CN108473330A - Method and apparatus for making porous ammonium nitrate granulate - Google Patents
Method and apparatus for making porous ammonium nitrate granulate Download PDFInfo
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- CN108473330A CN108473330A CN201780005831.XA CN201780005831A CN108473330A CN 108473330 A CN108473330 A CN 108473330A CN 201780005831 A CN201780005831 A CN 201780005831A CN 108473330 A CN108473330 A CN 108473330A
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- fluidized bed
- particle
- air stream
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- granulating tower
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2/00—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic
- B01J2/02—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic by dividing the liquid material into drops, e.g. by spraying, and solidifying the drops
- B01J2/04—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic by dividing the liquid material into drops, e.g. by spraying, and solidifying the drops in a gaseous medium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2/00—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic
- B01J2/16—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic by suspending the powder material in a gas, e.g. in fluidised beds or as a falling curtain
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/18—Nitrates of ammonium
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05C—NITROGENOUS FERTILISERS
- C05C1/00—Ammonium nitrate fertilisers
- C05C1/02—Granulation; Pelletisation; Stabilisation; Colouring
-
- C—CHEMISTRY; METALLURGY
- C06—EXPLOSIVES; MATCHES
- C06B—EXPLOSIVES OR THERMIC COMPOSITIONS; MANUFACTURE THEREOF; USE OF SINGLE SUBSTANCES AS EXPLOSIVES
- C06B31/00—Compositions containing an inorganic nitrogen-oxygen salt
- C06B31/28—Compositions containing an inorganic nitrogen-oxygen salt the salt being ammonium nitrate
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/30—Particle morphology extending in three dimensions
- C01P2004/32—Spheres
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Fertilizers (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to the productions of porous ammonium nitrate; wherein make ammonium nitrate component granulating to form ammoniumnitrate prill in ammoniumnitrate prill equipment; ammoniumnitrate prill is collected and cools down at least partly herein in a fluidized bed; and wherein, the flowing of the first air stream is flowed by second fluidized bed and/or other air stream by granulating tower by the first fluidized bed and/or the flowing of the second air stream.
Description
Technical field
The present invention relates to the productions of porous ammonium nitrate, wherein makes ammonium nitrate component particle in ammoniumnitrate prill equipment
Change to be formed in the granular ammonium that fluid bed is collected and cooled down at least partly at fluid bed.
Background technology
The method of ingredient granules is set to be known for producing by melt or by concentrated solution in the equipment of granulating
The commercial run of granular disintegration.The melt of supply or solution are dispersed as falling by spray nozzle
Air) droplet, and droplet is on the way cooled to the degree for being cured to form particle.When the material of supply is solution,
Solidification process is along with local evaporation.In such as urea fertilizer and other of offer or acquisition in the form of melt or concentrated solution
In the production of material, large scale industry scale granulating technology is used.
In order to produce porous ammonium nitrate, usually ammonium nitrate component is set to granulate in the adverse current cooling air of granulating tower.
This produces the still particle with certain water content (for example, calculating by weight about 4%), that is, uniform solid objects.It
Afterwards, water is rapidly extracted out in subsequent drying steps.The aperture or crack being consequently formed in particle penetrate through all the way so that it can
With for example filled with oil.
For this purpose, the ammonium nitrate component of about 96% intensity for example with 145-150 DEG C of temperature is cooled to by granulating tower
Transformation temperature below about 84 DEG C.Hole is formed in the drying cylinder of downstream and transfers to realize in the second drying cylinder positioned at downstream
Granulate the lower final water content that final product needs.In general, granulating tower has granulating channel, wherein wait granulating
Product flows by granulating channel, and the granulating channel constitute granulating tower free-falling height.In addition, particle
Changing tower usually has a discharge member, which is mounted on the top of granulating tower and by be granulated at being distributed into
It is granulated tower.In order to make ammonium nitrate component granulate, it usually needs such granulating equipment, with 60-70 meters of total height
Or the granulating tower of 40-50 meters of free-falling height.
In general, porous granulating ammonium nitrate is used as one of the component of explosive component.Therefore, porous granulating ammonium nitrate
Such as it is mixed with heating oil to produce the explosive component for being referred to as ANFO.
2009/0301618 A1 of US are related to porous granular material, are made of explosive ammonium nitrate and by melting
Ammonium nitrate production in two fluid beds being connected in series with.15 92 359 A1 of BG 63 296 B1 and DE also discloses use
In the method for production granular ammonium.3,539,326 A of US 4,190,622 A and US is disclosed for manufacturing graininess grain
The method of son.
It is well known, however, that for manufacture porous ammonium nitrate method and apparatus it is unsatisfactory in all fields, and
In the presence of the demand to improved method and apparatus.Therefore, the purpose of the present invention is to provide more for producing better than the prior art
The method and apparatus of hole ammonium nitrate.
Invention content
Above-mentioned purpose is realized by claimed subject matter.
The first aspect of the present invention is related to the method for producing porous ammonium nitrate, wherein the method includes following steps
Suddenly：
(a) make ammonium nitrate component granulating to form particle in the granulating tower of ammoniumnitrate prill equipment,
(b) particle formed in step (a) is collected in the first fluidized bed, and
(c) flowing of the first air stream is made to pass through second fluidized bed by the first fluidized bed (3) and/or the flowing of the second air stream
(4) and/or the flowing of other air stream is by granulating tower.
The method of the present invention the step of in (a), ammonium nitrate component introduces granulating tower, is preferably introduced granulating tower
Top.Preferably, ammonium nitrate component is ammonium nitrate melt, can be optionally watery.Preferably, ammonium nitrate component includes
Water.In a preferred embodiment, the water content that ammonium nitrate component has calculates by weight in the range of 1% to 6%, preferably by
Weight calculates in the range of 2% to 5.5%, calculates by weight in the range of 3% to 5% or calculate by weight and arrived 4%
In the range of 4.5%.The ingredient can include optionally other additives, particularly granulating additive.People in the art
Additive is suitably granulated known to member.
Preferably, ammonium nitrate component by one or more granulating nozzles be injected into granulating channel and later from
Top down flowing is by granulating tower.The manufacture of ammonium nitrate component known to those skilled in the art and injection ammonium nitrate component
Method.
Air is extraly flowed by granulating tower.Here preferably, air includes various gaseous components, particularly oxygen
And nitrogen.For the purposes of the present invention, term " air " preferably further includes aerosol so that air can include not only gaseous state
Ingredient further includes solid-state and/or liquid composition (it is preferably obtained in the granulating of ammonium nitrate).For example, air may include
Ammonium nitrate dust.For the purposes of the present invention, this admixture of gas and/or aerosol are collectively referred to as " air ".
Preferably, granulating tower is passed through in air flowing (that is, bottom-up) from bottom end to top.Preferably, air is inverse
The ammonium nitrate component flowing by granulating tower.
When ammonium nitrate component is flowed by granulating tower, ammoniumnitrate prill be consequently formed (in newborn state) and
It falls in granulation tower, and air surrounds ammonium nitrate component counter-current flow bottom-up.Air stream is insufficient to allow particle to be in
Floating state, particle deposits relative motion in a downward direction on the contrary, but the movement is reduced by counter-flow air.Preferably,
The air that the relative quantity of the air flowed around ammonium nitrate component uses every kilogram of ammonium nitrate component is at 1 to 20 kilograms
In range, more preferably in the range of 1.5 to 15 kilograms, in the range of 2 to 10 kilograms, in 2.5 to 8 kilograms of ranges
It is interior, in the range of 3 to 7 kilograms or in the range of 4 to 5.5 kilograms.
The method of the present invention the step of in (b), the particle formed in the step (a) is collected in the first fluidized bed.This
In, the particle by having already passed through granulating tower before forms fluid bed.
Fluid bed is adapted for use in many Chemical engineering methods of processing solid and liquid and its structure is this field skill
Art personnel are known.Fluid bed according to the present invention is formed by the particle collected, and the particle is by the fluid that flows up into becoming a mandarin
Change state.Here the state of the similar liquids of particle is generated, that is, term " fluid bed ".Thus best cooling and drying are generated
Condition.Preferably, fluid includes air.
The particle formed in the step of collecting the method for the present invention in the fluid bed formed by fluidized particles (a).When to
When up to the first fluidized bed, fluid (preferably air) preferably surrounds particle flow bottom-up, and fluid make particle into
Enter fluid state to make particle in perpetual motion, do not touch the bottom of fluid bed at least partly and thus become fluid bed
A part.
Preferably, the first fluidized bed binds directly granulating tower.Preferably, particle only falls under the effect of gravity substantially
And from top down by granulating tower and granulating tower lower end at leave granulating tower, later, particle also, it is preferred that
Ground only falls on the first fluidized bed down and is collected by the first fluidized bed under gravity substantially.Preferably, first-class
Change bed to be arranged under granulating tower.
In a preferred embodiment, ammonium nitrate component is when by granulating tower and as air is inverse around ammonium nitrate component
Stream is flowed and is cooled.Preferably, ammonium nitrate component is so cooled down so that the particle formed in granulating tower is in fluid bed
In be dimensionally stable when being collected.Preferably, ammonium nitrate component so cools down in granulating tower so that particle exists
Liquid phase when being collected in fluid bed in either case the total weight based on particle calculate by weight not more than 80%,
It more preferably calculates by weight not more than 75%, calculate by weight not more than 70%, calculate by weight not more than 65%, by weight
Not more than 60% is calculated, not more than 55% is calculated by weight, calculates by weight not more than 50%, calculates by weight not more than 45%
Or calculate by weight not more than 40%.
Temperature and particle of the ammonium nitrate component when introducing the top of granulating tower are collected moment institute in a fluidized bed
Preferably at least 20 DEG C, more preferably at least 25 DEG C, at least 30 DEG C, at least 35 DEG C, at least 40 DEG C of difference between the temperature at place,
At least 45 DEG C or at least 50 DEG C.
Ammonium nitrate component introduce granulating tower top when preferably at least 120 DEG C of temperature, more preferably at least 125
DEG C, at least 130 DEG C, at least 135 DEG C, at least 140 DEG C, at least 145 DEG C, at least 150 DEG C, at least 155 DEG C or at least 160 DEG C.
In a preferred embodiment, temperature when particle is collected in the first fluidized bed in the range of 90 to 120 DEG C,
More preferably in the range of 92 DEG C to 115 DEG C, in the range of 94 DEG C to 110 DEG C or in the range of 95 DEG C to 105 DEG C.
Preferably, particle leaves granulating tower at the lower end of granulating tower, and particle is preferably fallen on down first-class later
Change on bed and is collected by the first fluidized bed.Relative to conventional granulates method, particle is very gently in the first fluidized bed
It is collected.Specifically, particle is subjected to the mechanical stress greatly reduced.This not yet to cure or be dried to largely (that is,
It is fully hardened) particle even can be further processed.
Therefore, compared with the method for not adjacent fluid bed, the operation of method of the invention only needs particle in granulating tower
It is middle to carry out relatively small number of cooling.
According to the present invention, the temperature for the ammoniumnitrate prill being collected in the first fluidized bed after leaving granulating tower
And leave the conventional granulates tower of not adjacent fluid bed ammoniumnitrate prill temperature between difference can be preferably at least 5
DEG C, more preferably at least 10 DEG C, at least 15 DEG C, at least 20 DEG C, at least 25 DEG C or at least 30 DEG C.
Temperature when particle leaves granulating tower by residence time of the particle in granulating tower and thus by
It is granulated the conclusive influence of the free-falling height of tower.It is collected in the first fluidized bed after leaving granulating tower
In the production of particle, the free-falling height of the granulating tower needed is not more than 60m, more preferably no more than 55m, is not more than
50m, no more than 45m, no more than 40m, no more than 35m, no more than 30m, no more than 25m, no more than 20m, no more than 15m, no
More than 10m or it is not more than 5m.
In a preferred embodiment, particle is cooled down at least partly on the first fluidized bed.Preferably, particle is first
Carried out on fluid bed it is cooling so that its temperature when leaving the first fluidized bed than its arrival first fluidized bed when it is at least 5 DEG C low, more
At least 10 DEG C preferably low, at least 15 DEG C low, low at least 20 DEG C or at least 25 DEG C low.
In a preferred embodiment, particle leaves the first fluidized bed and temperature of the particle when leaving the first fluidized bed is less than
84 DEG C, even more preferably less than 80 DEG C.
In a preferred embodiment, particle leaves the first fluidized bed and is directed into second fluidized bed later.This field
Technical staff becomes known for the suitable mode that particle is transferred to second fluidized bed from the first fluidized bed.For example, first class
Bed can be not exclusively horizontally aligned with subsidiary level flow motion.
It would be recognized by those skilled in the art that can also be by can be alternately through can optionally have suitably more
It is large-sized single fluidised bed to be similarly implemented the effect of the first fluidized bed according to the present invention and second fluidized bed.
Preferably, particle carries out predrying in second fluidized bed at least partly.Preferably, particle is in second fluidized bed
Upper predrying is to the degree for no longer needing predrying cylinder in subsequent products finishing step.Particle is when leaving second fluidized bed
Water content in either case the total weight based on particle calculate by weight preferably not more than 5%, more preferably by
Weight calculates no more than 4%, calculates by weight no more than 3%, calculates by weight no more than 2%, calculating by weight and be not more than
1%, it calculates by weight no more than 0.9% or calculates by weight no more than 0.8%.
According to the present invention, the flowing of the first air stream passes through second by the first fluidized bed and/or the flowing of the second air stream
Change bed and/or the flowing of other air stream by granulating tower.
Preferably, the first air stream flow bottom-up by the first fluidized bed and/or the second air stream from bottom to
Second fluidized bed is passed through in upper flowing.First air stream preferably makes the particle in the first fluidized bed enter fluidized state and/or
Two air streams preferably make the particle in second fluidized bed enter fluidized state.Preferably, the first air stream is conveyed through
One fluid bed is for cooling particle.Preferably, the second air stream is conveyed through second fluidized bed for predrying particle.
In order to realize efficient granulating, preferably need than flowing by the first fluidized bed and/or second fluidized bed
The air total amount of the amount bigger of air.For this purpose, other air stream be preferably introduced granulating tower and preferably from bottom to
Upper flowing is by granulating tower.Preferably, air stream in addition introduces granulating tower in bottom end.Preferably, air in addition
Stream can introduce granulating tower a position or at different locations；Other air stream introduces preferably at a position
Granulate tower.Other air stream can also mix with the air stream of second fluidized bed and/or be added at least partly first
Fluid bed.
Preferably, air stream in addition includes surrounding air.In another preferred embodiment, air stream in addition is included in
The process air obtained at another point during for producing porous ammonium nitrate and/or during other.
In a preferred embodiment, at least part of flowing by the air stream of granulating tower passes through granulating tower in flowing
It is discharged later from granulating tower, in purification grade handle and be re-circulated into granulating tower at least partly.Preferably, empty
Air-flow is discharged in top end from granulating tower.Preferably, flowing passes through the calculation by volume of the air stream of granulating tower at least
10%, at least 20% is more preferably calculated by volume, is calculated at least 30% by volume, is calculated at least 40% by volume, by volume
At least 50% is calculated, at least 60% is calculated by volume, calculates at least 70% by volume, calculating at least 80% by volume or by volume
At least 90% is calculated from the discharge of granulating tower and is handled in purification grade.Preferably, purification grade is wet scrubber.
Preferably, the calculation by volume at least 10% of the air handled in purification grade is more preferably calculated by volume
At least 20%, at least 30% is calculated by volume, is calculated at least 40% by volume, is calculated at least 50% by volume, calculates by volume
At least 60%, at least 70% is calculated by volume, calculate at least 80% by volume or calculates at least 90% by volume is recycled to
It is granulated the bottom end of tower.Preferably, the air handled in purification grade is all recycled to the bottom end of granulating tower.
Other air stream may include only surrounding air or only process air or be only recycled to granulating tower
The air of bottom end or all possible combination carried out with all possible ratio with it.
First air stream and the second air stream can independent of one another or interactions.Therefore, the first air stream and the second sky
Both air-flows can be provided and be flowed independently of one another by the first fluidized bed or second fluidized bed independently of one another.
In a preferred embodiment,
The flowing of-the first air stream is by the first fluidized bed and later at least partially through granulating tower；And/or
The flowing of-the second air stream is by second fluidized bed and later at least partially through the first fluidized bed.
Preferably, the calculation by volume at least 10% of the first air stream, more preferably calculate at least 20% by volume, by body
Product calculates at least 30%, calculates at least 40% by volume, calculate at least 50% by volume, calculate at least 60% by volume, by body
Product calculates at least 70%, calculates at least 80% by volume or calculates at least 90% by volume after flowing by the first fluidized bed
Flowing is by granulating tower.Preferably, all granulating is passed through in flowing to the first air stream after flowing by the first fluidized bed
Tower.
In another preferred embodiment, the calculation by volume at least 10% of the second air stream, more preferably calculate by volume
At least 20%, at least 30% is calculated by volume, is calculated at least 40% by volume, is calculated at least 50% by volume, calculates by volume
At least 60%, at least 70% is calculated by volume, calculates at least 80% by volume or calculates at least 90% flowing by volume by the
The first fluidized bed is passed through in two fluid beds and later flowing.Preferably, the second air stream is after flowing by second fluidized bed
All the first fluidized bed is passed through in flowing.
In a preferred embodiment,
- the first air stream is humidified；And/or
Other air stream is humidified.
Preferably, the first air stream and/or other air stream are realized by adding water by adding liquid, preferably
Humidification, it is also possible to be humidified to air stream by adding other liquid.It to only the first air stream or only in addition can
Air stream or two air streams humidified.It can continuously or only be humidified in part-time.Preferably, right
Air stream is humidified the too early drying to avoid particle.Preferably, according to the water content of the particle in the first fluidized bed come
It is humidified.
Additional aspects of the present invention are related to the device for producing porous ammonium nitrate, and described device includes following interaction
Component：
(A) ammoniumnitrate prill equipment, be configured to by ammonium nitrate component formed particle and include granulating tower；With
(B) it is arranged in the first fluidized bed of the bottom end of granulating tower, which is configured to collect and cooling exists
The particle formed in granulating tower.
The component of the device of the invention interacts with each other, that is, by suitable pipeline etc. to ensure the overall work(of device
The mode of energy is connected to each other.It is known to those skilled in the art to this necessary mode.
All preferred embodiments described in association with the method for the present invention are also similarly applicable for the device of the invention
And it is not repeated herein.
Ammoniumnitrate prill equipment includes granulating tower, the free-falling of the granulating tower be highly preferable not more than 40m,
More preferably no more than 35m, no more than 30m, no more than 25m, no more than 20m, no more than 15m, no more than 10m or be not more than
5m。
Preferably, fluid bed is arranged in the bottom end of granulating tower.Preferably, fluid bed is arranged under granulating tower,
So that the particle formed in granulating tower falls under gravity into the first fluidized bed, is collected by the first fluidized bed and become
A part for the fluid bed.Fluid bed may include one or more beds.The area of base of the first fluidized bed and granulating channel
Area of base between difference be preferably not more than 10%, more preferably no more than 9%, no more than 8%, no more than 7%, no
More than 6%, no more than 5%, no more than 4%, no more than 3%, no more than 2% or be not more than 1%.Preferably, the first fluidized bed
Area of base with granulating the area of base in channel it is equal.
In a preferred embodiment, which includes second fluidized bed, which is arranged under the first fluidized bed
It swims and is configured to particle described in predrying.Second fluidized bed may include one or more beds.
In a preferred embodiment, which includes the additional component of at least partly time interior interaction between each other：
(C) the first humidifier is configured to the first air stream of humidification；And/or
(D) the second humidifier is configured to humidify other air stream.
Preferably, humidifier is humidified by the first air stream of adding liquid pair and/or other air stream.It is preferred that
Ground, humidifier are humidified by adding the first air stream of water pair and/or other air stream.It can be continuously or periodical
Implement the humidification to the first air stream and/or other air stream in ground.Preferably, according to the water content of particle in the first fluidized bed
To implement the humidification of the first air stream and/or other air stream.
Preferably, other air stream is so humidified so that the relative humidity of air is (that is, the steaming of other air stream
The percentage of the maximum possible steam content of vapour content and other air stream) in the range of 70% to 100%, more preferably
In the range of 75% to 90%.
In a preferred embodiment, which includes the additional component of at least partly time interior interaction between each other：
(E) discharge member is arranged in the top of granulating tower and is configured to that air is discharged from granulating tower
At least partially；
(F) grade is purified, the downstream of discharge member is arranged in and is configured to arrange impurity with via discharge member
The air separation gone out；With
(G) recirculation hardware is arranged in the downstream of purification grade and is configured to the sky for making to handle in purifying grade
At least part of gas is recycled to the bottom end of granulating tower.
Purification grade is by impurity from the air separation being discharged via discharge member and preferably wet scrubber.It is purifying
After grade, at least part of the air handled in purifying grade is recycled to the bottom of granulating tower via recirculation hardware
End.Preferably, the calculation by volume at least 10% of the air of purification grade processing, more preferably calculate at least 20% by volume,
Calculate at least 30% by volume, calculate at least 40% by volume, calculating at least 50% by volume, calculating at least 60% by volume,
At least 70% is calculated by volume, calculates at least 80% by volume or calculates at least 90% bottom for being recycled to granulating tower by volume
End.Preferably, the bottom end of granulating tower is all recycled in the air of purification grade processing.
Preferably, the cooling air in purifying grade.Preferably, purification grade include detergent and air cooling to close to
The temperature of the cooling limit temperature of existing detergent.Preferably, air cooling is to the cooling limit temperature from existing detergent
Degree deviates no more than 10 DEG C, more preferably no more than 5 DEG C or the temperature no more than 1 DEG C.Preferably, term cooling limit temperature is
Refer to the minimum temperature that may be implemented by direct evaporating-cooling.
Preferably, the device of the invention is used in a manner of corresponding with the method for the present invention.
Description of the drawings
Fig. 1 by Example schematic shows that the present invention's is used to use ammoniumnitrate prill equipment production porous ammonium nitrate
Method, but be not construed as limiting.
Specific implementation mode
Method shown in Fig. 1 includes the nitre for making to enter by one or more granulating nozzles (1) granulating channel (2)
The granulating of acid ammonium solution, wherein granulating channel (2) abuts directly against the first fluidized bed (3) and second fluidized bed (4).It is preferred that
Ground, granulate the free-falling height in channel length make particle have preferably in the temperature of 90 to 120 DEG C of ranges and
Thus enough intensity and dimensional stability are obtained when reaching the first fluidized bed (3).It is optional in order to avoid particle is dried too early
Water spray can be arranged in the upstream of the first fluidized bed (3) in ground.
In the first fluidized bed (3) of adjacent single-stage or multistage, it is preferable that particle is cool below 84 in the first step
DEG C and the predrying in second fluidized bed (4) in the second optional step later.Preferably, predrying is eliminated in subsequent products
To the needs of predrying cylinder in finishing step.
Due to for efficiently granulating, it may be necessary to the air of relative quantities more more than the first fluidized bed (3), so excellent
Other air stream is introduced granulating channel by selection of land.The other air stream may, for example, be, and be purified simultaneously in purification grade (5)
An and part for the cooling used granulating air capacity for being re-circulated into granulating channel (1) later.
Reference numerals list
1 granulating nozzle
2 granulating channels
3 first fluidized beds
4 second fluidized beds
5 purification grades
Claims (14)
1. a kind of method for producing porous ammonium nitrate, wherein the described method comprises the following steps：
(a) make ammonium nitrate component granulating to form particle in the granulating tower of ammoniumnitrate prill equipment, and
(b) particle formed in step (a) is collected in the first fluidized bed (3), and
(c) flowing of the first air stream is made to pass through second fluidized bed by the first fluidized bed (3) and/or the flowing of the second air stream
(4) and/or the granulating tower is passed through in the flowing of other air stream.
2. according to the method described in claim 1, wherein, the particle has when being collected in the first fluidized bed (3)
There is the temperature within the scope of 90 to 120 DEG C.
3. method according to claim 1 or 2, wherein described in being cooled down at least partly in the first fluidized bed (3)
Particle.
4. according to the method described in claim 3, wherein, the particle leaves the first fluidized bed (3) and the particle
Temperature when leaving the first fluidized bed (3) is less than 84 DEG C.
5. according to any method of the preceding claims, wherein the particle leaves the first fluidized bed (3) simultaneously
And it is directed into the second fluidized bed (4) later.
6. according to the method described in claim 5, wherein, in the second fluidized bed (4) at least partly described in predrying
Particle.
7. according to any method of the preceding claims, wherein after flowing by the granulating tower, flowing
At least part by the air stream of the granulating tower is discharged from the granulating tower, is handled in purification grade (5)
And it is recycled to the granulating tower at least partly.
8. according to the method described in claim 7, wherein,
First air stream is humidified；And/or
The other air stream is humidified.
9. according to claim 7 or 8 the methods, wherein
The first air stream flowing is by the first fluidized bed (3) and is flowed at least partly later by described
It is granulated tower；And/or
Second air stream flowing by the second fluidized bed (4) and later at least partly flowing by described the
One fluid bed (3).
10. according to any method of the preceding claims, wherein the ammonium nitrate component, which has, to be calculated by weight
Water content in 1% to 6% range.
11. a kind of device for producing porous ammonium nitrate, described device includes the component of following interaction：
(A) ammoniumnitrate prill equipment, be configured to by ammonium nitrate component formed particle and include granulating tower；With
(B) be arranged in it is described granulating tower bottom end the first fluidized bed, the first fluidized bed be configured to collect and
The cooling particle formed in the granulating tower.
12. according to the devices described in claim 11 comprising second fluidized bed, the second fluidized bed are arranged in described first
The downstream of fluid bed and it is configured to particle described in predrying.
13. device according to claim 11 or 12 comprising what is interacted with each other at least partly in the time is additional
Component：
(C) the first humidifier is configured to the first air stream of humidification；And/or
(D) the second humidifier is configured to humidify other air stream.
14. the device according to any one of claim 11 to 13 comprising at least partly interacted with each other in the time
Additional component：
(E) discharge member is arranged in the top of the granulating tower and is configured to be discharged from the granulating tower empty
At least part of gas；
(F) grade is purified, the downstream of the discharge member is arranged in and is configured to by impurity and via the discharge unit
The air separation of part discharge；With
(G) recirculation hardware is arranged in the downstream of the purification grade and is configured to make to handle in the purification grade
Air at least part be recycled to it is described granulating tower bottom end.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102016200108.6 | 2016-01-07 | ||
| DE102016200108.6A DE102016200108A1 (en) | 2016-01-07 | 2016-01-07 | Process and apparatus for prilling porous ammonium nitrate |
| PCT/EP2017/050110 WO2017118646A1 (en) | 2016-01-07 | 2017-01-04 | Method and apparatus for prilling porous ammonium nitrate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108473330A true CN108473330A (en) | 2018-08-31 |
Family
ID=57758625
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201780005831.XA Pending CN108473330A (en) | 2016-01-07 | 2017-01-04 | Method and apparatus for making porous ammonium nitrate granulate |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP3400200A1 (en) |
| CN (1) | CN108473330A (en) |
| DE (1) | DE102016200108A1 (en) |
| RU (1) | RU2700054C1 (en) |
| WO (1) | WO2017118646A1 (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62282629A (en) * | 1986-05-30 | 1987-12-08 | Okawara Mfg Co Ltd | Granulation apparatus for continuous fluidized bed |
| WO2000074837A1 (en) * | 1999-06-08 | 2000-12-14 | Niro A/S | A process and an apparatus for spray drying |
| CN1741844A (en) * | 2002-11-26 | 2006-03-01 | 奥姆尼亚肥料有限公司 | Apparatus for producing nitrate granules |
| CN1860351A (en) * | 2003-07-31 | 2006-11-08 | 德拉沃有限责任公司 | Calcium carbonate granulation |
| CN201592092U (en) * | 2010-01-19 | 2010-09-29 | 北京德厚朴化工技术有限公司 | Novel two-section fluidized bed |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1109410A (en) * | 1966-04-01 | 1968-04-10 | Toyo Koatsu Ind Inc | Production of granular fertilizer |
| FR1483944A (en) * | 1966-04-28 | 1967-06-09 | Nitrates & Engrais | Advanced process for making granulated ammonium nitrate |
| GB1493612A (en) * | 1974-07-06 | 1977-11-30 | Fisons Ltd | Prilling |
| US4190622A (en) * | 1978-05-04 | 1980-02-26 | Standard Oil Company (Ohio) | Process for prilling urea |
| BG63296B1 (en) * | 1999-07-01 | 2001-09-28 | Христо МИТЕВСКИ | Method and installation for the preparation of porous granulated ammonium nitrate |
| UA98306C2 (en) | 2006-08-02 | 2012-05-10 | Омния Фертилайзер Лимитед | Ammonium nitrate granules and methods for producing thereof |
| RU2411184C1 (en) * | 2009-08-17 | 2011-02-10 | Открытое акционерное общество "Научно-исследовательский и проектный институт азотной промышленности и продуктов органического синтеза" (ОАО "ГИАП") | Method of producing granular ammonium nitrate |
| CN202214298U (en) * | 2011-01-19 | 2012-05-09 | 湖北宜化化工股份有限公司 | Device for lowering temperature of urea particles |
-
2016
- 2016-01-07 DE DE102016200108.6A patent/DE102016200108A1/en not_active Ceased
-
2017
- 2017-01-04 RU RU2018128472A patent/RU2700054C1/en active
- 2017-01-04 CN CN201780005831.XA patent/CN108473330A/en active Pending
- 2017-01-04 WO PCT/EP2017/050110 patent/WO2017118646A1/en active Application Filing
- 2017-01-04 EP EP17700153.4A patent/EP3400200A1/en not_active Withdrawn
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62282629A (en) * | 1986-05-30 | 1987-12-08 | Okawara Mfg Co Ltd | Granulation apparatus for continuous fluidized bed |
| WO2000074837A1 (en) * | 1999-06-08 | 2000-12-14 | Niro A/S | A process and an apparatus for spray drying |
| CN1741844A (en) * | 2002-11-26 | 2006-03-01 | 奥姆尼亚肥料有限公司 | Apparatus for producing nitrate granules |
| CN1860351A (en) * | 2003-07-31 | 2006-11-08 | 德拉沃有限责任公司 | Calcium carbonate granulation |
| CN201592092U (en) * | 2010-01-19 | 2010-09-29 | 北京德厚朴化工技术有限公司 | Novel two-section fluidized bed |
Also Published As
| Publication number | Publication date |
|---|---|
| EP3400200A1 (en) | 2018-11-14 |
| WO2017118646A1 (en) | 2017-07-13 |
| DE102016200108A1 (en) | 2017-07-13 |
| RU2700054C1 (en) | 2019-09-12 |
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