CN1651354A - Preparation method of nitrogen phosphorus or nitrogen phosphorus potassium composite fertilizer - Google Patents
Preparation method of nitrogen phosphorus or nitrogen phosphorus potassium composite fertilizer Download PDFInfo
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Abstract
A process for preparing the compound NP or NPK fertilizer features that the powdered or granular monoammonium phosphate is used to replace dryer tubular reactor and control the reaction heat and avoid the overconcentrating of heat, and the phosphoric acid is added to the cyclone washing towder other than gas-liquid separator in tail gas washing system to use evaporation power of washing system to maximum, so it is possible to prepare said compound fertilizer with diluted phosphoric acid.
Description
Technical Field
The invention relates to a preparation method of a compound fertilizer, in particular to a preparation method of a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer.
Background
The prior art for producing compound fertilizer by using dilute phosphoric acid comprises the following steps:
a production process of a sulfur-based compound fertilizer comprises the following steps: dilute phosphoric acid (at a concentration of P) may be used2O520% to 28%) of the raw material. In the production process, dilute phosphoric acid and potassium hydrogen sulfate are mixed, and then the mixture is atomized and gunited after being neutralized in a neutralization tank, so that the dilute phosphoric acid carries more water, the material return ratio is high, the drying energy consumption is high, the mixture ratio of nitrogen, phosphorus and potassium is limited by the main component of potassium ammonium phosphate in the product, and the product mixture ratio is not flexible. Such as the production process of the sulfur-based compound fertilizer disclosed in the Chinese patent 93111207.9 of the Hongri company.
"slurry concentration method": a process for preparing composite fertilizer by slurry concentration method using diluted phosphoric acid (concentration is P)2O5Calculated as 20% -28%). The production process of the method comprises the following steps: the dilute phosphoric acid reacts with ammonia in the neutralization tank, and then the slurry is concentrated, but the slurry concentration also needs to evaporate the moisture in the slurry, and the energy consumption is still high.
"Pre-neutralization tank method": the pre-neutralization tank method commonly used at home and abroad can be used as P2O5The phosphoric acid with the concentration of 40-44% is calculated, but the heat loss of the preneutralization reaction is large, the utilization is insufficient, the moisture entering a system is high, the material return ratio is up to 1: 4-5, and the drying load is large.
"slurry concentration and phosphoric acid concentration co-production method": chinese patent 02113425.1 applied by Sichuan university discloses a technology for producing monoammonium by using dilute phosphoric acid to wash diammonium phosphate tail gas2O5Medium concentration phosphoric acid with the concentration of 40-44% and P2O5Dilute phosphoric acid with the concentration of 25-28 percent is calculated, but a pre-neutralization tank method is still adopted for producing diammonium, and tail gas in the diammonium production flow is washed by the dilute phosphoric acidAfter washing, the product is used for producing monoammonium by a slurry concentration method, and water balance cannot be realized.
"tubular reactor process": US patent US4134750 discloses a process in which a tubular reactor replaces a tank-type neutralization reactor, which simplifies the flow, reduces the investment and is convenient to operate. Requiring phosphoric acid to be P2O5The measured concentration is 30-54%, but the defect is that in the process of producing NPK compound fertilizer, the high-solubility salts of urea and ammonium nitrate are added, and the phosphoric acid concentration is required to be above 50% for controlling water balance and reducing feed-back ratio.
7. Shanghai chemical research institute discloses a 'production process of pipeline reactor ammonium phosphate sulfate' in Chinese patent 00127678.2, the process can use low-concentration phosphoric acid, but needs to add a large amount of sulfuric acid to provide reaction heat, the weight ratio of the phosphoric acid to the sulfuric acid is 0.3-0.7: 1, nitrogen, phosphorus and potassium compound fertilizer can be produced, but the final product has low total nutrient content, inflexible formula and higher requirements on the material of a tubular reactor.
8. Chinese patent application No. 1990.4.19 of Norwegian Dello company and published No. 11/6 in 199190102317.5 discloses a process for the production of granulated diammonium phosphate fertilizer using P2O5The phosphoric acid with the measured concentration of 36-50 percent is produced, but in order to control the reaction heat balance and the water balance, a single dryer tubular reactor process is adopted, the slurry cannot be sprayed into a granulator for granulation production, washing water and steam are added into the granulator for granulation, the material returning ratio is low, but the drying load is large.
9. To reduce the feed back ratio, the French GP company developed a double tube reactor which transfers part of the heat of reaction to a drier but requires the use of P2O5The concentrated phosphoric acid with the concentration of 50-57% is calculated, so the requirement on the quality of phosphorite is high, the operation condition of the tube type reactor of the drier is very harsh, the scab of a material copying plate of the drier is serious, the production efficiency is low, and the cleaning workload is large.
Disclosure of Invention
The invention aims to provide a method for reducing the drying load of returned materialsSmall size, high production efficiency, and use of P2O5A method for producing nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer by using dilute phosphoric acid with the measured concentration of 26% -45%.
The purpose of the invention is achieved by the following technical scheme:
a method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer comprises the following steps:
(1) adding diluted phosphoric acid, sulfuric acid, ammonia and part of washing liquid from a gas-liquid separator into a tubular reactor for neutralization reaction, spraying high-temperature slurry formed after the reaction into a granulator, simultaneously adding solid raw materials and return materials into the granulator to form a rolling solid material bed, and spraying ammonia into the solid material bed through an ammonia spraying shaft for granulation to form solid wet materials and granulation tail gas;
(2) the granulation tail gas enters a gas-liquid separator and is fully atomized and mixed with washing liquid from a circulating pump of the gas-liquid separator in a Venturi ejector, a formed gas-liquid mixture enters the gas-liquid separator for separation, one part of the obtained washing liquid enters the Venturi ejector through the circulating pump to be mixed with the granulation tail gas, the other part of the obtained washing liquid is conveyed to a tubular reactor through a conveying pump, and the obtained gas is pressurized through a fan and then enters a cyclone washing tower for further washing;
(3) the wet solid material of the granulator is dried in parallel flow with dry hot air in a dryer, the dried material is classified in a screening machine, dry tail gas enters a cyclone dust collector to recover most of dust, the recovered dust is returned to the granulator as a return material, and the separated gas is pressurized by a dry tail gas fan and enters a cyclone washing tower for further washing and dust removal;
(4) dry tail gas from a dry tail gas fan and gas from a gas-liquid separator enter the cyclone washing tower together, dilute phosphoric acid, sulfuric acid and water are added into the cyclone washing tower to form washing liquid, a part of the washing liquid is sprayed and washed on the dry tail gas entering the tower through a circulating pump, the rest of the washing liquid overflows to the gas-liquid separator, and the washed waste gas is emptied;
(5) crushing the large particles screened by the screening machine by a crusher and returning the fine powder screened by the screening machine as a return material to the granulator; and (4) after screening out the qualified particles, returning part of the qualified particles to the granulator to maintain stable material return amount, and cooling the rest qualified particles to obtain the product.
The dilute phosphoric acid is represented by P2O5The measured concentration is 26-45%; the sulfuric acid is represented by H2SO4The concentration is 93% or 98%.
The granulation temperature is 60-115 ℃; the temperature of the hot air for drying is 90-240 ℃; the temperature of the drying tail gas is 60-120 ℃; the water content (free water) of the wet material at the outlet of the granulator is 2.5-4.5%; the moisture content (free water) of the material at the outlet of the dryer is less than 1.5 percent.
The amount of sulfuric acid, diluted phosphoric acid, ammonia and washing liquid added into the tubular reactor enables the N/P in the tubular reactor to be 1.0-1.9.
The amount of the solid raw materials added into the granulator enables the N/P of materials discharged by the granulator to be 1.0-1.9.
The solid raw material is one of potassium sulfate, potassium chloride, potassium nitrate, ammonium sulfate, ammonium chloride, urea, ordinary superphosphate, triple superphosphate, calcium magnesium phosphate fertilizer and diammonium phosphate or a mixture of two or more of the potassium sulfate, the potassium chloride, the potassium nitrate, the ammonium sulfate, the ammonium chloride, the urea, the ordinary superphosphate, the triple superphosphate, the calcium magnesium phosphate fertilizer and; the filler can also be added according to the nutrient requirement, and is one of or a mixture of two or more of powdered bentonite, attapulgite powder, zeolite powder, sepiolite, kaolin, china clay, pottery clay, phosphogypsum, fly ash or talcum powder. The adding amount of the filler is 0 to 25 percent of the total dry basis weight of the feeding materials.
The returned materials comprise fine powder obtained by screening, recycled dust, small particles obtained by crushing the particles with the over-specification size and finished products partially returned.
The return ratio of the granulator (the feeding amount: the return amount, calculated on a dry basis) is 1: 2.5-1: 4.
The amount of the dilute phosphoric acid, the sulfuric acid and the process water entering the cyclone washing tower enables the pH value of washing liquid in the cyclone washing tower to be 0.5-2.5, and the pH value of the washing liquid in thegas-liquid separator to be 1-7.
The amount of the washing liquid of the gas-liquid separator which is conveyed to the tubular reactor through the conveying pump is adjusted according to the granulation requirement.
The ammonia entering the granulator through the ammonia spraying shaft accounts for 5-35% of the total ammonia, and the rest ammonia enters the tubular reactor.
The ammonia can be liquid ammonia or gaseous ammonia.
The solid feedstock may also include monoammonium phosphate (i.e., MAP, which may be in powder or granular form) added in an amount of up to 300 Kg/t.
The dilute phosphoric acid added into the cyclone washing tower accounts for 20-95% of the total input amount of the dilute phosphoric acid.
The following explains the effects of the technical solution of the present invention:
reaction principle of tubular reactor
(1) Wet process for ammonification of phosphoric acid
In the washing apparatus, granulator and tubular reactor, the main chemical reaction is the reaction between phosphoric acid and ammonia. The hydrogen ions in phosphoric acid can be instantaneously neutralized to form monoammonium phosphate (MAP), diammonium phosphate (DAP):
phosphoric acid reacts with ammonia to directly generate (NH) in the reaction process4)2HPO4Less, the first formed is NH4H2PO4Then re-issueThe following reactions occur:
the reaction of phosphoric acid with ammonia is a rapid reaction which can be achieved instantly, and the process speed depends on the mixing speed and the mixing degree of phosphoric acid and ammonia. The tubular reactor is used for carrying out the ammonification of phosphoric acid, namely, the strong mixing action in the tubular reactor is utilized, so that the neutralization process is shortened to about 1 second, and simultaneously, a large amount of reaction heat is fully utilized.
(2) Ammoniation of sulfuric acid
The sulfuric acid added in the tubular reactor and ammonia are subjected to a violent neutralization reaction to generate ammonium sulfate:
(3) reaction of various impurities in phosphoric acid
Free sulfuric acid contained in phosphoric acid and impurities such as iron, aluminum, magnesium, calcium, fluorine, silicon and the like also react in the ammonia neutralization process, and the impurities generate various complex compounds to enter slurry.
Ammonia is introduced into the material bed, and the main generation method is further ammoniation of monoammonium phosphate to form diammonium phosphate:
firstly, according to the production variety, the drying machine tubular reactor is replaced by powdery (or granular) monoammonium phosphate (MAP), and the reaction heat is controlled. Because a dryer tubular reactor is cancelled, the problem of scabbing of the shoveling plate is solved; the defect that the heat of a tubular reactor of a granulator is too concentrated when the tubular reactor is used independently is avoided, so that the heat balance of the system is easier to realize; the reaction load of the tubular reactor is reduced, and the corresponding reduction of the liquid phase quantity enables the system feed back ratio to be further reduced and the water balance to be more easily controlled.
After the pipe-type reactor of a drier is replaced by powdery (or granular) monoammonium phosphate (MAP), in the process of producing the nitrogen-phosphorus-potassium compound fertilizer by using concentrated phosphoric acid, most of phosphoric acid is directly put into the pipe-type reactor to bring in a large amount of free water, and a large amount of process water is brought in from a washing liquid to enter the pipe-type reactor, and actually, the washing liquid entering the pipe-type reactor is mixed with the concentrated phosphoric acid and then is taken as P2O5The measured concentration is about 28 to 37 percent. Meanwhile, a large amount of process water is required to be added in a washing system to keep the fluidity of washing liquid, supplement the evaporation water amount of the washing system and control the reaction temperature and the slurry fluidity of the tubular reactor. Thus, phosphoric acid with higher concentration is needed, a large amount of process water is wasted, and the production cost is increased. As used in the present invention with P2O5The phosphoric acid with the concentration of 26-45% is calculated, the reaction heat of the tubular reactor for producing the nitrogen-phosphorus-potassium compound fertilizer and the evaporation capacity of tail gas are fully utilized, the addition amount of washing process water is reduced, and the aim of producing dilute phosphoric acid is fulfilled.
After dilute phosphoric acid is used for replacing concentrated phosphoric acid, the water content of slurry of the tubular reactor is kept unchanged, the feeding amount of other raw materials is kept unchanged, and technological indexes such as granulation temperature, liquid-solid ratio, return ratio, product N/P ratio and the like are unchanged, so that the same effect as that of a concentrated acid process can be achieved.
In order to utilize the evaporating capacity of the washing system to the maximum, the position of the washing system to which the dilute phosphoric acid is added is changed from a first-stage washer (namely a gas-liquid separator) to a second-stage washer (namely a cyclone washing tower), and the amount of the dilute phosphoric acid added for washing can be flexibly adjusted between 20 percent and 95 percent of the total input amount of the dilute phosphoric acid according to the concentration of the dilute phosphoric acid and the variety of the product.
Meanwhile, monoammonium phosphate (MAP) is added as transfer reaction heat, and can be not added under the condition that the transfer reaction heat is not needed, so that the N/P of the sulfuric acid, the dilute phosphoric acid, the ammonia and the washing liquid added into the tubular reactor is 1.0-1.9.
The invention mainly aims at the characteristic of rich middle-low grade phosphorite reserves in China, and uses dilute phosphoric acid to replace P2O5The concentrated phosphoric acid with the concentration of more than 50 percent breaks through the phosphoric acid P in the process of a single granulator tubular reactor2O5The measured concentration is not lower than the limit value of 46 percent, the material return amount is not increased, the slurry temperature is ensured, the advantages of full utilization of reaction heat of the tubular reactor, short reaction time, convenient and quick adjustment of the material feeding amount, low water content (free water) of wet materials at the outlet of the granulator (2.5-4.5 percent), low material return ratio(1: 2.5-1: 4) and small drying load are kept on the premise of realizing water balance and heat balance, the production cost of the compound fertilizer is reduced, and certain direct economic benefit is achieved; the method can be used for producing the dilute phosphoric acid, can use medium-low grade phosphate ores, removes the dependence on high grade phosphate ores, improves the production capacity of a device, saves the steam consumption of concentrated phosphoric acid in the production process of phosphoric acid, and has unlimited indirect economic benefit.
The present invention is further illustrated by the following specific embodiments, which are not meant to limit the scope of the invention.
In particular toDetailed description of the preferred embodiments
Example 1:
the concentration is 40% (as P)2O5Metered by a metering pump) until the pressure is 1MPa, and respectively entering a tubular reactor and a cyclone washing tower in the amount of 8.0t/h and 6.4t/h after metering control by a flowmeter and an adjusting valve. Sulfuric acid with the concentration of 98 percent is pressurized to 1MPa by a sulfuric acid pump, and enters a tubular reactor and a cyclone washing tower in the amount of 6.0t/h and 2.3t/h after being metered and controlled by a flowmeter and an adjusting valve respectively. Liquid ammonia (or gas ammonia, with a concentration of 99.5%) enters the tubular reactor and the ammonia spraying shaft at a rate of 4.0t/h and 1.0t/h after being metered and controlled by a flowmeter and an adjusting valve respectively, and monoammonium phosphate (N11.2%, P)2O544.5 percent) of 6.1t/h and potassium sulfate (K)2O50.5%) 14.5t/h, ammonium nitrate (N34.2%) 11.5t/h, bentonite: 5t/h, adding into a granulator; the granulation temperature is 90-100 ℃.
In a tubular reactor, dilute phosphoric acid, sulfuric acid, ammonia and a washing solution are subjected to rapid neutralization reaction, high-temperature slurry generated after the reaction is sprayed into a granulator, the high-temperature slurry is mixed with a solid raw material, small particles obtained by crushing returned large particles, screened fine powder and dust collected and recycled, and part of returned finished products are granulated in a rotary granulator through introducing ammonia, generated granulation tail gas enters a Venturi ejector to be washed, a solid wet material discharged from the granulator contains about 4% of water and enters a dryer to be dried in parallel flow with dry hot air at the temperature of 120-160 ℃, the water content of the material is reduced to-1.0%, and the dried material enters a screening machine to be classified. And (3) enabling the dried tail gas out of the dryer to have a temperature of 85-105 ℃, enabling the dried tail gas to enter a cyclone dust collector to recover most of dust, enabling the recovered dust to return to a granulator as a return material, and enabling the separated gas to enter a cyclone washing tower for further washing and dust removal after being pressurized by a dried tail gas fan.
The tail gas discharged from the granulator contains a large amount of water vapor, ammonia, a small amount of dust and the like, and is fully atomized and mixed with the circulating washing liquid from the gas-liquid separator in the Venturi ejector to form a vapor-liquid mixture, and most of ammonia and dust are recovered. And separating a gas-liquid mixture in a gas-liquid separator, wherein a part of the obtained washing liquid enters the Venturi ejector through a circulating pump to be mixed with the granulation tail gas, the other part of the washing liquid enters the tubular reactor according to the granulation requirement, the separated gas enters a cyclone washing tower through a fan, enters the cyclone washing tower together with the dry tail gas from a dry tail gas fan, is sprayed and washed by the washing liquid from the circulating pump of the cyclone washing tower, the washed waste gas is emptied, a part of the washing liquid in the cyclone washing tower enters the circulating pump, and the rest of the washing liquid overflows to the gas-liquid separator.
In the cyclone washing tower, the addition amounts of sulfuric acid, diluted phosphoric acid and process water are controlled by a flow regulating valve, the pH values of the cyclone washing tower and the gas-liquid separator are controlled to be 1-2.5 and 3-7 respectively, and the liquid level of the gas-liquid separator is ensured to be normal.
And (3) grading the dried material in a sieving machine, crushing the sieved large particles into small particles by a crusher, returning the small particles and the sieved fine powder to the granulator as return materials, returning the sieved qualified particles to the granulator as return materials, maintaining the return material amount at about 180t/h, and cooling the rest qualified particles to obtain the product, wherein the specification of the product nitrogen-phosphorus-potassium compound fertilizer is 15-15-15.
Example 2:
otherwise the same raw material specification as in example 1 was used, except that the granulator was charged without monoammonium phosphate (MAP), without filler, and with a phosphoric acid concentration of 38% (expressed as P)2O5Meter). 5.0t/h of tubular reactor phosphoric acid, 4.6t/h of cyclone washing tower phosphoric acid, ammonia: 5.9t/h, 13.3t/h of sulfuric acid with the concentration of 98%, 22.0t/h of potassium sulfate, 15.1t/h of ammonium nitrate, 180t/h of return material, 95-100 ℃ of granulation temperature, 140-180 ℃ of drying hot air, 90-105 ℃ of drying tail gas, 4-4% of water in the material at the outlet of a granulator, 1.2% of water in the material at the outlet of a dryer, and the specification of the nitrogen-phosphorus-potassium compound fertilizer product is 16-6-18.
Example 3
Otherwise the same raw materials as in example 1 were used, except that no filler was added to the granulator and the phosphoric acid concentrations were 26% and 45% (as P)2O5In counts) of two. Tubular reactor phosphoric acid 9.1t/h (phosphoric acid as P)2O5The calculated concentration is 45 percent), and the phosphoric acid in the cyclone washing tower is 12.9t/h (the phosphoric acid is P)2O5The calculated concentration is 26%),ammonia: 8.3t/h, 98% sulfuric acid 15.5t/h, monoammonium phosphate (MAP)12.2t/h, potassium chloride (K)260.7 percent of O) 8.0t/h, 19.6t/h of ammonium nitrate, 200t/h of material returning amount, 85-95 ℃ of granulation temperature, 120-200 ℃ of drying hot air temperature, 95-110 ℃ of drying tail gas temperature, 4-4 percent of water content of granulator outlet material, 1.1 percent of water content of dryer outlet material, and the specification of the product nitrogen-phosphorus-potassium compound fertilizer is 18-16-6.
Example 4
Otherwise the same raw material specification as in example 1 was used, except that no filler was added to the granulator and the phosphoric acid concentration was 27.8% (in terms of P)2O5Meter). 4.0t/h of tubular reactor phosphoric acid, 23.0t/h of cyclone washing tower phosphoric acid, ammonia: 7.6t/h, sulfuric acid with the concentration of 98 percent 16.4t/h, monoammonium phosphate (MAP)12.2t/h and potassium chloride (K)2O60.7%) 10.8t/h, ammonium nitrate 17.2t/h, material return 200t/h, granulation temperature 80-95 ℃, and dry hot airThe temperature is 140-210 ℃, the temperature of the drying tail gas is 90-105 ℃, the water content of the material at the outlet of the granulator is 4%, the water content of the material at the outlet of the dryer is 1.1%, and the specification of the product nitrogen-phosphorus-potassium compound fertilizer is 16-16-8.
The quality index of the product obtained in the above example is shown in Table 1 below.
TABLE 1
| Examples | Total nitrogen (N) ％ | Available phosphorus (P2O5) ％ | Total potassium (K2O) ％ | Free water ％ | Particle size% | Remarks for note |
| 1～4.75 mm | ||||||
| 1 | 15.1 | 15.0 | 14.9 | 0.58 | ＞95 | Product quality index and inspection method symbol Quality standard of mixed fertilizer GB15063-2001 |
| 2 | 16.0 | 5.9 | 18.2 | 1.06 | ＞95 | |
| 3 | 17.9 | 16.1 | 6.2 | 0.86 | ＞95 | |
| 4 | 16.0 | 16.1 | 8.1 | 0.92 | ＞95 |
Claims (12)
1. A method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer comprises the following steps:
(1) adding diluted phosphoric acid, sulfuric acid, ammonia and part of washing liquid from a gas-liquid separator into a tubular reactor for neutralization reaction, spraying high-temperature slurry formed after the reaction into a granulator, simultaneously adding solid raw materials and return materials into the granulator to form a rolling solid material bed, and spraying ammonia into the solid material bed through an ammonia spraying shaft for granulation to form solid wet materials and granulation tail gas;
(2) the granulation tail gas entersa gas-liquid separator and is fully atomized and mixed with washing liquid from a circulating pump of the gas-liquid separator in a Venturi ejector, a formed gas-liquid mixture enters the gas-liquid separator for separation, one part of the obtained washing liquid enters the Venturi ejector through the circulating pump to be mixed with the granulation tail gas, the other part of the obtained washing liquid is conveyed to a tubular reactor through a conveying pump, and the obtained gas is pressurized through a fan and then enters a cyclone washing tower for further washing;
(3) the method comprises the following steps that solid wet materials of a granulator enter a dryer to be dried in parallel flow with dry hot air, the dried materials enter a screening machine to classify the materials, dry tail gas enters a cyclone dust collector to recover most of dust, the recovered dust returns to the granulator as returned materials, and the separated gas is pressurized by a dry tail gas fan to enter a cyclone washing tower for further washing and dust removal;
(4) dry tail gas from a dry tail gas fan and gas from a gas-liquid separator enter the cyclone washing tower together, dilute phosphoric acid, sulfuric acid and water are added into the cyclone washing tower to form washing liquid, a part of the washing liquid is sprayed and washed on the dry tail gas entering the tower through a circulating pump, the rest of the washing liquid overflows to the gas-liquid separator, and the washed waste gas is emptied;
(5) crushing the large particles screened by the screening machine by a crusher and returning the fine powder screened by the screening machine as a return material to the granulator; and (4) after screening out the qualified particles, returning part of the qualified particles to the granulator to maintain stable material return amount, and cooling the rest qualified particles to obtain the product.
2. The method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer as defined in claim 1, wherein: the dilute phosphoric acid added into the cyclone washing tower accounts for 20-95% of the total input amount of the dilute phosphoric acid.
3. The method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer as defined in claim 2, wherein: the concentration of the dilute phosphoric acid added into the tubular reactor in the step (1) and the dilute phosphoric acid added into the cyclone washing tower in the step (4) is P2O5Calculated by 26 to 45 percent.
4. The method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer as defined in claim 1, wherein: in the step (1), the solid raw material is one of potassium sulfate, potassium chloride, potassium nitrate, ammonium sulfate, ammonium chloride, urea, common calcium, triple superphosphate, calcium magnesium phosphate fertilizer and diammonium phosphate or a mixture of two or more of the potassium sulfate, the potassium chloride, the potassium nitrate, the ammonium sulfate, the ammonium chloride, the urea, the common calcium, the triple superphosphate, the calcium magnesium phosphate fertilizer and the diammonium.
5. The method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer as defined in claim 4, wherein: the solid feedstock also includes a filler.
6. The method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer as defined in claim 5, wherein: the filleris one or a mixture of two or more of powdered bentonite, attapulgite powder, zeolite powder, sepiolite, kaolin, china clay, argil, phosphogypsum, fly ash or talcum powder; the addition amount is 0-25% of the total dry basis weight of the feeding materials.
7. The method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer as defined in claim 1, wherein: the granulation temperature is 60-115 ℃; the temperature of the drying hot air is 90-240 ℃; the temperature of the drying tail gas is 60-120 ℃.
8. The method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer as defined in any one of claims 1 to 7, wherein: the amount of sulfuric acid, diluted phosphoric acid, ammonia and washing liquid added into the tubular reactor enables the N/P in the tubular reactor to be 1.0-1.9.
9. The method for preparing the nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer according to any one of claims 1 to 7, which comprises the following steps: the amount of the solid raw materials added into the granulator enables the N/P of materials discharged by the granulator to be 1.0-1.9.
10. The method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer as defined in any one of claims 1 to 7, wherein: the amount of the dilute phosphoric acid, the sulfuric acid and the process water entering the cyclone washing tower enables the pH value of washing liquid in the cyclone washing tower to be 0.5-2.5, and the pH value of the washing liquid in the gas-liquid separator is 1-7.
11. The method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer as defined in any one of claims 1 to 7, wherein: and (2) in the step (1), ammonia entering the granulator through an ammonia spraying shaft accounts for 5-35% of the total ammonia.
12. The method for preparing a nitrogen-phosphorus or nitrogen-phosphorus-potassium compound fertilizer as defined in any one of claims 1 to 7, wherein: the return ratio of the granulator is 1: 2.5-1: 4.
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Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3878561D1 (en) * | 1988-11-08 | 1993-03-25 | Norsk Hydro As | METHOD FOR PRODUCING GRANULATED DIAMMONE PHOSPHATE-CONTAINING FERTILIZERS. |
| CN1132802C (en) * | 2000-02-01 | 2003-12-31 | 江西贵溪化肥厂 | Process for producing compound N-P-K fertilizer |
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