ZA200504302B - Apparatus for producing nitrate granules - Google Patents
Apparatus for producing nitrate granules Download PDFInfo
- Publication number
- ZA200504302B ZA200504302B ZA200504302A ZA200504302A ZA200504302B ZA 200504302 B ZA200504302 B ZA 200504302B ZA 200504302 A ZA200504302 A ZA 200504302A ZA 200504302 A ZA200504302 A ZA 200504302A ZA 200504302 B ZA200504302 B ZA 200504302B
- Authority
- ZA
- South Africa
- Prior art keywords
- fluidised bed
- temperature
- heated
- granules
- air supplied
- Prior art date
Links
- 239000008187 granular material Substances 0.000 title claims description 108
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 title claims description 24
- 229910002651 NO3 Inorganic materials 0.000 title claims description 21
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 claims description 67
- 239000002245 particle Substances 0.000 claims description 46
- YIXJRHPUWRPCBB-UHFFFAOYSA-N magnesium nitrate Chemical compound [Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O YIXJRHPUWRPCBB-UHFFFAOYSA-N 0.000 claims description 40
- 230000001143 conditioned effect Effects 0.000 claims description 27
- 239000007921 spray Substances 0.000 claims description 19
- 238000000034 method Methods 0.000 claims description 18
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 claims description 14
- 238000004519 manufacturing process Methods 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 9
- 230000003750 conditioning effect Effects 0.000 claims description 6
- 238000004891 communication Methods 0.000 claims description 4
- 239000000155 melt Substances 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 2
- 239000003570 air Substances 0.000 description 60
- 238000010899 nucleation Methods 0.000 description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 239000007788 liquid Substances 0.000 description 12
- 239000012467 final product Substances 0.000 description 11
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 10
- 229910017604 nitric acid Inorganic materials 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 6
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 5
- 239000011575 calcium Substances 0.000 description 5
- 238000005469 granulation Methods 0.000 description 5
- 230000003179 granulation Effects 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 235000019738 Limestone Nutrition 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 239000006028 limestone Substances 0.000 description 4
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- 230000004888 barrier function Effects 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 229910000019 calcium carbonate Inorganic materials 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 239000010419 fine particle Substances 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 229910052749 magnesium Inorganic materials 0.000 description 3
- 238000004806 packaging method and process Methods 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 239000012080 ambient air Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 238000010923 batch production Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000012943 hotmelt Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000395 magnesium oxide Substances 0.000 description 2
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 2
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000012790 confirmation Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 235000010333 potassium nitrate Nutrition 0.000 description 1
- 239000004323 potassium nitrate Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
Landscapes
- Fertilizers (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Description
APPARATUS FOR PRODUCING NITRATE GRANULES
THIS invention relates to an apparatus for producing nitrate granules.
International Patent Publication No. WO 01/83374 discloses a method for producing nitrate granules, particularly calcium nitrate granules. A calcium nitrate melt is sprayed into a re-circulating bed of a first fluidised bed granulator, where the re-circulating bed is supplied with air that has been conditioned and heated to a temperature of between 60°C to 100°C.
Calcium nitrate granules formed in the granulator are introduced to a primary cooler in the form of a second fluidised bed where the granules are cooled to from 50°C to 60°C by conditioned air. The granules are sorted in a sorter and then cooled in a secondary cooler to a temperature of less that 40°C, before being bagged. The granules so produced are hard, dry and spherical in shape and do not break down easily during handling.
It is an object of this invention to provide a more compact and improved apparatus for producing nitrate granules.
CONFIRMATION COPY
’ According to a first aspect of the invention there is provided an apparatus : for producing granules, typically nitrate granules, the apparatus including: a first fluidised bed which is supplied with air that has preferably been conditioned to a relative humidity of less than 30% at 40°C and heated to a temperature of 40°C to 100°C, and one or more spray nozzles for spraying a nitrate melt into the first fluidised bed to form nitrate granules; and a second fluidised bed which is in direct communication with the first fluidised bed, for cooling nitrate granules formed in the first bed to a "temperature of 60°C or less, preferably 30°C to 60°C.
Advantageously, the first fluidised bed is divided into a conditioning Zone, and a granulating Zone which includes at least one spray nozzle.
Optionally, the granulating Zone may include a plurality of barriers in the form of vertically orientated planar baffles. Typically, each spray nozzle is located below a baffle.
Advantageously, the spray nozzles are pressurised with compressed air which has been heated to a temperature of 40°C to 70°C.
The spray nozzles typically provide a flat spray pattern which is perpendicular to the flow of air in the first fluidised bed.
The first fluidised bed may have a surface area of 0.8m’ to 2m?, preferably 1m? to 1.6m? typically about 1.4m>.
The conditioning Zone of the first fluidised bed may have a length of 0.5m - 1m, typically about 0.7m, and the granulating Zone of the first fluidised bed may have a length of 1.4m — 2m, typically about 1.7m.
The second fluidised bed may have a surface area of 0.4m” to 1m? preferably 0.6m? — 0.9m?, typically about 0.85m?.
Where the apparatus is for producing calcium nitrate granules, the air supplied to the first fluidised bed is preferably heated to a temperature of 60°C to 100°C, typically 80°C to 100°C, and the air supplied to the second fluidised bed is preferably heated to a temperature of 30°C to 60°C. : In a preferred apparatus for producing calcium nitrate granules the air supplied to the first fluidised bed is heated to a temperature of about 90°C and has a relative humidity of less than 10%.
Where the apparatus is for producing magnesium nitrate granules, the air supplied to the first fluidised bed is preferably heated to a temperature of 50°C to 100°C, typically 50°C to 70°C, and the air supplied to the second fluidised bed is preferably heated to a temperature of 30°C to 50°C.
In a preferred apparatus for producing magnesium nitrate granules the air supplied to the first fluidised bed is heated to a temperature of about 65°C and has a relative humidity of less than 15%.
Where the apparatus is for producing ammonium nitrate/calcium nitrate granules, the air supplied to the first fluidised bed is preferably heated to a temperature of 50°C to 100°C, typically 50°C to 80°C, and the air supplied . to the second fluidised bed is preferably heated to a temperature of 30°C to 50°C.
In a preferred apparatus for producing ammonium nitrate/calcium nitrate granules the air supplied to the first fluidised bed is heated to a temperature of about 70°C and has a relative humidity of less than 15%. © According to a second aspect of the invention there is provided a method for producing nitrate granules, the method including: a) forming nitrate granules in a first fluidised bed which is supplied with air that has preferably been conditioned to a relative humidity of less than 30% at 40°C and heated to a Ce temperature of 40°C to 100°C; and b) passing granules formed in the first fluidised bed directly to a second fluidised bed and cooling the nitrate granules to a temperature of 60°C or less, preferably 30°C to 60°C, in the second fluidised bed.
Granules from the second fluidised bed are typically sent to a sorter from which undersized granules are recycled to the first fluidised bed as seeding particles. Oversized granules from the sorter are first crushed and then also recycled to the first fluidised bed as seeding particles.
The drawing is a schematic representation of an apparatus and process according to the invention for producing nitrate granules.
. This invention relates to an improved apparatus for producing granules, in particular nitrate granules. The apparatus may be used for the formation of any nitrate granules including calcium nitrate granules, magnesium nitrate granules, potassium nitrate granules, other salts of nitrates such as ammonium nitrate (high dense and low dense), mixes of ammonium nitrate and calcium nitrate, and mixes of calcium and magnesium nitrate (or any combination thereof), and water soluble N, P, K granules with or without micro elements.
With reference to the drawing, a granulating apparatus according to the invention is shown generally by the numeral 10. The apparatus 10 includes a first and second fluidised bed 12 and 14 which are in direct communication with one another. “Direct communication” and “directly” means that there is no barrier between the fluidised beds and granules formed in the first fluidised bed 12 flow to the second fluidised bed 14 without the need of a conduit or a conveyor.
The first fluidised bed 12 is housed in a granulator 16 defined by a steel cabinet. The first fluidised bed is located above a horizontally oriented perforated plate 20. A stream of air 18 is pumped into the bottom of the granulator 16, through the perforated plate 20 into the fluidised bed 12 and extracted at a top exit 22, where after the air is passed through a scrubber and released into the atmosphere.
The perforated plate 20 has a surface area of 0.8m? to 2m? preferably 1m? to 1.6m?, typically about 1.4m? and the perforations have a diameter of 1 to 3mm, typically 1.6mm. The first fluidised bed 12 is divided into two zones which are shown as Zone 1 and Zone 2. Zone 1 may be from 0.5m -1m, typically about 0.7m in length and Zone 2 may be from 1.4m - 2m, typically about 1.7m in length. Zone 1 is a conditioning Zone and Zone 2, which includes a plurality of (in this case 6) atomised nozzles 26A-26F is a granulation Zone. The air atomised nozzles 26A-26F are arranged to deliver a nitrate melt in a flat spray pattern perpendicular to the flow of air 18 through the perforated plate 20. ‘Each nozzle 26A-26F is provided with : a valve (not shown) so that the spray of a nozzle can be switched off when a lower out-put is required. Optionally, Zone 2 may include a plurality of barriers, in this case six vertically orientated planar baffles 24A-24F. Each baffle 24A-24F is located above a nozzle 26A-26F. The size of each baffle 24A-24F is selected to ensure constant mass flow per cross-sectional area.
A feed screw 28 is provided for feeding seeding particles into the granulator 16.
The second fluidised bed 14 is housed in a primary cooler 30 defined by a steel cabinet. The second fluidised bed is located above a horizontally oriented perforated plate 31. The perforated plate 31 has a surface area of 0.4m? to 1 m2, preferably 0.6m? to 0.9m? typically about 0.85m”. A stream of air 32 is pumped into the bottom of the primary cooler 30, through the perforated plate 31 and extracted at a top exit 34, whereafter the air is passed through a scrubber and released to the atmosphere. The primary cooler 30 has an inspection window (not shown) through which the granules can be observed. An operator can see from the size of the granules passing through the primary cooler 30 whether the apparatus is operating correctly.
Nitrate granules are removed from the primary cooler 30 by a screw 36.
The granules removed by the screw 36 are sent to a sorter 38. Undersize fine particles 40 from the sorter 38 are recycled via a chute 42 to the feed screw 28 as seeding particles for the first fluidised bed 12. Oversized granules 44 are sent to a crusher 46, crushed, and also recycled via the chute 42 the feed screw 28 as seeding particles. If the recycled particles are not passed through the primary cooler 30 for cooling prior to recycling, a heat imbalance would result in the fluidised bed 12 when the particles are recycled. On-size particles 48 are sent to a secondary cooler 50 where they are cooled to a temperature of approximately 35°C and then sent for packaging 52.
In a first embodiment of the invention, which relates to the production of calcium nitrate granules, ambient air is drawn into a condenser and conditioned to remove the moisture of the air. The conditioned air preferably has a relative humidity of less than 30% at 40°C. The conditioned air is then passed through a steam-heater which heats the air to a temperature of 60°C to 100°C, typically 80°C to 100°C. The conditioned, heated air 18, is then pumped into the granulator 16 to form the first fluidised bed 12. In a preferred embodiment, the heated air 18 is at a temperature of 90°C and has a relative humidity of less than 10%.
A liquid calcium nitrate melt is pumped into the granulator 16 through the nozzles 26. The calcium nitrate melt is produced by reacting a calcium source, for example calcium carbonate with nitric acid. In this embodiment of the invention a 60% nitric acid solution is neutralised with limestone (CaCOs3). A slight excess of nitric acid is used to convert all of the lime.
Undissolved impurities are then removed by filtration and excess nitric acid in the solution is neutralised with limestone. This neutralisation with limestone ensures that the granules are white in colour. It is possible to neutralise the solution with ammonia. However, such a solution is more - difficult to filter which may lead to discolouration of the granules. After neutralisation with limestone, ammonium nitrate is added to provide a 1 mole concentration of ammonium nitrate in solution. The liquid calcium nitrate, which has a concentration of 70% - 80% (m/m), is passed to a concentration unit and is concentrated to 85% - 90% (m/m), with a 10% - 15% free moisture content, using steam at 8 — 10 bar (0,8 — 1 MPA) pressure. The concentrated calcium nitrate melt is then injected into the first fluidised bed 12 of the granulator 16 via spray nozzles 26 at a temperature of 130°C to 140°C. The liquid is forced through the spray nozzles by the action of a pump. In addition to pressurisation by the pump, the liquid is pressurised by compressed air at a pressure of 4-7 bar (0.4- 0.7 MPA). The compressed air is heated at a temperature of from 40°C to 70°C. The heated compressed air retards the crystallisation of the melt which promotes layering of the granules and enhances the formation of the preferred spherical granules of the invention.
Calcium nitrate seeding particles which have a size of approximately 1 to 5 mm are fed into the granulator 16 by the feed screw 28. The seeding particles pass through Zone 1 of the first fluidised bed 12 where they are preconditioned, i.e. heated by the hot air 18 and also dried. This preconditioning step ensures optimal layering on the seeds to ensure hardness, smoothness and sphericity of the granules when entering Zone 2. When the seeding particles enter Zone 2 of the first fluidised bed 12, liquid calcium nitrate sprayed from the nozzles 26 is deposited onto the calcium nitrate seeding particles, to form granules of calcium nitrate. The granules of calcium nitrate are very hygroscopic. The conditioned heated air 18, which has a relative humidity of less than 10% at. 90°C, is very important. If the air 18 was not conditioned, the granules may absorb moisture from the air, become sticky, and agglomerate. In Zone 2, atomised droplets of melt spray contact particles in the fluidised bed and form a layer on the particles, thus causing uniform growth size. The configuration of the baffles 24A-24F can optimize contact between droplets and particles and prevent back flow, which reduces over granulation and oversized particles.
Granules of calcium nitrate formed in the first fluidised bed 12 flow directly into the second adjacent fluidised bed 14 of the primary cooler 30. The primary cooler 30 cools the granules down to below 60°C, typically about 50°C to 60°C, with conditioned air 32 which has been heated to a temperature of 30°C to 40°C. Although, generally, the particles are cooled to between 50°C and 60°C, it is possible to cool the particles to a lower temperature above 30°C because, in the present configuration of the apparatus 10, cool seeding particles return to the feeder 28 and may be heated to the required temperature in the preconditioning Zone 1. If the granules were not passed through the primary cooler 30 for cooling, a heat imbalance would result when particles are recycled. Also, the granules would become too hot, resulting in melting or softening of the granules.
The primary cooler 30 also makes it possible to increase the production capacity of the granulator 16, as the flow rate of hot melt at 130°C to 140°C into the granulator 16 can be increased.
Calcium nitrate granules from the primary cooler 30 are removed by a screw 36. The granules removed by the screw 36 are sorted in the sorter 38 and fine particles are recycled to the feed screw 28 as seeding particles.
Oversized granules are crushed in the crusher 46 and also recycled to the feed screw 28. On-size granules (90% from 2mm to 4 mm) are sent from the sorter 38 to the secondary cooler 50 for cooling and then for packaging.
In a second embodiment of the invention, which relates to the production of magnesium nitrate granules, ambient air is drawn into a condenser and conditioned to remove the moisture of the air. The conditioned air preferably has a relative humidity of less than 30% at 40°C. The conditioned air is then passed through a steam-heater which heats the air to a temperature of 50°C to 100°C, typically 50°C to 70°C. The conditioned, heated air 18, is then pumped into the granulator 16 to form the first fluidised bed 12. In a preferred embodiment, the heated air 18 is at a temperature of 65°C and has a relative humidity of less than 15%.
A liquid magnesium nitrate melt is pumped into the granulator 16 through the nozzles 26. The magnesium nitrate melt is produced by reacting a magnesium source, for example magnesium oxide, with nitric acid. In this embodiment of the invention a 60% nitric acid solution is used. :
Undissolved impurities are removed from the liquid by filtration. The liquid magnesium nitrate, which has a concentration of 45% - 60% (m/m), is passed to a concentration unit and is concentrated to 90% - 95% (m/m), with a free moisture content of 5-10% using steam at 8 — 10 bar (0,8 — 1
MPA) pressure. The concentrated magnesium nitrate melt is then injected into the first fluidised bed 12 of the granulator 16 via spray nozzles 26 at a temperature of 135°C to 145°C. The liquid is forced through the spray nozzles by the action of a pump. In addition to pressurisation by the pump, the liquid is pressurised by compressed air at a pressure of 4-7 bar (0.4- : . 0.7 MPA). The compressed air is heated at a temperature of from 40°C to 70°C. The heated compressed air retards the crystallisation of the melt which promotes layering of the granules and enhances the formation of the preferred spherical granules of the invention.
Magnesium nitrate seeding particles which have a size of approximately 1 to 5 mm are fed into the granulator 16 by the feed screw 28. The seeding particles pass through Zone 1 of the first fluidised bed 12 where they are preconditioned, i.e. heated by the hot air 18 and also dried. This preconditioning step ensures optimal layering on the seeds to ensure hardness, smoothness and sphericity of the granules when entering Zone 2. When the seeding particles enter Zone 2 of the first fluidised bed 12, liquid magnesium nitrate sprayed from the nozzles 26 is deposited onto the magnesium nitrate seeding particles, to form granules of magnesium nitrate. The granules of magnesium nitrate are very hygroscopic. The heated conditioned air 18, which has a relative humidity of less than 15% at 65°C is very important. If the air 18 was not conditioned, the granules may absorb moisture from the air, become sticky, and agglomerate. In Zone 2, atomised droplets of melt spray contact particles in the fluidised bed and form a layer on the particles, thus causing uniform growth size. The configuration of the baffles 24A-24C can optimize the contact between droplets and particles and prevent back flow, which reduces over granulation and oversized particles.
Granules of magnesium nitrate formed in the first fluidised bed 12 flow directly into the second, adjacent fluidised bed 14 of the primary cooler 30.
The primary cooler 30 cools the granules down to below 60°C, typically about 40°C to 50°C, with conditioned air 32 which has been heated to a temperature of 30°C to 40°C. Typically, the air 32 is at a temperature of 40°C and has a relative humidity of 22%. If the granules were not passed through the primary cooler 30 for cooling, a heat imbalance would result when particles are recycled. Also, the granules would become too hot, . resulting in melting or softening of the granules. The primary cooler 30 also makes it possible to increase the production capacity of the granulator 16, as the flow rate of hot melt at 135°C to 145°C into the granulator 16 can be increased.
Magnesium nitrate granules from the primary cooler are removed by the screw 36. The granules removed by the screw 36 are sorted in the sorter 38 and fine particles are recycled to the feed screw 28 as seeding particles.
Oversize granules are crushed in the crusher 46 and also recycled to the feed screw 28. On-size granules (from 2mm to Smm) are sent from the sorter 38 to the secondary cooler 50 for cooling and then packaging.
In a third embodiment of the invention, which relates to the production ammonium nitrate/calcium nitrate granules, a batch process is used to produce a calcium nitrate / ammonium nitrate solution. Various ratios of calcium nitrate and ammonium nitrate may be prepared, with the calcium nitrate for example ranging from 10 — 50 %. The resulting solution is concentrated to remove water and then transferred to storage tanks.
This solution is then concentrated at atmospheric pressure by evaporating water. This may be accomplished by passing steam (8 bar / 0.8 Mpa) coils in a concentrator tank. With reference to the Figure, the concentrated solution (at 82- 90% concentration), with a temperature of 105- 120°C is pumped into the granulator 16 of the apparatus 10 through five nozzles 26 at a rate of 2.0 — 3.0 t/hr. The granulator 16 houses a first fluidised bed having a total fluidising surface area 20 of 1m? with 8% apertures of 1.5mm diameter holes. The air 18 supplied to this fluidised bed has a temperature of 70°C and a relative humidity of less than 15%.
Ammonium Nitrate/Calcium Nitrate granules formed in the granulator 16 flow directly to the primary cooler 30, which houses a second fluidised bed having a total fluidising surface area of 0.65m?. This second fluidised bed has the same apertures as the first fluidised bed. Conditioned air 32 supplied to the second fluidised bed is at a temperature of 40°C and a relative humidity of 21.7% at 40°C.
Granules from the primary cooler 30, with particle sizes ranging from <0.5mm to 10mm, are then sent to a sorter. The granules are sorted using a double deck screen with apertures sized between 2 -5 mm. As with the abovementioned methods, undersized particles are recycled to the first ’ fluidised bed 12 and oversized particles are crushed to a size of below 2.5 mm and also returned to the first fluidised bed, as seeding particles. The final product is passed into the secondary cooler with a total fluidising surface of 0.6m? and the same aperture size as the other fluidised beds.
The final product leaving the secondary cooler has a temperature of 35°C.
The final product is bagged directly into 1 ton (1000 kg) bags. These bags are then transported to a bagging unit where they were bagged into 25kg bags.
The nitrate granules produced by the apparatus and process of the invention are spherical in shape, hard and dry and do not break down easily during handling. Typically the granules have an average hardness of 3.5kg to 4.5kg. The hardness is determined by applying a force measured in kg onto a single granule in the size range 2 - 4 mm, with the hardness result being the force in kilograms that results in the fracture of the granule, i.e. the yield point. The granules also have a low caking tendency, are easily soluble in water and have a uniform particle size distribution.
A main advantage of the apparatus 10 according to the invention is that it is compact. The granulation section of a plant can fit into a space of 80 m2
Although it is compact, the apparatus 10 is capable of very high production rates of 3-5 tons/hr per m? of granulator perforated plate area. Thus, the apparatus shown in the Drawing and described herein can run at a production rate of 8 tons/hr. Although the apparatus can be run at very high production rates, if necessary the production rate can be lowered by switching one or more of the nozzles off during periods of low demand.
Lastly, the whole granulation unit can be operated by one operator.
The invention will now be described in more detail in the following non- limiting Examples.
EXAMPLE 1
A first liquid calcium nitrate solution was produced in a continuous process by neutralising nitric acid with calcium carbonate. 8,5 tons/hour of a 60% nitric acid solution was neutralised with 4,1 tons/hour calcium carbonate. A slight excess of nitric acid was used. The solution was then passed through a filter leaf press to remove insoluble matter and was then neutralised with 0,12 tons/hour ammonia to form ammonium nitrate in the solution. The mole ratio of calcium nitrate to ammonium nitrate in the solution was 5:1. The first solution had the following composition:
Calcium: 14.7% (m/m)
Nitrogen in ammoniacal form: 1.0% (m/m)
Nitrogen in nitrate form: 11.3% (m/m),
The first solution mentioned was then concentrated at atmospheric pressure by evaporating water from the solution using steam at a pressure of 8 bar (0.8 MPA) through steam coils in a concentrator tank, to form a second, concentrated, solution. The second solution had a water content of 13,2% (excluding water of crystallisation) and a composition of:
Calcium: 16.4% (m/m)
Nitrogen in ammoniacal form: 1.2% (m/m)
Nitrogen in nitrate form: 12.8% (m/m)
The second solution reaches a temperature of 139°C during the evaporation step.
With reference to the Figure, the second solution was then pumped into a granulator 16 through four air atomizing nozzles 26 at a rate of 4.5 tons/hour. The granulator 16 was supplied with heated conditioned air 18.
Conditioned air, which had been passed through a radiator-type condenser, had a relative humidity of 28% at 40°C, was heated to a temperature of
90°C to provide heated conditioned air 18 with a relative humidity of less than 10%. The granulator 16 housed a first fluidised bed with a total fluidising surface 20 of 1,00m? with 8% apertures of 1,5mm diameter holes.
Calcium nitrate granules produced in the granulator 16 flowed directly to a primary cooler 30 having a second fluidised bed with a total fluidising surface of 0,65m? and the same apertures as the first fluidised bed. The second fluidised bed was supplied with heated conditioned air from the radiator-type condenser. The conditioned air had a relative humidity of 28% at 40°C, and was heated to a temperature of 40°C.
Granules from the primary cooler 30, with particle sizes ranging from <0.5mm to 10mm, were then sent to a sorter. The granules were sorted using a double deck screen with apertures sized between 2-5 mm.
Undersized particles are recycled to the first fluidised bed and oversized particles are crushed to a size of below 2.5mm and also returned to the first fluidised bed, as seeding particles. The final product was passed into the secondary cooler with a total fiuidising surface of 0.6m? and the same aperture site as the other fluidised beds. The final product leaving the secondary cooler had a temperature of 35°C. The final product was bagged directly into 1 ton (1000 kg) bags. These bags were transported to a bagging unit where they were bagged into 25kg bags. The final product composition was:
Calcium: 18.4% (m/m) :
Nitrogen in ammoniacal form: 1.45% (m/m)
Nitrogen in nitrate form: 14.05% (m/m) 1ton=1x10%kg . EXAMPLE 2
A batch process is used to produce a magnesium nitrate solution. 1.8t of magnesium oxide was reacted with 5.4m> of 60% nitric acid and 7m’ of water. The resulting solution was then passed through a filter leaf press to remove any insoluble matter and then transferred to storage tanks. The ) following composition was obtained:
Magnesium: 5.33% (m/m)
Nitrogen 6.14% (m/m)
This solution was then concentrated at atmospheric pressure by evaporating water. This was accomplished by passing steam (8 bar / 0.8
Mpa) coils in a concentrator tank. With reference to the Figure, the second solution at 95% concentration, with a temperature of 135- 145°C was pumped into the granulator 16 of the apparatus 10 through five nozzles 26 at a rate of 1.5¢/hr. The granulator 16 housed a first fluidised bed having a total fluidising surface area 20 of 1m? with 8% apertures of 1.5mm diameter holes. The air 18 supplied to this fluidised bed had a temperature of 65°C and had a relative humidity of less than 15%.
Magnesium nitrate granules from the granulator 16 flowed directly to the primary cooler 30, which housed a second fluidised bed having a total fluidising surface area of 0.65m?. This second fluidised bed also had the same apertures as the first fluidised bed. Conditioned air 32 supplied to the second fluidised bed was at a temperature of 40°C and had a relative humidity of 21.7% at 40°C.
Granules from the primary cooler 30, with particle sizes ranging from <0.5mm to 10mm, were then sent to the sorter. The granules were sorted using a double deck screen with apertures sized between 2 -5 mm.
Undersized particles are recycled to the first fluidised bed and oversized particles are crushed to a size of below 2.5mm and also returned to the first fluidised bed, as seeding particles. The final product was passed into the secondary cooler with a total fluidising surface of 0.6m? and the same aperture site as the other fluidised beds. The final product leaving the secondary cooler had a temperature of 35°C. The final product was bagged directly into 1 ton (1000 kg) bags. These bags were transported to a bagging unit where they were bagged into 25kg bags. The final product composition was:
Magnesium 9.45% (m/m)
Nitrogen 10.90% (m/m) :
Claims (38)
- ’ 1. An apparatus for producing granules, the apparatus including: a first fluidised bed and one or more spray nozzles for spraying a melt into the first fluidised bed to form granules; and a second fluidised bed which is in direct communication with the first fluidised bed for cooling granules formed in the first bed.
- 2. The apparatus according to claim 1, wherein the first fluidised bed is supplied with air 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.
- 3. The apparatus according to claim 2, wherein the second fluidised bed is arranged to cool the granules to a temperature of 60°C or less.
- 4. The apparatus according to claim 3, wherein the second fluidised bed is arranged to cool the granules to a temperature of 30°C to 60°C.
- 5. The apparatus according to claim 1, wherein the first fluidised bed is divided into a conditioning Zone, and a granulating Zone which includes at least one spray nozzle.
- 6. The apparatus according to claim 1, wherein the spray nozzles are. pressurised with compressed air which has been heated to a temperature of 40°C to 70°C.
- 7. The apparatus according to claim 1, wherein the spray nozzles provide a flat spray pattern which is perpendicular to the flow of air in the first fluidised bed.
- ) 8. The apparatus according to claim 1, wherein the first fluidised bed has a surface area of 0.8m?” to 2m>
- 9. The apparatus according to claim 8, wherein the first fluidised bed has a surface area of 1m? to 1.6m?>
- 10. The apparatus according to claim 9, wherein the first fluidised bed has a surface area of about 1.4m?
- 11. The apparatus according to claim 8, wherein the conditioning Zone of the first fluidised bed has a length of 0.5m - 1m, and the granulating Zone of the first fluidised bed has a length of 1.4m — 2m.
- 12. The apparatus according to claim 11, wherein the conditioning Zone of the first fluidised bed has a length of about 0.7m and the granulating Zone of the first fluidised bed has a length of about1.7m.
- 13. The apparatus according to claim 8, wherein the second fluidised bed has a surface area of 0.4m? to 1m2.
- 14. The apparatus according to claim 13, wherein the second fluidised bed has a surface area of 0.6m? — 0.9m’.
- 15. The apparatus according to claim 14, wherein the second fluidised bed has a surface area of about 0.85m>.
- 16. The apparatus according to claim 1 for producing calcium nitrate granules, wherein the air supplied to the first fluidised bed is heated to a temperature of 60°C to 100°C, and the air supplied to the second fluidised bed is heated to a temperature of 30°C to 60°C.
- 17. The apparatus according to claim 16, wherein the air is supplied to the first fluidised bed is heated to a temperature of 80°C to 100°C.
- 18. The apparatus according to claim 17, wherein the air supplied to the first fluidised bed is heated to a temperature of 90°C and has a relative humidity of less than 10%.
- 19. The apparatus according to claim 1 for producing magnesium nitrate granules, wherein the air supplied to the first fluidised bed is heated to a temperature of 50°C to 100°C, and the air supplied to the second fluidised bed is heated to a temperature of 30°C to 50°C.
- 20. The apparatus according to claim 19, wherein the air supplied to the first fluidised bed is heated to a temperature of 50°C to 70°C.
- 21. The apparatus according to claim 20, wherein the air supplied to the first fluidised bed is heated to a temperature of about 65°C and has a relative humidity of less than 15%.
- 22. The apparatus according to claim 1 for producing ammonium nitrate/calcium nitrate granules, when the air supplied to the first fluidised bed is heated to a temperature of 50°C to 100°C, and the air supplied to the second fluidised bed is heated to a temperature of 30°C to 50°C.
- 23. The apparatus according to claim 22, wherein the air supplied to the : first fluidised bed is heated to a temperature of 50°C and 80°C.
- 24, The apparatus according to claim 23, wherein the air supplied to the first fluidised bed is heated to a temperature of about 70°C and has a relative humidity of less than 15%.
- 25. A method for producing nitrate granules, the method including: a) forming nitrate granules in a first fluidised bed; and b) passing granules formed in the first fluidised bed directly to a second fluidised bed and cooling the nitrate granules to a temperature of 60°C or less, in the second fluidised bed.
- 26. The method according to claim 25, wherein the first fluidised bed is supplied with air 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.
- 27. The method according to claim 26, wherein the granules in the second fluidised bed are cooled to a temperature of 30°C to 60°C.
- 28. The method according to claim 25 for producing calcium nitrate granules, wherein air supplied to the first fluidised bed is heated to a temperature of 60°C to 100°C, and the air supplied to the second fluidised bed is heated to a temperature of 30°C to 60°C.
- 29. The method according to claim 28, wherein the air is supplied to the first fluidised bed is heated to a temperature of 80°C to 100°C.
- 30. The method according to claim 29, wherein the air supplied to the. first fluidised bed is heated to a temperature of 90°C and has a relative humidity of less than 10%.
- 31. The method according to claim 25 for producing magnesium nitrate granules, wherein air supplied to the first fluidised bed is heated to a temperature of 50°C to 100°C, and the air supplied to the second fluidised bed is heated to a temperature of 30°C to 50°C.
- 32. The method according to claim 31, wherein the air supplied to the first fluidised bed is heated to a temperature of 50°C to 70°C.
- 33. The method according to claim 32, wherein the air supplied to the first fluidised bed is heated to a temperature of about 65°C and has a relative humidity of less than 15%.
- 34. The method according to claim 25 for producing ammonium nitrate/calcium nitrate granules, when air supplied to the first fluidised bed is heated to a temperature of 50°C to 100°C, and the air supplied to the second fluidised bed is heated to a temperature of 30°C to 50°C.
- 35. The method according to claim 34, wherein the air supplied to the first fluidised bed is heated to a temperature of 50°C and 80°C.
- 36. The method according to claim 35, wherein the air supplied to the first fluidised bed is heated to a temperature of about 70°C and has a relative humidity of less than 15%.
- 37. The method according to claim 25, wherein granules from ‘the second fluidised bed are sent to a sorter and undersized particles from the sorter are recycled to the first fluidised bed.
- 38. The method according to claim 25, wherein granules from the. second fluidised bed are sent to a crusher from which crushed particles are recycled to the first fluidised bed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ZA200504302A ZA200504302B (en) | 2002-11-26 | 2003-11-24 | Apparatus for producing nitrate granules |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ZA200209601 | 2002-11-26 | ||
| ZA200504302A ZA200504302B (en) | 2002-11-26 | 2003-11-24 | Apparatus for producing nitrate granules |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| ZA200504302B true ZA200504302B (en) | 2007-04-25 |
Family
ID=36093917
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| ZA200504302A ZA200504302B (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) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| UA98306C2 (en) * | 2006-08-02 | 2012-05-10 | Омния Фертилайзер Лимитед | Ammonium nitrate granules and methods for producing 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 |
| CN103480300B (en) * | 2013-09-03 | 2015-07-15 | 安徽淮化股份有限公司 | Ammonium nitrate granulator |
| DE102016200108A1 (en) * | 2016-01-07 | 2017-07-13 | Thyssenkrupp Ag | Process and apparatus for prilling porous ammonium nitrate |
| 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 |
| EP3639916A1 (en) * | 2018-10-18 | 2020-04-22 | Yara International ASA | Method and fluidized bed granulator for the production of granules from a slurry |
| 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 |
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
Also Published As
| Publication number | Publication date |
|---|---|
| CN100364654C (en) | 2008-01-30 |
| CN1741844A (en) | 2006-03-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8394153B2 (en) | Apparatus for producing nitrate granules | |
| EP1280736B1 (en) | Method for producing calcium nitrate granules | |
| AU2001274357A1 (en) | Method for producing calcium nitrate granules | |
| EP1630150B1 (en) | Method for producing a fertilizer with micronutrients | |
| EP2049239B1 (en) | Ammonium nitrate granules | |
| CN102083518B (en) | Method and device for processing of granules | |
| ZA200504302B (en) | Apparatus for producing nitrate granules | |
| EP3790654B1 (en) | Internal cooling system for fluid-bed granulation plants | |
| RU2717788C1 (en) | Obtaining fertilizer granules with given size distribution | |
| EP3315192B1 (en) | Fluidized bed granulation | |
| CN110198778A (en) | Method and apparatus for carrying out recuperation of heat in fluidized bed prilling | |
| EA041687B1 (en) | INTERNAL COOLING SYSTEM FOR FLUID BED GRANULATION PLANTS | |
| CN109422549A (en) | Calcium ammonium nitrate particle preparation system and preparation method | |
| Meessen et al. | Stamicarbon’s Granulation Technology: Diamonds, Pearls and Stamicarbon Granules |