CN101885630A - Dual-slurry ammonization granulation compound fertilizer production technology - Google Patents
Dual-slurry ammonization granulation compound fertilizer production technology Download PDFInfo
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- CN101885630A CN101885630A CN 201010222299 CN201010222299A CN101885630A CN 101885630 A CN101885630 A CN 101885630A CN 201010222299 CN201010222299 CN 201010222299 CN 201010222299 A CN201010222299 A CN 201010222299A CN 101885630 A CN101885630 A CN 101885630A
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Abstract
The invention discloses a dual-slurry ammonization granulation compound fertilizer production technology, which is characterized by high nitrogen content and adjustable available nutrients. The technology comprises the following steps: 1, carrying out secondary dechlorination at low temperature; 2, dissolving phosphorus and mixing slurries; 3, cooling and absorbing; 4, melting and dissolving urea; 5, aminating and granulating; 6, drying and cooling; 7, screening and smashing; and 8, packaging. By using the invention, nitrogen content of sulfanyl compound fertilizers rises to 25% from 13%, recycle ratio reduces to 20-30% from 40-50%, yield of single-pass granulation in a granulator is greatly improved, dechlorination time is shortened to 1h from over 2h by adopting the secondary dechlorination technology, the dechlorination is thorough, and the production efficiency is greatly improved.
Description
Technical field
The present invention relates to a kind of dual-slurry ammonization granulation compound fertilizer production technology.
Background technology
The S-based compound fertilizer of traditional ammoniation-granulation explained hereafter is nitrogen content lower (12.5%～13.5%) often, and dechlorination operation holding time is long, and production efficiency is low.
Summary of the invention
Technical problem to be solved by this invention is: provide a kind of nitrogen content higher, dechlorination operation holding time is short, the high nitrogen product of the sulfenyl that production efficiency is high compound fertilizer production technology.
For solving the problems of the technologies described above, dual-slurry ammonization granulation compound fertilizer production technology of the present invention comprises the steps:
1. low temperature secondary dechlorination; 2. molten phosphorus mixes slurry; 3. cooling and absorbing; 4. melting and dissolving urea; 5. ammoniation-granulation; 6. dry cooling; 7. screening is pulverized; 8. finished product packing.
The invention has the beneficial effects as follows: use production technique of the present invention, the nitrogen content that can make S-based compound fertilizer brings up to 25% by original 13%; Returning charge is than being reduced to 20%～30% by original 40%～50%, and therefore the qualification rate of one way granulation also is greatly improved in the tablets press; Adopt the secondary dechlorination process to make the dechlorination time shorten to present one hour by original more than two hour, and dechlorination is thorough, therefore production efficiency also be greatly improved.
Embodiment
(1) low temperature secondary dechlorination
A certain amount of vitriol oil is pumped in the dechlorination groove, again Repone K is joined in the feed bin with lift, evenly join the dechlorination groove by the opening for feed of screw feeder from dechlorination groove top, generate sal enixum and hydrogen chloride gas with strong sulfuric acid response, the chemical equation of this reaction is: KCl+H
2SO
4=KHSO
4+ HCl ↑ in the dechlorination process, the temperature of reaction mass is controlled between 125 ℃～135 ℃, type of heating employing steam indirect heating and steam directly spray in the dechlorination groove and heat dual mode, directly to spray into type of heating, indirect heating is auxilliary, regulate the conversion type of heating according to material moisture, the benefit of doing like this is that the water content of reaction mass can be controlled by the conversion type of heating, fundamentally having solved traditional processing technology adopts steam directly to spray into heating moisture is increased and to cause reaction not exclusively thereby the halfway problem of dechlorination, another benefit of bringing simultaneously is to have reduced material moisture, has reduced the load of dry materials.
For dechlorination thorough, traditional way is that reaction mass must stop more than 2 hours in the dechlorination groove, and reaction is carried out fully, produce little subnormal ambient by blower fan in the dechlorination groove again, the hydrogen chloride gas that reaction is generated overflows from reaction mass fully.In order to reduce the dechlorination time, enhance productivity, novel process adopts the technology of secondary dechlorination to solve, the concrete technology of so-called secondary dechlorination is: by installing baffle plate additional, the dechlorination groove is isolated into four reaction zones that size is impartial in the dechlorination groove, first district is a charging zone, second district is a main reaction region, the 3rd district and the 4th district are the dechlorination district, between four districts, realize the material transmission by culvert stream and overflow dual mode.
In process of production, pressure in the dechlorination groove is regulated by adjusting rotation speed of fan, generally is controlled at about 9500Pa, can guarantee that like this hydrogen chloride gas physical efficiency of dechlorination groove internal reaction generation is all removed, unlikelyly again siphon away too much water vapour, concentration of hydrochloric acid is reduced.
The hydrogen chloride gas that produces in the dechlorination groove is guided to cooling and absorbing workshop section by blower fan and is absorbed with de-salted water and become hydrochloric acid; The sal enixum and the excess sulfuric acid overflow that generate enter mixed stock tank.
(2) molten phosphorus mixes slurry
The ammonium phosphate solution that dissolving is good pumps into pump and mixes in the stock tank, overflows to the potassium hydrogen sulfate solution that mixes in the stock tank with the dechlorination groove and mix the formation nitration mixture under the effect of stirring, and surveys its proportion and gets final product about 1.55 (70 ℃).
(3) cooling and absorbing
After the hydrogen chloride gas that produces in the dechlorination groove is guided to cooling and absorbing workshop section by adjustable speed fan, be introduced into and carry out condensation in the graphite condenser, water vapor condensation is got off to enter into condensate trap, again the liquid in the condensate trap is driven into the hydrochloric acid medial launder with pump.
(4) melting and dissolving urea
With certain amount of urea join add in the melting and dissolving urea groove hot melt molten after, be driven in the spray granulating machine reaction slurry that comes with the tubular reactor spray with pump and be sprayed onto coating granulation on the material curtain that constitutes by returning charge simultaneously.
(5) ammoniation-granulation
From the gas ammonia at ammonia station with enter into tubular reactor simultaneously from the nitration mixture that mixes stock tank and react; discharge a large amount of heat in the reaction process; temperature and pressure in the tubular reactor is all improved rapidly, and reaction slurry sprays under pressure in the tablets press and is sprayed on coating granulation on the material curtain that is made of returning charge with the molten slurry of the urea that sprays into simultaneously.
(6) dry cooling
Material leaves tablets press and enters whizzer; in whizzer with from the stack gas of hotblast stove is reverse, contact; redundant moisture and a little dust leave whizzer drying blower fan with stack gas and enter and wash dust in the spray scrubber off in the material, and gas directly is discharged in the atmosphere.Material enters after the whizzer drying in the rotating cylinder Air cooler and the chilled air cools of being introduced by blower fan; freezing air leaves and enters dust-settling compartment behind the Air cooler and remove the part big dust particle; enter spiral dust catcher again and remove part small-particle dust, the dust of removing is fallen belt conveyor from the particle collector of dust-settling compartment and spiral dust catcher bottom and is delivered to tablets press as returning charge.Residual gas enters atmosphere after entering and washing the residue dust in the circulation cleaning tower off.
(7) screening is pulverized
Cooled material is sent in the trommel screen extension set through feed belt, and sieve apparatus is divided into two districts, and a district removes thin dirt and small-particle, and the material that sieve falls is collected through loading head and fallen on the feed belt, turns back to secondary granulation in the tablets press again; Undersized in two districts is work in-process, collects to fall into through loading head and sends into the coating machine inner investment on the feed belt, and remaining large granular materials enters the pulverizer pulverizing after leaving sieve apparatus, and the material after the pulverizing also is sent to secondary granulation in the tablets press again through feed belt.
(8) finished product packing
The work in-process that fall from sieve apparatus are collected through loading head and are fallen into feed belt and send into the coating machine coating, leave coating machine behind the coating again and enter feed bin, pack through electronic scale metering back and are finished product.
Claims (1)
1. dual-slurry ammonization granulation compound fertilizer production technology is characterized in that comprising the steps:
(1) low temperature secondary dechlorination
A certain amount of vitriol oil is pumped in the dechlorination groove, again Repone K is joined in the feed bin with lift, evenly join the dechlorination groove by the opening for feed of screw feeder from dechlorination groove top, generate sal enixum and hydrogen chloride gas with strong sulfuric acid response, the chemical equation of this reaction is: KCl+H
2SO
4=KHSO
4+ HCl ↑ in the dechlorination process, the temperature of reaction mass is controlled between 125 ℃～135 ℃, type of heating employing steam indirect heating and steam directly spray in the dechlorination groove and heat dual mode, directly to spray into type of heating, indirect heating is auxilliary, regulate the conversion type of heating according to material moisture, the secondary dechlorination: in the dechlorination groove by installing baffle plate additional, the dechlorination groove is isolated into four reaction zones that size is impartial, first district is a charging zone, second district is a main reaction region, the 3rd district and the 4th district are the dechlorination district, between four districts, realize the material transmission by culvert stream and overflow dual mode, the pressure in the dechlorination groove is regulated by adjusting rotation speed of fan, generally is controlled at about 9500Pa, the hydrogen chloride gas that produces in the dechlorination groove is guided to cooling and absorbing workshop section by blower fan becomes hydrochloric acid with the de-salted water absorption, and the sal enixum of generation and excess sulfuric acid overflow enter mixed stock tank;
(2) molten phosphorus mixes slurry
The ammonium phosphate solution that dissolving is good pumps into pump and mixes in the stock tank, overflows to the potassium hydrogen sulfate solution that mixes in the stock tank with the dechlorination groove and mix the formation nitration mixture under the effect of stirring, and surveys its proportion to get final product about 1.55 (70 ℃);
(3) cooling and absorbing
After the hydrogen chloride gas that produces in the dechlorination groove is guided to cooling and absorbing workshop section by adjustable speed fan, be introduced into and carry out condensation in the graphite condenser, water vapor condensation is got off to enter into condensate trap, again the liquid in the condensate trap is driven into the hydrochloric acid medial launder with pump;
(4) melting and dissolving urea
With certain amount of urea join add in the melting and dissolving urea groove hot melt molten after, be driven in the spray granulating machine reaction slurry that comes with the tubular reactor spray with pump and be sprayed onto coating granulation on the material curtain that constitutes by returning charge simultaneously;
(5) ammoniation-granulation
From the gas ammonia at ammonia station with enter into tubular reactor simultaneously from the nitration mixture that mixes stock tank and react, discharge a large amount of heat in the reaction process, temperature and pressure in the tubular reactor is all improved rapidly, and reaction slurry sprays under pressure in the tablets press and is sprayed on coating granulation on the material curtain that is made of returning charge with the molten slurry of the urea that sprays into simultaneously;
(6) dry cooling
Material leaves tablets press and enters whizzer, in whizzer with from the stack gas of hotblast stove is reverse, contact, redundant moisture and a little dust leave whizzer drying blower fan with stack gas and enter and wash dust in the spray scrubber off in the material, gas directly is discharged in the atmosphere, material enters after the whizzer drying in the rotating cylinder Air cooler and the chilled air cools of being introduced by blower fan, freezing air leaves and enters dust-settling compartment behind the Air cooler and remove the part big dust particle, enter spiral dust catcher again and remove part small-particle dust, the dust of removing is fallen belt conveyor from the particle collector of dust-settling compartment and spiral dust catcher bottom and is delivered to tablets press as returning charge, and residual gas enters atmosphere after entering and washing the residue dust in the circulation cleaning tower off;
(7) screening is pulverized
Cooled material is sent in the trommel screen extension set through feed belt, sieve apparatus is divided into two districts, one district removes thin dirt and small-particle, the material that sieve falls is collected through loading head and is fallen on the feed belt, turn back to secondary granulation in the tablets press again, undersized in two districts is work in-process, collects to fall into through loading head and sends into the coating machine inner investment on the feed belt, remaining large granular materials enters the pulverizer pulverizing after leaving sieve apparatus, and the material after the pulverizing also is sent to secondary granulation in the tablets press again through feed belt;
(8) finished product packing
The work in-process that fall from sieve apparatus are collected through loading head and are fallen into feed belt and send into the coating machine coating, leave coating machine behind the coating again and enter feed bin, pack through electronic scale metering back and are finished product.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102222997A CN101885630B (en) | 2010-06-28 | 2010-06-28 | Dual-slurry ammonization granulation compound fertilizer production technology |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102222997A CN101885630B (en) | 2010-06-28 | 2010-06-28 | Dual-slurry ammonization granulation compound fertilizer production technology |
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| Publication Number | Publication Date |
|---|---|
| CN101885630A true CN101885630A (en) | 2010-11-17 |
| CN101885630B CN101885630B (en) | 2012-07-25 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102294159A (en) * | 2011-07-04 | 2011-12-28 | 南京工业大学 | Integrated treatment device and treatment process for tail gas containing dust and damp and hot gases |
| CN105254374A (en) * | 2015-11-25 | 2016-01-20 | 刘彬 | Method for producing chlorine-based guniting compound fertilizer |
| CN105294212A (en) * | 2015-11-25 | 2016-02-03 | 刘彬 | Chlorine-based gunited organic-inorganic fertilizer production method |
| CN106241765A (en) * | 2016-08-24 | 2016-12-21 | 湖北祥云(集团)化工股份有限公司 | The production method of a kind of Diammonium phosphate (DAP) and system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1907918A (en) * | 2005-08-05 | 2007-02-07 | 董波 | Technique for producing multi-crop special-purpose sulfur-based composite fertilizer by ammonification granulation |
| CN101391934A (en) * | 2008-10-24 | 2009-03-25 | 江苏阿波罗复合肥有限公司 | Ammoniation granulator and composite fertilizer production novel technique |
-
2010
- 2010-06-28 CN CN2010102222997A patent/CN101885630B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1907918A (en) * | 2005-08-05 | 2007-02-07 | 董波 | Technique for producing multi-crop special-purpose sulfur-based composite fertilizer by ammonification granulation |
| CN101391934A (en) * | 2008-10-24 | 2009-03-25 | 江苏阿波罗复合肥有限公司 | Ammoniation granulator and composite fertilizer production novel technique |
Non-Patent Citations (3)
| Title |
|---|
| 《安徽化工》 20061231 金桂娥等 管式反应器氨化造粒工艺在硫基复合肥生产中的应用 第39～41页 1 , 第5期 * |
| 《磷肥与复肥》 20030930 杨培营等 氨化造粒生产硫基复合肥 第39～40页 1 第18 卷, 第5 期 * |
| 《磷肥与复肥》 20090731 焦士杰等 尿基复合肥氨化造粒控制要点 第54～55页 1 第24卷, 第4期 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102294159A (en) * | 2011-07-04 | 2011-12-28 | 南京工业大学 | Integrated treatment device and treatment process for tail gas containing dust and damp and hot gases |
| CN105254374A (en) * | 2015-11-25 | 2016-01-20 | 刘彬 | Method for producing chlorine-based guniting compound fertilizer |
| CN105294212A (en) * | 2015-11-25 | 2016-02-03 | 刘彬 | Chlorine-based gunited organic-inorganic fertilizer production method |
| CN106241765A (en) * | 2016-08-24 | 2016-12-21 | 湖北祥云(集团)化工股份有限公司 | The production method of a kind of Diammonium phosphate (DAP) and system |
| CN106241765B (en) * | 2016-08-24 | 2018-09-28 | 湖北祥云(集团)化工股份有限公司 | A kind of production method of Diammonium phosphate (DAP) |
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| Publication number | Publication date |
|---|---|
| CN101885630B (en) | 2012-07-25 |
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