CN102030318B - Sulfur-economizing method for extracting phosphoric acid - Google Patents
Sulfur-economizing method for extracting phosphoric acid Download PDFInfo
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- CN102030318B CN102030318B CN201010528091A CN201010528091A CN102030318B CN 102030318 B CN102030318 B CN 102030318B CN 201010528091 A CN201010528091 A CN 201010528091A CN 201010528091 A CN201010528091 A CN 201010528091A CN 102030318 B CN102030318 B CN 102030318B
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- phosphoric acid
- acid
- reaction
- decalcification
- extraction
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Abstract
The invention relates to a sulfur-economizing method for extracting phosphoric acid, wherein liquid phase of SO3 (sulfur trioxide) in the extraction of the phosphoric acid is reacted with phosphate pulp for removing calcium oxide in phosphorite and reducing the consumption of sulfuric acid during extracting the phosphoric acid; and the process steps are as follows: (1) dividing filtered acid obtained by filtering slurry for extracting the phosphoric acid into two parts, enabling one part of the filtered acid to be concentrated directly or be used for producing other phosphorus chemical products, and enabling the other part of the filtered acid and the part for washing a filter cake to be diluted by diluted phosphoric acid containing 15%-18% of P2O5 (phosphorus oxide) and further enter into a decalcification reaction system; (2) adding the diluted phosphoric acid after dilution and the phosphate pulp into a decalcification reaction tank, and stirring for reaction; and (3) settling and thickening the decalcified slurry, wherein clear solution refers to feeding desulfurized phosphoric acid into a feed-grade calcium hydrogen phosphate production system, and heavy paste is a phosphoric acid extraction system for using the phosphate pulp which removes part of the calcium oxide to produce the phosphoric acid through the dehumidification process. By utilizing the method, the calcium oxide in the removed phosphorite in the phosphoric acid production process by utilizing the feed grade calcium hydrogen phosphate for desulfurization through the diluted acid process can be utilized, the consumption of the sulfuric acid during extracting the phosphoric acid through the wet process can be reduced, and the production cost can be further saved.
Description
Technical field
The present invention relates to save sulphur phosphoric acid extraction method, particularly the joint sulphur phosphoric acid extraction method of phosphate fertilizer or the used phosphoric acid by wet process of other phosphate production and the coproduction of calcium hydrophosphate fodder desulfurization phosphoric acid.
Background technology
The sulfuric acid cost of phosphoric acid by wet process phosphoric acid extraction accounts for 45～50% of whole phosphoric acid by wet process cost, moreover the sulphur resource also is China's Nonrenewable resources in short supply.Joint sulphur phosphoric acid extraction technology is that the new technology that pursuit reduces production costs is explored by phosphorous chemical industry enterprise always.The sulphur-economizing type new technology has some improvement in recent years; Like one Chinese patent application 96117513 sulphur-economizing ammonium phosphate-producing slurry process; Its technical characterictic only is that the sulfuric acid reaction with phosphorus ore slurry or ground phosphate rock and excessive 3～7% makes phosphoric acid by wet process; Make monoammonium phosphate with the gas ammonia neutralization reaction again, it is characterized in that in the phosphoric acid by wet process that makes (or phosphor ammonium slurry), adding the secondary phosphorus ore slurry or the ground phosphate rock of respective amount; Its technical characterictic of working method of one Chinese patent application 96117680 industrial monoammonium phosphates and industrial monoammonium phosphate and calcium hydrogen phosphate fodder is; Phosphoric acid by wet process with the higher mid low grade phosphate rock production of iron, aluminium, magnesium addition content is a raw material; It is characterized in that comprising pre-treatment, filtration successively, once neutralize, filtration, secondary neutralization, spraying drying operation; Pre-treatment is in phosphoric acid by wet process, to add sodium salt or sylvite and ground phosphate rock, makes contained fluorine silicon ion SiF6 in they and the phosphoric acid by wet process
2-React from sulfuric acid, to remove fluorine silicon ion SiF6
2-With sulfate radical SO4
2-Thereby, voluminous phosphoric acid, once neutralization is in the filtrating of pre-treatment after-filtration gained, to feed gas ammonia, control 2.0≤pH＜4.0, the secondary neutralization is in once and after-filtration, feeds gas ammonia in the gained filtrating, the pH value is controlled at 4.0～5.0.These technology are only stressed to be used for following process after the purifying treatment to phosphoric acid by wet process, not to the processing of phosphoric acid extraction with the ore deposit.
Summary of the invention
The object of the invention just provides a kind of dilute phosphoric acid of concentrated phosphoric acid and joint sulphur phosphoric acid extraction method of calcium hydrophosphate fodder desulfurization phosphoric acid coproduction of being used for; This method is to utilize in the diluted acid method calcium hydrophosphate fodder desulfurization production process of phosphoric acid to remove the quicklime in the phosphorus ore; Sulfuric acid consumption when reducing the phosphoric acid by wet process phosphoric acid extraction saves production cost thereby reach.
For achieving the above object, the method that the contriver provides may further comprise the steps:
A kind of method that saves the sulphur phosphoric acid extraction is characterized in that, liquid phase SO3 in phosphoric acid extraction and the phosphoric acid extraction and the reaction of phosphorus ore slurry remove the quicklime in the phosphorus ore, the sulfuric acid consumption when reducing phosphoric acid extraction; This process step comprises:
(1) using extracted phosphoric acid liquor is filtered gained and filter sour separated into two parts, a part of filter acid directly removes to concentrate or produce other phosphorus chemical products, and another part filter acid and the part of washing leaching cake are used and contained P2O5 and remove the decalcification reactive system after 15%～18% the light phosphoric acid dilution;
(2) light phosphoric acid after will diluting and concentration are that 67%～72% phosphorus ore slurry adds the decalcification reactive tank in 1: 1.1～1.5 ratios; Fully reaction under stirring action; 65 ℃～80 ℃ of its temperature of reaction; 2～4 hours reaction times, reaction stirring intensity 87r/min, decalcification pulp density (1.25～1.30) * 10
3Kg/m
3
(3) the decalcification slip is through the sedimentation stiff, and its clear liquid parameter is SO3＜5.5g/l, CaO 12～15g/l; Clear liquid is that desulfurization phosphoric acid goes the calcium hydrophosphate fodder production system; The dry phosphoric acid extraction system of method phosphoric acid of the phosphorus ore slurry that thick slurry promptly removes partially oxidation calcium.
The prerequisite that the inventive method has an exploitativeness is that the soluble calcium salt dilute phosphoric acid that contains that is used for after the decalcification does not influence the subsequent product quality.Need the phosphorus chemical product coproduction of Wet-process Phosphoric Acid Production to have the advantage of practicing thrift cost for the calcium hydrophosphate fodder production of diluted acid method and other especially.
Use the inventive method, can not only guarantee that each sour index of coproduction is able to guarantee, can practice thrift the sulfuric acid cost of phosphoric acid by wet process phosphoric acid extraction simultaneously.
Embodiment
At the 30kt/a of applicant Kunming Chuanjinnuo Chemical Co., Ltd. concentrated phosphoric acid and the coproduction of 15kt/a desulfurization phosphoric acid, the liquid phase SO in phosphoric acid extraction and the phosphoric acid extraction
3With the reaction of phosphorus ore slurry, remove the quicklime in the phosphorus ore, the sulfuric acid consumption when reducing phosphoric acid extraction.Implement by following step.
(1) with 19.0～20.0m
3/ h (CaO/P
2O
51.4, P
2O
5: 30%, H
2O 35～37%) phosphorus ore slurry send into the decalcification reactive tank and filter filter acid and be diluted to the light phosphoric acid of part and contain P
2O
5Diluted acid 9.5～10.5m of 15～18%
3/ h keeps 65～80 ℃ of temperature of reaction, and reaction is 2～4 hours under stirring action, reaction stirring intensity 87r/min;
(2) reacted decalcification slip being sent into the sedimentation of stiff device handles.Clear liquid SO
3＜5.5g/l, CaO 12～15g/l is desulfurization phosphoric acid and sends into the calcium hydrophosphate fodder production system, and thick slurry promptly removes the phosphorus ore slurry of partially oxidation calcium and sends into phosphoric acid by wet process extraction workshop section;
(3) slip behind the extractive reaction is got part filtrating 12.5～13.5m after filtering
3(22～25%P2O5) directly go to concentrated phosphoric acid workshop section to/h; Another part filtrating 2.5～3.5m
3/ h (22～25%P2O5) with light phosphoric acid 7～8m
3(12～14%P2O5) mixed dilute phosphoric acids directly remove decalcification slurry reaction groove to/h;
Pass through above-mentioned steps; Dilute phosphoric acid and the reaction of phosphorus ore slurry; Remove the quicklime 9～11.5kg/t (doing the ore deposit) of phosphorus ore slurry; On the liquid extraction phosphoric acid plant of the 45kt/a of applicant contriver company, practice thrift sulfuric acid 56～70kg (100%H2SO4)/TP2O5, year practice thrift 2520～3150 tons in sulfuric acid, make profits surplus in the of 100 ten thousand yuan.
Claims (1)
1. a method that saves the sulphur phosphoric acid extraction is characterized in that, the liquid phase SO in phosphoric acid extraction and the phosphoric acid extraction
3With the reaction of phosphorus ore slurry, remove the quicklime in the phosphorus ore, the sulfuric acid consumption when reducing phosphoric acid extraction; This process step comprises:
(1) using extracted phosphoric acid liquor is filtered gained and filter sour separated into two parts, a part of filter acid directly removes to concentrate or produce other phosphorus chemical products, and the part of another part filter acid and washing leaching cake is with containing P
2O
5Be to remove the decalcification reactive system after 15%～18% the light phosphoric acid dilution;
(2) light phosphoric acid after will diluting and concentration are that 67%～72% phosphorus ore slurry adds the decalcification reactive tank in 1: 1.1～1.5 ratios; Fully reaction under stirring action; 65 ℃～80 ℃ of its temperature of reaction; 2～4 hours reaction times, reaction stirring intensity 87r/min, decalcification pulp density (1.25～1.30) * 10
3Kg/m
3
(3) the decalcification slip is through the sedimentation stiff, and its clear liquid parameter is SO
3＜5.5g/l, CaO 12～15g/l; Clear liquid is that desulfurization phosphoric acid goes the calcium hydrophosphate fodder production system; The dry phosphoric acid extraction system of method phosphoric acid of the phosphorus ore slurry that thick slurry promptly removes partially oxidation calcium.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010528091A CN102030318B (en) | 2010-11-02 | 2010-11-02 | Sulfur-economizing method for extracting phosphoric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010528091A CN102030318B (en) | 2010-11-02 | 2010-11-02 | Sulfur-economizing method for extracting phosphoric acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102030318A CN102030318A (en) | 2011-04-27 |
| CN102030318B true CN102030318B (en) | 2012-10-10 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010528091A Active CN102030318B (en) | 2010-11-02 | 2010-11-02 | Sulfur-economizing method for extracting phosphoric acid |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102674286B (en) * | 2012-05-25 | 2013-11-13 | 四川龙蟒磷化工有限公司 | Method for preparing high-quality feed-grade calcium hydrophosphate by by-product waste acid of titanium dioxide |
| CN113651300A (en) * | 2021-08-16 | 2021-11-16 | 四川绵竹市盘龙矿物质有限责任公司 | Method for improving phosphorus yield by using phosphorite with high calcium-phosphorus ratio for wet-process phosphoric acid purification |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1283584A (en) * | 1999-08-04 | 2001-02-14 | 四川大学 | Process for preparing calcium hydrogen phosphate from middle-and low-grade phosphorus ore |
| CN1789118A (en) * | 2004-12-17 | 2006-06-21 | 冯孝桂 | Method for producing feed calcium hydrogen phosphate using sulphuric acid method |
| CN101318643A (en) * | 2008-06-10 | 2008-12-10 | 云南新龙矿物质饲料有限公司 | Sulphur-calcium conserving method for preparing feedstuff level hydrogen phosphate with phosphoric acid and wet-process |
-
2010
- 2010-11-02 CN CN201010528091A patent/CN102030318B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1283584A (en) * | 1999-08-04 | 2001-02-14 | 四川大学 | Process for preparing calcium hydrogen phosphate from middle-and low-grade phosphorus ore |
| CN1789118A (en) * | 2004-12-17 | 2006-06-21 | 冯孝桂 | Method for producing feed calcium hydrogen phosphate using sulphuric acid method |
| CN101318643A (en) * | 2008-06-10 | 2008-12-10 | 云南新龙矿物质饲料有限公司 | Sulphur-calcium conserving method for preparing feedstuff level hydrogen phosphate with phosphoric acid and wet-process |
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| CN102030318A (en) | 2011-04-27 |
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Address after: 654100 Sifang Industrial Park, Dongchuan District, Kunming, Yunnan Applicant after: Kunming Chuanjinnuo Chemical Shares Co., Ltd. Address before: 654100 Sifang Industrial Park, Dongchuan District, Kunming, Yunnan Applicant before: Kunming Chuanjinnuo Chemical Co., Ltd. |
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