PROCESS FOR PREPARING AMMONIUMNITRATE-CONTAINING GRANULES OF HIGH BULK DENSITY

Abstract: High dense NH₄NO₃-containing granules are pre­ pared by spraying an NH₄NO₃-containing liquid including ≦ 15% wt water and 0,3-0,50% wt Ca(NO₃)₂, having a temperture ≧ 5°C above its crystallization point into a fluidized bed of NH₄NO₃ particles having a temperature of between 95 and 145°C, with the aid of a current of air having the same or a slightly lower temperature than that of the liquid, at such a rate that the air: liquid mass ratio amounts to 1 : 1 to 1 : 4. The product obtained has a very high bulk density and an extremely low water content.

Description: PROCESS FOR PREPARING AMMONIUMMITRATE-CONtAINING GRANULES OF HIGH BULK DENSITY The invention relates to a process for preparing ammoniumnitrate-containing granules of high bulk density, on the basis of a liquid composition containing calcium nitrate and ammonium nitrate. A process of this kind is described in, for example, British Patent Specification No. 1,136,019, according to which process a substantially water-free ammoniumnitrate melt containing magnesiumnitrate and/or calciumnitrate is granulated by prilling. A disadvantage of this process is that a prilling process imposes rather narrow limits on the product granule size. For preparing granules with a diameter of, say, more than 3 mm, for example, a very high prilling tower or extremely forced cooling of the falling drops is required. Since there is a growing demand for larger-diameter granules (especially for use in so-called bulk-blends) and since there is a need for processes which are highly flexible with respect to product granule size, say up to 6 mm, a prilling method is not very attractive. Another disadvantage of the abovementioned process is that, in order to obtain granules of high bulk density, a substantially water-free melt has to be used. A process by which a product of larger granule diameter can be obtained is known from US Patent Specification No. 4.316.736. According to this process an ammoniumnitrate-containing solution, which includes at most 20% wt., in particular 5-10X wt., water and 0.5-3% wt. magnesiumnitrate, is sprayed onto a fluidized bed of ammoniumnitrate seed particles having a temperature of between 120 and 135"C, after which the granules discharged from the bed are cooled at such a slow rate that they remain virtually homogeneous in temperature in the range between 70 and 5O0C. A disadvantage of this known process is that the finished product has a rather high water content (about 0.3X wit.). When stored, granules with such a high water content show increased caking tendency and poorer hygroscopic behaviour, which in general makes it necessary to apply rather a large quantity of coating agent to them. In addition, such a product can hardly be stored or shipped in bulk, and cloyed bags should be used instead. Another disadvantage of this process is that in the 70 + 500C range the granules need to be cooled slowly, which means that for a given quantity of product a relatively big cooling unit is required. In addition, application of this cooling method implies the necessity of using more than one cooling stage, in general three discrete stages (one for cooling down to 700C, one fdr the 70 + 50 C range, one for the range below 500C). Finally, this process has the disadvantage that its flexibility, for example in terms of the quantity of recycle material, and hence of production capacity, is limited by the narrow temperature range mandatory for the bed of seed particles. According to another known process (see British Patent Specification No. 990,478) an ammoniumnitrate solution or melt, which may or may not contain calciumnitrate, magnesiumnitrate or aluminiumnitrate, is granulated by the so-called cold spherodizer process. In dependence on the water content of the ammoniumnitrate feed, this results in a more or less porous product. For instance, if the product is made from a 99.82 melt, at a bed temperature of 1080C, its bulk density will be about 910 gil and if it is made from a 95% solution, at a bed temperature of 106"C, its bulk density will be about 835 g/l. A disadvantage of this known process is that the bulk density of the product is rather low, especially if an ammoniumnitrate solution is started from. The invention provides a process which rules out the abovementioned disadvantages completely or almost completely, and which yields a granular product combining a very high bulk density ()950 g/l) with an extremely low water content ( < 0.1 % wt., in particular < 0.05 Z wt.). According to the invention, this is achieved in that an ammoniumnitrate-containing liquid composition, including at most 15 % wt. water and 0.3 - 3.5 % wt. calciumnitrate, calculated relative to tae quantity of ammoniumnitrate, and having a temperature at least 50C above its crystallization point, is sprayed into a fluidized bed of ammoniumnitrate-containing seed particles having a temperature of between 95 and 145"C, with the aid of a current of air having a temperature about equal to or slightly lower than that of the liquid composition, at such a rate that the air to liquid composition mass ratio amounts to I 1 to 1 : 4, and the granules formed are discharged from the bed. According to the Invention a liquid ammoniumnitrate-containing composition is used which may include up to 15 % wt. water. If a composition is used which has a high water content, i.e. which contains, say, more than 5 % wt., in particular 5-lO % wt., water, a bed temperature of more than 1150C, more in particular 120-140 C, is applied. An advantage of this is that a feed of lower concentration can be used, which means a saving in cost of evaporation. If a feed with a low water content, for example lower than 3% wt., in particular lower than 1 % wt., is used, the bed temperature applied preferably is between 95 and 1150C, more in particular between 100 and l100C. An advantage of this mode of realization is that the fluidization gas need hardly be pre-heated, if at all. The amount of calciumnitrate in the liquid composition is preferably 0.5 - 1 % wt., calculated relative to the quantity of ammoniumnitrate. The calciumnitrate can be added as such to an ammoniumnitrate-containing melt or solution, but it is also possible to add calcium oxide, or a calcium salt reacting in situ while forming calciumnitrate, to the nitric acid started from or to the ammoniumnitrate resulting after ammoniation and, possibly, evaporation. The composition should have a temperature at least 50C higher than its crystallization temperature and generally lower than its boiling temperature at atmospheric pressure. For safety reasons, temperatures over 1800C are avoided. The spraying of the composition is effected in known manner, for example in a two-phase spray. By preference, the composition is sprayed from the bottom upward into the bed. The gas is passed through the bed of seeds from bottom to top, in general at a superficial velocity about twice the minimum fluidization velocity. By 'minimum fluidization velocity' is meant the minimum velocity which is sufficient to support the weight of the seeds in the bed (in the case of NH4N03 with a mean particle size of 3 mm, it is about 1.2 m/sec). The temperature of the fluidization gas (air) may vary, for example between 20 and 1700C. In general, such a temperature is applied that, in combination with the temperature of the seeds, the desired bed temperature is achieved. The seeds used are preferably the oversize and undersize fractions resulting after screening of the granules discharged from the bed, the oversize fraction being first crushed. If desired, part of the product fraction can also be returned after having.been crushed. The amount of material returned may vary, and is preferably such that the weight ratio of material returned to liquid composition fed in is 1 : 1 to 1 2. The diameter of the seeds introduced into the bed is preferably between 0.75 and 2,0 mm. The height of the bed is in general 0.5 to 1.0 m. If a high bed temperature is desired, the fluidization gas can be preheated, and the material returned will not in general be cooled. The fluidization gas can be preheated by heat exchange with the product granules after screening. In order to achieve a low temperature, cold fluidization gas can be used and/or the material returned can be cooled. It is possible to screen the granules discharged from the bed at once, and next cool the product fraction, but it is also possible to cool first and screen next, and cool the product fraction further if desired. Since fast cooling of the granules has proved to result in a product of increased bulk density, it is preferred to use a fast cooling procedure, in particular fluid-bed cooling. The advantage of this is that cooling equipment of relatively small size is sufficient for the purpose. In het fluid bed cooler(s), by preference conditioned air of ambient or slightly higher temperature is used, while further it is possible to make advantageous use of the heated air issuing from the cooler, as fluidization air for the bed of particles. The air issuing from the fluidized bed can be purified of dust particles in a known manner, for instance by washing with water or with a dilute, ammoniumnitrate-containing solution. The product granules resulting after screening and cooling C?.n be further processed in a known manner; they can, for example, be provided with a coating agent. Drying is not necessary for the product obtained by the present process. It may be of importance, though, to subject the granules to a regular rolling motion in a rotary drum, optionally before cooling, to effect a further increase in bulk density. Although the present process is of special importance for the preparation of ammoniumnitrate granules, it can also be used for the preparation of granules which, besides ammoniumnitrate and calciumnitrate, contain other components, such as fillers (marlstone or dolomite), trace elements, agrochemicÅals (herbicides etc.) and fertilizer salts. It is particularly advantageous to incorporate a thermal stabilizer for ammoniumnitrate in the liquid composition to be sprayed, for example a finely divided, insoluble, inert material containing silica, as described in the non-prepublished Dutch Patent Application 81.02958. The invention will be elucidated in the following examples. Example 1 To a circular fluid-bed granulator (diameter 45 cm) provided with a perforated bottom and containing a bed of NH4N03 seed particles (mean diameter 3.05 mm; height of the bed 40 cm), a liquid NH4N03 composition was continuously supplied with the aid of a strong current of air, via a two-phase sprayer, and sprayed laterally into the bed. The composition contained 0.31 % wt. calciumnitrate, calculated as calcium oxide relative to the quantity of ammoniumnitrate. The bed (temp. 1280 C) was fluidized with the aid of an upward current of air supplied through the bottom plate. Via an overflow, granules were continuously discharged to a screen, where they were separated into a fine fraction ( < 2 mm), a product fraction (2-4 mm) and a coarse fraction () 4 mm). The latter fraction was crushed on crusher rollers, and continuously returned to the bed together with the fine fraction. The product fraction was quickly cooled to about 35"C in a fluid-bed cooler. Part of this product was five times heated and cooled between 15 and 50 C. The process conditions used and the properties of the product obtained and of the product after 5 cycles are summarized in the table below. Examples 2 through 10 In the same manner as in Example 1, liquid NH4N03 compositions containing calciumnitrate were granulated in a fluidized bed of NH4N03 seed particles. In Examples 4, 5 and 6, an amount of finely divided calciumcarbonate had been added to the NH4N03 melt. The results are, again, summarized in the table below. Example 1 2 3 4 5 6 7 8 9 10 Process conditions bed temp., C 128 128 135 105 125 115 110 130 105 120 H2O content of NH4NO3, % wt. 4.90 4.90 4.90 0.53 0.53 0.82 0.75 0.75 0.58 0.58 temp. of NH4NO3, C 147 147 147 171 168 171 171 173 171 169 quantity of NH4NO3, kg/h 97 97 97 94 94 94 92 92 92 92 temp. of spraying air, C 160 160 160 159 153 158 161 161 159 158 quantity of spraying air, 83 65 83 78 47 76 75 75 81 81 kg/h temp. of fluidization air, 143 148 148 104 145 117 121 152 100 123 C quantity of fluidization 1180 1180 1180 1180 1180 1180 1180 1180 1180 1180 air, kg/h velocity of fluidization 2.59 1.59 2.63 2.44 2.57 2.51 2.49 2.60 2.44 2.53 air, m/sec quantity of Ca(NO3)2, % wt. 0.31 0.34 0.38 - - - 0.29 0.28 0.34 0.35 CaO quantity of CaCO3 - - - 2 2 2 - - - Product quality uitrogen content, % wt. 34.20 34.45 34.65 33.80 33.85 34.40 34.50 34.40 34.25 34.45 H2O content, % wt. 0.04 0.05 0.04 0.06 0.09 0.08 0.08 0.03 0.07 0.05 bulk density, g/l 960 920 935 955 955 970 945 990 945 980 rolling capacity, 95 95 95 28 25 70 80 50 75 65 % round impact resistance, % 100 100 100 100 100 100 100 100 100 100 crushing strength, bar 35 35 35 46 35 60 40 45 40 45 oil-absorption capacity, 0.50 0.40 0.40 0.25 0.70 0.20 0.30 0.45 0.20 0.35 % wt. D50, mm 3.05 2.55 2.80 2.65 1.90 2.85 2.20 2.45 3.10 2.15 mercury penetration, cm3/g 0.030 0.039 0.032 0.045 0.049 0.026 0.039 0.032 - Product after 5 cylcles crushing strength, bar 10 10 10 10 5 15 15 20 20 20 oil-absorption capacity, 4.90 5.20 6.00 4.10 7.0 4.40 7.50 4.60 4.10 6.10 % wt. volume increase, % 25 25 25 25 25 26 33 21 30 26

Claims: CLAIMS 1. Process for preparing ammoniumnitrate-containing granules of high bulk density, on the basis of a liquid composition containing calcium nitrate and ammoniumnitrate, this process being charac terized in that an ammoniumnitrate-containing liquid composition, including at most 15 % wt. water and 0.3 - 3.5 % wt. calcium nitrate, calculated relative to the quantity of ammoniumnitrate, and having a temparature at least 50C above its crystallization point, is sprayed into a fluidized bed of ammoniumnitrate-containing seed particles having a temperature of between 95 and 1450C, with the aid of a current of air having a temperature about equal to or slightly lower than that of the liquid composition, at such a rate that the air-to-liquid composition mass ratio amounts to 1 : 1 to 1 : 4, and the granules formed are discharged from the bed. 2. Process according to claim 1, characterized in that an ammoniumnitrate-containing melt with at most 3 % wt. water is sprayed into a bed of seed particles having a temperature of between 95 and l150C. 3. Process according to claim 2, characterized in that an ammoniumnitrate-containing melt with at most 1 % wt. water is sprayed into a bed of seed particles having a temperature of between 100 and 110 C. 4. Process according to claim 1; characterized in that an ammoniumnitrate-containing solution with more than 5 % wt. water is sprayed into a bed of seed particles having a temperature of over 1150C. 5. Process according to claim 4, characterized in that an ammoniumnitrate-containing solution with 5-10 % wt. water is sprayed into a bed of seed particles having a temperature of 120-140 C. 6. Process according to any one of the claims 1-5, characterized in that an ammoniumnitrate-containing liquid composition is used which includes 0.5 - 1.0 % wt. calcium nitrate, calculated relative to the quantity of ammoniumnitrate. 7. Process according to any one of the claims 1-6, characterized in that the fluidization gas used is air, flowing through the bed from bottom to top at a superficial velocity about twice the minimum fluidization velocity. 8. Process according to any one of the claims 1-7, characterized in that the granules discharged from the bed are rapidly cooled, at once or after screening, by means of one or more fluid-bed coolers. 9. Process according to claim 8, characterized in that at least part of the gas from the fluid-bed cooler(s) is used as fluidization gas for the bed of seed particles. 10. Process according to any one of the claims 1-9, characterized in that the ammoniumnitrate-containing liquid includes one or more fillers, trace elements, agrochemicals, thermal stabilizers and/or fertilizer salts.

Inventors: HOEK, CORNELIS, MUTSERS, STANISLAUS MARTINUS PETRUS, WAGEMANS, GERARDUS MATHIAS CORNELIS
Applicants: UNIE VAN KUNSTMESTFABRIEKEN B.V.
Application year: 1982
Main classification: C05C1
IPC codes: C05C1