CN105417515A - Co-production method of feed-grade calcium phosphate dibasic and fertilizer-grade monoammonium phosphate - Google Patents
Co-production method of feed-grade calcium phosphate dibasic and fertilizer-grade monoammonium phosphate Download PDFInfo
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- CN105417515A CN105417515A CN201510808531.8A CN201510808531A CN105417515A CN 105417515 A CN105417515 A CN 105417515A CN 201510808531 A CN201510808531 A CN 201510808531A CN 105417515 A CN105417515 A CN 105417515A
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Abstract
The invention provides a co-production method of feed-grade calcium phosphate dibasic and fertilizer-grade monoammonium phosphate. The method includes the following steps that fertilizer-grade calcium phosphate dibasic obtained after sedimentation concentration, namely white fertilizer slurry, is made to conduct a pre-reaction with white fertilizer extraction filtrate returned through the co-production method; after slurry is subjected to sediment, supernatant liquid enters a fertilizer-grade monoammonium phosphate reaction system, and after wash water of the filtering process is added to lower-layer thickened mud, serving as the raw material of production of the fertilizer-grade monoammonium phosphate, for dilution, vitriol is added for an extraction reaction; after the extraction slurry is filtered, filtrate returns to the white fertilizer slurry for a pre-extraction reaction, and filter residues serve as the raw material for producing a compound mixed phosphatic fertilizer. By means of the method, the yield of phosphorus pentoxide of the feed-grade calcium phosphate dibasic can be raised to 92-95%; by the adoption of the method, the phosphorus pentoxide brought away by white fertilizer only accounts for 5-8% of the total amount of phosphorus pentoxide, only 1.1-1.6 tons of sulfuric acid needs to be consumed by recycling 1 ton of phosphorus pentoxide, and the method is the ideal method for enterprises for preparing feed-grade calcium phosphate dibasic through a slurry method.
Description
Technical field
The invention relates to phosphoric acid to be in a wet process raw material, to carry out in multistage neutralisation purification of wet process phosphoric acid production calcium hydrophosphate fodder process, to improve the method for phosphoric acid by wet process Vanadium Pentoxide in FLAKES yield, more particularly, by processing and the Vanadium Pentoxide in FLAKES reclaimed in fertilizer grade secondary calcium phosphate for the production of the raw material of fertilizer grade monoammonium phosphate, reach the Vanadium Pentoxide in FLAKES yield improving calcium hydrophosphate fodder and the technology reducing calcium hydrophosphate fodder production cost;
Technical background
Phosphoric acid is that raw material carries out multistage neutralization reaction, purification and impurity removal to produce calcium hydrophosphate fodder in a wet process, add in calcium carbonate or lime slurry neutralization purification of wet process phosphoric acid process with operation in one section, generate a large amount of solid wet containing Vanadium Pentoxide in FLAKES fertile in vain, and in phosphoric acid by wet process, have the P of about 20%
2o
5enter in white fertilizer, and the P in white fertilizer
2o
5about 60% is had to be exist with the form of secondary calcium phosphate and monocalcium phosphate.Because white fertile value is low, output is large, and (ratio of the Vanadium Pentoxide in FLAKES in feed grade and fertilizer grade secondary calcium phosphate reaches (80 ︰ 20), thus reduces the value of Vanadium Pentoxide in FLAKES, adds the production cost of calcium hydrophosphate fodder.
At present, the utilization ways of fertilizer grade secondary calcium phosphate is mainly contained: (1) is by wet white fertile oven dry or be sold to compound fertilizer factory after naturally drying, as a supplement with the raw material adjusting phosphoric in composite fertilizer; (2) Vanadium Pentoxide in FLAKES reclaimed wherein with the mineral acids such as sulfuric acid, phosphoric acid or hydrochloric acid and white fertile reaction, generates the dilute phosphoric acid etc. containing Vanadium Pentoxide in FLAKES;
The processing mode of above dialogue fertilizer can cause: (1) is using the white fertile raw material as composite fertilizer, although the Vanadium Pentoxide in FLAKES in white fertilizer is fully used, but reduce the value of Vanadium Pentoxide in FLAKES, thus reduce the benefit of calcium hydrophosphate fodder factory; (2) add the mineral acids such as sulfuric acid, phosphoric acid or hydrochloric acid and reclaim Vanadium Pentoxide in FLAKES in white fertilizer, because the foreign matter contents such as the iron in dilute phosphoric acid after extractive reaction, aluminium, magnesium, fluorine are higher, adding in water-ground limestone or limestone vegetation process, wherein the impurity such as iron, aluminium, magnesium can be precipitated out again in the form of phosphate, thus effectively cannot improve the rate of recovery reclaiming Vanadium Pentoxide in FLAKES and the value promoting Vanadium Pentoxide in FLAKES in white fertilizer;
Summary of the invention
The object of the invention is for the deficiencies in the prior art part, Vanadium Pentoxide in FLAKES in a kind of high efficiente callback fertilizer grade secondary calcium phosphate is provided and for the production of the technology of fertilizer grade monoammonium phosphate, provides a kind of method that Vanadium Pentoxide in FLAKES reducing calcium hydrophosphate fodder product consumes;
First core of the present invention is that the phosphoric acid in the white fertilizer extraction filtrate utilizing the present invention to return and the secondary calcium phosphate in part free sulfuric acid and fresh white fertilizer react the monocalcium phosphate generating solubility, is namely undertaken by following reaction:
H
3PO
4+CaHPO
4·2H
2O→Ca(H
2PO
4)
2·H
2O+H
2O
CaHPO
4·2H
2O+H
2SO
4→CaSO
4·2H
2O↓+H
3PO
4
Second core of the present invention is the acidolysis reaction adding sulfuric acid, namely dissolves or the phosphatic slip such as undissolved secondary calcium phosphate, monocalcium phosphate and the sulfuric acid reaction added and generate calcium sulfate precipitation and phosphoric acid containing a large amount of:
Ca(H
2PO
4)
2+H
2SO
4+2H
2O→CaSO
4·2H
2O↓+2H
3PO
4
CaHPO
4·2H
2O+H
2SO
4→CaSO
4·2H
2O↓+H
3PO
4
Because depositing a large amount of iron, aluminium, the phosphoric acid salt of magnesium and Calcium Fluoride (Fluorspan) in white fertilizer, with generate the iron of solubility, aluminium, magnesium vitriol and fluorochemical after sulfuric acid reaction and enter in dilute phosphoric acid solution, but to be mostly precipitated out again after reacting with the secondary calcium phosphate in fresh white fertilizer and the unreacted water-ground limestone of part;
By above step, the secondary calcium phosphate in white fertilizer is become phosphoric acid or the monocalcium phosphate of solubility, thus reach the object reclaiming Vanadium Pentoxide in FLAKES from white fertilizer;
In Wet-process Phosphoric Acid Production process, during with sulfuric acid decomposition phosphorus ore, the sulfuric acid consumption of Vanadium Pentoxide in FLAKES per ton is 2.4 ~ 2.7 tons.Because reactive behavior phosphatic in white fertilizer is high, sulfuric acid consumption is low, and the sulfuric acid consumption often reclaiming 1 ton of Vanadium Pentoxide in FLAKES is only 1.1 ~ 1.6 tons.Pass through present method, in recyclable white fertilizer 55 ~ 70% Vanadium Pentoxide in FLAKES, the Vanadium Pentoxide in FLAKES yield of whole production system can bring up to 92 ~ 95%, and namely after the inventive method process, the white fertile Vanadium Pentoxide in FLAKES taken away only accounts for and drops into 5 ~ 8% of Vanadium Pentoxide in FLAKES total amount., both obtained the Vanadium Pentoxide in FLAKES of low cost, solved again a process difficult problem for white fertilizer;
The object of the invention is by realize with following technical scheme;
A method for calcium hydrophosphate fodder coproduction fertilizer grade monoammonium phosphate, as shown in Figure 1, feature of the present invention is, adopts following technological process:
A method for calcium hydrophosphate fodder coproduction fertilizer grade monoammonium phosphate, the present invention is characterised in that: as shown in Figure 1, comprises following process: fresh white fertilizer slurry is carried out pre-reaction with the extraction filtrate that white fertilizer adds sulfuric acid; After reaction slurry sedimentation, supernatant liquid goes slurry process fertilizer grade monoammonium phosphate production system, and to produce fertilizer grade monoammonium phosphate further, the thick slurry of lower floor goes extractive reaction operation; After slurry filtration after extractive reaction, the extraction liquid after namely white fertile extraction filtrate add sulfuric acid returns front operation and fresh white fertilizer and starches and carry out mixing pre-extracted and react, and filtered filtration residue is as the raw material of complex phosphate fertilizer.
The white fertile extraction filtrate of the present invention and fresh white fertilizer are starched and are carried out pre-extracted reaction, the pH value controlling reaction is 1.2 ~ 1.5, and slurry reaction temperature is 20 ~ 45 DEG C (natural reaction temperature, without the need to other heating), 1.5 ~ 3.0 hours reaction times, reaction slurry solid content 10 ~ 15%.
The fresh white fertilizer slurry of the present invention and white fertilizer add sulfuric acid extract after filtrate carry out hybrid reaction after slip carry out sedimentation concentration after, supernatant liquid is containing Vanadium Pentoxide in FLAKES 15 ~ 20%, enter slurry process fertilizer grade monoammonium phosphate production system to produce fertilizer grade monoammonium phosphate, the thick slurry of the solid content 20 ~ 30% of releasing bottom thickener enters next step extractive reaction adding sulfuric acid.
After the present invention adds the filtration washing water dilution of rear operation in the white fertile thick slurry of the reacted sedimentation of pre-extracted, then add the vitriol oil and carry out extractive reaction; The pH value controlling reaction slurry is 0.5 ~ 1.0, slurry reaction temperature 30 ~ 50 DEG C (being natural reaction temperature, without the need to other heating), controls 1.5 ~ 3.0 hours reaction times, and the solid content controlling reaction slurry is 10 ~ 15%;
The present invention carries out the slurry filtration after extractive reaction by adding sulfuric acid, and adds a small amount of clear water washing filter residue; Filtrate containing Vanadium Pentoxide in FLAKES 15 ~ 20% returns the first step and fresh white fertilizer and starches and carry out pre-extracted reaction, the dilution water of white fertilizer slurry extractive reaction made by washings containing Vanadium Pentoxide in FLAKES 1 ~ 3%, and the white fertile filter residue of the compositions such as phosphoric acid iron, aluminum phosphate makes the raw material of complex phosphate fertilizer.
Technology of the present invention, compared with existing calcium hydrophosphate fodder producing and manufacturing technique, has following beneficial effect:
1, as shown in Figure 1, technological process of the present invention mainly comprises once the pre-extraction reaction of white fertilizer slurry, a sedimentation, one sulfoxylic acid extractive reaction and a filter progress, compared with starching filter progress with one section of conventional at present white fertilizer, although add the pre-extraction reaction of fresh white fertilizer slurry, sedimentation and add sulfuric acid extractive reaction, but in recyclable white fertilizer 55 ~ 70% Vanadium Pentoxide in FLAKES, the Vanadium Pentoxide in FLAKES yield of whole production system can bring up to 92 ~ 95%, namely after the inventive method process, the Vanadium Pentoxide in FLAKES that white fertilizer is taken away only accounts for and drops into 5 ~ 8% of Vanadium Pentoxide in FLAKES total amount., greatly reduce the production cost of calcium hydrophosphate fodder.
2, by containing the higher impurity such as iron, aluminium, magnesium, fluorine in the white fertile filtrate after acidolysis reaction, and by with fresh white fertile slurry reaction after, most of impurity in dilute phosphoric acid is precipitated out along with the rising of pH value again, thus obtains quality preferably dilute phosphoric acid solution;
4, by after Technology process of the present invention, five oxidation two content of drying in white fertilizer are reduced to 6 ~ 10% from before treatment 20 ~ 33%, and the filter residue after sulfuric acid decomposition and low-phosphorous white fertilizer still can be used as the raw material of production Chemical Mixed Fertilizer and all utilized;
5, by after present invention process technical finesse, the Vanadium Pentoxide in FLAKES be worth in lower white fertilizer is converted into the Vanadium Pentoxide in FLAKES in the higher fertilizer grade monoammonium phosphate of value, thus greatly improves the economic benefit of calcium hydrophosphate fodder manufacturer;
6, from white fertilizer, reclaim Vanadium Pentoxide in FLAKES, the sulfuric acid consumption of Vanadium Pentoxide in FLAKES per ton is 1.1 ~ 1.6 tons, far below the sulfuric acid consumption of 2.40 ~ 2.70 tons in Wet-process Phosphoric Acid Production.
Accompanying drawing explanation
Fig. 1 is production technological process of the present invention.
Embodiment
A method for calcium hydrophosphate fodder coproduction fertilizer grade monoammonium phosphate, the present invention is characterised in that: as shown in Figure 1, comprises following process: fresh white fertilizer slurry is carried out pre-reaction with the extraction filtrate that white fertilizer adds sulfuric acid; After reaction slurry sedimentation, supernatant liquid goes slurry process fertilizer grade monoammonium phosphate production system, and to produce fertilizer grade monoammonium phosphate further, the thick slurry of lower floor goes extractive reaction operation; After slurry filtration after extractive reaction, add the extraction liquid after sulfuric acid and return front operation and fresh white fertilizer and starch and carry out mixing pre-extracted and react, filtered filtration residue is as the raw material of complex phosphate fertilizer.
The white fertile extraction filtrate of the present invention and fresh white fertilizer are starched and are carried out pre-extracted reaction, and the pH value controlling reaction is 1.2 ~ 1.5, and slurry reaction temperature is 20 ~ 45 DEG C, for the temperature of reaction under natural environmental condition, without the need to other heating, 1.5 ~ 3.0 hours reaction times, reaction slurry solid content 10 ~ 15%.
The fresh white fertilizer slurry of the present invention and white fertilizer add sulfuric acid extract after filtrate carry out hybrid reaction after slip carry out sedimentation concentration after, supernatant liquid is containing Vanadium Pentoxide in FLAKES 15 ~ 20%, enter slurry process fertilizer grade monoammonium phosphate production system to produce fertilizer grade monoammonium phosphate, the thick slurry of the solid content 20 ~ 30% of releasing bottom thickener enters next step extractive reaction adding sulfuric acid.
After the present invention adds the filtration washing water dilution of rear operation in the white fertile thick slurry of the reacted sedimentation of pre-extracted, then add the vitriol oil and carry out extractive reaction; The pH value controlling reaction slurry is 0.5 ~ 1.0, slurry reaction temperature 30 ~ 50 DEG C (being natural reaction temperature, without the need to other heating), controls 1.5 ~ 3.0 hours reaction times, and the solid content controlling reaction slurry is 10 ~ 15%;
Slip after adding sulfuric acid extractive reaction filters by the present invention, and adds a small amount of clear water washing filter residue; Filtrate containing Vanadium Pentoxide in FLAKES 15 ~ 20% returns the first step and fresh white fertilizer and starches and carry out pre-extracted reaction, the dilution water of white fertilizer slurry extractive reaction made by washings containing Vanadium Pentoxide in FLAKES 1 ~ 3%, and the white fertile filter residue of the compositions such as phosphoric acid iron, aluminum phosphate makes the raw material of complex phosphate fertilizer.
Case study on implementation one
Be 25% fresh white fertilizer slurry by the solid content after sedimentation and add the filtrate after sulfuric acid extractive reaction from the white fertilizer of rear operation and carry out hybrid reaction, the pH value of slip is 1.2, slurry reaction temperature 35 DEG C, 1.5 hours reaction times, slip solid content 11.5%; White fertilizer slurry thickener after pre-reaction is carried out natural subsidence, and the clear liquid containing Vanadium Pentoxide in FLAKES 15.5% enters fertilizer grade monoammonium phosphate production system, as the raw material producing fertilizer grade monoammonium phosphate; The thick slurry of the solid content 25.1% of releasing bottom thickener enters next step extractive reaction adding sulfuric acid.The solid content of extractive reaction slip is 11%, and adding the pH value after strong sulfuric acid response is 0.6, temperature of reaction 31 DEG C, 1.5 hours reaction times; Extractive reaction slip is filtered, and adds a small amount of clear water washing filter residue; Filtrate phosphorus pentoxide content 16.9%, enters the pre-extraction reaction process of white fertilizer slurry.Washings is containing Vanadium Pentoxide in FLAKES 1.2%, and make the dilution water of white fertilizer slurry acidolysis reaction, the white fertile filter residue containing Vanadium Pentoxide in FLAKES 5.2% makes the raw material of complex phosphate fertilizer.
After aforementioned process process, in white fertilizer, the rate of recovery of Vanadium Pentoxide in FLAKES is 65.7%, sulfuric acid consumption is 1.33 tons of sulfuric acid/ton Vanadium Pentoxide in FLAKES, the ratio (assorted phosphorus ratio) that ferric oxide, aluminum oxide and magnesium oxide total impurities in fresh white premix reaction clear liquor account for Vanadium Pentoxide in FLAKES is 11.50%, phosphorus fluorine ratio (P
2o
5/ F) be 38.5, and the assorted phosphorus ratio of sulfuric acid process phosphoric acid by wet process is generally 13 ~ 15%, phosphorus fluorine ratio is 9 ~ 16, and the quality of white fertile treatment solution is better than phosphoric acid by wet process.
Case study on implementation two
Be that 27.3% fresh white fertilizer is starched and carries out hybrid reaction from the filtrate after the white fertile extractive reaction of rear operation by the solid content after sedimentation, the pH value of slip is 1.3, slurry reaction temperature 33 DEG C, 2.5 hours reaction times, slip solid content 13.2%; White fertilizer slurry thickener after pre-reaction is carried out natural subsidence, and the clear liquid containing Vanadium Pentoxide in FLAKES 16.1% enters fertilizer grade monoammonium phosphate production system, as the raw material producing fertilizer grade monoammonium phosphate; The thick slurry of the solid content 27.2% of releasing bottom thickener enters next step extractive reaction adding sulfuric acid.The solid content of extractive reaction slip is 13%, and adding the pH value after strong sulfuric acid response is 0.9, temperature 41 DEG C, 2.0 hours reaction times; The slip of extractive reaction is filtered, and adds a small amount of clear water washing filter residue; Filtrate containing phosphorus pentoxide content 18.3% enters the pre-extraction reaction process of white fertilizer slurry.Washings is containing Vanadium Pentoxide in FLAKES 2.3%, and make the dilution water of white fertilizer slurry extractive reaction, the white fertile filter residue containing Vanadium Pentoxide in FLAKES 5.8% makes the raw material of complex phosphate fertilizer.
After aforementioned process process, in white fertilizer, the rate of recovery of Vanadium Pentoxide in FLAKES is 69.3%, sulfuric acid consumption is 1.45 tons of sulfuric acid/ton Vanadium Pentoxide in FLAKES, the ratio (assorted phosphorus ratio) that fresh white fertilizer ferric oxide, aluminum oxide and the magnesium oxide total impurities extracted in advance in reaction clear liquor accounts for Vanadium Pentoxide in FLAKES is 10.60%, phosphorus fluorine ratio (P
2o
5/ F) be 33.2, and the assorted phosphorus ratio of sulfuric acid process phosphoric acid by wet process is generally 13 ~ 15%, phosphorus fluorine ratio is 9 ~ 16, and the quality of white fertile treatment solution is better than phosphoric acid by wet process.
Case study on implementation three
Be that 28.9% fresh white fertilizer is starched and carries out hybrid reaction from the reacted filtrate of rear operation white adipic acid solution by the solid content after sedimentation, the pH value of slip is 1.5, slurry reaction temperature 43 DEG C, 3.0 hours reaction times, slip solid content 15.0%; White fertilizer slurry thickener after pre-reaction is carried out natural subsidence, and the clear liquid containing Vanadium Pentoxide in FLAKES 17.6% enters fertilizer grade monoammonium phosphate production system, as the raw material that fertilizer grade monoammonium phosphate is produced; The thick slurry of the solid content 29.5% of releasing bottom thickener enters next step extractive reaction adding sulfuric acid.The solid content of extractive reaction slip is 15%, and adding the pH value after strong sulfuric acid response is 1.0, temperature 43 DEG C, 3.0 hours reaction times; Extractive reaction slip is filtered, and adds a small amount of clear water washing filter residue; Filtrate containing phosphorus pentoxide content 18.9% enters the pre-extracted reaction process of white fertilizer slurry.Washings is containing Vanadium Pentoxide in FLAKES 1.9%, and make the dilution water of white fertilizer slurry extractive reaction, the white fertile filter residue containing Vanadium Pentoxide in FLAKES 6.1% makes the raw material of complex phosphate fertilizer.
After aforementioned process process, in white fertilizer, the rate of recovery of Vanadium Pentoxide in FLAKES is 60.7%, sulfuric acid consumption is 1.35 tons of sulfuric acid/ton Vanadium Pentoxide in FLAKES, the ratio (assorted phosphorus ratio) that ferric oxide, aluminum oxide and magnesium oxide total impurities in fresh white premix reaction clear liquor account for Vanadium Pentoxide in FLAKES is 11.80%, phosphorus fluorine ratio (P
2o
5/ F) be 37.2, and the assorted phosphorus ratio of sulfuric acid process phosphoric acid by wet process is generally 13 ~ 15%, phosphorus fluorine ratio is 9 ~ 16, and the quality of white fertile treatment solution is better than phosphoric acid by wet process.
Claims (5)
1. a method for calcium hydrophosphate fodder coproduction fertilizer grade monoammonium phosphate, is characterized in that: comprise following process: fresh white fertilizer slurry is carried out pre-reaction with the extraction filtrate that white fertilizer adds sulfuric acid; After reaction slurry sedimentation, supernatant liquid goes slurry process fertilizer grade monoammonium phosphate production system, and to produce fertilizer grade monoammonium phosphate further, the thick slurry of lower floor goes extractive reaction operation; After slurry filtration after extractive reaction, white fertile extraction filtrate returns front operation and fresh white fertilizer and starches and carry out hybrid reaction, and filtered filtration residue is as the raw material of complex phosphate fertilizer.
2. the method for a kind of calcium hydrophosphate fodder coproduction fertilizer grade monoammonium phosphate according to claim 1, it is characterized in that: white fertile extraction filtrate and fresh white fertilizer are starched and carried out pre-extracted reaction, the pH value controlling reaction is 1.2 ~ 1.5, slurry reaction temperature is 20 ~ 45 DEG C, 1.5 ~ 3.0 hours reaction times, reaction slurry solid content 10 ~ 15%.
3. the method for a kind of calcium hydrophosphate fodder coproduction fertilizer grade monoammonium phosphate according to claim 1, it is characterized in that: fresh white fertilizer slurry and white fertilizer add sulfuric acid extract after filtrate carry out hybrid reaction after slip carry out sedimentation concentration after, supernatant liquid is containing Vanadium Pentoxide in FLAKES 15 ~ 20%, enter slurry process fertilizer grade monoammonium phosphate production system to produce fertilizer grade monoammonium phosphate, the thick slurry of the solid content 20 ~ 30% of releasing bottom thickener enters next step extractive reaction adding sulfuric acid.
4. the method for a kind of calcium hydrophosphate fodder coproduction fertilizer grade monoammonium phosphate according to claim 1, it is characterized in that: add the filtration washing water dilution of rear operation in the white fertile thick slurry of the reacted sedimentation of pre-extracted after, then add the vitriol oil and carry out extractive reaction; The pH value controlling reaction slurry is 0.5 ~ 1.0, slurry reaction temperature 30 ~ 50 DEG C, controls 1.5 ~ 3.0 hours reaction times, and the solid content controlling reaction slurry is 10 ~ 15%.
5. the method for a kind of calcium hydrophosphate fodder coproduction fertilizer grade monoammonium phosphate according to claim 4, is characterized in that: carry out the slurry filtration after extractive reaction by adding sulfuric acid, and adds a small amount of clear water washing filter residue; Filtrate containing Vanadium Pentoxide in FLAKES 15 ~ 20% returns the first step and fresh white fertilizer and starches and carry out pre-extracted reaction, the dilution water of white fertilizer slurry extractive reaction made by washings containing Vanadium Pentoxide in FLAKES 1 ~ 3%, and the white fertile filter residue of the compositions such as phosphoric acid iron, aluminum phosphate makes the raw material of complex phosphate fertilizer.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107151026A (en) * | 2017-06-08 | 2017-09-12 | 四川理工学院 | A kind of method of low concentration fluorine-containing hydrochloric acid comprehensive utilization |
| CN110902665A (en) * | 2019-12-12 | 2020-03-24 | 昆明川金诺化工股份有限公司 | Method for improving semi-hydrated phosphoric acid concentration and washing rate |
| CN113104827A (en) * | 2021-04-25 | 2021-07-13 | 湖北云翔聚能新能源科技有限公司 | Method for preparing battery-grade anhydrous iron phosphate from industrial ammonium phosphate clear solution or industrial ammonium phosphate mother solution |
| CN113603070A (en) * | 2021-08-27 | 2021-11-05 | 云南善施化工有限公司 | Production method for preparing phosphoric acid from white fertilizer |
| CN115124009A (en) * | 2022-06-28 | 2022-09-30 | 新希望化工投资有限公司 | Method for producing magnesium hydrogen phosphate and potassium dihydrogen phosphate and co-producing high-purity gypsum by using calcium hydrogen phosphate reclaimed material |
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| CN104140088A (en) * | 2014-07-31 | 2014-11-12 | 四川龙蟒钛业股份有限公司 | Method for producing fertilizer-level monoammonium phosphate through fertilizer-level calcium hydrophosphate |
| CN104261898A (en) * | 2014-10-09 | 2015-01-07 | 龙蟒大地农业有限公司 | Method for improving water-soluble phosphorus content in fertilizer grade calcium hydrophosphate |
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| CN1485269A (en) * | 2002-09-26 | 2004-03-31 | 四川大学 | Method for producing calcium hydrophosphate from high-magnesium phosphorite |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107151026A (en) * | 2017-06-08 | 2017-09-12 | 四川理工学院 | A kind of method of low concentration fluorine-containing hydrochloric acid comprehensive utilization |
| CN110902665A (en) * | 2019-12-12 | 2020-03-24 | 昆明川金诺化工股份有限公司 | Method for improving semi-hydrated phosphoric acid concentration and washing rate |
| CN110902665B (en) * | 2019-12-12 | 2022-11-15 | 昆明川金诺化工股份有限公司 | Method for improving semi-hydrated phosphoric acid concentration and washing rate |
| CN113104827A (en) * | 2021-04-25 | 2021-07-13 | 湖北云翔聚能新能源科技有限公司 | Method for preparing battery-grade anhydrous iron phosphate from industrial ammonium phosphate clear solution or industrial ammonium phosphate mother solution |
| CN113104827B (en) * | 2021-04-25 | 2022-04-29 | 湖北云翔聚能新能源科技有限公司 | Method for preparing battery-grade anhydrous iron phosphate from industrial ammonium phosphate clear solution or industrial ammonium phosphate mother solution |
| CN113603070A (en) * | 2021-08-27 | 2021-11-05 | 云南善施化工有限公司 | Production method for preparing phosphoric acid from white fertilizer |
| CN115124009A (en) * | 2022-06-28 | 2022-09-30 | 新希望化工投资有限公司 | Method for producing magnesium hydrogen phosphate and potassium dihydrogen phosphate and co-producing high-purity gypsum by using calcium hydrogen phosphate reclaimed material |
| CN115124009B (en) * | 2022-06-28 | 2023-12-12 | 新希望化工投资有限公司 | Method for producing magnesium hydrogen phosphate and potassium dihydrogen phosphate and combining high-purity gypsum by utilizing calcium hydrogen phosphate reclaimed material |
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Application publication date: 20160323 |