CN1160018A - Process for preparing phosphoric acid and phosphate by melting reduction heat method - Google Patents
Process for preparing phosphoric acid and phosphate by melting reduction heat method Download PDFInfo
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- CN1160018A CN1160018A CN 97100773 CN97100773A CN1160018A CN 1160018 A CN1160018 A CN 1160018A CN 97100773 CN97100773 CN 97100773 CN 97100773 A CN97100773 A CN 97100773A CN 1160018 A CN1160018 A CN 1160018A
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Abstract
A process for preparing phosphoric acid and phosphate based on fused reduction principle features that in a reactor with top and bottom spray guns, the matter sprayed from bottom spray gun has atom ratio of C to O of 1.2-2.0, when smelting pool reaches 1450-1550 deg.C, mixture of powdered phosphorous ore and coal with weight ratio of 3:1 is sprayed from top spray gum, and oxygen is sprayed in it from middle ring seam to make atom ratio of C to O be 0.9-1.2. After reaction end, ferrophosphorus containing 17-20% phosphorus content is discharged from bottom of reactor. P2O5 is discharged from top and then absorbed by water or diluted phosphoric acid to obtain industrial phosphoric acid. The gas after absorption tower may be used in industry.
Description
The invention belongs to the chemical industry metallurgical field, particularly relate to the melting and reducing principle is used to produce phosphoric acid and phosphatic a kind of technology, be called for short the SRPA method.
Thermal phosphoric acid technology has been passed through the development in one-stage process and two stages of two-phase method.Modern factories mostly adopts two-phase method, namely makes earlier pure solid or liquid yellow phosphorus, then with element phosphor in combustion chamber internal combustion oxidation, generate P
2O
5, water or diluted acid absorb, and make phosphoric acid product.But the phosphoric acid product that this method is produced exists the cost height, and power consumption reaches greatly the shortcomings such as heat energy of not utilizing coal gas and element phosphor burning to emit.If realize with coal for electricity, briquet replacing coke and directly utilize sensible heat that furnace gas burns to cut down the consumption of energy and keep the measured advantage of thermal phosphoric acid matter, new thermal phosphoric acid technology will have very strong competitiveness.For many years, exploitation more cheap thermal phosphoric acid new technology and reactor are all being explored in countries in the world.The husky research institute of mining and metallurgy of the minister of China Metallurgical Industry, " a kind of direct reduction Rock Phosphate (72Min BPL) is produced the method for phosphoric acid " (CN 1096273 A) of people such as Hou Yonghe, Huang Zhuoshu invention.This technology be with Rock Phosphate (72Min BPL), coke and flux, caking agent by a certain percentage mixing levigate, make ball, oven dry, curing, in rotary kiln, carry out the gas-solid reduction reaction, in same reactor, finish oxidizing fire reaction simultaneously and make phosphoric acid.But this arts demand adds water and caking agent makes the ball oven dry, because gas (CO), solid reduction reaction speed are slow, rotary kiln has the shortcoming of easy ring formation in addition, so plant factor is low, large-scale production still acquires a certain degree of difficulty.
The objective of the invention is to overcome above-mentioned defective, provide a kind of smelting reduction process that utilizes to produce phosphoric acid and phosphoric acid salt fast, there is no the shortcoming of ring formation of rotary kiln, improve plant factor, cut down the consumption of energy, in the hope of reaching large-scale production.
Technical scheme of the present invention is achieved in that this technology is with spraying metallurgy technology, melting and reducing technology and coal gas, element phosphor oxidizing fire prepare the phosphoric acid technology and are combined as a whole, it is coal-oxygen-ore deposit composite blowing, under melting condition, finish the reduction of element phosphor and in same reactor, finish the oxidizing fire of element phosphor, and then produce phosphoric acid or phosphoric acid salt.
It is the supporting use of vertical iron liquid furnace body of expansion type that the present invention has adopted the top spray gun in multithread road and spray gun of the premixed end of double flow duct and top.Top spray gun is divided into two kinds of water-cooled multithread road spray gun (A) and double flow duct spray guns (B), looks the furnace volume size and selects the top spray gun kind for use.Furnace volume is less than 2m
3The time, can adopt double-channel spray gun, furnace volume is greater than 2m
3The time, adopt the multiple flow passages spray gun, the mixed powder of oxygen-ground phosphate rock-coal dust is sprayed into the molten iron surface from furnace roof, the second-time burning oxygen supply is provided, element phosphor is become P with gas-fired
2O
5Make phosphoric acid.Reactor is divided into reduction zone, bottom and top oxidation zone, and the centre is a zone of transition.
Smelting reduction process preparing phosphoric acid of the present invention and phosphatic technology, it is characterized in that in same reactor, realize that simultaneously the bottom finishes phosphatic fusion reduction reaction, oxidation reaction and the gas secondary combustion reaction of elementary gas phosphorus finished on top, during blow-on, the ferrophosphorus melt that keeps certain capacity in the stove, the bath surface height is about 1/3rd of maximum molten bath amount in the stove, before being blended into the ferrophosphorus melt, end spray gun will constantly be blown into nitrogen, when beginning to be blended into ferrophosphorus water, end spray gun blows coal dust and oxygen, namely by the annular space coal dust runner of end spray gun, coal dust is sprayed in the stove take nitrogen as carrier, nitrogen with the central tube of end spray gun switches to oxygen subsequently, keep end winding-up carbon oxygen atom than C: O=1.2-2.0, simultaneously, top spray gun is down to apart from the bath surface certain altitude, the oxygen runner of top spray gun and coal dust and breeze runner also will be kept certain tolerance, bath temperature is when reaching 550 ℃ of 1450-1, begin again to be blown by the central tube of top spray gun the mixed powder of ground phosphate rock and coal dust, ratio is (weight ratio) 3: 1, be blown into oxygen by middle circumferential weld, keep top spray to blow the carbon oxygen atom than C: O=0.9-1.2, adjust top spray gun and each injection parameter of end spray gun, make bath temperature remain on 1450-1550 ℃, in course of reaction, by the furnace roof flux of access control basicity of slag in batches, make basicity of slag be controlled at R=1.0-1.5, when liquid level surpasses normal operating permission height, promote top spray gun, and it is reinforced to stop winding-up, have under the sufficient reducing condition at element phosphor, when reaction reached balance, reduction finished, not during coal injection, end spray gun switches to nitrogen-blow, and the ferrophosphorus phosphorus content that reactor bottom is emitted is 17-20%, and reactor head is come out contains P
2O
5Furnace gas, after dedusting, enter the absorption tower, with repeatedly Sprayer Circulation absorption of absorbent, can obtain PHOSPHORIC ACID TECH.GRADE, top spray gun is water-cooled multiple flow passages spray gun or double-channel spray gun, and end winding-up carbon oxygen atom is C: O=1.3-1.5 than the best, flux is silica or lime stone, add flux and can contain block coke, basicity the best is R=1.10-1.15, and top spray is blown the carbon oxygen atom than best C: the O=1.0-1.1 of being.
This technology is raw materials used to be comprised: coal dust, ground phosphate rock, flux, oxygen, nitrogen, the granularity of powder is all below 60 orders, employed miscellaneous equipment of process implementing process such as pulverizing mill, air feed delivery system, powder injection system, gas dust removal system and gathering system are proven technique.Basicity of slag adds the flux amount by furnace roof and adjusts.Flux is added by furnace roof in batches, and continuous detectable level: used flux is silica (SiO
2), Wingdale (CaCO
3) etc.Decide on injecting velocity the blanking time that adds flux, and the flux addition is decided on winding-up powder composition and basicity of slag requirement.For preventing foamed slag splash and protection furnace lining, add the block coke of part with flux.For keeping furnace atmosphere, the interior carbon oxygen flow of control stove is that operation is crucial in the fusion process.During coal injection, end spray gun does not switch to nitrogen-blow with anti-clogging plug.
Being reflected in same coal-oxygen-ore deposit-ore-solvent compound jet ferrophosphorus bath reactor of technology of the present invention carried out.In same reactor, realized the melting and reducing of phosphorous oxides and the oxidation of elementary gas phosphorus in the ore, reduction and oxidation are carried out synchronously, thereby made phosphoric acid or phosphate.This technology namely takes full advantage of the chemical energy of coal, again the oxidation reaction of element phosphor has been incorporated into the fusion reduction reaction device, and not only reaction speed has obtained quickening, obtains the P of high-load
2O
5Furnace gas, the P of low content
2O
5Slag, and saved equipment, improved benefit, reduce phosphoric acid and phosphatic cost, thereby realized the reasonable comprehensive utilization of rock phosphate in powder and coal resource.
Below in conjunction with accompanying drawing technical scheme of the present invention is further described:
Fig. 1 is the structure iron of reactor
1. 2. end of top spray gun spray gun 3. iron are bathed
4. bell 5. Vanadium Pentoxide in FLAKES carbon monoxide carbonic acid gas hydrogen
6. breeze 7, oxygen 8. coal dusts
9. flux 10. slags 11. ferrophosphorus
Reactor is by top spray gun 1, end spray gun 2, and top is that the vertical iron of expanding bathes 3,4, four of bells Part forms. Top spray gun is installed on the body of heater in order to spray coal-oxygen-ore deposit-flux. End spray gun is that dual channel is pre-Mixing spray gun is installed in furnace bottom, in order to spray coal dust and oxygen. For end spray gun, the structure of top spray gun and property Can the present inventor detailed description there be (Chinese patent CN 91216746.7, ZL 93104740.4) in the patent obtaining, Designed furnace bottom coal oxygen injection lance need not the cold gas protection, and is protected by the coal dust pyrolyzing, and top spray gun is Water-cooled.
End spray gun and body of heater support the use, and knotting is in furnace lining, and spray gun premix termination, the end is equal with the furnace bottom surface to be Suitable.
During blow-on, the ferrophosphorus melt of certain capacity must be arranged in the stove, melt pool height is preferably maximum molten bath amount in the stove About 1/3rd. Before being blended into the ferrophosphorus melt, end spray gun will constantly be blown into nitrogen, stops up with preventing spray head. Beginning end spray gun blows coal dust and oxygen, namely by the annular space coal dust runner of end spray gun, with the coal dust below 60 orders with Nitrogen is that carrier sprays in the stove, and the nitrogen with the central tube of end spray gun switches to oxygen subsequently, keeps end winding-up carbon Oxygen atom is than C: O=1.2-2.0, and the best is C: O=1.3-1.5. Simultaneously, top spray gun is down to apart from the molten bath The liquid level certain altitude, the oxygen runner of top spray gun and coal dust and breeze runner also will be kept certain tolerance, with blowout prevention Head stops up. Bath temperature reaches 1450-1550 ℃ of central tube that begins again by top spray gun and blows phosphorus ore-coal dust Mixed powder, its weight ratio are 3: 1 (P2O
5Content is 25% phosphorus ore), be blown into oxygen by middle circumferential weld, Keep top spray to blow the carbon oxygen atom than C: O=0.9-1.2, the best is C: O=1.0-1.1. End winding-up C: O ratio Example is big, causes reducing atmosphere, and top spray is blown C: the O ratio is little, causes oxidizing atmosphere. Adjust the spray of top spray gun and the end Each injection parameter of rifle is normal. Make best bath temperature between 1450～1550 ℃, by control coal dust amount and phosphorus It is measured to align in the ore deposit, increases the coal dust amount and can improve bath temperature, increases the phosphorus ore amount, can reduce furnace temperature. Furnace gas goes out Mouthful temperature is less than 1600 ℃, basicity of slag R=1.0～1.5, and the best is R=1.10-1.15. By control gas Amount is controlled the solid powder amount, and carries mixed powder by gas.
Carrying out along with winding-up, bath surface raises gradually, when liquid level surpasses normal operating permission height, promote top spray gun, it is reinforced to stop top spray gun winding-up, stops up for preventing end spray gun, during stop-spraying coal-oxygen, keeping in end spray gun central tube and the annular space has suitable nitrogen flow, with slag P2O
5Required utilization rate is declared Whether disconnected reaction finishes (being generally (percentage by weight) 1-2%), the grate slag that overflows then, and emit part liquid The attitude ferrorphosphorus. Contain P by what reactor head was come out2O
5Furnace gas enters the absorption tower after dedusting, with absorbing Agent: water or phosphoric acid,diluted repeatedly Sprayer Circulation absorb, and temperature is controlled at 40-60 ℃, can obtain PHOSPHORIC ACID TECH.GRADE, Coal gas behind the absorption tower can be used as industrial coal gas, and after reduction finished, the ferrophosphorus that reactor bottom is emitted was phosphorous Amount can be used as the metallurgy ferrorphosphorus generally 17～20%.
Embodiment 1:
The ferrophosphorus melt of in the vertical iron liquid furnace of 100KW, packing into, phosphorus content is 17-20%, the bath surface height is about 1/3rd of maximum molten bath amount in the stove, before being blended into the ferrophosphorus melt, end spray gun will constantly be blown into nitrogen, when beginning to be blended into ferrophosphorus water, end spray gun blows coal dust and oxygen, namely by the annular space coal dust runner of end spray gun, coal dust is sprayed in the stove take nitrogen as carrier, nitrogen with the central tube of end spray gun switches to oxygen subsequently, keep end winding-up carbon oxygen atom than C: O=1.2, simultaneously, top spray gun is down to apart from the bath surface certain altitude, the oxygen runner of top spray gun and coal dust and breeze runner also will be kept certain tolerance, when bath temperature reaches 1450 ℃, begin again to be blown by the central tube of top spray gun the mixed powder of siliceous ground phosphate rock and coal dust, ratio is (weight ratio) 3: 1, be blown into oxygen by middle circumferential weld, keep top spray to blow the carbon oxygen atom than C: O=1.3, adjust top spray gun and each injection parameter of end spray gun, bath temperature is remained on about 1450 ℃, in course of reaction, by the furnace roof lime stone (CaCO of access control basicity of slag in batches
3), constantly chemical examination makes basicity of slag be controlled at R=1.15, when liquid level surpasses normal operating permission height, promote top spray gun, and it is reinforced to stop winding-up, has under the sufficient reducing condition at element phosphor, chemically examines slag P
2O
5Content, when reaching required utilization rate (percentage by weight) 1.8%, reduction finishes, the grate slag that overflows, during coal injection, end spray gun does not switch to nitrogen-blow, the ferrophosphorus phosphorus content that reactor bottom is emitted is 17-20%, reactor head is released contains P
2O
5Furnace gas enters the absorption tower after dedusting, the absorption tower water temperature is controlled at 40～60 ℃, and water repeatedly Sprayer Circulation absorbs, and can obtain concentration and be 17% phosphoric acid solution, contains P in the slag
2O
5Be 1.8%, percent reduction reaches more than 90%.Embodiment 2:
Used iron bath and production method are with embodiment 1.Selected is the calcareous phosphorous ore powder, ferrophosphorus melt in iron is bathed, and its phosphorus content is 17-20%, that adjust basicity of slag is silica (SiO
2), and being controlled at R=1.1, top spray gun winding-up carbon oxygen atom is than C: O=1.0, and end spray gun winding-up carbon oxygen atom is than C: O=2.0, and the reaction in furnace temperature is about 1550 ℃, can obtain concentration and be 17% phosphoric acid solution, contains P in the slag
2O
5Be 1.5%, percent reduction reaches more than 90%.
Claims (7)
1. the hot method preparing phosphoric acid of melting and reducing and phosphatic technology, it is characterized in that in same reactor, realize that simultaneously the bottom finishes phosphatic fusion reduction reaction, oxidation reaction and the gas secondary combustion reaction of elementary gas phosphorus finished on top, during blow-on, the ferrophosphorus melt that keeps certain capacity in the stove, the bath surface height is about 1/3rd of maximum molten bath amount in the stove, before being blended into the ferrophosphorus melt, end spray gun will constantly be blown into nitrogen, when beginning to be blended into ferrophosphorus water, end spray gun blows coal dust and oxygen, namely by the annular space coal dust runner of end spray gun, coal dust is sprayed in the stove take nitrogen as carrier, nitrogen with the central tube of end spray gun switches to oxygen subsequently, keep end winding-up carbon oxygen atom than C: O=1.2-2.0, simultaneously, top spray gun is down to apart from the bath surface certain altitude, the oxygen runner of top spray gun and coal dust and breeze runner also will be kept certain tolerance, bath temperature is when reaching 1450-1550 ℃, begin again to be blown by the central tube of top spray gun the mixed powder of ground phosphate rock and coal dust, ratio is (weight ratio) 3: 1, be blown into oxygen by middle circumferential weld, keep top spray to blow the carbon oxygen atom than C: O=0.9-1.2, adjust top spray gun and each injection parameter of end spray gun, make bath temperature remain on 1450-1550 ℃, in course of reaction, by the furnace roof flux of access control basicity of slag in batches, make basicity of slag be controlled at R=1.0-1.5, when liquid level surpasses normal operating permission height, promote top spray gun, and it is reinforced to stop winding-up, have under the sufficient reducing condition at element phosphor, when reaction reached balance, reduction finished, not during coal injection, end spray gun switches to nitrogen-blow, and the ferrophosphorus phosphorus content that reactor bottom is emitted is 17-20%, and reactor head is come out contains P
2O
5Furnace gas enters the absorption tower after dedusting, with repeatedly Sprayer Circulation absorption of absorbent, can obtain PHOSPHORIC ACID TECH.GRADE.
2. the hot legal system of melting and reducing according to claim 1 is got phosphoric acid and phosphatic technology, it is characterized in that described top spray gun is water-cooled multithread road spray gun or double flow duct spray gun.
3. the hot legal system of melting and reducing according to claim 1 is got phosphoric acid and phosphatic technology, it is characterized in that described end winding-up carbon Sauerstoffatom is than best C: the O=1.3-1.5 of being.
4. the hot legal system of melting and reducing according to claim 1 is got phosphoric acid and phosphatic technology, it is characterized in that described flux is silica or Wingdale.
5. the hot legal system of melting and reducing according to claim 1 is got phosphoric acid and phosphatic technology, it is characterized in that described adding flux can contain block coke.
6. the hot legal system of melting and reducing according to claim 1 is got phosphoric acid and phosphatic technology, it is characterized in that the best R=1.10-1.15 of being of described basicity.
7. the hot legal system of the described melting and reducing of claim 1 is got phosphoric acid and phosphatic technology, it is characterized in that described top winding-up carbon Sauerstoffatom is than best C: the O=1.0-1.1 of being.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97100773A CN1060139C (en) | 1997-02-25 | 1997-02-25 | Process for preparing phosphoric acid and phosphate by melting reduction heat method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97100773A CN1060139C (en) | 1997-02-25 | 1997-02-25 | Process for preparing phosphoric acid and phosphate by melting reduction heat method |
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| Publication Number | Publication Date |
|---|---|
| CN1160018A true CN1160018A (en) | 1997-09-24 |
| CN1060139C CN1060139C (en) | 2001-01-03 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97100773A Expired - Fee Related CN1060139C (en) | 1997-02-25 | 1997-02-25 | Process for preparing phosphoric acid and phosphate by melting reduction heat method |
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| CN101172590A (en) * | 2007-10-16 | 2008-05-07 | 李进 | Method for direct production of phosphorus pentoxide with phosphorus ore |
| CN101650120A (en) * | 2009-06-25 | 2010-02-17 | 中国恩菲工程技术有限公司 | Reduction oxidation furnace for refining phosphorus by hot method |
| CN101172589B (en) * | 2007-10-16 | 2010-08-25 | 四川川恒化工股份有限公司 | Method for direct production of phosphorus pentoxide with phosphorus ore |
| CN101172587B (en) * | 2007-10-16 | 2010-08-25 | 四川川恒化工股份有限公司 | Method for producing phosphorus pentoxide by phosphorus ore fusion |
| CN101531352B (en) * | 2009-04-22 | 2010-10-27 | 瓮福（集团）有限责任公司 | Method for using phosphoric oxide to concentrate diluted phosphoric acid to prepare crystal polyphosphoric acid |
| CN101172588B (en) * | 2007-10-16 | 2010-11-10 | 四川川恒化工股份有限公司 | Method for producing phosphorus pentoxide by phosphorus ore fusion |
| WO2010148899A1 (en) * | 2009-06-25 | 2010-12-29 | 中国恩菲工程技术有限公司 | Reduction-oxidation furnace for making phosphorus by thermal process |
| WO2010148902A1 (en) * | 2009-06-25 | 2010-12-29 | 中国恩菲工程技术有限公司 | Device making phosphorus by thermal process |
| CN102765706A (en) * | 2012-08-20 | 2012-11-07 | 黄靖元 | Method for producing phosphoric acid through ground phosphate rock in fast hot-melting mode |
| CN102796838A (en) * | 2012-08-27 | 2012-11-28 | 黄靖元 | Method for producing pig iron and phosphate using ferro-phosphorus |
| CN104211032A (en) * | 2013-06-04 | 2014-12-17 | 四川玖长科技有限公司 | Rotary kiln for reducing phosphate rock in kiln method phosphoric acid technology and method for solving ring forming of kiln tail of kiln method phosphoric acid technology |
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| US9982947B2 (en) | 2013-06-04 | 2018-05-29 | Sichuan Ko Chang Technology Co., Ltd. | Rotary kiln for reducing phosphate ore in kiln phosphoric acid process and method for solving ring forming in kiln tail in kiln phosphoric acid process |
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| WO2018145157A1 (en) * | 2017-02-09 | 2018-08-16 | Commonwealth Scientific And Industrial Research Organisation | Process for recovering phosphorus from phosphoritic materials |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU691664A1 (en) * | 1973-05-30 | 1979-10-15 | Опытно-Конструкторское Бюро Энерготехнологических Процессов Химической Промышленности | Ore melting furnace |
| DE3009732C2 (en) * | 1980-03-13 | 1983-10-20 | Leningradskij gosudarstvennyj naučno-issledovatel'skij i proektnyj institut osnovnoj chimičeskoj promyšlennosti, Leningrad | Process for the production of phosphoric acid |
| CN1039401C (en) * | 1995-01-09 | 1998-08-05 | 化学工业部上海化工研究院 | Prodn of high-concentration defluorinated phosphate with powdered coal as fuel |
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1997
- 1997-02-25 CN CN97100773A patent/CN1060139C/en not_active Expired - Fee Related
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| CN101172589B (en) * | 2007-10-16 | 2010-08-25 | 四川川恒化工股份有限公司 | Method for direct production of phosphorus pentoxide with phosphorus ore |
| CN101172587B (en) * | 2007-10-16 | 2010-08-25 | 四川川恒化工股份有限公司 | Method for producing phosphorus pentoxide by phosphorus ore fusion |
| CN101172590B (en) * | 2007-10-16 | 2010-09-29 | 四川川恒化工股份有限公司 | Method for direct production of phosphorus pentoxide with phosphorus ore |
| CN101172590A (en) * | 2007-10-16 | 2008-05-07 | 李进 | Method for direct production of phosphorus pentoxide with phosphorus ore |
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| WO2010148902A1 (en) * | 2009-06-25 | 2010-12-29 | 中国恩菲工程技术有限公司 | Device making phosphorus by thermal process |
| CN101650120B (en) * | 2009-06-25 | 2014-03-26 | 中国恩菲工程技术有限公司 | Reduction oxidation furnace for refining phosphorus by hot method |
| US8741226B2 (en) | 2009-06-25 | 2014-06-03 | China Enfi Engineering Corp. | Reduction-oxidation furnace for making phosphorus by thermal process |
| CN102765706A (en) * | 2012-08-20 | 2012-11-07 | 黄靖元 | Method for producing phosphoric acid through ground phosphate rock in fast hot-melting mode |
| CN102796838A (en) * | 2012-08-27 | 2012-11-28 | 黄靖元 | Method for producing pig iron and phosphate using ferro-phosphorus |
| CN104211032A (en) * | 2013-06-04 | 2014-12-17 | 四川玖长科技有限公司 | Rotary kiln for reducing phosphate rock in kiln method phosphoric acid technology and method for solving ring forming of kiln tail of kiln method phosphoric acid technology |
| US9982947B2 (en) | 2013-06-04 | 2018-05-29 | Sichuan Ko Chang Technology Co., Ltd. | Rotary kiln for reducing phosphate ore in kiln phosphoric acid process and method for solving ring forming in kiln tail in kiln phosphoric acid process |
| CN106744758A (en) * | 2016-11-11 | 2017-05-31 | 长沙有色冶金设计研究院有限公司 | A kind of method that decomposing phosphate rock stone produces phosphoric acid |
| CN106744758B (en) * | 2016-11-11 | 2019-02-12 | 长沙有色冶金设计研究院有限公司 | A kind of method of decomposing phosphate rock stone production phosphoric acid |
| WO2018145157A1 (en) * | 2017-02-09 | 2018-08-16 | Commonwealth Scientific And Industrial Research Organisation | Process for recovering phosphorus from phosphoritic materials |
| CN110494389A (en) * | 2017-02-09 | 2019-11-22 | 联邦科学和工业研究组织 | From the method for phosphorite material recovery phosphorus |
| EP3580170A4 (en) * | 2017-02-09 | 2020-10-28 | Commonwealth Scientific and Industrial Research Organisation | Process for recovering phosphorus from phosphoritic materials |
| CN108300826A (en) * | 2018-01-31 | 2018-07-20 | 贵州仁聚业科技股份有限公司 | The method for extracting element phosphor and elemental iron from yellow phosphorus by-product ferrophosphorus slag |
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| Publication number | Publication date |
|---|---|
| CN1060139C (en) | 2001-01-03 |
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