CN101734950A - Method for producing ammoniated triple superphosphate - Google Patents
Method for producing ammoniated triple superphosphate Download PDFInfo
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- CN101734950A CN101734950A CN200910102966A CN200910102966A CN101734950A CN 101734950 A CN101734950 A CN 101734950A CN 200910102966 A CN200910102966 A CN 200910102966A CN 200910102966 A CN200910102966 A CN 200910102966A CN 101734950 A CN101734950 A CN 101734950A
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Abstract
The invention relates to a method for producing ammoniated triple superphosphate, which is characterized by comprising the following steps of: (1) mixing concentrated phosphoric acid and the ore pulp of phosphorus refined ore into two reaction tanks in cascade to react; (2) then pumping the material pulp into a granulator by a pulp spraying pump to coat and granulate with a return material; meanwhile, charging liquid ammonia into the granulator to neutralize free acid; (3) leading granulated materials to enter a drier from an outlet of the granulator and carrying out dehydration and drying in parallel with hot air from a hot-blast stove; (4) drawing a qualified granules as a product by a breakage screening system, leading an unqualified particle to enter the granulator by a material return system to coat and granulate again and recycling. The ammoniated triple superphosphate produced by the method has wider soil application range, is not only suitable for the fertilization of acid soil but also suitable for the fertilization of alkaline soil, therefore, the product competitiveness is larger, and the market value is higher.
Description
Technical field
The present invention relates to phosphate fertilizer, furthermore, relate to double superhosphate (abbreviation coarse whiting), relate in particular to ammoniated triple superphosphate.
Background technology
Traditional double superhosphate production method is to be 48%～52% phosphorolytic cleavage phosphorus ore with concentration after concentrating, and spray granulating forms then.The production of double superhosphate is to use the phosphorolytic cleavage ore deposit, breaks the molecular structure of calcium monofluorophosphate, makes it be reassembled into monocalcium phosphate (being coarse whiting) molecule, CaO in the calcium monofluorophosphate molecule: P
2O
5Be 5: 1.5, and should be 1: 1 in the monocalcium phosphate, so must replenish P when being the raw material production monocalcium phosphate with the phosphorus ore
2O
5, promptly replenish phosphoric acid.Chemical reaction is as follows:
Ca
5(PO
4)
3F+7H
3PO
4+5H
2O＝5Ca(H
2PO
4)
2·H
2O+HF
There is free acid in traditional coarse whiting (calcium superphosphate product), the coarse whiting product belongs to the product of acidic medium, the crop applying of suitable alkaline soil only, and the free acid that contains in the common calcium superphosphate is generally about 2.5%～6.5%, in soil, combine with moisture, form fluid loss easily, be unfavorable for the absorption of plant.Therefore must reduce free acid as far as possible when producing the coarse whiting product, or neutralize with alkaline fertilizer and to use, visible coarse whiting product is used inconvenience, market is limited.Adopt ammonating process to reduce the central free acid of coarse whiting, allow the coarse whiting product form the wider scope of using, be the problem that people study always.
Do not retrieve at present the patent relevant with ammoniated triple superphosphate.
Summary of the invention
Purpose of the present invention just is to provide a kind of production method of ammoniated triple superphosphate, to improve the nutritive ingredient of coarse whiting product, enlarges it and uses scope.
The production method of the ammoniated triple superphosphate that the contriver provided comprises:
(1) strong phosphoric acid and phosphorus concentrate pulp are mixed in the reactive tank of two tandems and react;
(2) then slip is squeezed in the tablets press and the returning charge coating granulation with spray pump, in tablets press, fed in the liquefied ammonia simultaneously and free acid;
(3) granulated materials enters drying machine from the tablets press outlet, and the hot blast that comes with hotblast stove dewaters side by side, drying;
(4) afterwards through the crushing and screening system, qualified particle is taken out is product, and underproof particle is coating granulation again in revert system enters tablets press again, and cyclic production is gone down so always.
In the above-mentioned the first step, strong phosphoric acid acid is dense to be 52%; The granularity of above-mentioned phosphorus concentrate pulp is 80% mistake, 200 orders, moisture≤30%; The sour ore deposit ratio of above-mentioned adding is 1: 2.4; Reaction times was controlled at about 40 minutes, and temperature of reaction is controlled at 90 ℃～100 ℃; Reaction back slip proportion is 1.80～1.85, and slurry temperature is 90 ℃～100 ℃, free P in the slip
2O
5Be 14%～16%; Ratio of calcium and phosphorus is 0.89.
The contriver points out, temperature of reaction such as deficiency can add the low-pressure steam heating.
In above-mentioned second step, the amount of neutralization back control free acid is in 1%, and the free acid of material is reduced to about 1% from 6%, and the pH value of material rises to 6～7 from 3～4; Tablets press internal return ratio was less than 8: 1, and prilling temperature is 90 ℃～100 ℃, tablets press outlet free acid≤0.5%, granulation material moisture≤5%.
The liquefied ammonia amount that adds in above-mentioned second step is pressed following calculating: whitewashing amount * 1.2=product volume, and total ammonia amount=product volume * 2%, wherein, 2% is the nitrogen content controlling index in the product, the 1.2nd, the ratio of whitewashing amount and product volume.
In above-mentioned the 3rd step, the entrance end hot blast temperature of drying machine is controlled at 350 ℃～500 ℃; The material outlet temperature is 90 ℃～100 ℃, and the tail gas temperature out is 85 ℃～95 ℃; The discharging water content is less than 3.0%.
In above-mentioned the 4th step, described qualified particle size is 1～4mm, and underproof particle is greater than 4mm; Described revert system comprises that the returning charge bucket puies forward operation, once sieves operation, regrading operation, and product is extracted operation out.
After the above-mentioned once screening, greater than the coarse fodder of 4mm by broken retrieval system; Less than the regrading that enters of 4mm, the 1～4mm particle after the screening is extracted out as product once more, less than the particle of 1mm retrieval system once more.
Product quality indicator is: effective P
2O
5〉=40%, total nitrogen 〉=2%, moisture≤3.0%, granularity (2～4.75mm) 〉=90%, free acid≤0.5%.
Does promptly citric acid soluble phosphorus increase, available phosphorus reduces for whether the rise characteristic of back material of the pH value that proves material changes? through experiment and analysis, the product nitrogen content rises to about 1%～2%, and citric acid soluble phosphorus does not increase, and available phosphorus does not reduce; Product increases little from the composition that mono-calcium phosphate transfers Lin Suanergai to.
The ammoniated triple superphosphate that the inventive method is produced, the soil of adaptation is wideer, not only is fit to acidity, be more suitable for the fertilising of alkaline soil, so its product competitiveness is bigger, and marketable value is higher.
Description of drawings
Fig. 1 is the structural representation of tablets press, and among the figure: 1 is tablets press, and 2 is the tablets press motor, and 3 for the returning charge chute, and 4 be the tablets press feed opening, and 5 take out mouth for tail gas, and 6 is the shotcrete pipe wire system, and 7 is secondary benefit ammonia pipe.
Fig. 2 is the revert system process flow diagram.
Embodiment
Two series of embodiment Wengfu Group Co., Ltd. diammonium phosphate device all adopt diammonium phosphate device to produce sulfur-bearing phosphate fertilizer product.Specific practice is:
At first powdery sulphur adding sulfur melting system is melted and make liquid-state sulfur, secondly in reactive tank, add the diammonium phosphate slurry that reactions such as ammonia, phosphoric acid are made, add sulfuric acid again by producing load, its vitriol oil amount is pressed 1: 0.10308 adding (whitewashing amount and sulfuric acid ratio); In the import by spray pump of the blending ratio of the slip of 1: 0.06 ratio and liquid-state sulfur, squeeze into spray granulating in the tablets press by spray pump afterwards again, the whitewashing amount is by producing load adjustment.
For the slurry temperature that makes reaction reaches more than 120 ℃, the reactive tank slip is heated (setting up steam coils in reactive tank) with low-pressure steam, simultaneously in order to guarantee that molten sulfur is under mixing with slip, thorough mixing is even, does not solidify agglomeratingly below 118 ℃ in its sulphur zero pour, and its slip transfer lime is taked the mode of jacket pipe, interior pipe is the slip transfer lime, outer tube is a steam companions, takes low-pressure steam companion heat, slurry temperature is made eventually remain on more than 120 ℃;
In the process of carrying, feed steam tracing preheating slip transfer lime earlier, carry slip then, after under meter is checked the whitewashing amount, calculate required sulphur amount by 1: 0.06 proportional meter, add needed molten sulfur amount by molten sulfur transferpump and molten sulfur variable valve then; Also by 1: 0.10308 quantity adding sulfuric acid, be responsible for control reactive tank temperature, indexs such as degree of neutralization in its reactive tank by producing;
Its returning charge is regulated in 4: 1 ratio, then in tablets press with the anti-slip of pipe spray granulating inside, enter in the drying machine dry then with hot blast.Drying machine is imported and exported control indexes: advance drying machine flue-gas temperature T≤250 ℃, go out T=95 ℃ of drying machine flue-gas temperature, advance drying machine inventory G=400t/h, advance drying machine material moisture W
1=3.5%, go out drying machine material moisture W
2≤ 2.0%, advance T=89.5 ℃ of drying machine temperature of charge.
After after twice crushing and screening, extract qualified product pellet (1-4mm) out, underproof product enters revert system again, enters coating granulation in the tablets press.
Two series of Wengfu Group Co., Ltd.'s diammonium phosphate device all adopt this explained hereafter ammoniated triple superphosphate product, and inner quality, cost control are all very good, and the product appearance quality is also good, can create the economic worth of more than one hundred million units, is subjected to user's favorable comment.
Claims (7)
1. the production method of an ammoniated triple superphosphate, its feature comprises:
(1) strong phosphoric acid and phosphorus concentrate pulp are mixed in the reactive tank of two tandems and react;
(2) then slip is squeezed in the tablets press and the returning charge coating granulation with spray pump, in tablets press, fed in the liquefied ammonia simultaneously and free acid;
(3) granulated materials enters drying machine from the tablets press outlet, and the hot blast that comes with hotblast stove dewaters side by side, drying;
(4) afterwards through the crushing and screening system, qualified particle is taken out is product, coating granulation, the circulation so repeatedly again in revert system enters tablets press again of underproof particle.
2. the method for claim 1 is characterized in that in the first step of described method, and strong phosphoric acid acid is dense to be 52%; The granularity of above-mentioned phosphorus concentrate pulp is 80% mistake, 200 orders, moisture≤30%; The sour ore deposit ratio of above-mentioned adding is 1: 2.4; Reaction times was controlled at about 40 minutes, and temperature of reaction is controlled at 90 ℃～100 ℃; Reaction back slip proportion is 1.80～1.85, and slurry temperature is 90 ℃～100 ℃, free P in the slip
2O
5Be 14%～16%; Ratio of calcium and phosphorus is 0.89.
3. the method for claim 1 is characterized in that in second step of described method, and the amount of neutralization back control free acid is in 1%, and the free acid of material is reduced to about 1% from 6%, and the pH value of material rises to 6～7 from 3～4; Tablets press internal return ratio was less than 8: 1, and prilling temperature is 90 ℃～100 ℃, tablets press outlet free acid≤0.5%, granulation material moisture≤5%.
4. as the described method in one of claim 1 or 3, the liquefied ammonia amount that it is characterized in that described adding is by following calculating: whitewashing amount * 1.2=product volume, and total ammonia amount=product volume * 2%, wherein, 2% is the nitrogen content controlling index in the product, the 1.2nd, and the ratio of whitewashing amount and product volume.
5. the method for claim 1 is characterized in that the entrance end hot blast temperature of drying machine is controlled at 350 ℃～500 ℃ in the 3rd step of described method; The material outlet temperature is 90 ℃～100 ℃, and the tail gas temperature out is 85 ℃～95 ℃; The discharging water content is less than 3.0%.
6. the method for claim 1 is characterized in that described qualified particle size is 1～4mm in the 4th step of described method, and underproof particle is greater than 4mm; Described revert system comprises that the returning charge bucket puies forward operation, once sieves operation, regrading operation, and product is extracted operation out.
7. as the described method in one of claim 1 or 6, it is characterized in that described once screening after, greater than the coarse fodder of 4mm by broken retrieval system; Less than the regrading that enters of 4mm, the 1～4mm particle after the screening is extracted out as product once more, less than the particle of 1mm retrieval system once more.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910102966A CN101734950A (en) | 2009-12-23 | 2009-12-23 | Method for producing ammoniated triple superphosphate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910102966A CN101734950A (en) | 2009-12-23 | 2009-12-23 | Method for producing ammoniated triple superphosphate |
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| CN101734950A true CN101734950A (en) | 2010-06-16 |
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| CN200910102966A Pending CN101734950A (en) | 2009-12-23 | 2009-12-23 | Method for producing ammoniated triple superphosphate |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102757273A (en) * | 2012-06-26 | 2012-10-31 | 宜兴申利化工有限公司 | Production method of high-concentration phosphorus-potassium binary compound fertilizer |
| CN105418167A (en) * | 2015-11-19 | 2016-03-23 | 昆明川金诺化工股份有限公司 | Method of reducing triple superphosphate free acid with fertilizer grade calcium hydrophosphate |
| CN106831002A (en) * | 2017-01-20 | 2017-06-13 | 昆明川金诺化工股份有限公司 | A kind of granular double superhosphate energy-saving production method |
| CN114307921A (en) * | 2021-12-15 | 2022-04-12 | 防城港盛农磷化有限公司 | Device and method for controlling slurry fluidity and curing efficiency |
-
2009
- 2009-12-23 CN CN200910102966A patent/CN101734950A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102757273A (en) * | 2012-06-26 | 2012-10-31 | 宜兴申利化工有限公司 | Production method of high-concentration phosphorus-potassium binary compound fertilizer |
| CN105418167A (en) * | 2015-11-19 | 2016-03-23 | 昆明川金诺化工股份有限公司 | Method of reducing triple superphosphate free acid with fertilizer grade calcium hydrophosphate |
| CN106831002A (en) * | 2017-01-20 | 2017-06-13 | 昆明川金诺化工股份有限公司 | A kind of granular double superhosphate energy-saving production method |
| CN114307921A (en) * | 2021-12-15 | 2022-04-12 | 防城港盛农磷化有限公司 | Device and method for controlling slurry fluidity and curing efficiency |
| CN114307921B (en) * | 2021-12-15 | 2023-07-21 | 防城港盛农磷化有限公司 | Device and method for controlling fluidity and curing efficiency of slurry |
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Application publication date: 20100616 |