CN104987158A - Ammonia-acid method composite fertilizer production technology - Google Patents
Ammonia-acid method composite fertilizer production technology Download PDFInfo
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- CN104987158A CN104987158A CN201510422503.2A CN201510422503A CN104987158A CN 104987158 A CN104987158 A CN 104987158A CN 201510422503 A CN201510422503 A CN 201510422503A CN 104987158 A CN104987158 A CN 104987158A
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Abstract
An ammonia-acid method composite fertilizer production technology is characterized in that low-added value sulfuric acid, ammonia water and monoammonium phosphate are converted to form high-added value ammonium sulfate, diammonium phosphate and heat, and generated steam is combined to realize a slip with good viscosity, so a heat source for heating, steam and a viscous material which are originally needed are omitted; the self viscosity is used to granulate, so the water content of obtained granules is low, and the drying load is reduced; the surface of the granules is smooth and rounded and has no roughness, the inner wall of a granulator basically has no adhesion, working environment basically has no dusts or odorous ammonia gas smell, the qualified rate of one-time formed granules reaches above 90%, and the production efficiency is improved; and amino acids and an organic fertilizer are added in the granulation process to participate in granulation in order to produce an amino acid organic-inorganic composite fertilizer, and the temperature is reduced to a certain degree when the amino acids and the organic fertilizer are added, so the destroys to the fertility of the amino acids and the organic fertilizer are reduced, and the validity of the finally obtained fertilizer is guaranteed.
Description
Technical field
The present invention relates to technical field of fertilizer production, particularly a kind of sour method compound fertilizer production technology.
Background technology
Soil is the basis of agricultural, and fertilizer is farm crop " grains ".Chemical fertilizer is indispensable material during current agricultural is produced.Composite fertilizer has that nutrient content is high, minor component is few and the advantage such as physical behavior is good, for balance fertilizing, improves utilization rate of fertilizer, promotes that the stable high yield of crop has very important effect.Test result according to national chemical fertilizer try net: reasonably high concentration N-P-K coordinates, and can make increasing production of rice 40.8%, corn yield increasing 46.1%, wheat increase yield 56.6%, Yield Increase In Cotton 48.6%, Semen Brassicae campestris volume increase 64.4%, soybean yield-increasing 17.9%, therefore develops high-concentration compound fertilizer imperative.
In traditional composite heat transfer, in order to granulation, general all can absorb fillers, but the Chemical Mixed Fertilizer containing weighting agent traditional is at present dissolved with residue because existing, disintegration is poorly soluble, product colour is obvious by weighting agent Color influences, Compound fertilizer production technology simultaneously containing weighting agent affects comparatively large by raw-material, can not meet market to the more and more harsh specification of quality of product and the requirement of producing technique.Based on this, on the basis of ammoniation process urea-base compound fertilizer production new technology, ammoniation process production of sulfur-based compound fertilizer new technology, develop sour method filler-free new pelleting technology, this technology not only solves product quality defect and the production problem of the existence of traditional Chemical Mixed Fertilizer, and traditional production of compound fertilizer has been risen to the degree of Composite, substantially increase class and the market competitiveness of product, raw materials cost, coal, electric consumption obviously reduce simultaneously, and throughput and economical efficiency significantly improve.
Summary of the invention
Technical problem to be solved by this invention cannot produce high-concentration compound fertilizer for prior art, and produce the problem that Chemical Mixed Fertilizer needs weighting agent, the problem of mass energy will be consumed aborning simultaneously, a kind of method of sour method production composite fertilizer is provided, to produce high-concentration compound fertilizer when there is no weighting agent, and utilize heat that raw material thing id reaction produces to reduce energy loss, to improve product quality and to reduce energy loss.
For solving the problems of the technologies described above, the technical solution adopted in the present invention is a kind of sour method compound fertilizer production technology, it is characterized in that comprising the steps.
(1) first solid state feed stock N P and K is pulverized respectively, then measure respectively and mix again, obtain raw mixture A.
(2) meter is got urea and is dissolved device by urea and change into urine.
(3), by alternate with urine for raw mixture A input and the batch mixing end being sprayed onto rotary drum granulator, obtain raw mixture B.
(4) diluting concentrated sulfuric acid is become dilute sulphuric acid, then put into after dilute sulphuric acid and ammoniacal liquor metering in tubular reactor simultaneously, generate ammonium sulfate slurry, and produce high temperature heat and high pressure impulse force.
(5), under high pressure impulse action, in the raw mixture B ammonium sulfate slurry containing high temperature heat whitewashed in batch mixing end, under the effect of high temperature heat, each storeroom generation replacement(metathesis)reaction, generates the liquid phase sosoloid double salt of mixing.
(6) liquid phase sosoloid double salt is put into the scroll end of rotary drum granulator, tentatively roll granulation and preliminary cooling.
(7) from the batch mixing end of rotary drum granulator to discharge end; its internal temperature drops to 60-70 DEG C gradually from 125-135 DEG C, drops to the position of 80-90 DEG C at rotary drum granulator internal temperature, drops into amino acid pulverulent material and humic acids pulverulent material; and continued granulation, obtain compound fertilizer granules A.
(8) be provided with steam ammonia induced draft fan at rotary drum granulator discharge end and the Venturi scrubbing device of dilute sulphuric acid washings is housed; the steam produced during granulation and ammonia dilute sulphuric acid are carried out absorbing and washing; reclaim steam and ammonia; after reaching finite concentration; by washings reclaim, participate in step (4) in diluting concentrated sulfuric acid is become dilute sulphuric acid.
(9) compound fertilizer granules A is put in cooler and first carry out drying with hot blast, then carry out drying and cooling with cold wind, until the temperature of charge of cooler discharge end is 45-50 DEG C; Obtain compound fertilizer granules B.
(10) be provided with whirlwind water washing dedust device at cooler discharge end, dust adsorption is also washed, and obtains dust washing liquid;
(11) compound fertilizer granules B is sieved, get the particle of composite-grain diameter specification, obtain compound fertilizer granules C, macrobead and small-particle are reclaimed.
(12) the macrobead of recovery and small-particle are pulverized, then mix with dust washing liquid, obtain mixture; (7) after the middle amino acid pulverulent material dropped into participates in granulation in step, then mixture is put in rotary drum granulator, again participate in granulation.
(13) compound fertilizer granules C is carried out coating, then carry out metering packing, obtain composite fertilizer's finished product.
A kind of further sour method compound fertilizer production technology, is characterized in that comprising the steps:
(1) first solid state feed stock N P and K is pulverized respectively, then measure respectively and mix again, obtain raw mixture A; Described solid state feed stock N P and K comprises Repone K, monoammonium phosphate.
(2) meter is got urea and is dissolved device by urea and change into urine.
(3) the raw mixture A planning to drop within the unit time and urine are respectively divided into ten equal portions; alternate input and be sprayed onto the batch mixing end of rotary drum granulator, often drops into a raw mixture A and evenly sprays a urine again, then mix thoroughly; so repeatedly, raw mixture B is obtained.
(4) the vitriol oil of massfraction 98% is diluted to the dilute sulphuric acid that massfraction is 53%-59% at 26-32 DEG C of temperature, dilution time controls within 43-49 minute; Then by dilute sulphuric acid and massfraction be after the ammoniacal liquor metering of 18% according to step (3) same equal portions of same period evenly put in tubular reactor simultaneously, generate ammonium sulfate slurry, and produce water vapor, high temperature heat and high pressure impulse force.
(5) under high pressure impulse action; in raw mixture B ammonium sulfate slurry containing high temperature heat whitewashed in rotary drum granulator batch mixing end; under the effect of high temperature heat; each storeroom generation replacement(metathesis)reaction; generate the liquid phase sosoloid double salt of mixing, these liquid phase sosoloid comprise ammonium chloride potassium, ammonium-potassium sulfate, ammonium-potassium phosphate.
(6) liquid phase sosoloid double salt is rotated the scroll end putting into rotary drum granulator, rotate when dropping into and adopt pressurized air to stir, to prevent inwall from gluing wall, and then tentatively roll granulation and preliminary cooling.
(7) from the batch mixing end of rotary drum granulator to discharge end; its internal temperature drops to 60-70 DEG C gradually from 125-135 DEG C, drops to the position of 80-90 DEG C at rotary drum granulator internal temperature, drops into amino acid pulverulent material and humic acids pulverulent material; and continued granulation, obtain compound fertilizer granules A.
(8) be provided with steam ammonia induced draft fan and Venturi scrubbing device at rotary drum granulator discharge end; Venturi scrubbing device is the dilute sulphuric acid washings of 8%-14% built with massfraction; the steam produced during granulation and ammonia are incorporated in dilute sulphuric acid and carry out absorbing and washing; reclaim steam and ammonia; after reaching finite concentration; by washings reclaim, participate in step (4) in diluting concentrated sulfuric acid is become dilute sulphuric acid.
(9) compound fertilizer granules A is put in cooler and first carry out drying with hot blast, then carry out drying and cooling with cold wind, until the temperature of charge of cooler discharge end is 45-50 DEG C; Obtain compound fertilizer granules B.
(10) be provided with whirlwind water washing dedust device at cooler discharge end, dust adsorption is also washed, and obtains dust washing liquid;
(11) compound fertilizer granules B is sieved, get the particle that particle diameter meets gauge, obtain compound fertilizer granules C, the macrobead exceeded outside gauge and small-particle are reclaimed.
(12) the macrobead of recovery and small-particle are pulverized, then mix with dust washing liquid, obtain mixture; (7) after the middle amino acid pulverulent material dropped into participates in granulation in step, then mixture is put in rotary drum granulator, again participate in granulation.
(13) compound fertilizer granules C is carried out coating, then carry out metering packing, obtain composite fertilizer's finished product.
The invention has the beneficial effects as follows and low value-added sulfuric acid, ammoniacal liquor and monoammonium phosphate are changed into high added value ammonium sulfate, diammonium phosphate and heat, and the steam combining generation presents the good slip state of viscosity, can omit its energy that should heat, steam and cohesive material; Simultaneously owing to utilizing the viscosity of himself to granulate, make moisture wherein fewer, can drying load be reduced when drying like this, saving the energy further; Simultaneously owing to utilizing the viscosity of himself to granulate, make its particle surface smooth mellow and full, without harsh feeling, tablets press inwall is substantially without adhesion, Working environment does not have dust substantially, do not have unpleasant ammonia smell, and the qualification rate of disposable granulating can reach more than 90% yet, greatly reduce returning charge rate, improve production efficiency; Add amino acid and fertilizer when granulating to a certain extent and participate in granulation, produce amino-acid organic/inorganic compound fertilizer, because temperature when adding amino acid and fertilizer is reduced to a certain degree, decrease the destruction to its fertility, the validity of the fertilizer of guarantee.
Accompanying drawing explanation
Fig. 1 is sour method compound fertilizer production technology schema of the present invention.
Embodiment
Below in conjunction with embodiment, the invention will be further described, and following examples are intended to the present invention instead of limitation of the invention further are described, should not limit the scope of the invention with this.
Embodiment 1.
Be N-P according to the inventive method production product specification
2o
5-K
2the amino-acid organic/inorganic compound fertilizer of O=16-16-8.
(1) first Repone K, monoammonium phosphate are pulverized respectively, then count potassium chloride 150kg, monoammonium phosphate 305kg respectively and mix, obtaining raw mixture A.
(2) meter is got urea 50kg and is dissolved device by urea and change into urine.
(3) the raw mixture A and urine that plan the above-mentioned component dropped in 1 hour are respectively divided into ten equal portions; alternate input and be sprayed onto the batch mixing end of rotary drum granulator; often drop into a raw mixture A and evenly spray a urine again; then mix thoroughly; so repeatedly; until by complete for the mixing of materials being divided into ten equal portions, obtain raw mixture B.
(4) the vitriol oil 284kg of massfraction 98% is diluted to the dilute sulphuric acid that massfraction is 53% at 26 DEG C of temperature, dilution time controls within 43 minutes; Then by dilute sulphuric acid and massfraction be 18% ammoniacal liquor 789kg evenly put in tubular reactor according to the period simultaneously, generate ammonium sulfate slurry, and produce water vapor, high temperature heat and high pressure impulse force.
(5) under high pressure impulse action; in raw mixture B ammonium sulfate slurry containing high temperature heat whitewashed in rotary drum granulator batch mixing end; under the effect of high temperature heat; each storeroom generation replacement(metathesis)reaction; generate the liquid phase sosoloid double salt of mixing, these liquid phase sosoloid comprise ammonium chloride potassium, ammonium-potassium sulfate, ammonium-potassium phosphate.
(6) liquid phase sosoloid double salt is rotated the scroll end putting into rotary drum granulator, rotate when dropping into and adopt pressurized air to stir, to prevent inwall from gluing wall, and then tentatively roll granulation and preliminary cooling.
(7) from the batch mixing end of rotary drum granulator to discharge end; its internal temperature drops to 60 DEG C gradually from 125 DEG C; the position of 80 DEG C is dropped at rotary drum granulator internal temperature; amino acid pulverulent material 25kg and humic acids pulverulent material 50kg got by meter; be divided into that ten equal portions are alternate to be put in rotary drum granulator; and continued granulation, obtain compound fertilizer granules A.
(8) be provided with steam ammonia induced draft fan and Venturi scrubbing device at rotary drum granulator discharge end; Venturi scrubbing device is the dilute sulphuric acid washings of 8% built with massfraction; the steam produced during granulation and ammonia are incorporated in dilute sulphuric acid and carry out absorbing and washing; reclaim steam and ammonia; after reaching finite concentration; by washings reclaim, participate in step (4) in diluting concentrated sulfuric acid is become dilute sulphuric acid.
(9) compound fertilizer granules A is put in cooler and first carry out drying with hot blast, then carry out drying and cooling with cold wind, until the temperature of charge of cooler discharge end is 45 DEG C; Obtain compound fertilizer granules B.
(10) be provided with whirlwind water washing dedust device at cooler discharge end, dust adsorption is also washed, and obtains dust washing liquid;
(11) compound fertilizer granules B is sieved, get the particle that particle diameter meets gauge, obtain compound fertilizer granules C, the macrobead exceeded outside gauge and small-particle are reclaimed.
(12) the macrobead of recovery and small-particle are pulverized, then mix with dust washing liquid, obtain mixture; (7) after the middle amino acid pulverulent material dropped into participates in granulation in step, then mixture is put in rotary drum granulator, again participate in granulation.
(13) compound fertilizer granules C is carried out coating, then carry out metering packing, obtaining product specification is N-P
2o
5-K
2the amino-acid organic/inorganic compound fertilizer finished product 905.2kg of O=16-16-8; Tablets press inwall is substantially without adhesion, and Working environment does not have dust substantially, does not also have unpleasant ammonia smell, and disposable qualified granulating rate to reach 90.5% returning charge rate little.
Embodiment 2.
Be N-P according to the inventive method production product specification
2o
5-K
2the amino-acid organic/inorganic compound fertilizer of O=10-10-10.
(1) first Repone K, monoammonium phosphate are pulverized respectively, then respectively meter get effective potassium content be 50 Repone K 200kg, nitrogen content 11, available phosphorus content be the monoammonium phosphate 227.3kg of 44 and mix, obtain raw mixture A.
Meter get nitrogen content be 46 urea 54.3kg dissolve device by urea and change into urine.
(3) the raw mixture A and urine that plan the above-mentioned component dropped in 1 hour are respectively divided into ten equal portions; alternate input and be sprayed onto the batch mixing end of rotary drum granulator; often drop into a raw mixture A and evenly spray a urine again; then mix thoroughly; so repeatedly; until by complete for the mixing of materials being divided into ten equal portions, obtain raw mixture B.
(4) the vitriol oil 189.4kg of massfraction 98% is diluted to the dilute sulphuric acid that massfraction is 56% at 29 DEG C of temperature, dilution time controls within 46 minutes; Then the ammoniacal liquor 521.7kg being 18% by dilute sulphuric acid and massfraction is divided into ten equal portions and evenly puts in tubular reactor, generates ammonium sulfate slurry, and produces water vapor, high temperature heat and high pressure impulse force.
(5) under high pressure impulse action; in raw mixture B ammonium sulfate slurry containing high temperature heat whitewashed in rotary drum granulator batch mixing end; under the effect of high temperature heat; each storeroom generation replacement(metathesis)reaction; generate the liquid phase sosoloid double salt of mixing, these liquid phase sosoloid comprise ammonium chloride potassium, ammonium-potassium sulfate, ammonium-potassium phosphate.
(6) liquid phase sosoloid double salt is rotated the scroll end putting into rotary drum granulator, rotate when dropping into and adopt pressurized air to stir, to prevent inwall from gluing wall, and then tentatively roll granulation and preliminary cooling.
(7) from the batch mixing end of rotary drum granulator to discharge end; its internal temperature drops to 65 DEG C gradually from 130 DEG C; the position of 85 DEG C is dropped at rotary drum granulator internal temperature; amino acid pulverulent material 50kg and humic acids pulverulent material 331.2kg got by meter; be divided into that ten equal portions are alternate to be put in rotary drum granulator; and continued granulation, obtain compound fertilizer granules A.
(8) be provided with steam ammonia induced draft fan and Venturi scrubbing device at rotary drum granulator discharge end; Venturi scrubbing device is the dilute sulphuric acid washings of 11% built with massfraction; the steam produced during granulation and ammonia are incorporated in dilute sulphuric acid and carry out absorbing and washing; reclaim steam and ammonia; after reaching finite concentration; by washings reclaim, participate in step (4) in diluting concentrated sulfuric acid is become dilute sulphuric acid.
(9) compound fertilizer granules A is put in cooler and first carry out drying with hot blast, then carry out drying and cooling with cold wind, until the temperature of charge of cooler discharge end is 47.5 DEG C; Obtain compound fertilizer granules B.
(10) be provided with whirlwind water washing dedust device at cooler discharge end, dust adsorption is also washed, and obtains dust washing liquid;
(11) compound fertilizer granules B is sieved, get the particle that particle diameter meets gauge, obtain compound fertilizer granules C, the macrobead exceeded outside gauge and small-particle are reclaimed.
(12) the macrobead of recovery and small-particle are pulverized, then mix with dust washing liquid, obtain mixture; (7) after the middle amino acid pulverulent material dropped into participates in granulation in step, then mixture is put in rotary drum granulator, again participate in granulation.
(13) compound fertilizer granules C is carried out coating, then carry out metering packing, obtaining product specification is N-P
2o
5-K
2the amino-acid organic/inorganic compound fertilizer finished product 923.3kg of O=10-10-10; Tablets press inwall is substantially without adhesion, and Working environment does not have dust substantially, does not also have unpleasant ammonia smell, and disposable qualified granulating rate reaches 92.3%, and returning charge rate is little.
Embodiment 3.
Be N-P according to the inventive method production product specification
2o
5-K
2the amino-acid organic/inorganic compound fertilizer of O=20-10-10.
(1) first Repone K, monoammonium phosphate are pulverized respectively, then respectively meter get effective potassium content be 60 Repone K 200kg, nitrogen content be 11, available phosphorus content is the monoammonium phosphate 227.3kg of 44 and mixes, and obtains raw mixture A.
(2) the urea 260kg that nitrogen content 46.3 got by meter dissolves device by urea and changes into urine.
(3) the raw mixture A and urine that plan the above-mentioned component dropped in 1 hour are respectively divided into ten equal portions; alternate input and be sprayed onto the batch mixing end of rotary drum granulator; often drop into a raw mixture A and evenly spray a urine again; then mix thoroughly; so repeatedly; until by complete for the mixing of materials being divided into ten equal portions, obtain raw mixture B.
(4) the vitriol oil 206.8kg of massfraction 98% is diluted to the dilute sulphuric acid that massfraction is 59% at 32 DEG C of temperature, dilution time controls within 49 minutes; Then by dilute sulphuric acid and massfraction be 18% ammoniacal liquor 544.5kg evenly put in tubular reactor according to the period simultaneously, generate ammonium sulfate slurry, and produce water vapor, high temperature heat and high pressure impulse force.
(5) under high pressure impulse action; in raw mixture B ammonium sulfate slurry containing high temperature heat whitewashed in rotary drum granulator batch mixing end; under the effect of high temperature heat; each storeroom generation replacement(metathesis)reaction; generate the liquid phase sosoloid double salt of mixing, these liquid phase sosoloid comprise ammonium chloride potassium, ammonium-potassium sulfate, ammonium-potassium phosphate.
(6) liquid phase sosoloid double salt is rotated the scroll end putting into rotary drum granulator, rotate when dropping into and adopt pressurized air to stir, to prevent inwall from gluing wall, and then tentatively roll granulation and preliminary cooling.
(7) from the batch mixing end of rotary drum granulator to discharge end; its internal temperature drops to 70 DEG C gradually from 135 DEG C; the position of 90 DEG C is dropped at rotary drum granulator internal temperature; amino acid pulverulent material 25kg and humic acids pulverulent material 48kg got by meter; be divided into that ten equal portions are alternate to be put in rotary drum granulator; and continued granulation, obtain compound fertilizer granules A.
(8) be provided with steam ammonia induced draft fan and Venturi scrubbing device at rotary drum granulator discharge end; Venturi scrubbing device is the dilute sulphuric acid washings of 14% built with massfraction; the steam produced during granulation and ammonia are incorporated in dilute sulphuric acid and carry out absorbing and washing; reclaim steam and ammonia; after reaching finite concentration; by washings reclaim, participate in step (4) in diluting concentrated sulfuric acid is become dilute sulphuric acid.
(9) compound fertilizer granules A is put in cooler and first carry out drying with hot blast, then carry out drying and cooling with cold wind, until the temperature of charge of cooler discharge end is 50 DEG C; Obtain compound fertilizer granules B.
(10) be provided with whirlwind water washing dedust device at cooler discharge end, dust adsorption is also washed, and obtains dust washing liquid;
(11) compound fertilizer granules B is sieved, get the particle that particle diameter meets gauge, obtain compound fertilizer granules C, the macrobead exceeded outside gauge and small-particle are reclaimed.
(12) the macrobead of recovery and small-particle are pulverized, then mix with dust washing liquid, obtain mixture; (7) after the middle amino acid pulverulent material dropped into participates in granulation in step, then mixture is put in rotary drum granulator, again participate in granulation.
(13) compound fertilizer granules C is carried out coating, then carry out metering packing, obtaining product specification is N-P
2o
5-K
2the amino-acid organic/inorganic compound fertilizer finished product 912.5kg of O=20-10-10; Tablets press inwall is substantially without adhesion, and Working environment does not have dust substantially, does not also have unpleasant ammonia smell, and disposable qualified granulating rate reaches 91.2%, and returning charge rate is little.
Claims (3)
1. a sour method compound fertilizer production technology, is characterized in that making method comprises the steps:
(1) first solid state feed stock N P and K is pulverized respectively, then measure respectively and mix again, obtain raw mixture A;
(2) meter is got urea and is dissolved device by urea and change into urine;
(3), by alternate with urine for raw mixture A input and the batch mixing end being sprayed onto rotary drum granulator, obtain raw mixture B; Raw material I be the same, also, its expression method is different, also can not authorize; ; ; ; ;
(4) diluting concentrated sulfuric acid is become dilute sulphuric acid, put in tubular reactor after then dilute sulphuric acid and ammoniacal liquor being measured respectively simultaneously, generate ammonium sulfate slurry, and produce high temperature heat and high pressure impulse force;
(5), under high pressure impulse action, in the raw mixture B ammonium sulfate slurry containing high temperature heat whitewashed in batch mixing end, under the effect of high temperature heat, each storeroom generation replacement(metathesis)reaction, generates the liquid phase sosoloid double salt of mixing;
(6) liquid phase sosoloid double salt is put into the scroll end of rotary drum granulator, tentatively roll granulation and preliminary cooling;
(7) from the batch mixing end of rotary drum granulator to discharge end, its internal temperature drops to 60-70 DEG C gradually from 125-135 DEG C, drops to the position of 80-90 DEG C at rotary drum granulator internal temperature, drops into amino acid pulverulent material and humic acids pulverulent material, and continued granulation, obtain compound fertilizer granules A;
(8) be provided with steam ammonia induced draft fan at rotary drum granulator discharge end and the Venturi scrubbing device of dilute sulphuric acid washings is housed, the steam produced during granulation and ammonia dilute sulphuric acid are carried out absorbing and washing, reclaim steam and ammonia, after reaching finite concentration, by washings reclaim, participate in step (4) in diluting concentrated sulfuric acid is become dilute sulphuric acid;
(9) compound fertilizer granules A is put in cooler and first carry out drying with hot blast, then carry out drying and cooling with cold wind, until the temperature of charge of cooler discharge end is 45-50 DEG C; Obtain compound fertilizer granules B;
(10) be provided with whirlwind water washing dedust device at cooler discharge end, dust adsorption is also washed, and obtains dust washing liquid;
(11) compound fertilizer granules B is sieved, get the particle of composite-grain diameter specification, obtain compound fertilizer granules C, macrobead and small-particle are reclaimed;
(12) the macrobead of recovery and small-particle are pulverized, then mix with dust washing liquid, obtain mixture; (7) after the middle amino acid pulverulent material dropped into participates in granulation in step, then mixture is put in rotary drum granulator, again participate in granulation;
(13) compound fertilizer granules C is carried out coating, then carry out metering packing, obtain composite fertilizer's finished product.
2. sour method compound fertilizer production technology according to claim 1, is characterized in that comprising the steps:
(1) first solid state feed stock N P and K and/or batching thing are pulverized respectively, then measure respectively and mix again, obtain raw mixture A; Described solid state feed stock N P and K comprises Repone K, monoammonium phosphate;
(2) meter is got urea and is dissolved device by urea and change into urine;
(3) the raw mixture A planning to drop within the unit time and urine are respectively divided into some equal portions, alternate input and be sprayed onto the batch mixing end of rotary drum granulator, often drops into a raw mixture A and evenly sprays a urine again, then mix thoroughly, so repeatedly, raw mixture B is obtained;
(4) the vitriol oil of massfraction 98% is diluted to the dilute sulphuric acid that massfraction is 53%-59% at 26-32 DEG C of temperature, dilution time controls within 43-49 minute; Then by dilute sulphuric acid and massfraction be after the ammoniacal liquor metering of 18% according to step (3) same equal portions of same period evenly put in tubular reactor simultaneously, generate ammonium sulfate slurry, and produce water vapor, high temperature heat and high pressure impulse force;
(5) under high pressure impulse action, in raw mixture B ammonium sulfate slurry containing high temperature heat whitewashed in rotary drum granulator batch mixing end, under the effect of high temperature heat, each storeroom generation replacement(metathesis)reaction, generate the liquid phase sosoloid double salt of mixing, these liquid phase sosoloid comprise ammonium chloride potassium, ammonium-potassium sulfate, ammonium-potassium phosphate;
(6) liquid phase sosoloid double salt is rotated the scroll end putting into rotary drum granulator, rotate when dropping into and adopt pressurized air to stir, to prevent inwall from gluing wall, and then tentatively roll granulation and preliminary cooling;
(7) from the batch mixing end of rotary drum granulator to discharge end, its internal temperature drops to 60-70 DEG C gradually from 125-135 DEG C, drops to the position of 80-90 DEG C at rotary drum granulator internal temperature, drops into amino acid pulverulent material and humic acids pulverulent material, and continued granulation, obtain compound fertilizer granules A;
(8) be provided with steam ammonia induced draft fan and Venturi scrubbing device at rotary drum granulator discharge end, Venturi scrubbing device is the dilute sulphuric acid washings of 8%-14% built with massfraction, the steam produced during granulation and ammonia are incorporated in dilute sulphuric acid and carry out absorbing and washing, reclaim steam and ammonia, after reaching finite concentration, by washings reclaim, participate in step (4) in diluting concentrated sulfuric acid is become dilute sulphuric acid;
(9) compound fertilizer granules A is put in cooler and first carry out drying with hot blast, then carry out drying and cooling with cold wind, until the temperature of charge of cooler discharge end is 45-50 DEG C; Obtain compound fertilizer granules B;
(10) be provided with whirlwind water washing dedust device at cooler discharge end, dust adsorption is also washed, and obtains dust washing liquid;
(11) compound fertilizer granules B is sieved, get the particle that particle diameter meets gauge, obtain compound fertilizer granules C, the macrobead exceeded outside gauge and small-particle are reclaimed;
(12) the macrobead of recovery and small-particle are pulverized, then mix with dust washing liquid, obtain mixture; (7) after the middle amino acid pulverulent material dropped into participates in granulation in step, then mixture is put in rotary drum granulator, again participate in granulation;
(13) compound fertilizer granules C is carried out coating, then carry out metering packing, obtain composite fertilizer's finished product.
3. sour method compound fertilizer production technology according to claim 2, is characterized in that comprising the steps:
(1) first Repone K, monoammonium phosphate are pulverized respectively, then measure respectively and mix again, obtain raw mixture A;
(2) meter is got urea and is dissolved device by urea and changes into urine;
(3) the raw mixture A and urine that plan the above-mentioned component dropped within a certain period of time are respectively divided into ten equal portions, alternate input and be sprayed onto the batch mixing end of rotary drum granulator, often drop into a raw mixture A and evenly spray a urine again, then mix thoroughly, so repeatedly, until by complete for the mixing of materials being divided into ten equal portions, obtain raw mixture B;
(4) the vitriol oil of massfraction 98% is diluted to the dilute sulphuric acid that massfraction is 56% at 29 DEG C of temperature, dilution time controls within 46 minutes; Then the ammoniacal liquor being 18% by dilute sulphuric acid and massfraction is divided into ten equal portions and evenly puts in tubular reactor, generates ammonium sulfate slurry, and produces water vapor, high temperature heat and high pressure impulse force;
(5) under high pressure impulse action, in raw mixture B ammonium sulfate slurry containing high temperature heat whitewashed in rotary drum granulator batch mixing end, under the effect of high temperature heat, each storeroom generation replacement(metathesis)reaction, generate the liquid phase sosoloid double salt of mixing, these liquid phase sosoloid comprise ammonium chloride potassium, ammonium-potassium sulfate, ammonium-potassium phosphate;
(6) liquid phase sosoloid double salt is rotated the scroll end putting into rotary drum granulator, rotate when dropping into and adopt pressurized air to stir, to prevent inwall from gluing wall, and then tentatively roll granulation and preliminary cooling;
(7) from the batch mixing end of rotary drum granulator to discharge end, its internal temperature drops to 65 DEG C gradually from 130 DEG C, the position of 85 DEG C is dropped at rotary drum granulator internal temperature, meter gets amino acid pulverulent material and humic acids pulverulent material, be divided into that ten equal portions are alternate to be put in rotary drum granulator, and continued granulation, obtain compound fertilizer granules A;
(8) be provided with steam ammonia induced draft fan and Venturi scrubbing device at rotary drum granulator discharge end, Venturi scrubbing device is the dilute sulphuric acid washings of 11% built with massfraction, the steam produced during granulation and ammonia are incorporated in dilute sulphuric acid and carry out absorbing and washing, reclaim steam and ammonia, after reaching finite concentration, by washings reclaim, participate in step (4) in diluting concentrated sulfuric acid is become dilute sulphuric acid;
(9) compound fertilizer granules A is put in cooler and first carry out drying with hot blast, then carry out drying and cooling with cold wind, until the temperature of charge of cooler discharge end is 47.5 DEG C; Obtain compound fertilizer granules B;
(10) be provided with whirlwind water washing dedust device at cooler discharge end, dust adsorption is also washed, and obtains dust washing liquid;
(11) compound fertilizer granules B is sieved, get the particle that particle diameter meets gauge, obtain compound fertilizer granules C, the macrobead exceeded outside gauge and small-particle are reclaimed;
(12) the macrobead of recovery and small-particle are pulverized, then mix with dust washing liquid, obtain mixture; (7) after the middle amino acid pulverulent material dropped into participates in granulation in step, then mixture is put in rotary drum granulator, again participate in granulation;
(13) compound fertilizer granules C is carried out coating, then carry out metering packing, obtain amino-acid organic/inorganic compound fertilizer finished product.
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| CN106518348A (en) * | 2016-10-26 | 2017-03-22 | 丹阳正联知识产权运营管理有限公司 | Compound fertilizer production process |
| CN106946605A (en) * | 2017-03-17 | 2017-07-14 | 黑龙江禾馗农业科技有限公司 | A kind of environmentally friendly enhanced fertilizer |
| CN107216220A (en) * | 2017-07-28 | 2017-09-29 | 车莉 | A kind of production method for high nitrogen fertilizer of whitewashing |
| CN107619315A (en) * | 2017-03-29 | 2018-01-23 | 济南航晨生物科技有限公司 | A kind of high nitrogen water-soluble fertilizer of amino acid and preparation method thereof |
| CN108046868A (en) * | 2017-11-29 | 2018-05-18 | 亳州司尔特生态肥业有限公司 | A kind of sour method rotary drum chloro fertilizer and its production method |
| CN111943784A (en) * | 2020-09-17 | 2020-11-17 | 嘉施利（宜城）化肥有限公司 | Compound fertilizer production method |
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