CN1321883C - Method for producing calcium hydrogen phosphate fodder - Google Patents
Method for producing calcium hydrogen phosphate fodder Download PDFInfo
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- CN1321883C CN1321883C CNB011072156A CN01107215A CN1321883C CN 1321883 C CN1321883 C CN 1321883C CN B011072156 A CNB011072156 A CN B011072156A CN 01107215 A CN01107215 A CN 01107215A CN 1321883 C CN1321883 C CN 1321883C
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Abstract
The present invention relates to a method for producing calcium dihydrogenphoshate used as an animal feed mineral additive. The is mainly characterized in that wet-process phosphoric acids are used as raw materials, the phosphonic acids as raw materials are processed in a trash extraction and purification mode; then, slurry reaction is carried out to the phosphonic acids; slurry obtain after reaction are sprayed into hot air in a drop shape through a nozzle, so that the slurry is crystallized, solidified and dried into calcium dihydrogenphoshate as a product in the process of falling in the hot air. The invention has the advantage of low production cost, and the product produced by the present invention has a particle shape; the present invention is convenient to disperse uniformly in main feed, and conforms to the shape requirement of feed additives.
Description
One, technical field
Invention relates to the production technology of animal-feed mineral additive, and particularly relating to phosphoric acid is the method that main material production is used as the monocalcium phosphate of animal-feed mineral additive.
Two, background technology
Fodder additives is the indispensable nutritive ingredient of animal-feed, and it is to promoting that growing of animal has important effect.At present, the animal-feed mineral additive mainly contains two kinds, and a kind of is monocalcium phosphate (CaHpHO
42H
2O), another kind is secondary calcium phosphate (Ca (HpHO
4)
2H
2O).Secondary calcium phosphate is as animal feedstuff additive, beast-like animals there is effect preferably, but to poultry, particularly to hydrocoles, because its poorly water-soluble, to the DeGrain that grows of promotion animal, and monocalcium phosphate is as the animal-feed mineral additive, not only beast-like animals there is good effect, poultry and hydrocoles are also had very good effect.Because the advantage that monocalcium phosphate had and the development of culture fishery, market is in great demand to monocalcium phosphate.
The technology of producing monocalcium phosphate still adopts traditional Technology at present, and promptly the thermal phosphoric acid with limestone powder and high density reacts, and generates the monocalcium phosphate of solid state, makes the product monocalcium phosphate through pulverizing again.Adopt this Technology to produce monocalcium phosphate and have two relatively distinct issues.One, because must the working concentration very high thermal phosphoric acid of this technology is as raw materials for production, and the production cost height of thermal phosphoric acid, price is expensive, and is therefore also correspondingly high with the monocalcium phosphate cost of this explained hereafter, and price is also expensive.Its two, adopt the monocalcium phosphate of this explained hereafter, form in the form of sheets with the powdered mixture, to the appearance requirement of feed mineral additive, promptly micronize, homogenizing are convenient to additive and are uniformly dispersed not consistent in the main body feed with at present.
Three, summary of the invention
It is low to the objective of the invention is to disclose a kind of production cost at the weak point of prior art, and its mode of appearance of the product of production meets the monocalcium phosphate producing and manufacturing technique that at present feed mineral additive mode of appearance is required.
Foregoing invention purpose of the present invention can be achieved through the following technical solutions.
1, with Impurity removal agent and P
2O
5Weight content is that 15～22% raw material phosphoric acid by wet process purifies reaction, generates impure solid phase, and the reaction feed liquid is removed the impurity solid phase, the P of purifying phosphoric acid after filtration
2O
5Weight content is 13～24%;
2, purifying phosphoric acid and calcium salt are 60～80 ℃ in temperature, have and carry out the slip reaction under the stirring condition, and the solid concentration that reacts to the slip entered next workshop section at these 30～50% o'clock, and phosphoric acid is 100: 15～100: 40 with the weight of material ratio of calcium salt;
3, after the slip of slip reaction end enters the crystallization granulation dryer section, become to drip the shape ejection from the nozzle that is positioned at crystallization granulation moisture eliminator top, enter temperature and be in 150～260 ℃ the warm air, slip drops in the process of whereabouts by crystallization, solidify, be dried to microgranular finished product.
For the purification process section in the such scheme, the kind of its Impurity removal agent, processing step and processing condition all will be decided according to raw material phosphoric acid by wet process impurities situation.
When only containing a spot of fluorine impurity in as the phosphoric acid by wet process of raw material, in the purification process section of such scheme, sylvite or sodium salt are adopted in the Impurity removal agent, as vitriolate of tartar, sodium sulfate, Repone K, sodium-chlor etc.Raw material phosphoric acid and potassium/sodium salt are 60～80 ℃ in temperature, have under the stirring condition and react, and the reaction times is 30～60 minutes.Phosphoric acid is 100: 1～100: 5 with the weight of material ratio of potassium/sodium salt.
When the impurity in the raw material phosphoric acid by wet process except that containing a spot of fluorine impurity, when also containing a spot of iron, aluminium, magnesium addition, purification process section at such scheme, the Impurity removal agent is a calcium cpd, as limestone powder, unslaked lime, white lime etc., phosphoric acid and Impurity removal agent are 40～50 ℃ in temperature, have to purify under the stirring condition and reacted 30～70 minutes that the weight of material beguine of raw material phosphoric acid and calcium cpd determines that according to the pH value that purifies reaction solution the scope of pH value is 2.6～3.1.
When containing in the phosphoric acid by wet process as raw material outside a spot of fluorine, also contain many iron, aluminium, during magnesium addition, purification process section at such scheme, with the calcium cpd is the Impurity removal agent, as limestone powder, unslaked lime, white lime etc., the step type purification process that employing is made up of two to three clean units that are made of reaction member and filtering unit, in the purification reaction of each grade, phosphoric acid and calcium cpd all are to be 40～50 ℃ in temperature, have and purify reaction 30～40 minutes under the stirring condition, the reaction phosphoric acid of next stage is from the filtered liquid of upper level, the weight of material beguine of phosphoric acid and calcium cpd is determined according to the pH value of reaction solution, the pH value increases step by step, every grade increases by 0.2～0.6, and the pH value of last step is 2.6～3.1.The progression that the step type clean-up stage is contained depends on the foreign matter content in the raw material phosphoric acid.
When containing more fluorine, iron, aluminium, magnesium addition in the phosphoric acid by wet process as raw material, purification process section in the such scheme adopts two sections purifications, first section is the Impurity removal agent with sylvite or sodium salt, the processing condition of its purification reaction as previously mentioned, be that temperature of reaction is 60～80 ℃ and has under the stirring condition and react, reaction times is 30～60 minutes, and the weight of material ratio is 100: 1～100: 5.Second section is the Impurity removal agent with the calcium cpd, the processing condition of its purification reaction as previously mentioned, promptly adopt the step type reaction purification process of forming by two to three clean units that constitute by reaction member and filtering unit, in the purification reaction of each grade, phosphoric acid and calcium cpd all are to be 40～50 ℃ in temperature, have and reacted under the stirring condition 30～40 minutes, the reaction phosphoric acid of next stage is from the filtered liquid of upper level, the weight of material beguine of phosphoric acid and calcium cpd is determined according to the pH value of reaction solution, the pH value increases step by step, every grade increases by 0.2～0.6, and the scope of the pH value of last step is 2.6～3.1.
In order to realize above-mentioned purpose of the present invention better, also can further take following technical measures;
When the Impurity removal agent is calcium cpd, when promptly being the Impurity removal agent with limestone powder, unslaked lime, white lime etc., in last step clean unit reaction slurry or the filter residue 1/3～1/2 can be turned back to initial first order reaction unit, provide crystal seed for purifying reaction.
In the purification reaction that with sylvite or sodium salt is the Impurity removal agent, add an amount of being used to and quicken the additive that fluorion is separated out.Additive can be hydroxyl ethylidene tetra-sodium, diatomite, phosphoric acid fat starch etc.
In order to improve the filterableness of feed liquid, when material should not filter, can in feed liquid, add an amount of flocculating aids.Flocculating aids can be polyacrylamide, diatomite, this sour sodium of ten disulfos etc.
The present invention compared with the prior art; its advantage is that with cheap phosphoric acid by wet process be raw materials for production; is raw materials for production than prior art with the thermal phosphoric acid of high density; production cost greatly reduces; the monocalcium phosphate of producing becomes microgranular; be convenient in the main body feed, be uniformly dispersed, meet current the micronized requirement of animal-feed mineral additive.And the present invention can be by transforming and can produce existing calcium hydrogen phosphate fodder production technique a little, and the utmost point promptly of the present invention is convenient to implement, and cost of equipment is low.The ability that simultaneously can also keep producing secondary calcium phosphate is promptly produced the main technique equipment of calcium hydrogen phosphate fodder, not only can be used for producing secondary calcium phosphate, but also can produce monocalcium phosphate, has not only improved plant factor, has also increased the kind of product.
Because monocalcium phosphate is than the phosphorus content height of common secondary calcium phosphate, good water solubility not only can be used for the beast-like animals fodder additives, also can be used for the fodder additives of poultry and hydrocoles, be particularly useful for the latter, its effect is fairly obvious, therefore, and as fodder additives, can prepare all kinds of animal-feeds, good effect is all arranged, use without limits, convenient, flexible.The market has openings of monocalcium phosphate is very big at present, and along with the development of poultry Developing of Animal Industry, particularly culture fishery, the demand of monocalcium phosphate will increase considerably.It is a kind of new that the production that is disclosed as monocalcium phosphate of the present invention provides, and very feasible production technique.
Four, description of drawings
Accompanying drawing 1 is the technological process of production figure of the present invention when being used for the raw material phosphoric acid by wet process and containing small amount of fluorine impurity.
Accompanying drawing 2 is that the present invention is used for the raw material phosphoric acid by wet process except that containing small amount of fluorine impurity, the technological process of production figure when also containing many iron, aluminium, magnesium addition.
Accompanying drawing 3 is the present invention technological process of production figure when being used for the raw material phosphoric acid by wet process and containing than polyfluoro, iron, aluminium, magnesium addition.
Five, embodiment
Provide three specific embodiments of the present invention below, and in conjunction with the embodiments the present invention is carried out more concrete description.
Embodiment 1:
P with the production of Sichuan Jin He phosphorus ore
2O
5Content is about 18%, fluorine content is about 2.23% 100 parts of phosphoric acid by wet processes (weight), 2 parts in sodium sulfate (weight) as the Impurity removal agent, 0.02 part of hydroxyethyl tetra-sodium (weight) as additive, add and be provided with in the reactive tank of agitator, remain on about 70 ℃ in temperature of reaction, have under the stirring condition and reacted about 45 minutes.Reacted feed liquid joins centrifugal filter and filters, get rid of filter residue, filtrate enters the purification reactor that is provided with agitator once more, and add limestone powder simultaneously and purify reaction, temperature of reaction is about 45 ℃, stirs in the process of reaction, and the add-on of limestone powder is controlled at about 2.6 the pH value of reaction feed liquid, reacted about 50 minutes, impurity is separated out from phosphoric acid.Feed liquid is sent into centrifugal filter separate, remove filter residue, filtrate is the clean phosphoric acid of producing monocalcium phosphate.Again clean phosphoric acid is sent into the slip reactor that is provided with agitator, the limestone powder that adds 12.5 parts (weight) simultaneously reacts, temperature of reaction is controlled at about 75 ℃, stir simultaneously, the solid concentration that reacts to the slip reaches about 35%, slip is sent into the dry workshop section of crystallization granulation, make slip become to drip the shape ejection from the nozzle that is arranged in crystallization granulation moisture eliminator top, entering temperature is about in the warm air about 180 ℃, gob in the dropping process of warm air by crystallization, solidify, dry, drop to bottom of device and be product, it is microgranular that monocalcium phosphate becomes, totally 28 parts (weight).
Embodiment 2:
P with the production of Kaiyang, Guizhou phosphorus ore
2O
5Content is about 20.9%, fluorine content is about 100 parts of 1.74% phosphoric acid by wet processes, as 2.2 parts in the sodium sulfate of Impurity removal agent, as 0.015 part of the hydroxyethyl tetra-sodium of additive, add in the reactive tank that is provided with agitator and react, temperature of reaction is about 70 ℃, stirs in the reaction, and the reaction times is about 45 minutes.Feed liquid is sent into centrifugal filter filter, remove filter residue, filtrate is the clean phosphoric acid of producing monocalcium phosphate.Phosphoric acid after purifying is sent into the slip reactor that is provided with agitator, and the limestone powder that adds 15.6 parts (weight) simultaneously carries out the slip reaction, temperature of reaction is about 75 ℃, stir in the reaction, react solid concentration to slip when reaching 40% left and right sides, slip is sent into the dry workshop section of crystallization granulation, make slip become to drip the shape ejection from the nozzle that is positioned at crystallization granulation moisture eliminator top, entering temperature is about in the warm air about 200 ℃, in the process that falls by crystallization, solidify, be dried to the product monocalcium phosphate, it is microgranular that product becomes, and can obtain 37.5 parts of (weight) products in the bottom of equipment.
Embodiment 3:
P with the production of Yichang phosphorus ore
2O
5Content is about 15%, and fluorine content is about 1.85% 100 parts of phosphoric acid by wet processes (weight), and 2.1 parts of Paris whites (weight) add the reactor be provided with agitator, and the pH value of feed liquid is controlled at about 2.8.Temperature of reaction is about 45 ℃, stir in the reaction, reacted about 40 minutes, feed liquid is sent into centrifugal filter and is filtered, and removes filter residue, filtrate enters subordinate's purification reactor, and add 1.1 parts of (weight) limestone powders, and the pH value of feed liquid is controlled at about 3.1, temperature of reaction keeps about 40 ℃, stir simultaneously, the reaction times was about about 40 minutes.Feed liquid is sent into centrifugal filter filters, remove filter residue, filtrate entering is provided with the slip reactor of agitator, add 37.5 parts of secondary calcium phosphate powder simultaneously and carry out the slip reaction, temperature of reaction is about 70 ℃, stir simultaneously, react when the slip solid concentration reaches 45% left and right sides, slip is sent into the dry workshop section of crystallization granulation, make slip become drip the shape ejection, enter temperature and be in the warm air about 170 ℃ from the nozzle that is arranged in the equipment top, in dropping process by crystallization, solidify, be dried to the product monocalcium phosphate, it is microgranular that product becomes, and obtains 51 parts of products in device bottom.
It needs to be noted that here embodiment that the present invention provides and process flow sheet are used for that the invention will be further described, are not used to limit protection domain of the present invention, those skilled in the art has the ability it is made some change fully.
Claims (1)
1, a kind of production method of monocalcium phosphate is characterized in that:
A, usefulness Impurity removal agent and P
2O
5Weight content is that 15～22% raw material phosphoric acid by wet process purifies reaction, generates impure solid phase, removes solid phase after filtration, the P of purifying phosphoric acid
2O
5Weight content is 13～24%;
B, purifying phosphoric acid and calcium salt be 60～80 ℃ in temperature, have and carry out the slip reaction under the stirring condition, reacts solid concentration to the slip and reach at 30～50% o'clock and enter next workshop section, and phosphoric acid is 100: 15～100: 40 with the weight of material ratio of calcium salt;
C, enter the slip of the dry workshop section of crystallization granulation, become to drip the shape ejection from the nozzle that is positioned at crystallization granulation moisture eliminator top, enter temperature and be in 150～260 ℃ the warm air, slip drops in the process of whereabouts by crystallization, solidify, be dried to microgranular finished product.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011072156A CN1321883C (en) | 2001-02-28 | 2001-02-28 | Method for producing calcium hydrogen phosphate fodder |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011072156A CN1321883C (en) | 2001-02-28 | 2001-02-28 | Method for producing calcium hydrogen phosphate fodder |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1371862A CN1371862A (en) | 2002-10-02 |
| CN1321883C true CN1321883C (en) | 2007-06-20 |
Family
ID=4656162
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011072156A Expired - Fee Related CN1321883C (en) | 2001-02-28 | 2001-02-28 | Method for producing calcium hydrogen phosphate fodder |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1321883C (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101618974B (en) * | 2009-07-22 | 2011-09-21 | 西北师范大学 | Method for preparing triple superphosphate fertilizer by using waste water generated in synthetic process of 2, 4, 6-trichloropyrimidine |
| CN102815681B (en) * | 2012-06-21 | 2014-05-28 | 中化云龙有限公司 | Method for producing feed-grade calcium dihydrogen phosphate from wet-process phosphoric acid |
| CN105417516A (en) * | 2015-12-18 | 2016-03-23 | 瓮福（集团）有限责任公司 | Production method for feed-grade monocalcium phosphate |
| CN109437135A (en) * | 2018-11-09 | 2019-03-08 | 湖北富邦科技股份有限公司 | A kind of method of phosphoric acid by wet process decoloration |
| CN114890399A (en) * | 2022-05-27 | 2022-08-12 | 重庆瑞富食品添加剂有限公司 | Preparation method of monocalcium phosphate monohydrate |
-
2001
- 2001-02-28 CN CNB011072156A patent/CN1321883C/en not_active Expired - Fee Related
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|---|---|
| CN1371862A (en) | 2002-10-02 |
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