than 200 purposes and is no less than 100 parts in 85% high-magnesium-phosphorus ore powder, insert in the de-magging groove reactor, add concentration and be 18 parts in 98% sulfuric acid, 3 parts in nitric acid, 5 parts of silicofluoric acid, EDTA1.2 part, by adding water material liquid pH is adjusted to about 4.0, about 50 ℃, react about 80min down, magnesium and calcium in the phosphorus ore are dissolved under the effect of compound de-magging agent, wherein precipitate under the effect of sulfuric acid of calcium in compound de-magging agent, magnesium ion by complexing, is stayed in the solution under the effect of compound de-magging agent.
(2) slip after de-magnesium reaction finishes carries out solid-liquid separation in the mode of centrifuging, makes the smart phosphorus ore and the liquid phase de-magging slip solid-liquid separation that contains magnesium ion of de-magging.
(3) the de-magging slip through vacuum filtration enters precipitation tank in term, adds commercially available ammoniacal liquor and the pH of slip is adjusted to about 10, about 35 ℃ of left and right sides precipitin reaction 70min, makes the resultant of reaction magnesium hydroxide separate out precipitation fully.
(4) the precipitation slip after precipitin reaction finishes carries out solid-liquid separation with strainer, and isolated solid phase washes with water, and separating, washing liquid returns the de-magging groove and recycles.
(5) solid phase behind the filtration washing was descended about 75 ℃ dry about 1.5 hours, promptly prepared MgOH content and can reach 95% magnesium hydroxide products.
Claims (9)
1. from high-magnesium-phosphorus ore, reclaim the processing method of magnesium, it is characterized in that comprising following processing step:
(1) will contain magnesium phosphorus ore powder and compound de-magging agent and insert the mixing of de-magnesium reaction device, add water and adjust pH to 3～4, under 50～70 ℃ of conditions, react 30～120min, remove magnesium and calcium in the phosphorus ore, described compound de-magging agent contains sulfuric acid and is selected from a kind of component in disodium ethylene diamine tetraacetate and the nitric acid at least;
(2) de-magnesium reaction carries out solid-liquid separation after finishing, and solid phase is for removing the smart phosphorus ore of magnesium, and liquid phase is the de-magging slip, enters next process to reclaim magnesium;
(3) precipitin reaction is carried out in de-magging slip adding neutralization precipitation agent adjustment pH to 8～14, and at 30～60 ℃ of following precipitin reaction 40～90min, precipitation is separated out magnesium hydroxide;
(4) the precipitation slip after the precipitin reaction end is carried out solid-liquid separation, solid phase is a magnesium hydroxide, promptly prepares magnesium hydroxide products after drying.
2. the processing method that reclaims magnesium from high-magnesium-phosphorus ore according to claim 1, the liquid phase that it is characterized in that precipitating slip solid-liquid separation gained turns back to the de-magnesium reaction operation and recycles.
3. the processing method that from high-magnesium-phosphorus ore, reclaims magnesium according to claim 1 and 2, it is characterized in that the sulfuric acid weight content is 2～5 times of other each composition weight content sums, each component of disodium ethylene diamine tetraacetate, silicofluoric acid and nitric acid shared weight ratio in compound de-magging agent is not more than 30% of compound de-magging agent gross weight.
4. the processing method that reclaims magnesium from high-magnesium-phosphorus ore according to claim 1 and 2 is characterized in that described neutralization precipitation agent is selected from milk of lime, sodium hydroxide solution and ammoniacal liquor.
5. the processing method that reclaims magnesium from high-magnesium-phosphorus ore according to claim 1 and 2 is characterized in that the milk of lime weight concentration is 10～20%, and the sodium hydroxide solution weight concentration is 5～20%, and ammoniacal liquor is commercially available ammoniacal liquor.
6. the processing method that reclaims magnesium from high-magnesium-phosphorus ore according to claim 1 and 2 is characterized in that the de-magging slip carries out solid-liquid separation in the mode of vacuum filtration.
7. the processing method that reclaims magnesium from high-magnesium-phosphorus ore according to claim 1 and 2 is characterized in that precipitating slip and carries out the solid-liquid separation washing in the mode of media filtration, and filtered wash solution turns back to the de-magnesium reaction operation and recycles.
8. the processing method that reclaims magnesium from high-magnesium-phosphorus ore according to claim 1 and 2 is characterized in that containing magnesium phosphorus ore powder and is particle diameter and is not more than 200 purpose ratios and is no less than 85%.
9. the processing method that from high-magnesium-phosphorus ore, reclaims magnesium according to claim 1 and 2, it is characterized in that precipitin reaction after separating obtained magnesium hydroxide drying under 60～100 ℃ of conditions be no less than 30min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100216478A CN100392124C (en) | 2006-08-25 | 2006-08-25 | Method of retrieving magnesium from high magnesium phosphorus ore |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100216478A CN100392124C (en) | 2006-08-25 | 2006-08-25 | Method of retrieving magnesium from high magnesium phosphorus ore |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1924046A CN1924046A (en) | 2007-03-07 |
| CN100392124C true CN100392124C (en) | 2008-06-04 |
Family
ID=37816870
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100216478A Expired - Fee Related CN100392124C (en) | 2006-08-25 | 2006-08-25 | Method of retrieving magnesium from high magnesium phosphorus ore |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100392124C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2016025165A1 (en) * | 2014-08-11 | 2016-02-18 | Arr-Maz Products, L.P. | Process and chemistry for reducing dolomite concentrations in phosphate processing |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101880772B (en) * | 2010-06-07 | 2012-07-04 | 中国恩菲工程技术有限公司 | Method for recycling magnesium from magnesium-containing waste solution |
| BRPI1003193B1 (en) * | 2010-08-09 | 2019-09-10 | Vale Do Rio Doce Co | process for wastewater treatment and metal recovery |
| CN102115819A (en) * | 2011-01-27 | 2011-07-06 | 中化重庆涪陵化工有限公司 | Method for recycling magnesium from middle-low grade high-magnesium phosphate rock |
| CN103073034B (en) * | 2013-01-17 | 2014-09-10 | 贵州开磷（集团）有限责任公司 | Method for removing magnesium from ultralow-quality phosphate rock and producing magnesium hydroxide |
| 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 |
| CN105233966A (en) * | 2015-10-08 | 2016-01-13 | 云南磷化集团有限公司 | Chemical magnesium removal and phosphorite reverse flotation coupling technology |
| CN106745105A (en) * | 2016-12-29 | 2017-05-31 | 云南磷化集团有限公司 | A kind of gypsum stack backwater is used for the method that high-magnesium-phosphorus ore drop magnesium carries phosphorus |
| CN106987023B (en) * | 2017-03-14 | 2018-11-06 | 武汉工程大学 | A method of it carrying out phosphorus ore de-magging using organic acid and prepares fire retardant |
| CN107128890B (en) * | 2017-06-20 | 2019-08-27 | 四川龙蟒磷化工有限公司 | Titanium white waste acid is used for the closed circulation process of phosphorus ore de-magging |
| CN111549239B (en) * | 2019-02-08 | 2022-04-22 | 北京中金瑞丰环保科技有限公司 | Resourceful treatment method of magnesium-containing raw material |
| CN110255591A (en) * | 2019-07-29 | 2019-09-20 | 四川大学 | The method of phosphorus ore de-magging co-production magnesium carbonate and calcium carbonate |
| CN110592379A (en) * | 2019-09-11 | 2019-12-20 | 武汉工程大学 | Method for treating high-magnesium phosphorus tailings by using diethylenetriamine pentamethylenephosphonic acid |
| CN113800956B (en) * | 2021-10-27 | 2024-10-11 | 湖北祥云(集团)化工股份有限公司 | Method and device for producing calcium magnesium phosphate fertilizer by magnesium removal clear liquid |
| CN114438344B (en) * | 2022-01-28 | 2023-09-01 | 湖南烯富环保科技有限公司 | Method for selectively precipitating magnesium in zinc-magnesium solution |
| CN114436227A (en) * | 2022-02-17 | 2022-05-06 | 四川省汉源化工总厂 | Circulation thickening water-saving and acid-saving technology for magnesium removal liquid |
| CN114736061B (en) * | 2022-04-29 | 2024-01-30 | 湖北艾迪普生物科技有限公司 | Method for producing compound fertilizer by using phosphate ore tailings |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3867511A (en) * | 1972-12-20 | 1975-02-18 | United States Steel Corp | Solvent extraction of h{hd 3{b po{hd 4 |
| SU1002235A1 (en) * | 1981-06-12 | 1983-03-07 | Ленинградский Государственный Научно-Исследовательский И Проектный Институт Основной Химической Промышленности | Method of producing phosphoric acid |
| US4435370A (en) * | 1981-09-29 | 1984-03-06 | Pennzoil Company | Preparation of monocalcium phosphate and/or phosphoric acid from phosphate rock |
| CN1806931A (en) * | 2006-01-27 | 2006-07-26 | 湖北宜化大江复合肥有限公司 | Mineral dressing method of mid-low grade collophane |
-
2006
- 2006-08-25 CN CNB2006100216478A patent/CN100392124C/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3867511A (en) * | 1972-12-20 | 1975-02-18 | United States Steel Corp | Solvent extraction of h{hd 3{b po{hd 4 |
| SU1002235A1 (en) * | 1981-06-12 | 1983-03-07 | Ленинградский Государственный Научно-Исследовательский И Проектный Институт Основной Химической Промышленности | Method of producing phosphoric acid |
| US4435370A (en) * | 1981-09-29 | 1984-03-06 | Pennzoil Company | Preparation of monocalcium phosphate and/or phosphoric acid from phosphate rock |
| CN1806931A (en) * | 2006-01-27 | 2006-07-26 | 湖北宜化大江复合肥有限公司 | Mineral dressing method of mid-low grade collophane |
Non-Patent Citations (2)
| Title |
|---|
| 湿法磷酸副产氟硅酸用于磷矿脱镁试验研究. 云南三环化工有限公司研发中心.磷肥与复肥，第18卷第6期. 2003 |
| 湿法磷酸副产氟硅酸用于磷矿脱镁试验研究. 云南三环化工有限公司研发中心.磷肥与复肥，第18卷第6期. 2003 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2016025165A1 (en) * | 2014-08-11 | 2016-02-18 | Arr-Maz Products, L.P. | Process and chemistry for reducing dolomite concentrations in phosphate processing |
| US10556978B1 (en) | 2014-08-11 | 2020-02-11 | Arr-Maz Products, L.P. | Process and chemistry for reducing dolomite concentrations in phosphate processing |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1924046A (en) | 2007-03-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100392124C (en) | Method of retrieving magnesium from high magnesium phosphorus ore | |
| CN100558633C (en) | The method for preparing PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate with phosphoric acid by wet process | |
| CN102502720B (en) | Process for producing battery-grade lithium carbonate through processing carbonate type lithium concentrate by deep carbonation method | |
| CN103213964B (en) | Low-grade phosphate ore is utilized to produce the method for phosphoric acid by wet process | |
| CN104152687B (en) | Aluminium, vanadium, molybdenum, the production technology of nickel element three-waste free discharge are extracted from black shale | |
| CN103303886B (en) | Novel method for producing industrial phosphoric acid by purification with wet process phosphoric acid | |
| CN101186284B (en) | Method for preparing phosphoric acid from phosphorus block ore by wet method and extracting rare earth from phosphorus block ore | |
| CN101921001B (en) | Technology for preparing cobalt hydroxide from cobaltous sulfate solution | |
| CN102220488A (en) | Method for separating rare earth from phosphate ore | |
| CN101597688A (en) | From phosphogypsum, reclaim a kind of method of rare earth | |
| CN103193213B (en) | Method for comprehensively utilizing low-grade phosphate ores | |
| CN104445300A (en) | Method of preparing magnesium hydroxide and calcium carbonate and separating out phosphorus ores by taking phosphate tailings as raw materials through ammonia circulation process | |
| CN101386909A (en) | Method for extracting rare-earth from ardealite | |
| CN101440430A (en) | Method for recycling rare earth from phosphogypsum leaching solution by fluoride precipitation method | |
| CN103073034B (en) | Method for removing magnesium from ultralow-quality phosphate rock and producing magnesium hydroxide | |
| CN107879321B (en) | Method for demagging phosphate rock and co-producing sodium fluosilicate and magnesium sulfate | |
| CN105039746A (en) | Method for directly extracting high-purity vanadium pentoxide from stone coal vanadium ore | |
| CN104071818A (en) | Method for separating calcium, magnesium and phosphorus elements from phosphate tailings by adopting water leaching and ammonium leaching | |
| CN100441502C (en) | Method of classification utilizing wet-process phosphoric acid | |
| CN102776367B (en) | Method for demagging ground phosphorite and preparing MgHPO4.3H2O | |
| CN204237562U (en) | A kind of phosphorus ammonium and magnesium hydroxide with coproduction system | |
| CN100519416C (en) | Method for producing basic magnesium carbonate by using boron magnesium fertilizer with coproduction of nano magnesium oxide | |
| CN101293640B (en) | Method for preparing ammonium phosphate salt with hydrochloric acid leaching deficient phosphorus ore | |
| CN103539170B (en) | Method for producing magnesium sulfate and industrial-grade monoammonium phosphate by using tail solution from refining of wet process phosphoric acid by solvent extraction method | |
| CN101830493A (en) | Method for processing waste salt slurry of calcined soda with sodium carbonate and sodium sulfate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080604 Termination date: 20090925 |