CN1741844A - Apparatus for producing nitrate granules - Google Patents
Apparatus for producing nitrate granules Download PDFInfo
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- CN1741844A CN1741844A CN 200380109201 CN200380109201A CN1741844A CN 1741844 A CN1741844 A CN 1741844A CN 200380109201 CN200380109201 CN 200380109201 CN 200380109201 A CN200380109201 A CN 200380109201A CN 1741844 A CN1741844 A CN 1741844A
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Abstract
This invention relates to an apparatus (10) for producing nitrate granules. The apparatus (10) includes a first fluidised bed (12) which is supplied with air (18) that has been conditioned to a relative humidity of less than 30% at 40(C and heated to a temperature of 40(C to 100(C. One or more spray nozzles (26) are provided for spraying a nitrate melt into the first fluidised bed (12) to form nitrate granules. The apparatus (10) also includes a second fluidised bed (14) which is in direct communication with the first fluidised bed (12). Nitrate granules formed in the first fluidised bed (12) flow directly to the second fluidised bed (14) where they are cooled to a temperature of less than 60(C. The nitrate granules produced by the apparatus (10) and process of the invention are spherical in shape, hard and dry and do not break down easily during handling. A main advantage of the apparatus (10) according to the invention is that it is compact, capable of very high product rates, and can be operated by one operator.
Description
Background of invention
The present invention relates to be used to prepare the equipment of nitrate granules.
The open WO 01/83374 of international monopoly has disclosed a kind of method of preparation nitrate granules, particularly calcium nitrate granules.Calcium nitrate melt is sprayed the circulation fluidized bed that enters first fluidized bed comminutor, and wherein circulation fluidized bed disposes and regulates and be heated to 60 ℃～100 ℃ gas.The calcium nitrate granules that will form in comminutor imports in the primary cooler of the second fluid bed form, and wherein particle is conditioned gas (conditioned air) and is cooled to 50 ℃～60 ℃.Before dress bag, sorting particle in sorter afterwards, is cooled in second cooler then and is lower than 40 ℃, and preparation is hard, dry also spherical in shape like this, is difficult for destroying in disposal process.
The purpose of this invention is to provide the compacter and improved equipment that is used to prepare nitrate granules.
Summary of the invention
A first aspect of the present invention provides a kind of equipment that is used to prepare particle, particularly nitrate granules, and this equipment comprises:
The first fluidized bed, it disposes gas and one or more spray nozzle, and described gas is adjusted to preferably that relative humidity is lower than 30% in the time of 40 ℃, and is heated to 40 ℃～100 ℃; Described spray nozzle is used for nitrate melt is sprayed into the first fluidized bed to form nitrate granules; And
With second fluid bed that the first fluidized bed directly is communicated with, be used for the nitrate granules that the first fluidized bed forms is cooled to 60 ℃ or lower, be preferably 30 ℃～60 ℃.
Advantageously, the first fluidized bed is divided into regulatory region and the granulation zone that comprises at least one spray nozzle.
Randomly, granulation zone can comprise the dividing plate (barrier) of horizontal baffle (flat baffle) form of a large amount of perpendicular positionings.Usually, each spray nozzle all places the baffle plate below.
Advantageously, the spray nozzle pressurized with compressed air that has been heated to 40 ℃～70 ℃.
Spray nozzle provides flat spray pattern (flat spray pattern) usually, and this pattern is vertical with the airflow direction of the first fluidized bed.
The surface area of the first fluidized bed is 0.8m
2～2m
2, be preferably 1m
2～1.6m
2, be generally about 1.4m
2
The length of first fluidized bed regulatory region is 0.5～1m, be generally about 0.7m, and the length of first fluidized bed granulation zone is 1.4m～2m, about usually 1.7m.
The surface area of second fluid bed is 0.4m
2～1m
2, be preferably 0.6m
2～0.9m
2, be generally about 0.85m
2
When equipment was used to prepare calcium nitrate granules, the gas of supplying with the first fluidized bed preferably was heated to 60 ℃～100 ℃, is generally 80 ℃～100 ℃, and the gas of supplying with second fluid bed preferably is heated to 30 ℃～60 ℃.
At the preferred equipment that is used for preparing calcium nitrate granules, the gas of supplying with the first fluidized bed is heated to about 90 ℃, and relative humidity is lower than 10%.
When equipment was used to prepare granules of magnesium nitrate, the gas of supplying with the first fluidized bed preferably was heated to 50 ℃～100 ℃, is generally 50 ℃～70 ℃, and the gas of supplying with second fluid bed preferably is heated to 30 ℃～50 ℃.
At the preferred equipment that is used for preparing granules of magnesium nitrate, the gas of supplying with the first fluidized bed is heated to about 65 ℃, and relative humidity is lower than 15%.
When equipment was used to prepare ammonium nitrate/calcium nitrate granules, the gas of supplying with the first fluidized bed preferably was heated to 50 ℃～100 ℃, is generally 50 ℃～80 ℃, and the gas of supplying with second fluid bed preferably is heated to 30 ℃～50 ℃.
At the preferred equipment that is used for preparing ammonium nitrate/calcium nitrate granules, the gas of supplying with the first fluidized bed is heated to about 70 ℃, and relative humidity is lower than 15%.
A second aspect of the present invention is provided for preparing the method for nitrate granules, and this method comprises:
A) form nitrate granules at the first fluidized bed that is disposing gas, this gas is adjusted to preferably that relative humidity is lower than 30% in the time of 40 ℃, and is heated to 40 ℃～100 ℃; With
B) directly forward the particle that forms in the first fluidized bed to second fluid bed, in second fluid bed, nitrate granules is cooled to 60 ℃ or lower, be preferably 30 ℃～60 ℃.
Usually send into sorter by the particle that second fluid bed comes out, wherein the particle of undersize is circulated to the first fluidized bed as kind of a nuclear particle (seeding particles).Oversize particle is pulverized earlier and is circulated to the first fluidized bed as kind of a nuclear particle then in the sorter.
Description of drawings
This figure is that the present invention is used to prepare the equipment of nitrate granules and the schematic diagram of technology.
The specific embodiment
The present invention relates to be used to prepare the improved equipment of particle, particularly nitrate granules.This equipment can be used for forming the particle of any nitrate, comprise calcium nitrate granules, granules of magnesium nitrate, the potassium nitrate particle, other Nitrates such as ammonium nitrate (high densification and low densification), the mixture of ammonium nitrate and calcium nitrate, the mixture of calcium nitrate and magnesium nitrate (or their any combination), with the water miscible N that contains or do not contain trace element, P, K particle.
With reference to the accompanying drawings, Granulation Equipments of the present invention generally is shown 10.Equipment 10 comprises first and second fluid beds 12 and 14 that are in direct communication with one another." directly connection " and " directly " mean between the fluid bed and do not intercept, and the particle that forms in the first fluidized bed 12 need not conduit or conveyer just can flow in second fluid bed 14.
The first fluidized bed 12 is placed in the comminutor of fixing with the steel cupboard 16.The first fluidized bed is positioned at the top of the orifice plate 20 of horizontal orientation.Air-flow 18 is pumped into the bottom of comminutor 16, enter into fluid bed 12 and discharged by top exit 22 by orifice plate 20, wherein gas is discharged in the atmosphere by after the washer.
The surface area of orifice plate 20 is 0.8m
2～2m
2, be preferably 1m
2～1.6m
2, be generally about 1.4m
2, and the diameter of through hole is 1～3mm, is generally 1.6mm.The first fluidized bed 12 is divided into two districts, is shown 1 district and 2 districts.1 section length can be 0.5m～1m, be generally about 0.7m, and 2 section length can be 1.4m～2m, is generally about 1.7m.1 district is a regulatory region, and comprises that 2 districts of a plurality of (being 6) atomizing spray nozzle 26A-26F are granulation zones here.The distribution of arranging gas atomization spray nozzle 26A-26F is to pass through orifice plate 20 with nitrate melt with the flat spray pattern perpendicular to air-flow 18.Each spray nozzle 26A-26F disposes a valve (not shown) so that can close the injection of spray nozzle when requiring low output.Randomly, 2 districts can comprise a plurality of dividing plates, are the horizontal baffle 24A-24F of 6 perpendicular positionings herein.Each baffle plate 24A-24F places on the spray nozzle 26A-26F.Select the size of each baffle plate 24A-24F constant with the mass flow that guarantees each cross section.
Nitrate granules shifts out primary cooler 30 by screw rod 36.Send into sorter 38 by the particle that screw rod 36 shifts out.The fine particle 40 of the undersize of coming out from sorter 38 is circulated to feed worm 28 as the kind nuclear particle of the first fluidized bed 12 through chute 42.Oversize particle 44 is admitted to pulverizer 46, pulverizes as planting nuclear particle, is circulated to feed worm 28 through chute 42.If before the circulation, the particle of circulation is not through primary cooler 30 coolings, when the particle circulation time will cause thermal unbalance in the first fluidized bed 12.(on-size) particle 48 that size is suitable is admitted to second cooler 50, and wherein they are cooled to about 35 ℃, deliver to packing 52 then.
In the present invention relates to first embodiment of production of calcium nitrate granules,, and regulate to remove airborne moisture with surrounding air suction compressor.The gas of regulating preferably is lower than 30% 40 ℃ of relative humidity.Then, the gas of adjusting is by steam heater, and this heater is heated to 60 ℃～100 ℃ with gas, is generally 80 ℃～100 ℃.Afterwards, the gas 18 through overregulating, heating is pumped into comminutor 16 to constitute the first fluidized bed 12.In preferred embodiments, gas 18 temperature of heating are 90 ℃, and relative humidity is lower than 10%.
Liquid calcium nitrate melt is pumped in the comminutor 16 by spray nozzle 26.Calcium nitrate melt is by calcium source such as calcium carbonate and nitric acid reaction acquisition.In the present embodiment, with lime stone (CaCO
3) in and 60% salpeter solution.Use excessive slightly nitric acid to transform whole lime stones.Remove undissolved impurity then after filtration, and with nitric acid superfluous in the lime stone neutralization solution.In the lime stone and guaranteed that particle is white in color.Solution can neutralize with ammoniacal liquor.But the more sad filter of such solution can cause the particle variable color.With in the lime stone and after, add ammonium nitrate to obtain the ammonium nitrate solution of 1 molar concentration.With concentration be the calcium nitrate liquid of 70%～80% (m/m) by enrichment facility, (steam of 0.8～1MPA) pressure is concentrated into 85%～90% (m/m), has 10%～15% free water content with 8～10bar.Then the calcium nitrate melt that concentrates is passed through spray nozzle 26, at the first fluidized bed 12 of 130 ℃～140 ℃ of injection comminutors 16.Under the effect of pump, force liquid to pass through spray nozzle.Outside pump pressure, liquid is also by pressure 4～7bar (pressurized with compressed air of 0.4～0.7MPA).Heated compressed air under 40 ℃～70 ℃ temperature.The compressed air of heating prevents the crystallization of melt, and it promotes the lamination (layering) of particle, and improves the formation of the preferred spheric granules of the present invention.
The calcium nitrate kind nuclear particle that particle diameter is about 1～5mm is sent into comminutor 16 by feed worm 28.Plant 1 district of nuclear particle through the first fluidized bed 12, wherein they are by preconditioning, promptly by hot gas 18 heating and dry.The preconditioning step guarantees hardness, smoothness and the sphericity of best lamination when guaranteeing that particle enters 2 districts of the first fluidized bed 12 on kind of the nuclear.When kind of nuclear particle entered 2 districts of the first fluidized bed 12, the liquid calcium nitrate that is sprayed by spray nozzle 26 was deposited on the calcium nitrate kind nuclear particle, forms calcium nitrate granules.This calcium nitrate granules hygroscopicity is the height moisture absorption.It is extremely important that relative humidity is lower than the gas 18 of 10% adjusting heating in the time of 90 ℃.If there is not adjustments of gas 18, particle can absorb moisture from gas, and it is also coalescent to become sticky.In 2 districts, the particle in the atomised droplets of the melt spray contact fluid bed, and on particle, form layer, thus obtain the growth size of homogeneous.The structure of dividing plate 24A-24F can be optimized contacting and anti-backflow (back flow) between droplet and the particle, reduces excessive granulation (over granulation) and oversize particle.
The calcium nitrate granules that forms in the first fluidized bed 12 flows directly into second fluid bed 14 of adjacent primary cooler 30.Primary cooler 30 usefulness have been heated to 30 ℃～40 ℃ adjustments of gas 32 particle have been cooled to below 60 ℃, are about 50 ℃～60 ℃ usually.Though normally particle is cooled to 50 ℃～60 ℃, but particle can be cooled to the lower temperature more than 30 ℃, because the kind nuclear particle that cools off in front construction of equipment 10 turns back to feeder 28, and can be heated to desired temperature in preconditioning 1 district.Cool off without primary cooler 30 as fruit granule, the particle circulation time can produce thermal unbalance.In addition, particle can overheat, and causes the fusion of particle or softening.Owing to can increase hot melt enters comminutor 16 in the time of 130 ℃～140 ℃ flow velocity, primary cooler 30 can also increase the output of comminutor 16.
Removed by screw rod 36 by the calcium nitrate granules that primary cooler 30 comes out.The particle of being removed by screw rod 36 carries out sorting in sorter 38, fine particle is circulated to feed worm 28 as kind of a nuclear particle.Oversize particle is pulverized in grinder 46, also is circulated to feed worm 28.(90%, 2～4mm) delivers to second cooler 50 by sorter 38 cools off the particle that size is suitable, then packing.
In second embodiment that the present invention relates to the granules of magnesium nitrate preparation,, and regulate to remove airborne moisture with surrounding air suction compressor.The gas of regulating preferably in the time of 40 ℃ relative humidity be lower than 30%.Then, the gas of adjusting is by steam heater, this heater heated air to 50 ℃～100 ℃.Be generally 50 ℃～70 ℃.Afterwards, will pump into comminutor 16 to constitute the first fluidized bed 12 through gas 18 that overregulate, heating.In preferred embodiments, gas 18 temperature of heating are 65 ℃, and relative humidity is lower than 15%.
The liquid magnesium nitrate melt is pumped in the comminutor 16 by spray nozzle 26.Magnesium nitrate melt is by magnesium source such as magnesia and nitric acid reaction acquisition.Used 60% salpeter solution in the present embodiment.Remove undissolved impurity in the liquid after filtration, the magnesium nitrate liquid that with concentration is 45%～60% (m/m) is by enrichment facility, and (steam of 0.8～1MPA) pressure is concentrated into 85%～90% (m/m), contains 5～10% free water content with 8～10bar.Then the magnesium nitrate melt that concentrates is passed through spray nozzle 26, at the first fluidized bed 12 of 135 ℃～145 ℃ of following injection comminutors 16.Under the effect of pump, force liquid to pass through spray nozzle.Outside pump pressure, liquid is also by pressure 4～7bar (pressurized with compressed air of 0.4～0.7MPA).Heated compressed air under 40 ℃～70 ℃ temperature.The compressed air of heating prevents the crystallization of melt, and it promotes the lamination of particle, and improves the formation of the preferred spheric granules of the present invention.
The magnesium nitrate kind nuclear particle that particle diameter is about 1-5mm is sent into comminutor 16 by feed worm 28.Plant 1 district of nuclear particle through the first fluidized bed 12, wherein they are by preconditioning, promptly by hot gas 18 heating and dry.The preconditioning step guarantees hardness, smoothness and the sphericity of best lamination when guaranteeing that particle enters 2 districts on kind of the nuclear.When kind of nuclear particle entered 2 districts of the first fluidized bed 12, the liquid magnesium nitrate that is sprayed by spray nozzle 26 was deposited on the magnesium nitrate kind nuclear particle, forms granules of magnesium nitrate.This granules of magnesium nitrate hygroscopicity is the height moisture absorption.It is extremely important that relative humidity is lower than the gas 18 of 15% adjusting heating in the time of 65 ℃.If there is not adjustments of gas 18, particle can absorb moisture from gas, and it is also coalescent to become sticky.In 2 districts, the particle in the atomised droplets of the melt spray contact fluid bed, and on particle, form layer, thus obtain the growth size of homogeneous.The structure of dividing plate 24A-24C can be optimized contacting and anti-backflow between droplet and the particle, reduces excessive granulation and oversize particle.
The granules of magnesium nitrate that is formed by the first fluidized bed 12 flows directly into second fluid bed 14 of adjacent primary cooler 30.Primary cooler 30 is cooled to particle below 60 ℃ by being heated to 30 ℃～40 ℃ adjustments of gas 32, is about 40 ℃～50 ℃ usually.Generally, gas 32 temperature are 40 ℃, and relative humidity is 22%.Without primary cooler 30 coolings, at the particle circulation time thermal unbalance can take place as fruit granule.In addition, particle can overheat, and causes particle fusion or softening.Owing to can increase hot melt enters comminutor 16 in the time of 135 ℃～145 ℃ flow velocity, primary cooler 30 can also increase the output of comminutor 16.
Removed by screw rod 36 by the granules of magnesium nitrate that primary cooler 30 comes out.The particle of being removed by screw rod 36 carries out sorting in sorter 38, fine particle is circulated to feed worm 28 as kind of a nuclear particle.Oversize particle is pulverized in grinder 46, also is circulated to feed worm 28.(2～5mm) deliver to second cooler 50 by sorter 38 cools off the particle that size is suitable, then packing.
In the 3rd embodiment that the present invention relates to the ammonium nitrate/calcium nitrate granules preparation, used batch process to prepare calcium nitrate/ammonium nitrate solution.The calcium nitrate and the ammonium nitrate that can prepare different proportion, for example the ratio of calcium nitrate is 10～50%.Resulting solution concentration is removed moisture, deliver to storage tank then.
Under atmospheric pressure concentrate this solution subsequently by water evaporates.This can finish by steam (8bar/0.8Mpa) coil pipe in concentrator tank.With reference to the accompanying drawings, be 105～120 ℃ concentrated solution (concentration is 82～90%) with temperature, by 5 spray nozzles 26, pump in the comminutor 16 of equipment 10 with the speed of 2.0～3.0t/hr.Comminutor 16 is laid total fluidisation surface 20 and is 1m
2, through-hole diameter is the first fluidized bed of 1.5mm, 8% perforate.Gas 18 temperature of supplying with this fluid bed are 70 ℃, and relative humidity is lower than 15%.
The ammonium nitrate/calcium nitrate granules that forms in comminutor 16 flows directly into primary cooler 30, and it is 0.65m that this cooler is laid total fluidisation surface area
2Second fluid bed.Second fluid bed has the perforate identical with the first fluidized bed.Adjustments of gas 32 temperature of supplying with second fluid bed are 40 ℃, and are 21.7% 40 ℃ relative humidity.
Subsequently, the particle size that primary cooler 30 is come out is that the particle of 0.5～10mm is delivered to sorter.Using aperture size is the double-deck screen cloth sorting particle of 2～5mm.According to the method described above, the particle of undersize is circulated to the first fluidized bed 12,2.5mm is following also to be back to the first fluidized bed as kind of nuclear particle and oversize particle is crushed to.。End product is delivered in second cooler, total fluidisation area 0.6m of this cooler
2, aperture size is identical with other fluid bed.The temperature of leaving the end product of second cooler is 35 ℃.End product is bagged directly into the packaging bag of 1 ton (1000kg).Subsequently packaging bag is delivered to the packaging bag that packing device is packaged into 25kg.
The nitrate granules of equipment of the present invention and method preparation is spherical in shape, hard and dry, and is not fragile in disposal.Usually the average hardness of particle is 3.5kg～4.5kg.Be used to be of a size of by the masterpiece with kg metering on the individual particle of 2～4mm and measure hardness, the measurement result of hardness is exactly the kg power that causes particle to destroy, i.e. yield point.In addition, particle caking trend is lower, be easy to be dissolved in water, and particle diameter is evenly distributed.
The main advantage of equipment 10 of the present invention is compact.The granulation zone in workshop is installed in 80m
2The space within.Though compact, equipment 10 can reach very high productivity ratio, the productive rate of every square metre of comminutor orifice plate can reach 3～5 tons/hour.Therefore, diagram and equipment productive rate described herein can move under 8 tons/hour productivity ratio.Though this equipment can move under very high productivity ratio, when requirement is low, can closes one or more spray nozzles if necessary and reduce productivity ratio.At last, whole Granulation Equipments can be by operator's operation.
In following infinite embodiment, the present invention is described in more detail.
Embodiment 1
By with in the calcium carbonate and nitric acid prepare the first liquid calcium nitrate solution with continuity method.With in 4.1 tons/hour the calcium carbonate and 8.5 tons/hour 60% salpeter solution.Use excessive slightly nitric acid.Then with solution by the filter leaf filter press removing insoluble matter, then neutralize in solution, to form ammonium nitrate with 0.12 ton/hour ammoniacal liquor.The mol ratio of calcium nitrate and ammonium nitrate is 5: 1 in the solution.First solution comprises following composition:
Calcium: 14.7% (m/m)
The nitrogen of ammonia form: 1.0% (m/m)
The nitrogen of nitrate form: 11.3% (m/m),
In concentration tank, utilize the water vapour under 8bar (0.8MPA) pressure to pass through steam pipe coil then, under atmospheric pressure concentrate described first solution, to form the second concentrated solution by transpiring moisture.The second solution water content was 13.2% (not comprising the crystallization water), and its composition is:
Calcium: 16.4% (m/m)
The nitrogen of ammonia form: 1.2% (m/m)
The nitrogen of nitrate form: 12.8% (m/m),
Second solution reaches 139 ℃ during evaporation step.
With reference to the accompanying drawings, subsequently, the speed of second solution with 4.5 tons/hour is pumped in the comminutor 16 by four gas atomization spray nozzles 26.Comminutor 16 disposes the adjustments of gas 18 of heating.By the adjustments of gas of radiator-type condenser, be 28% 40 ℃ of relative humidity, be heated to 90 ℃ to provide relative humidity to be lower than the adjustments of gas 18 of 10% heat.Comminutor 16 is laid total fluidisation surface 20 and is 1m
2, through-hole diameter is the first fluidized bed of 1.5mm, 8% perforate.
The calcium nitrate granules of comminutor 16 preparations flows directly into primary cooler 30, and this primary cooler 30 is laid total fluidisation surface and is 0.65m
2, second fluid bed that position of opening is identical with the first fluidized bed.Second fluidized bed configuration has the adjustments of gas of the heat of being come out by the radiator-type condenser.This gas is 28% 40 ℃ relative humidity, and is heated to 40 ℃.
By the particle that primary cooler 30 comes out, particle size is＜0.5mm to 10mm to deliver to sorter subsequently.Particle is the double-deck screen cloth sorting of 2～5mm by aperture size.The particle of undersize is circulated to the first fluidized bed, also returns the first fluidized bed as kind of nuclear particle and oversize particle is crushed to size after less than 2.5mm.End product enters total fluidisation surface and is 0.6m
2, second cooler that position of opening is identical with other fluid bed.The temperature of leaving the end product of second fluid bed is 35 ℃.End product is bagged directly into the packaging bag of 1 ton (1000kg).Subsequently packaging bag is delivered to the packaging bag that packing device is packaged into 25kg.The composition of end product is:
Calcium: 18.4% (m/m)
The nitrogen of ammonia form: 1.45% (m/m)
The nitrogen of nitrate form: 14.05% (m/m)
1 ton=1 * 10
3Kg
Adopted batch process to prepare magnesium nitrate solution.1.8 ton magnesia and 5.4m
3, 60% nitric acid and 7m
3Water reaction, then with the solution of gained by the filter leaf filter press to remove whole insoluble matters, be delivered to storage tank again.Obtain following composition:
Magnesium: 5.33% (m/m)
Nitrogen: 6.14% (m/m)
Under atmospheric pressure concentrate this solution then through water evaporates.This is by finishing through the steam pipe coil in the concentration tank.With reference to the accompanying drawings, be 95% with concentration, temperature is 135～145 ℃ second solution, is pumped into the comminutor 16 of equipment 10 with 1.5 tons/hour speed by 5 spray nozzles 26.Comminutor 16 is laid total fluidisation surface 20 and is 1m
2, through-hole diameter is the first fluidized bed of 1.5mm, 8% perforate.The temperature of supplying with the gas 18 of this fluid bed is 65 ℃, and relative humidity is lower than 15%.
The granules of magnesium nitrate of being come out by comminutor 16 flows directly into primary cooler 30, and it is 0.65m that this cooler is placed in total fluidisation surface area
2Second fluid bed.Second fluid bed has the perforate identical with the first fluidized bed.Adjustments of gas 32 temperature of supplying with second fluid bed are 40 ℃, are 21.7% 40 ℃ relative humidity.
The particle diameter that primary cooler 30 is come out is the particle of＜0.5mm to 10mm, and delivering to sorter, to use the aperture be the double-deck screen cloth sorting particle of 2～5mm.The particle of undersize is circulated to the first fluidized bed, also returns the first fluidized bed as kind of nuclear particle and oversize particle is crushed to size after less than 2.5mm.End product enters total fluidisation surface 0.6m
2, second cooler that position of opening is identical with other fluid bed.The temperature that end product leaves second fluid bed is 35 ℃.End product directly is packaged as the packaging bag of 1 ton (1000kg).Subsequently packaging bag is delivered to the packaging bag that packing device is packaged as 25kg.The composition of end product is:
Magnesium: 9.45% (m/m)
Nitrogen: 10.90% (m/m)
Claims (38)
1. equipment that is used to prepare particle, this equipment comprises:
The first fluidized bed and spray nozzle are used for melt is sprayed the first fluidized bed to form one or more spray nozzles of particle; With
Second fluid bed that directly is communicated with the first fluidized bed, be used for cooling off the particle that forms at the first fluidized bed.
2. the equipment of claim 1, wherein the first fluidized bed is supplied with gas, and the relative humidity that this gas is adjusted under 40 ℃ is lower than 30%, and is heated to 40 ℃～100 ℃.
3. the equipment of claim 2 wherein is provided with second fluid bed and is used for particle is cooled to 60 ℃ or lower.
4. the equipment of claim 3 wherein is provided with second fluid bed and is used for particle is cooled to 30 ℃～60 ℃.
5. the equipment of claim 1, wherein the first fluidized bed is divided into regulatory region and comprises the granulation zone of at least one spray nozzle.
6. the equipment of claim 1, wherein spray nozzle is by the pressurized with compressed air that is heated to 40 ℃～70 ℃.
7. the equipment of claim 1, wherein spray nozzle provides flat spray pattern, and this pattern is vertical with air-flow in the first fluidized bed.
8. the equipment of claim 1, wherein the surface area of the first fluidized bed is 0.8m
2～2m
2
9. the equipment of claim 8, wherein the surface area of the first fluidized bed is 1m
2～1.6m
2
10. the equipment of claim 9, wherein the surface area of the first fluidized bed is about 1.4m
2
11. the equipment of claim 8, wherein the length of the regulatory region of the first fluidized bed is 0.5m～1m, and the length of the granulation zone of the first fluidized bed is 1.4m～2m.
12. the equipment of claim 11, wherein the length of the regulatory region of the first fluidized bed is about 0.7m, and the length of the granulation zone of the first fluidized bed is about 1.7m.
13. the equipment of claim 8, wherein the surface area of second fluid bed is about 0.4m
2～1m
2
14. the equipment of claim 13, wherein the surface area of second fluid bed is about 0.6m
2～0.9m
2
15. the equipment of claim 14, wherein the surface area of second fluid bed is about 0.85m
2
16. the equipment that is used to prepare calcium nitrate granules of claim 1, the gas of wherein supplying with the first fluidized bed is heated to 60 ℃～100 ℃, and the gas of supplying with second fluid bed is heated to 30 ℃～60 ℃.
17. the equipment of claim 16, the gas of wherein supplying with the first fluidized bed is heated to 80 ℃～100 ℃.
18. the equipment of claim 17, the gas of wherein supplying with the first fluidized bed is heated to 90 ℃, and it has and is lower than 10% relative humidity.
19. the equipment that is used to prepare granules of magnesium nitrate of claim 1, the gas of wherein supplying with the first fluidized bed is heated to 50 ℃～100 ℃, and the gas of supplying with second fluid bed is heated to 30 ℃～50 ℃.
20. the equipment of claim 19, the gas of wherein supplying with the first fluidized bed is heated to 50 ℃～70 ℃.
21. the equipment of claim 20, the gas of wherein supplying with the first fluidized bed is heated to about 65 ℃, and it has and is lower than 15% relative humidity.
22. the equipment that is used to prepare ammonium nitrate/calcium nitrate granules of claim 1, the gas of wherein supplying with the first fluidized bed is heated to 50 ℃～100 ℃, and the gas of supplying with second fluid bed is heated to 30 ℃～50 ℃.
23. the equipment of claim 22, the gas of wherein supplying with the first fluidized bed is heated to 50 ℃～80 ℃.
24. the equipment of claim 23, the gas of wherein supplying with the first fluidized bed is heated to about 70 ℃, and it has and is lower than 15% relative humidity.
25. a method for preparing nitrate granules, this method comprises:
A) in the first fluidized bed, form nitrate granules; With
B) particle that will form in the first fluidized bed directly is sent to second fluid bed, and in second fluid bed nitrate granules is cooled to 60 ℃ or lower.
26. the method for claim 25, wherein the first fluidized bed is supplied with has gas, this gas to be adjusted to that relative humidity is lower than 30% in the time of 40 ℃, and is heated to 40 ℃～100 ℃.
27. the method for claim 26, wherein the particle in second fluid bed is cooled to 30 ℃～60 ℃.
28. the method that is used to prepare calcium nitrate granules of claim 25, the gas of wherein supplying with the first fluidized bed is heated to 60 ℃～100 ℃, and the gas of supplying with second fluid bed is heated to 30 ℃～60 ℃.
29. the method for claim 28, the gas of wherein supplying with the first fluidized bed is heated to 80 ℃～100 ℃.
30. the method for claim 29, the gas of wherein supplying with the first fluidized bed is heated to 90 ℃, and it has and is lower than 10% relative humidity.
31. the method that is used to prepare granules of magnesium nitrate of claim 25, the gas of wherein supplying with the first fluidized bed is heated to 50 ℃～100 ℃, and the gas of supplying with second fluid bed is heated to 30 ℃～50 ℃.
32. the method for claim 31, the gas of wherein supplying with the first fluidized bed is heated to 50 ℃～70 ℃.
33. the method for claim 32, the gas of wherein supplying with the first fluidized bed is heated to about 65 ℃, and it has and is lower than 15% relative humidity.
34. the method that is used to prepare ammonium nitrate/calcium nitrate granules of claim 25, when the gas of supplying with the first fluidized bed was heated to 50 ℃～100 ℃, the gas of supplying with second fluid bed was heated to 30 ℃～50 ℃.
35. the method for claim 34, the gas of wherein supplying with the first fluidized bed is heated to 50 ℃～80 ℃.
36. the method for claim 35, the gas of wherein supplying with the first fluidized bed is heated to about 70 ℃, and it has and is lower than 15% relative humidity.
37. the method for claim 25 wherein will be delivered to sorter from the particle of second fluid bed, and will be circulated to the first fluidized bed by the undersized grain that sorter comes out.
38. the method for claim 25 wherein will be delivered to pulverizer from the particle of second fluid bed, will be circulated to the first fluidized bed by the broken particle that this pulverizer comes out.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ZA2002/9601 | 2002-11-26 | ||
| ZA200209601 | 2002-11-26 | ||
| ZA2003/2874 | 2003-04-11 |
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| Publication Number | Publication Date |
|---|---|
| CN1741844A true CN1741844A (en) | 2006-03-01 |
| CN100364654C CN100364654C (en) | 2008-01-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2003801092015A Expired - Fee Related CN100364654C (en) | 2002-11-26 | 2003-11-24 | Apparatus for producing nitrate granules |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN100364654C (en) |
| ZA (1) | ZA200504302B (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102320885A (en) * | 2011-08-17 | 2012-01-18 | 交城县金兰化工有限公司 | Spherical magnesium nitrate and tower granulation method thereof |
| CN103252195A (en) * | 2012-02-17 | 2013-08-21 | 北京丰汉工程咨询有限公司 | Fluidized bed granulation system |
| CN101522295B (en) * | 2006-08-02 | 2013-10-02 | 奥姆尼亚肥料有限公司 | Ammonium nitrate granules |
| CN103480300A (en) * | 2013-09-03 | 2014-01-01 | 安徽淮化股份有限公司 | Ammonium nitrate granulator |
| CN106179113A (en) * | 2016-01-28 | 2016-12-07 | 无锡市阳光干燥设备有限公司 | A kind of cryogenic sterile fluidisation continuous granulation drying machine |
| CN107381599A (en) * | 2017-09-08 | 2017-11-24 | 天津华景化工新技术开发有限公司 | A kind of bulky grain ammonium nitrate products and preparation method thereof |
| CN107475532A (en) * | 2017-07-07 | 2017-12-15 | 江苏海光金属有限公司 | Fountain aluminium lime-ash nitrogen removing device |
| CN108473330A (en) * | 2016-01-07 | 2018-08-31 | 蒂森克虏伯工业解决方案股份公司 | Method and apparatus for making porous ammonium nitrate granulate |
| CN112058178A (en) * | 2020-07-30 | 2020-12-11 | 广东三向智能科技股份有限公司 | Raw material processing equipment based on teaching and practical training |
| CN112839732A (en) * | 2018-10-18 | 2021-05-25 | 亚拉国际有限公司 | Method for producing granules from a slurry and fluid bed granulator |
| RU2800070C2 (en) * | 2018-10-18 | 2023-07-17 | Яра Интернейшнл Аса | Method and granulator with fluidized bed for obtaining granules from suspension |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NO312712B1 (en) * | 1999-12-15 | 2002-06-24 | Norsk Hydro As | A sorting fluid bed granulator and method of fluid bed granulation |
| DE10016905B4 (en) * | 2000-04-05 | 2005-06-16 | Braunschweigische Maschinenbauanstalt Ag | Process for the preparation of a gelling assistant |
| AR028064A1 (en) * | 2000-05-03 | 2003-04-23 | Omnia Fertilizer Ltd | METHOD TO PRODUCE CALCIUM NITRATE GRANULES |
-
2003
- 2003-11-24 ZA ZA200504302A patent/ZA200504302B/en unknown
- 2003-11-24 CN CNB2003801092015A patent/CN100364654C/en not_active Expired - Fee Related
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101522295B (en) * | 2006-08-02 | 2013-10-02 | 奥姆尼亚肥料有限公司 | Ammonium nitrate granules |
| CN102320885A (en) * | 2011-08-17 | 2012-01-18 | 交城县金兰化工有限公司 | Spherical magnesium nitrate and tower granulation method thereof |
| CN102320885B (en) * | 2011-08-17 | 2013-07-31 | 交城县金兰化工有限公司 | Spherical magnesium nitrate and tower granulation method thereof |
| CN103252195A (en) * | 2012-02-17 | 2013-08-21 | 北京丰汉工程咨询有限公司 | Fluidized bed granulation system |
| CN103480300A (en) * | 2013-09-03 | 2014-01-01 | 安徽淮化股份有限公司 | Ammonium nitrate granulator |
| CN103480300B (en) * | 2013-09-03 | 2015-07-15 | 安徽淮化股份有限公司 | Ammonium nitrate granulator |
| CN108473330A (en) * | 2016-01-07 | 2018-08-31 | 蒂森克虏伯工业解决方案股份公司 | Method and apparatus for making porous ammonium nitrate granulate |
| CN106179113A (en) * | 2016-01-28 | 2016-12-07 | 无锡市阳光干燥设备有限公司 | A kind of cryogenic sterile fluidisation continuous granulation drying machine |
| CN107475532A (en) * | 2017-07-07 | 2017-12-15 | 江苏海光金属有限公司 | Fountain aluminium lime-ash nitrogen removing device |
| CN107381599A (en) * | 2017-09-08 | 2017-11-24 | 天津华景化工新技术开发有限公司 | A kind of bulky grain ammonium nitrate products and preparation method thereof |
| CN112839732A (en) * | 2018-10-18 | 2021-05-25 | 亚拉国际有限公司 | Method for producing granules from a slurry and fluid bed granulator |
| RU2800070C2 (en) * | 2018-10-18 | 2023-07-17 | Яра Интернейшнл Аса | Method and granulator with fluidized bed for obtaining granules from suspension |
| CN112058178A (en) * | 2020-07-30 | 2020-12-11 | 广东三向智能科技股份有限公司 | Raw material processing equipment based on teaching and practical training |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100364654C (en) | 2008-01-30 |
| ZA200504302B (en) | 2007-04-25 |
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