CN101857213B - Method for preparing food-grade diammonium phosphate from wet-process phosphoric acid - Google Patents
Method for preparing food-grade diammonium phosphate from wet-process phosphoric acid Download PDFInfo
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Abstract
The invention discloses a method for producing food-grade diammonium phosphate from wet-process phosphoric acid. The low-cost wet-process phosphoric acid is adopted as a raw material, is subjected to impurity removal and undergoes neutralization reaction with ammonia twice to prepare the food-grade diammonium phosphate; a pickling procedure is adopted, so that volatile gas materials are recycled, crystallization mother liquor is recycled or concentrated for recycling, the food-grade diammonium phosphate product is obtained, and the product yield is improved; meanwhile, byproducts in the production process are used as compound fertilizer materials. The method greatly reduces the production cost of the food-grade diammonium phosphate, ensures the stability of product quality, avoids secondary pollution, and has low energy consumption and good economic and social benefits.
Description
Technical field:
The invention belongs to the foodstuff additive preparing technical field, relate to a kind of method with preparing food-grade diammonium phosphate from wet-process phosphoric acid.
Background technology:
Diammonium phosphate claims again Secondary ammonium phosphate, and molecular formula is (NH
4)
2HPO
4Diammonium phosphate is used as raising agent, dough conditioning agent, yeast food, brewages fermentation assistant, buffer reagent etc.
In prior art, the preparation monoammonium phosphate belongs to technical grade more.Such as Chinese patent 88104525.X a kind of method for preparing diammonium phosphate with Rock Phosphate (72Min BPL), the vitriol oil and ammonia as raw material has been proposed, through operations such as concentrated dilute phosphoric acid, pre-neutralization, reaction choosing grain, drying and screenings, obtain granular diammonium phosphate product, product is a kind of agrochemical.The advantage of the method is not need main equipment just can obtain high-quality diammonium phosphate chemical fertilizer.Chinese patent 90102317.5 has proposed a kind of technique for preparing the diammonium phosphate granular chemical fertilizer; be included in the tubular reactor ammonification phosphoric acid that is arranged in drying machine; with whole phosphoric acid and basically all ammonia feed in the drying machine by tubular reactor, make NP or NPK fertilizer.The method is a kind of low recycle ratio of preparation diammonium phosphate and the technique of less energy-consumption.Chinese patent 92106621.X discloses a kind of production method of diammonium phosphate, and its processing step is: a, dilute phosphoric acid and gas ammonia carry out neutralization reaction one time, make degree of neutralization reach 1.1～1.2; B, slip concentrate, and moisture drops to 30%; C, the slip after concentrated overflows to neutralizing well and gas ammonia carries out the secondary neutralization reaction, makes the slip degree of neutralization bring up to 1.5～1.8, and moisture is down to about 25%, and the neutralizing well slurry temperature is at 100～110 ℃; D, the slip after the secondary neutralization reaction is delivered to spray granulation drier carry out granulation, drying.Although aforesaid method can obtain to meet the diammonium phosphate of 10205-88 national standard salable product, but have the following disadvantages: the slip degree of neutralization that 1, carries out concentration operation is higher, therefore the enriching slurry moisture content is high, not only energy consumption for drying is large, and subsequent process can only adopt the spray granulating drying process; 2, spray granulating technique not only can not ammonification in granulation process because drying temperature is high, and material ammonia escaped quantity is large in the drying process, and the product N/P ratio can not reach the index of traditional diammonium phosphate (DAP) fertilizer; 3, in the enriching slurry secondary and adopt the loss of groove type reactor ammonia large.Chinese patent 99101150.3 discloses a kind of method of producing diammonium phosphate with external circulation ammoniation reactor, the phosphoric acid of the method take 32～38% is as raw material, phosphoric acid and gas ammonia carry out neutralization reaction in ammoniation reactor, temperature of reaction is controlled at 100～120 ℃, the slip degree of neutralization is controlled at 1.40～1.55, reaction slurry is flowed out in the slurry vessel by the upflow tube that is located on the ammoniation reactor, a part of slip in the slurry vessel is sent to whitewashing, granulation, obtain desired product, another part slip in the slurry vessel is delivered to ammoniation reactor downtake bottom by recycle pump, to add the flowability of slip in the bassoon.This kind method weak point be: 1, adopt concentrated phosphoric acid production diammonium phosphate, belong to traditional Phosphoric Acid Concentration technique, higher to the specification of quality of phosphorus ore; 2, phosphoric acid once is neutralized to the product degree of neutralization, and the ammonia escaped quantity is very large; 3, granulating and drying adopts spray granulating technique equally, has the same deficiency of Chinese patent 92106621.X.Chinese patent 200610021182.6 adopts method and the secondary ammoniation reactor of the concentrated production diammonium phosphate of acid slime, take the wet method dilute phosphoric acid as raw material, processing step is followed successively by that aminating reaction, acid slime are concentrated, secondary ammoniation reaction, rotary drum ammoniation-granulation and drying, the ammonia-containing exhaust that rotary drum ammoniation-granulation and drying step produce and dust wash with the wet method dilute phosphoric acid, and the washings that obtains is used for an aminating reaction.The processing parameter of above-mentioned steps: an aminating reaction, preparation degree of neutralization are 0.5～1.0 Acidic Ammonium Phosphate Pulp; Acid slime is concentrated, and the terminal point water content that makes Acidic Ammonium Phosphate Pulp is 13～20% (massfractions); The secondary ammoniation reaction is carried out under gauge pressure 0～0.15MPa, and 110～150 ℃ of temperature of reaction bring up to 1.30～1.50 with the degree of neutralization of phosphor ammonium slurry; The rotary drum ammoniation-granulation; secondary ammoniation is reacted the atomizing of prepared phosphor ammonium slurry to be spilled on the bed of material in the conventional drum ammoniation granulating machine; in granulation process, spray into liquefied ammonia or gas ammonia; with the further ammonification of material to degree of neutralization 1.60～1.90; keep 70～100 ℃ prilling temperature; the water content that goes out the tablets press material is controlled at 2～4% dryings, and the water content of diammonium phosphate is controlled at 1.0～1.5% (massfractions).The mass concentration of the wet method dilute phosphoric acid that aforesaid method uses is 18～30%, the mid low grade phosphate rock preparation that both available foreign matter content is high, again available high-quality phosphorus ore preparation.
From prior art as can be known, produce at present food grade phosphoric acid two ammoniums and adopt traditional method more, namely utilize thermal phosphoric acid, refining is that food grade phosphoric acid and ammonia react generate.Although production process equipment is simple, quality product is high, and the apparatus and process technical requirements is high, and cost is large, and energy consumption is high, pollutes large.
Summary of the invention:
Order of the present invention: in order to overcome the problem that exists in the prior art, guarantee that whole production process avoids secondary pollution and reduce energy consumption, make it have preferably economic benefit and social benefit, a kind of method with preparing food-grade diammonium phosphate from wet-process phosphoric acid is provided.
Technical scheme of the present invention is:
Adopt cheaply that phosphoric acid by wet process and ammonia are raw material, carry out neutralization reaction twice, strictly control processing condition, guarantee the stability of quality product, crystalline mother solution reclaims and uses, and adopts simultaneously pickling process that the Ammonia recovery of volatilization is used, cut down the consumption of raw materials, and avoid secondary pollution.
The present invention is achieved in that
Method with preparing food-grade diammonium phosphate from wet-process phosphoric acid, as raw material take phosphoric acid by wet process, after removal of impurities, make with the ammonia neutralization reaction, comprise: removal of impurities, once filtration, once neutralization, secondary filtration, secondary neutralization, pickling, concentrated, crystallization, centrifugal and drying process, concrete operation step is as follows:
A. dropping into weight concentration in the raw materials pretreatment still is 38～42%P
2O
5Phosphoric acid by wet process, and add dearsenic agent, stir dearsenifications reaction 10～60 minutes 30～90 ℃ of temperature are lower, the beavy metal impurities such as wherein arsenic of precipitation, lead, the impurity such as part sulphur, calcium, fluorine, aluminium, silicon in the while precipitate phosphoric acid;
B. the treatment solution that a step is obtained carries out the solid-liquid separation first time, and filtrate is for subsequent use for a reactor, and filter cake is sent to the Solid waste disposal center;
C. in a reactor, drop into the crystalline mother solution that reactor volume 5～20% loops back, start agitator, slowly add through removal of impurities phosphoric acid, and passing into ammonia, neutralization reaction is first time carried out in control pH=4.4～4.6 under 30～100 ℃ of temperature, be back to after the ammonia absorption of pickling process with volatilization simultaneously in reactor, control PH=4.4～4.6 are the neutralization reaction terminal point first time, after stopping to feed intake, continue to stir 10～90 minutes, obtain intermediates food grade phosphoric acid one ammonium slip;
D. the intermediates food grade phosphoric acid one ammonium slip that the c step is obtained carries out the solid-liquid separation second time, removes impurity, and in No. two reactors of food grade phosphoric acid one ammonium slip input of filtration, filter cake is sent to composite fertilizer source mill;
E. start the agitator of No. two reactors, then slowly pass into ammonia and carry out the neutralization reaction second time, control reaction solution PH=7.8～8.0 be neutralization reaction terminal point for the second time, obtain food grade phosphoric acid two ammonium solutions, are back to after the ammonia absorption of pickling process with volatilization in reactor;
F. it is concentrated that food grade phosphoric acid two ammonium solutions that the e step obtained are delivered in the concentrating unit heating, until relative density is 1.20 ~ 1.30, the ammonia of volatilization returns after pickling process absorbs in reactor;
G. the concentrated solution with the f step moves in the crystallizer tank, at temperature crystallisation by cooling below 40 ℃, forms food grade phosphoric acid two crystalline ammonium bodies;
H. with the food grade phosphoric acid two crystalline ammonium bodies of g step, carry out for the third time solid-liquid separation, mother liquor returns c or f step, and xln makes food grade phosphoric acid two ammoniums after super-dry.
Above-described dearsenic agent is P
2S
5, add-on is 1～1.3 times of arsenic amount in the acid.
Above-described reactor and pre-treatment still equipment comprise in stainless steel cauldron, inner liner polytetrafluoroethylene reactor and the enamel reaction still one or more.
The equipment that above-described solid-liquid separation adopts, first and second time solid-liquid separation adopts plate-and-frame filter press, and solid-liquid separation adopts whizzer for the third time.
The equipment that above-described pickling is adopted comprises bubble absorbing tower, packed absorber and tray absorption columns.
The equipment of above-described concentrated employing is vacuum concentrator.
The above-described dry equipment that adopts comprises rotating drum dryer and vibratory screening apparatus drying machine.
The connection of above-described equipment, comprise being connected of raw materials pretreatment still and a reactor, reactor respectively with being connected of plate-and-frame filter press and absorption tower, No. two reactors respectively with being connected of plate-and-frame filter press, vacuum concentrator and absorption tower, vacuum concentrator respectively with being connected of crystallizer tank and absorption tower, crystallizer tank is connected with whizzer, and whizzer is connected with moisture eliminator.
Advantage of the present invention and positively effect:
1. take phosphoric acid by wet process as raw material, reclaim crystalline mother solution and volatilization raw material, improve the product yield, greatly reduce production cost;
2. strictly control processing condition, quality product is high, good stability;
3. the byproduct in the production process can be made composite fertilizer material, and the volatilization raw materials recovery uses, and Recycling Mother Solution is used, and avoids secondary pollution, and both protection of the environment reduced again the three wastes and energy consumption, had preferably economic benefit and social benefit.
Description of drawings:
Accompanying drawing 1: be process flow diagram of the present invention.
As shown in the figure, technical process of the present invention mainly comprises: removal of impurities, once filtration, once neutralization, secondary filtration, secondary neutralization, pickling, concentrated, crystallization, centrifugal and drying process.
Embodiment:
The invention will be further described below in conjunction with drawings and Examples, and listed embodiment only is the present invention is described and never is limited to the present invention.
Embodiment one
Dropping into weight concentration in the raw materials pretreatment still is 40%P
2O
5Phosphoric acid by wet process, add the P of 1.1 times of arsenic amounts according to arsenic content wherein
2S
5, 60 ℃ of lower stirrings 50 minutes, obtain containing the precipitation slip; While hot above-mentioned slip is carried out the first time with plate-and-frame filter press and filter, filtrate is for subsequent use for an enamel reaction still, and filter cake is sent to the Solid waste disposal center; In an enamel reaction still, drop into the recovery crystalline mother solution of reactor volume 20%, start agitator, slowly add through removal of impurities phosphoric acid, and slowly pass into ammonia, and control PH=4.4 carries out neutralization reaction first time under 55 ℃ of temperature, and the ammonia of volatilization is back to reaction kettle for reaction No. one after the absorption of pickling bubble absorbing tower, control PH=4.4 is the neutralization reaction terminal point first time, after stopping to feed intake, continue to stir 20 minutes, obtain intermediates food grade phosphoric acid one ammonium slip; The intermediates food grade phosphoric acid one ammonium slip that obtains is filtered with plate-and-frame filter press, remove impurity, in No. two enamel reaction stills of food grade phosphoric acid one ammonium solution input after the filtration, filter cake is sent to composite fertilizer source mill; Start the agitator of No. two enamel reaction stills, then slowly pass into ammonia and carry out the neutralization reaction second time, control reaction solution PH=7.8 is the neutralization reaction terminal point second time, obtain food grade phosphoric acid two ammonium solutions, after the ammonia absorption of pickling bubble absorbing tower with volatilization, be back to reaction kettle for reaction No. one; Food grade phosphoric acid two ammonium solutions that obtain are delivered in the vacuum concentrator heating concentrated, until relative density is 1.30, after the pickling bubble absorbing tower absorbs the ammonia of volatilization, be back to reaction kettle for reaction No. one; Concentrated solution is moved in the crystallizer tank, form food grade phosphoric acid two crystalline ammonium bodies at 40 ℃ of lower crystallisation by cooling of temperature, then carry out centrifugation with whizzer, during mother liquor returns once and operation recycle or through concentration and recovery food grade phosphoric acid two ammonium products, xln makes food grade phosphoric acid two ammoniums after the rotating drum dryer drying.
Embodiment two
Dropping into weight concentration in the raw materials pretreatment still is 38%P
2O
5Phosphoric acid by wet process, add the P of 1.3 times of arsenic amounts according to arsenic content wherein
2S
5, 50 ℃ of lower stirrings 60 minutes, obtain containing the precipitation slip; While hot above-mentioned slip is carried out the first time with plate-and-frame filter press and filter, filtrate is for subsequent use for a stainless steel cauldron, and filter cake is sent to the Solid waste disposal center; In a stainless steel cauldron, drop into the recovery crystalline mother solution of reactor volume 15%, start agitator, slowly add through removal of impurities phosphoric acid, and slowly pass into ammonia, and control PH=4.6 carries out the neutralization reaction first time under temperature 70 C, and the ammonia of volatilization is back to reaction kettle for reaction No. one after the pickling packed absorber absorbs, control PH=4.6 is the neutralization reaction terminal point first time, after stopping to feed intake, continue to stir 30 minutes, obtain intermediates food grade phosphoric acid one ammonium slip; The intermediates food grade phosphoric acid one ammonium slip that obtains is filtered with plate-and-frame filter press, remove impurity, in No. two stainless steel cauldrons of food grade phosphoric acid one ammonium solution input after the filtration, filter cake is sent to composite fertilizer source mill; Start the agitator of No. two stainless steel cauldrons, then slowly pass into ammonia and carry out the neutralization reaction second time, control reaction solution pH=7.9 is the neutralization reaction terminal point second time, obtain food grade phosphoric acid two ammonium solutions, be back to reaction kettle for reaction No. one after the ammonia absorption of pickling packed absorber with volatilization; Food grade phosphoric acid two ammonium solutions that obtain are delivered in the vacuum concentrator heating concentrated, until relative density is 1.20, the pickling packed absorber is back to reaction kettle for reaction No. one after the ammonia of volatilization is absorbed; Concentrated solution is moved in the crystallizer tank, form food grade phosphoric acid two crystalline ammonium bodies at 35 ℃ of lower crystallisation by cooling of temperature, then carry out centrifugation with whizzer, during mother liquor returns once and operation recycle or through concentration and recovery food grade phosphoric acid two ammonium products, xln makes food grade phosphoric acid two ammoniums after vibratory screening apparatus drying machine drying.
Claims (1)
1. method with preparing food-grade diammonium phosphate from wet-process phosphoric acid, as raw material take phosphoric acid by wet process, after removal of impurities, make with ammonia secondary neutralization reaction, it is characterized in that: comprise removal of impurities, once filtration, once neutralization, secondary filtration, secondary neutralization, pickling, concentrated, crystallization, centrifugal and drying process, concrete operation step is as follows:
A. drop into weight concentration in the raw materials pretreatment still and be 38% or 40%P
2O
5Phosphoric acid by wet process, and add dearsenic agent P
2S
5, stir dearsenifications reaction 50 minutes or 60 minutes 30 ℃ of temperature or 50 ℃ or 60 ℃ are lower, the beavy metal impurities such as wherein arsenic of precipitation, lead, part sulphur, calcium, fluorine, aluminium or sila matter in the while precipitate phosphoric acid;
B. the treatment solution that a step is obtained adopts plate-and-frame filter press to carry out the solid-liquid separation first time, and filtrate is for subsequent use for a reactor, and filter cake is sent to the Solid waste disposal center;
C. in a reactor, drop into the crystalline mother solution that reactor volume 5～20% loops back, start agitator, slowly add through removal of impurities phosphoric acid, and slowly pass into ammonia, control pH4.4 or pH4.6, under 30 ℃ or 55 ℃ or 70 ℃ of temperature, carry out the neutralization reaction first time, after absorbing the ammonia of volatilization, pickling process is back to simultaneously in reactor, control pH4.4 or pH4.6 are the neutralization reaction terminal point first time, after stopping to feed intake, continue to stir 20 minutes or 30 minutes or 90 minutes, obtain intermediates food grade phosphoric acid one ammonium slip;
D. the intermediates food grade phosphoric acid one ammonium slip that the c step is obtained adopts plate-and-frame filter press to carry out the solid-liquid separation second time, removes impurity, and in No. two reactors of food grade phosphoric acid one ammonium slip input of filtration, filter cake is sent to composite fertilizer source mill;
E. start the agitator of No. two reactors, then slowly pass into ammonia and carry out the neutralization reaction second time, control reaction solution pH=7.8 or 7.9 obtains food grade phosphoric acid two ammonium solutions as neutralization reaction terminal points for the second time, is back to after pickling process absorbs the ammonia of volatilization in reactor;
F. it is concentrated that food grade phosphoric acid two ammonium solutions that the e step obtained are delivered in the concentrating unit heating, until relative density is 1.20～1.30, the ammonia of volatilization returns after pickling process absorbs in reactor;
G. the concentrated solution with the f step moves in the crystallizer tank, at 40 ℃ of temperature or 35 ℃ of crystallisation by cooling, forms food grade phosphoric acid two crystalline ammonium bodies;
H. the food grade phosphoric acid two crystalline ammonium bodies with the g step adopt whizzer to carry out for the third time solid-liquid separation, and mother liquor returns c or f step, and xln makes food grade phosphoric acid two ammoniums after super-dry,
Described dearsenic agent is P
2S
5, add-on is 1～1.3 times of arsenic content in the phosphoric acid by wet process.
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| CN102530900B (en) * | 2011-12-29 | 2014-02-05 | 广西利达磷化工有限公司 | Method for concentrating ammonium phosphate mother solution by using heat energy generated during combustion of yellow phosphorus |
| CN103058157A (en) * | 2013-02-26 | 2013-04-24 | 贵州开磷（集团）有限责任公司 | Production method of industrial grade diammonium phosphate with wet-process phosphoric acid |
| CN103848407B (en) * | 2013-04-02 | 2016-01-13 | 襄阳泽东化工集团有限公司 | A kind of production method of monoammonium phosphate |
| CN104261937B (en) * | 2014-09-19 | 2016-01-06 | 贵州开磷集团股份有限公司 | A kind of production method preparing primary ammonium phosphate by-product Chinese yam special fertilizer |
| CN104276550B (en) * | 2014-09-19 | 2016-08-17 | 贵州开磷集团股份有限公司 | A kind of production method preparing diammonium phosphate by-product Fructus Colocasiae Esculentae special fertilizer |
| CN107954406B (en) * | 2017-11-03 | 2020-05-08 | 菏泽金正大生态工程有限公司 | Method for producing high-quality industrial diammonium phosphate by using composite salt purification wet-process phosphoric acid |
| CN110577202A (en) * | 2019-09-27 | 2019-12-17 | 瓮福达州化工有限责任公司 | battery-grade phosphate preparation system and preparation process thereof |
| CN110681487A (en) * | 2019-09-27 | 2020-01-14 | 瓮福达州化工有限责任公司 | Iron removing system and preparation process thereof |
| CN110877901B (en) * | 2019-12-16 | 2023-02-28 | 瓮福达州化工有限责任公司 | Method and system for producing industrial-grade monoammonium phosphate and industrial-grade diammonium phosphate by wet-process phosphoric acid |
| CN111498821A (en) * | 2020-04-23 | 2020-08-07 | 湖北兴发化工集团股份有限公司 | Process and device for producing diammonium hydrogen phosphate and ammonium dihydrogen phosphate by taking phosphoric acid as raw material |
| CN113501509B (en) * | 2021-08-19 | 2022-12-30 | 云南云天化红磷化工有限公司 | System and method for preparing 66% powdery monoammonium phosphate by one-step method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0161704A2 (en) * | 1984-04-18 | 1985-11-21 | ENICHEM AGRICOLTURA S.p.A. | Process for the production of water soluble ammonium phosphates |
| CN1907843A (en) * | 2006-08-24 | 2007-02-07 | 四川川大中德环保技术有限公司 | Method of classification utilizing wet-process phosphoric acid |
| CN101337664A (en) * | 2008-08-11 | 2009-01-07 | 湖北祥云(集团)化工股份有限公司 | Process for co-producing diammonium phosphate and monoammonium phosphate by slurry concentration method |
| RU2368567C1 (en) * | 2008-05-29 | 2009-09-27 | Закрытое акционерное общество "Научно-производственная компания "Интерфос" | Method of obtaining edible ammonium phosphates |
-
2010
- 2010-06-04 CN CN 201010191966 patent/CN101857213B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0161704A2 (en) * | 1984-04-18 | 1985-11-21 | ENICHEM AGRICOLTURA S.p.A. | Process for the production of water soluble ammonium phosphates |
| CN1907843A (en) * | 2006-08-24 | 2007-02-07 | 四川川大中德环保技术有限公司 | Method of classification utilizing wet-process phosphoric acid |
| RU2368567C1 (en) * | 2008-05-29 | 2009-09-27 | Закрытое акционерное общество "Научно-производственная компания "Интерфос" | Method of obtaining edible ammonium phosphates |
| CN101337664A (en) * | 2008-08-11 | 2009-01-07 | 湖北祥云(集团)化工股份有限公司 | Process for co-producing diammonium phosphate and monoammonium phosphate by slurry concentration method |
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