CN104108967A - Production process for preparing compound fertilizer through urea sulfate ammoniation method - Google Patents
Production process for preparing compound fertilizer through urea sulfate ammoniation method Download PDFInfo
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Abstract
The invention discloses a production process for preparing a compound fertilizer through a urea sulfate ammoniation method. The production process includes the steps of urea sulfate solution preparation, material preparation, granulation, drying, crushing, sieving, cooling, coating, packing and other steps. The production process has the advantages that urea can be dissolved without steam, side reactions generating biuret are reduced, the granulation granule-forming rate is high, drying energy consumption is low, the process adaptability is strong, and the product quality is good.
Description
Technical field
The present invention relates to a kind of production technique of composite fertilizer, specifically a kind of ureasulfuric acid ammoniation process is prepared the production technique of composite fertilizer, belongs to composite fertilizer's preparation field.
Background technology
At present, along with formulation respectively and the enforcement of China composite fertilizer and Chemical Mixed Fertilizer standard, China's steam agglomeration and urine mortar jetting method compound fertilizer process are badly in need of transformation, are upgraded to the compound fertilizer production technology that has chemical reaction.At present, the simplest propylhomoserin method of general employing.But propylhomoserin method is mainly applicable to the production of high phosphate fertilizer peace weighing apparatus type fertilizer, and the adaptability of technique is not strong.
Summary of the invention
In order to address the above problem, the present invention has designed a kind of ureasulfuric acid ammoniation process and has prepared the production technique of composite fertilizer, and this technique can realize urea without steam and dissolve, the side reaction that generates biuret reduces, and granulation granulating rate is high, and energy consumption for drying is low, Technological adaptability is strong, good product quality.
Technical scheme of the present invention is:
Ureasulfuric acid ammoniation process is prepared a production technique for composite fertilizer, comprises the following steps:
(1) preparation of ureasulfuric acid solution
Urea adds buffering hopper, after measuring, with conveying belt, delivers to ureasulfuric acid preparing tank by belted electronic balance; The vitriol oil that water, mass concentration are 98% by flow measurement control system separately, is delivered to ureasulfuric acid preparing tank according to the weight ratio of water, the vitriol oil, the urea proportional flow of 1: 20: 100 respectively; In ureasulfuric acid preparing tank, urea and the vitriol oil and water react in well-beaten situation, form ureasulfuric acid liquid, and discharge reaction heat; In this system, for controlling temperature of reaction at 80-90 ℃, at preparing tank, be provided with ureasulfuric acid interchanger outward, using water coolant (or steam) as heat exchanger media, by thiocarbamide recycle pump pump circulation, by humidity control system cooling water inflow (or quantity of steam), temperature of reaction is strict controlled in suitable temperature range; In order to guarantee the level stability of reaction system, be beneficial to sufficient reacting, stable, liquid level is controlled in 1/3 altitude range, and ureasulfuric acid preparing tank is provided with liquid level local supervising and measuring equipment, thereby by regulating add amount of preparation and the preparation time of the vitriol oil, urea, water to reach the object of controlling liquid level; In ureasulfuric acid preparing tank, through stop, residence time 15min, reaction mass finally forms ureasulfuric acid; The ureasulfuric acid solution preparing is filtered laggard people's ureasulfuric acid pump, is then delivered to after metering tablets press and participates in granulation production; Consider the special property of ureasulfuric acid and the actual needs of granulation, when ureasulfuric acid configures in production, must strictly control each component proportion;
(2) get the raw materials ready
By each solid material, comprise urea, monoammonium phosphate, Repone K, stopping composition etc., consumption is fixed according to formula for a product, rises to respectively each raw material feed bin, then after weigher metering, by return conveyer, deliver into rotary drum granulator, the weight ratio of solid material and ureasulfuric acid solution is 10: 1;
(3) granulation
The solid materials of step (2) enters after tablets press, and ureasulfuric acid solution prepared by step (1) is delivered to the ureasulfuric acid nozzle in tablets press after pressurised metered, is sprayed to the material particle surface of the cycle stock bed constantly rolling in tablets press; By the liquefied ammonia from ammonia station or ammoniacal liquor through metering; the weight ratio of liquefied ammonia and ureasulfuric acid solution is 1: 2, after by the spray ammonia axle in tablets press, send in tablets press material bed, react with material; promote granulation material granulation, improve granulation material physical property and participate in granulation process.Meanwhile, according to granulation situation, can in material bed, pass into appropriate steam and washing water, control temperature, the humidity of tablets press material by the consumption of steam regulation and washing water, 90 ℃ of temperature, humidity 5%, to promote the continuous granulating of material; Material particles after reuniting, bond, being coated with flows out from tablets press;
(4) dry
Material after step (3) granulation is entered to rotary dryer, carry out and fluidized drying with the warm air from hotblast stove, by regulating hot blast air quantity 92000M
3, the index such as 220 ℃ of temperature controls granulation material drying conditions, makes dried material moisture reach the index request of water content 3%;
(5) fragmentation, screening, cooling
The material flowing out after step (4) is dry sends into through rotary conveyor the coarse fraction that particle is carried out in one-level scalping, scalping particle diameter 4.5mm, large grain after scalping returns to tablets press granulation again after fragmentation, scalping material screens out the fine powder of < 2mm again through dusting cover, fine powder mixes with raw material and returns to tablets press granulation again, the finished particle of 2～4mm enter in cooling drum, carry out cooling, 50 ℃ of cooling temperatures, cooling employing natural wind reflux type carries out, the further fine screen of cooled material, fine screen particle diameter 3～4mm, screen out fine powder and obtain finished particle material,
(6) coating, packing
The finished particle material that step (5) is obtained fully contacts, rolls with the rotating cylinder of the parcel oil spraying into through metering adjusting at coating machine, make material surface oiling or face powder equably, anti-caking powder, completes the parcel operation of granule materials, parcel oiling 1-1.5Kg, face powder 3-6Kg; The object that fertiliser granulates wraps up is to prevent bonding, caking.After the metering of coating agent passing ratio, by coating agent transferpump, send into (or using helical feed metering face powder) in the coating agent nozzle being located in parcel cylinder; The ammonium sulfate finished particle completing after parcel is delivered to finished product bin by finished product belt conveyer, after automatic gauge, packs.
(7) vent gas treatment
The tail gas producing in step (3) granulation process contains a small amount of ammonia and dust, through tail gas generated by granulation blower fan, directly delivers to spray scrubber washing, then emptying through chimney;
The tail gas producing in step (4) drying process contains a small amount of ammonia and a large amount of dust, in drying exhaust fan suction tornado dust collector after dedusting, through air channel, cause again gravity settling chamber gravitational dust collection again, finally emptying through the laggard chimney of spray washing together with tail gas generated by granulation;
In the tail gas producing, contain a certain amount of dust in step (5) process of cooling, through carrying out the cyclone dust removal of one-level dry method in cooled exhaust gas blower fan suction cooled exhaust gas tornado dust collector, dust under removing is sent into returning charge granulating system, tail gas after dedusting causes cooling sack cleaner by air channel again and carries out final dusting, and the tail gas after final dusting is directly emptying through chimney;
The dust-containing tail gas that other solid materialss produce in fragmentation and course of conveying, respectively by after corresponding cleaning shaft is collected, is undertaken after the recovery of two-stage dust removal process finally emptying by chimney by blower fan successively suction tornado dust collector, sack cleaner everywhere.
In addition, thiourea solution temperature is 80～110 ℃; 60～70 ℃ of tablets press temperature of charge; Tablets press outlet material is (H2O): 2.5%～4%; Returning charge ratio is 1～2; Granulation material pH value is 5.5～6.5.
Adding of urea and sulfuric acid is combined into thermopositive reaction, and the 1st mole of urea emit amount of heat when sulfuric acid is combined, and causes that temperature is acute to be risen, and when the urea of the 2nd mole dissolves, heat release is less.In addition, due to the heat release of urea and sulfuric acid adduction process, the heat producing during acid hydrolysis solution preparation may make system overheat and the side reactions such as condensation occur, and even likely sets off an explosion.Thereby require acid hydrolysis solution preparation temperature is the highest to be no more than 130 ℃, general control is below 110 ℃, and in process for preparation, controls the ratio of suitable urea and sulfuric acid, adds appropriate water to reduce the viscosity of ureasulfuric acid and to keep the stable of ureasulfuric acid simultaneously.
Ureasulfuric acid is evenly sprayed on the bed of material as cakingagent reinforce the pelletizing, with liquefied ammonia and MAP, the sulfuric acid of laggard people's bed of material, reacts and generates DAP and ammonium sulfate, emits reaction heat simultaneously, and material is heated up rapidly.Utilize the stickiness of urea and reactant that material is wrapped up layer by layer, under mechanical effect, form qualified particle.Main chemical reactions:
2NH
3+H
2SO
4＝(NH
4)
2SO
4+Q； (1)
NH
4H
2PO
4+NH
3＝(NH
4)
2HPO
4+Q。(2)
Chemical reaction occurs in granulation process increases the effects such as the dissolving of storeroom, absorption, Intermolecular Forces, the stickiness of material is increased, the density of product and intensity improve, especially can reduce secondary response again and crystal conversion in material storage process, make the stable in properties of product, be not easy to occur efflorescence and caking.
The invention has the advantages that:
(1) without steam, can realize urea dissolves
Ureasulfuric acid method makes full use of the reaction heat of urea, sulfuric acid, water formation ureasulfuric acid, makes solid urea not need heating can form runny stable ureasulfuric acid liquid, and urea melting method has been saved the required a large amount of steam of dissolved urea relatively, has reduced production cost;
(2) side reaction that generates biuret reduces
In the process for preparation of ureasulfuric acid, temperature of reaction can be controlled in low temperature range relatively easily, and the method for other high-temperature fusion urea, can effectively reduce the condensation reaction between urea relatively.In process for preparation, generate the side reaction of biuret seldom, in product, the content of biuret is low, more effectively guarantees the inner quality of product;
(3) granulation granulating rate is high
Ureasulfuric acid liquid viscosity is higher, at 60 ℃, can reach 50 * 10.PaIs; in spray people tablets press with the easier granulating of other base fertilizers; add the granulation of sulfuric acid aminating reaction; granulation granulating rate is high; returning charge mass ratio is in 1～2 scope; the scope that is better than urine mortar jetting method returning charge mass ratio 2～3, can realize without filler granulation, solves the problem of powdery ammonium sulfate granulating difficulty.Particularly, when kind requires ammonium sulfate add-on more, this technique can be brought into play capacity of equipment better, and save energy improves throughput.Simultaneously due to reaction temperature and, bring water few (propylhomoserin method and urine method) into, stickiness is strong, granulation is difficult for and mud, easily controls;
(4) energy consumption for drying is low
Take full advantage of the reaction heat of urea, sulfuric acid, water generation ureasulfuric acid solution, and the aminating reaction of ureasulfuric acid heat, make granulating system moisture content lower, also greatly reduce the hot blast load of drying machine, for some formula, can realize without the dry or slightly dry requirement that can reach moisture content;
(5) Technological adaptability is strong
Other techniques are produced urea-base compound fertilizer difficulty in hot and humid situation, but while producing by this technique, the aminate of ureasulfuric acid and can reach more than 60% with the critical relative humidity of product pellet after other base fertilizer mixing granulating, even also can realize normal operation continuously at the production in summer of high temperature, high humidity, while particularly producing high nitrogen fertilizer material, effect is more obvious;
(6) good product quality
Utilize the formation reaction heat of ureasulfuric acid and the aminating reaction of ureasulfuric acid heat, can make prilling temperature reach 70 ℃, make the more traditional granulation process of particle intensity want high, outward appearance is more mellow and fuller, if additional tubular reactor spray granulating makes particle intensity higher.
Ureasulfuric acid ammoniation process Technology is through updating lifting, reach its maturity, compare with current other urine base manure production technique, there is the plurality of advantages such as production cost is low, quality product is high, Technological adaptability is strong, if adopt existing propylhomoserin processing unit to produce, transformation amount is very little, and technique and operation change little, but in quality product, output and operation, being all significantly improved, is the upgrading optimization technique of urea soln whitewashing and ammonia acid technological process.Along with the development of China's fertilizer industry, market improves constantly the requirement of quality product, and ureasulfuric acid ammoniation process Production technology of ureabased compound fertilizer has become the new direction of urine base manure development with its unique technique, superior product performance.
Below in conjunction with accompanying drawing, the invention will be further described with enforcement.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the embodiment of the present invention.
Embodiment
Below the preferred embodiments of the present invention are described, should be appreciated that preferred embodiment described herein, only for description and interpretation the present invention, is not intended to limit the present invention.
Embodiment 1
Ureasulfuric acid ammoniation process is prepared a production technique for composite fertilizer, comprises the following steps:
(1) preparation of ureasulfuric acid solution
Urea adds buffering hopper, after measuring, with conveying belt, delivers to ureasulfuric acid preparing tank by belted electronic balance; The vitriol oil that water, mass concentration are 98% by flow measurement control system separately, is delivered to ureasulfuric acid preparing tank according to the weight ratio of water, the vitriol oil, the urea proportional flow of 1: 20: 100 respectively; In ureasulfuric acid preparing tank, urea and the vitriol oil and water react in well-beaten situation, form ureasulfuric acid liquid, and discharge reaction heat; In this system, for controlling temperature of reaction at 80-90 ℃, at preparing tank, be provided with ureasulfuric acid interchanger outward, using water coolant (or steam) as heat exchanger media, by thiocarbamide recycle pump pump circulation, by humidity control system cooling water inflow (or quantity of steam), temperature of reaction is strict controlled in suitable temperature range; In order to guarantee the level stability of reaction system, be beneficial to sufficient reacting, stable, liquid level is controlled in 1/3 altitude range, and ureasulfuric acid preparing tank is provided with liquid level local supervising and measuring equipment, thereby by regulating add amount of preparation and the preparation time of the vitriol oil, urea, water to reach the object of controlling liquid level; In ureasulfuric acid preparing tank, through stop, residence time 15min, reaction mass finally forms ureasulfuric acid; The ureasulfuric acid solution preparing is filtered laggard people's ureasulfuric acid pump, is then delivered to after metering tablets press and participates in granulation production; Consider the special property of ureasulfuric acid and the actual needs of granulation, when ureasulfuric acid configures in production, must strictly control each component proportion;
(2) get the raw materials ready
By each solid material, comprise urea, monoammonium phosphate, Repone K, stopping composition etc., consumption is fixed according to formula for a product, rises to respectively each raw material feed bin, then after weigher metering, by return conveyer, deliver into rotary drum granulator, the weight ratio of solid material and ureasulfuric acid solution is 10: 1;
(3) granulation
The solid materials of step (2) enters after tablets press, and ureasulfuric acid solution prepared by step (1) is delivered to the ureasulfuric acid nozzle in tablets press after pressurised metered, is sprayed to the material particle surface of the cycle stock bed constantly rolling in tablets press; By the liquefied ammonia from ammonia station or ammoniacal liquor through metering, liquefied ammonia consumption 60Kg, the weight ratio of liquefied ammonia and ureasulfuric acid solution is 1: 2; by the spray ammonia axle in tablets press, send into material bed in tablets press afterwards; react with material, promote granulation material granulation, improve granulation material physical property and participate in granulation process.Meanwhile, according to granulation situation, can in material bed, pass into appropriate steam and washing water, control temperature, the humidity of tablets press material by the consumption of steam regulation and washing water, 90 ℃ of temperature, humidity 5%, to promote the continuous granulating of material; Material particles after reuniting, bond, being coated with flows out from tablets press;
(4) dry
Material after step (3) granulation is entered to rotary dryer, carry out and fluidized drying with the warm air from hotblast stove, by regulating hot blast air quantity 92000M
3, the index such as 220 ℃ of temperature controls granulation material drying conditions, makes dried material moisture reach the index request of water content 3%;
(5) fragmentation, screening, cooling
The material flowing out after step (4) is dry sends into through rotary conveyor the coarse fraction that particle is carried out in one-level scalping, scalping particle diameter 4.5mm, large grain after scalping returns to tablets press granulation again after fragmentation, scalping material screens out the fine powder of < 2mm again through dusting cover, fine powder mixes with raw material and returns to tablets press granulation again, the finished particle of 2～4mm enter in cooling drum, carry out cooling, 50 ℃ of cooling temperatures, cooling employing natural wind reflux type carries out, the further fine screen of cooled material, fine screen particle diameter 3～4mm, screen out fine powder and obtain finished particle material,
(6) coating, packing
The finished particle material that step (5) is obtained fully contacts, rolls with the rotating cylinder of the parcel oil spraying into through metering adjusting at coating machine, make material surface oiling or face powder equably, anti-caking powder, completes the parcel operation of granule materials, parcel oiling 1-1.5Kg, face powder 3-6Kg; The object that fertiliser granulates wraps up is to prevent bonding, caking.After the metering of coating agent passing ratio, by coating agent transferpump, send into (or using helical feed metering face powder) in the coating agent nozzle being located in parcel cylinder; The ammonium sulfate finished particle completing after parcel is delivered to finished product bin by finished product belt conveyer, after automatic gauge, packs.
(7) vent gas treatment
The tail gas producing in step (3) granulation process contains a small amount of ammonia and dust, through tail gas generated by granulation blower fan, directly delivers to spray scrubber washing, then emptying through chimney;
The tail gas producing in step (4) drying process contains a small amount of ammonia and a large amount of dust, in drying exhaust fan suction tornado dust collector after dedusting, through air channel, cause again gravity settling chamber gravitational dust collection again, finally emptying through the laggard chimney of spray washing together with tail gas generated by granulation;
In the tail gas producing, contain a certain amount of dust in step (5) process of cooling, through carrying out the cyclone dust removal of one-level dry method in cooled exhaust gas blower fan suction cooled exhaust gas tornado dust collector, dust under removing is sent into returning charge granulating system, tail gas after dedusting causes cooling sack cleaner by air channel again and carries out final dusting, and the tail gas after final dusting is directly emptying through chimney;
The dust-containing tail gas that other solid materialss produce in fragmentation and course of conveying, respectively by after corresponding cleaning shaft is collected, is undertaken after the recovery of two-stage dust removal process finally emptying by chimney by blower fan successively suction tornado dust collector, sack cleaner everywhere.
In addition, thiourea solution temperature is 80～110 ℃; 60～70 ℃ of tablets press temperature of charge; Tablets press outlet material is (H2O): 2.5%～4%; Returning charge ratio is 1～2; Granulation material pH value is 5.5～6.5.
Affect granulation factor analysis
The impact of 1 granulation humidity of materials
Amount of liquid phase and the humidity of materials of granulation have the most direct relation.Along with the raising of humidity of materials, the meltage of various materials increases, and amount of liquid phase increases.Different material systems become graininess and amount of liquid phase closely related.Under identical working condition, urine phosphorus ammonium be material compared with the lower material moisture of unclassified stores system granulation requirement, the best ω (H that cries
2o) in 3% left and right.
The impact of 2 prilling temperatures
Improve prilling temperature, the chemical reaction between inorganic salt comes to life, and the chance of storeroom chemical bonds increases.And, the solubleness of inorganic salt generally increases with the rising of temperature, so the amount of liquid phase of system increases when prilling temperature is high thereupon, mutual dissolving and reaction generate double salt amount to be increased, degree of uniformity improves, and at this moment outer liquid volume added should suitably reduce, and granulation moisture content (moisture) should be adjusted with the changes in solubility of temperature and raw material, for example, when urinating phosphorus ammonium prilling temperature and changing 90 ℃ into by 60 ℃, its material moisture content ω (H
2o) should reduce to 1.2% from 3.2%.Rising temperature also makes liquid phase viscosity and surface tension reduce, thereby can obtain more solid particle under mechanical external force effect.
The impact of 3 granulation material solubleness
The solubleness of material has a great impact granulation, and the in the situation that of uniform temp and humidity, the amount of liquid phase that the material that solubleness is large forms is large.In ureasulfuric acid spray granulating technique, conventional raw material mainly contains urea, sulphur ammonium, ammonium chloride, carbon ammonium, MAP, calcium superphosphate, Repone K, potassium sulfate, and under its normal temperature, the solubleness of (20 ℃) is in Table 1.
The solubleness g/100g water of (20 ℃) conventional mineral manure under table 1 normal temperature
Along with the rising solubleness of temperature can strengthen.The situation that urea, ammonium sulfate, ammonium chloride, Repone K, the potassium sulfate solubility with temperature in water changes is in Table 2.
The changes in solubility of conventional mineral manure under table 2 differing temps
In the formula of urea sulfuric acid compound fertilizer, because the solubleness of urea is larger, so the amount of liquid phase in high-nitrogen compound fertilizer is very high.As the form of fruit part urea with agramon adds and can make moderate progress; But be noted that urea dissolving and heat absorbing can make prilling temperature reduce, operation easier strengthens, so the additional proportion of agramon must be controlled well in formula.
The impact of 4 granulation material potential of hydrogen
PH value is the whether suitable important indicator of compatibleness of material system.Material pH value is too low, and granulation easily becomes large ball; PH value is too high, and material agglutinating value(of coal) is poor, is difficult for granulating.In the granulation system that has phosphorus ammonium to exist, more suitable when in knowhow tablets press, material pH is between 5.5～6.5.
5 impacts of material fusing point on viscosity
The eutectic point of mixture generally can be lower than the fusing point of the minimum component of fusing point, and the eutectic point of urea, Repone K, MAP system is about 115 ℃, also can cause the amount of liquid phase of material to increase when system temperature is higher than eutectic point like this, and stickiness increases simultaneously.The eutectic point of mixture system is called viscid temperature.In tablets press, material should be near viscid temperature, must be lower than viscid temperature in drying machine.
The impact of 6 returning charges
The quality of returning charge quantity, returning charge (as stability, size-grade distribution, temperature, water content etc.) has important impact to granulation, is mainly the impact on temperature, humidity and granulation core.Increase returning charge amount prilling temperature, humidity are reduced, core increases.Adopt hot returning charge technology can improve material air-teturning temperature, and then improve the temperature of granulation.General control systems returning charge than (returning charge amount: charging capacity) between 1～2, the liquid-solid mass ratio of tablets press material (liquid feed: (solid charging capacity+returning charge amount)) according to prilling temperature general control between 0.1～0.2.
Except as otherwise noted, the percentage ratio adopting in the present invention is weight percentage.
Finally it should be noted that: the foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, although the present invention is had been described in detail with reference to previous embodiment, for a person skilled in the art, its technical scheme that still can record aforementioned each embodiment is modified, or part technical characterictic is wherein equal to replacement.Within the spirit and principles in the present invention all, any modification of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.
Claims (3)
1. ureasulfuric acid ammoniation process is prepared a production technique for composite fertilizer, it is characterized in that comprising the following steps:
(1) preparation of ureasulfuric acid solution
Urea adds buffering hopper, after measuring, with conveying belt, delivers to ureasulfuric acid preparing tank by belted electronic balance; Water and mass concentration be 98% the vitriol oil respectively by flow measurement control system separately, according to the weight ratio of water, the vitriol oil, the urea proportional flow of 1: 20: 100, be delivered to ureasulfuric acid preparing tank; In ureasulfuric acid preparing tank, urea and the vitriol oil and water react in well-beaten situation, form ureasulfuric acid liquid, and discharge reaction heat; In this system, for controlling temperature of reaction at 80-90 ℃, at preparing tank, be provided with ureasulfuric acid interchanger outward, using water coolant or steam as heat exchanger media, by thiocarbamide recycle pump pump circulation, by humidity control system cooling water inflow or quantity of steam, temperature of reaction is strict controlled in temperature range; Reaction liquid level is controlled to 1/3 height simultaneously; In ureasulfuric acid preparing tank, through stop, residence time 15min, reaction mass finally forms ureasulfuric acid;
(2) get the raw materials ready
Each solid material is risen to respectively to each raw material feed bin, then after weigher metering, by return conveyer, deliver into rotary drum granulator, the weight ratio of solid material and ureasulfuric acid solution is 10: 1;
(3) granulation
The solid materials of step (2) enters after tablets press, and ureasulfuric acid solution prepared by step (1) is delivered to the ureasulfuric acid nozzle in tablets press after pressurised metered, is sprayed to the material particle surface of the cycle stock bed constantly rolling in tablets press; By the liquefied ammonia from ammonia station or ammoniacal liquor through metering, the weight ratio of liquefied ammonia and ureasulfuric acid solution is 1: 2, then by the spray ammonia axle in tablets press, send into material bed in tablets press, react with material, pass into appropriate steam and washing water, the temperature of controlling tablets press material by the consumption of steam regulation and washing water is that 90 ℃, humidity are 5% simultaneously; Material particles after reuniting, bond, being coated with flows out from tablets press again;
(4) dry
Material after step (3) granulation is entered to rotary dryer, carry out and fluidized drying with the warm air from hotblast stove, regulate 220 ℃ of hot blast air quantity 92000M3, temperature, make dried material moisture reach water content 3%;
(5) fragmentation, screening, cooling
The material flowing out after step (4) is dry sends into through rotary conveyor the coarse fraction that particle is carried out in one-level scalping, scalping particle diameter 4.5mm, large grain after scalping returns to tablets press granulation again after fragmentation, scalping material screens out through dusting cover the fine powder that is less than 2mm again, fine powder mixes with raw material and returns to tablets press granulation again, the finished particle of 2～4mm enter in cooling drum, carry out cooling, 50 ℃ of cooling temperatures, cooling employing natural wind reflux type carries out, the further fine screen of cooled material, fine screen particle diameter 3～4mm, obtains finished particle material after screening out fine powder;
(6) coating, packing
The finished particle material that step (5) is obtained fully contacts, rolls with the rotating cylinder of the parcel oil spraying into through metering adjusting at coating machine, make material surface oiling or face powder equably, anti-caking powder, completes the parcel operation of granule materials, parcel oiling 1-1.5Kg, face powder 3-6Kg; After the metering of coating agent passing ratio, by coating agent transferpump, send in the coating agent nozzle being located in parcel cylinder or use helical feed metering face powder; The ammonium sulfate finished particle completing after parcel is delivered to finished product bin by finished product belt conveyer, after automatic gauge, packs.
2. production technique according to claim 1, is characterized in that:
The tail gas producing in step (3) granulation process contains a small amount of ammonia and dust, through tail gas generated by granulation blower fan, directly delivers to spray scrubber washing, then emptying through chimney;
The tail gas producing in step (4) drying process contains a small amount of ammonia and a large amount of dust, in drying exhaust fan suction tornado dust collector after dedusting, through air channel, cause again gravity settling chamber gravitational dust collection again, finally emptying through the laggard chimney of spray washing together with tail gas generated by granulation;
In the tail gas producing, contain a certain amount of dust in step (5) process of cooling, through carrying out the cyclone dust removal of one-level dry method in cooled exhaust gas blower fan suction cooled exhaust gas tornado dust collector, dust under removing is sent into returning charge granulating system, tail gas after dedusting causes cooling sack cleaner by air channel again and carries out final dusting, and the tail gas after final dusting is directly emptying through chimney;
The dust-containing tail gas that other solid materialss produce in fragmentation and course of conveying, respectively by after corresponding cleaning shaft is collected, is undertaken after the recovery of two-stage dust removal process finally emptying by chimney by blower fan successively suction tornado dust collector, sack cleaner everywhere.
3. production technique according to claim 2, is characterized in that: thiourea solution temperature is 80～110 ℃; 60～70 ℃ of tablets press temperature of charge; Tablets press outlet material is (H2O): 2.5%～4%; Returning charge ratio is 1～2; Granulation material pH value is 5.5～6.5.
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| CN104496613A (en) * | 2015-01-13 | 2015-04-08 | 四川美丰化工股份有限公司 | Compound fertilizer finished product cooling method and device |
| CN105036988A (en) * | 2015-08-18 | 2015-11-11 | 广西亿润生物科技有限公司 | Compound fertilizer processing system |
| CN105036868A (en) * | 2015-08-18 | 2015-11-11 | 灵山县骄丰化工有限公司 | Compound fertilizer pelletizing and spraying system and operating method thereof |
| CN105859340A (en) * | 2016-03-31 | 2016-08-17 | 登封快丰收农业发展有限公司 | Production line for bio-organic fertilizer |
| CN107056366A (en) * | 2016-12-28 | 2017-08-18 | 郑州阿波罗肥业有限公司 | A kind of method that composite fertilizer is made of ureasulfuric acid |
| CN109134105A (en) * | 2018-11-08 | 2019-01-04 | 白银丰宝农化科技有限公司 | A kind of attapulgite modified compound fertilizer |
| CN112387236A (en) * | 2020-11-19 | 2021-02-23 | 安徽国祯生态科技有限公司 | Soil repairing agent granulator auxiliary assembly |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1651359A (en) * | 2004-02-06 | 2005-08-10 | 河北天人化工股份有限公司 | Production method of urocomposite fertilizer |
| CN101613244A (en) * | 2009-08-07 | 2009-12-30 | 中国-阿拉伯化肥有限公司 | A kind of method that improves granulation performance of urine-based fertilizer |
| CN102503622A (en) * | 2011-09-17 | 2012-06-20 | 山东金山化肥有限公司 | Process for producing urea sulfate ammoniated compound fertilizer |
| CN102503719A (en) * | 2011-10-13 | 2012-06-20 | 贵州川恒化工有限责任公司 | Preparation method of strong-acidic water-soluble fertilizer special for alkaline soil |
| CN103011982A (en) * | 2012-12-29 | 2013-04-03 | 山东金正大生态工程股份有限公司 | Industrial production method and device of urea-formaldehyde slow-release compound fertilizer |
-
2013
- 2013-04-19 CN CN201310164408.8A patent/CN104108967A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1651359A (en) * | 2004-02-06 | 2005-08-10 | 河北天人化工股份有限公司 | Production method of urocomposite fertilizer |
| CN101613244A (en) * | 2009-08-07 | 2009-12-30 | 中国-阿拉伯化肥有限公司 | A kind of method that improves granulation performance of urine-based fertilizer |
| CN102503622A (en) * | 2011-09-17 | 2012-06-20 | 山东金山化肥有限公司 | Process for producing urea sulfate ammoniated compound fertilizer |
| CN102503719A (en) * | 2011-10-13 | 2012-06-20 | 贵州川恒化工有限责任公司 | Preparation method of strong-acidic water-soluble fertilizer special for alkaline soil |
| CN103011982A (en) * | 2012-12-29 | 2013-04-03 | 山东金正大生态工程股份有限公司 | Industrial production method and device of urea-formaldehyde slow-release compound fertilizer |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104496613A (en) * | 2015-01-13 | 2015-04-08 | 四川美丰化工股份有限公司 | Compound fertilizer finished product cooling method and device |
| CN105036988A (en) * | 2015-08-18 | 2015-11-11 | 广西亿润生物科技有限公司 | Compound fertilizer processing system |
| CN105036868A (en) * | 2015-08-18 | 2015-11-11 | 灵山县骄丰化工有限公司 | Compound fertilizer pelletizing and spraying system and operating method thereof |
| CN105036988B (en) * | 2015-08-18 | 2018-06-19 | 广西亿润生物科技有限公司 | A kind of composite fertilizer's system of processing |
| CN105859340A (en) * | 2016-03-31 | 2016-08-17 | 登封快丰收农业发展有限公司 | Production line for bio-organic fertilizer |
| CN107056366A (en) * | 2016-12-28 | 2017-08-18 | 郑州阿波罗肥业有限公司 | A kind of method that composite fertilizer is made of ureasulfuric acid |
| CN109134105A (en) * | 2018-11-08 | 2019-01-04 | 白银丰宝农化科技有限公司 | A kind of attapulgite modified compound fertilizer |
| CN112387236A (en) * | 2020-11-19 | 2021-02-23 | 安徽国祯生态科技有限公司 | Soil repairing agent granulator auxiliary assembly |
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