Fluidized Bed Granulation of Rehydratable Alumina

This invention relates to the granulation of rehydratable alumina in small particle sizes.

Alumina, as a chemical compound by itself or in combination with one or more other refractory inorganic oxides, is widely employed in industrial process applications as a catalyst, as a catalyst base, as a support or chemical carrier material, or as an adsorbent. The granulation of alumina powders to form granular aluminas is one of the crucial tasks in preparing aIumina for one of the various types of industrial process applications. Granulation improves the bulk properties of the alumina in particulate form. The substitution of granular aluminas for fine powders can create beneficial effects including improved pore structure, improved flow properties, reduced dusting loss, and improved product appearance. The beneficiation of granulation can be accomplished by techniques classified into several categories according to the principal method used for the beneficiation including, e.g., agitation in a tumbling drum, pressure, thermal, spray in a fluidized bed, and agglomeration from liquids by an oil drop method. As each method is different in technique of beneficiation, the resulting granular product also is characteristically different in properties.

In the granulation of powdered materials, binding is partially achieved by liquid-solid capillary energy reduction. In both alumina granulation and alumina hydrate granulation, water sometimes has been used as the liquid binder.

Alumina has numerous crystalline forms. Strictly speaking, so-called "activated" alumina includes eta, chi, gamma, and rho-alumina, of which the specific surfaces are in the range of about 100-400 m.sup.2 /g. These activated alumina forms are important substrates for the various industrial process applications. Activated alumina generally is produced by dehydration reactions from alumina hydrate such as gibbsite, bayerite, boehmite, and an amorphous gel. The alumina hydrates can be converted into various forms of alumina depending on dehydration conditions.

It is an object of the present invention to prepare small granules of activated alumina.

It is another object of the present invention to prepare activated alumina having a high surface area and small granular particle size.

It is yet another object of the present invention to prepare an activated eta-alumina or gamma-alumina having a high surface area in a small granular particle size.

The process of the present invention for preparing granules of alumina includes pretreating an alumina powder by admixing with cold water in a mixer at a temperature below room temperature, e.g., such as below about 20.degree. C., to form a pretreated alumina having a pore volume saturated with water and further having a surface area of gel structure, and agglomerating the pretreated alumina in a fluidized bed to form granules sized in the range of about 1-3 mm. The process is particularly suited to producing activated alumina in macroporous granules. The process in one aspect further includes a cold hopper for cooling alumina powder prior to the pretreating step.

FIG. 1 depicts a schematic process for carrying out the process of the present invention.

FIG. 2 depicts a schematic diagram of a fluidized bed granulator in accordance with the present invention.

FIG. 3 shows a graphical comparison of pore volume and pore diameter for activated alumina particles prepared in accordance with the present invention compared to prior art granulation processes.

FIG. 4 shows a graphical comparison of pore volume and pore diameter for activated alumina particles prepared by fluidized bed granulation.

Referring now to FIG. 1, rehydratable alumina is fed as shown to cold hopper 1 where the alumina is cooled to a temperature below room temperature, e.g., such as below about 20.degree. C. The alumina is cooled in cold hopper 1 to a temperature preferably in the range of about 5.degree.-10.degree. C., and more preferably, to a temperature of about 5.degree. C. Coolant at a temperature of about 0.degree. C. is passed in line 2 to provide cooling for cold hopper 1. Cooled powder is then passed from cold hopper 1 through line 3 to mixer 4. Water also is fed as shown to mixer 4 at a temperature below room temperature, e.g., such as below about 20.degree. C., preferably at a temperature in the range of about 5.degree.-10.degree. C., and more preferably at a temperature of about 5.degree. C.

The first step of the process of the present invention generally takes place in mixer 4 and includes pretreating the alumina powder by admixing the powder with the cold water fed to the mixer at a temperature below room temperature, e.g., below about 20.degree. C., preferably at a temperature in the range of about 5.degree.-10.degree. C., and more preferably at a temperature of about 5.degree. C. A cooling jacket (not shown) can be used in conjunction with mixer 4 for cooling the content therein during mixing. Such a cooling jacket can use a water bath for cooling mixer 4. The pretreatment step carried out in mixer 4 preferably includes mixing alumina powder and water in a ratio of about 2:1 by weight. The pretreatment step is performed in such a way to saturate the pore volume of the alumina partially with water and to form a surface layer on the alumina in the form of a gel or gel-like structure. The pretreatment step is carried out in such a way not to rehydrate the powder extensively.

Pretreated alumina from mixer 4 is fed in line 6 to a spouted fluidized bed granulator 7. The operation of the fluidized bed granulator 7 includes maintaining a constant superficial velocity of fluidizing air fed as shown to the fluidized bed. Preferably, air making up the fluidized air consists of air having a high relative humidity of 80% or greater. The high relative humidity air is supplied by feeding air as shown to humidifier 8 prior to feeding fluidized air at the proper relative humidity to fluidized bed granulator as shown. A portion of the high relative humidity air preferably is used to provide a spouted jet air stream as shown in the fluidized bed granulator unit (FBG) of FIGS. 2 to maintain better circulation of solids in the bed. It has been found that 20-70% of the total air introduced as feed into the fluidized bed should be introduced as the jet air as shown. Nevertheless, the constant superficial velocity of air should be maintained at about 0.8 to 1.4 m/sec, preferably at about 1.1 m/sec in fluidized bed granulator 7 for particle sizes in the range of about 1-3 mm. At velocities below 0.8 m/sec, growth rate is undesirably slow. At velocities higher than 1.4 m/sec, entrainment problems affect the stability of the fluidized bed. The preferred velocity will vary directly with the particle size to be produced. The high relative humidity air used as fluidizing air and as jet air is controlled to have 80% or higher relative humidity to reduce the loss of water from the bed while the alumina is agglomerating.

Residence time in the fluidized bed is maintained between about 10-60 minutes. The specific residence time within the specified range depends upon the desired size distribution. Granules growing beyond the size supported by the incoming fluidized air are withdrawn through the bottom of the bed in line 9, along with the agglomerated granules sized in the range of about 1-3 mm diameter in accordance with the present invention.

Agglomerates withdrawn from the fluidized bed granulator in line 9 are passed to screen 11 to be screened into desirable products. Oversize agglomerates are withdrawn as shown from screen unit 11 and fed to crusher 12. The oversized agglomerates are crushed in crusher 12 and passed in line 13 to be used as seeds in the fluidized bed granulator. Optionally, the crushed oversized agglomerate can be recirculated (not shown) to screen 11. Undersized agglomerates from screen 11 are recycled to join line 13 and are fed back to the bed for seed feed. Carried-over fine particles from fluidized bed 7 are passed in line 14 to cyclone 16 to be captured and returned in line 17 to the fluidized bed. Fine particles escaping the cyclone in line 18 in the exit gas are removed by a wet scrubber unit (not shown).

After screening in screen 11, the granules of desired size in the range of about 1-3 mm diameter are passed in line 19 to steam aging tank 21. The granules are steam aged in tank 21, e.g., such as at a temperature of about 110.degree. C. for about 0.5 hour and then passed in line 22 to water aging tank 23. The granules are water aged in tank 23, by way of example at a temperature of about 60.degree.-90.degree. C. for 4 hours. The steam aged and water aged particles then are passed in line 24 to activator 26. Activation is carried out in activator 26 to develop porosity and surface area. Activated alumina is withdrawn from activator 26 as shown.

Referring now to FIG. 2, a detailed diagram of fluidized bed granulation unit 7a is shown as having automatic controls including moisture sensor 31 and pressure sensor 32.

The fluidized bed granulation in accordance with the process of the present invention provides granules of a relatively small size on the order of about 1-3 mm diameter. The fluidized bed granulation provides the further advantage of a higher one-pass efficiency than either pan or drum granulators as used in the prior art. Further, a lower rate of recirculation provides a lower capital and operational cost.

The fluidized bed granulation in the process of the present invention provides a continuous and automatic process even in a large-scale facility. Granules having a controlled pore structure are produced.

The process of the present invention including a cold pretreatment step inhibits rehydration during the granulation. Rehydration to develop solid bridges is controlled to occur only at aging under a controlled atmosphere.

It has been found that the mechanism of agglomeration in the fluidized bed in accordance with the process of the present invention enhances the formation of granules having high porosity and low density. The pore size distribution and other structural parameters of agglomerates are controlled by manipulating hydrodynamic parameters in the fluidized bed. Further, the strength of the agglomerate is closely related to pore structure. The stronger granules produced by the process of the present invention are developed by selecting the appropriate mechanism of particle growth. The fluidized bed provides the flexibility of changing turbulent fluid flow in the bed to provide the desired growth mechanism.

The fluidized bed granulation in accordance with the present invention also provides a mechanism for controlling temperature. The turbulent agitation in the bed exposes most of the surface area of the alumina for heat transfer. The high heat capacity of the bed, relative to the gas within the bed, stabilizes the temperature of the bed. The advantage of a facilitated temperature control is important to the system involving chemical reaction sensitivity to temperature changes in the bed, such as the rehydration of the alumina powder.

The process of the present invention in providing a system for operating continuously and automatically overcomes the problem in the practice of prior art processes attributable to the difficulty of process automation and control. Since agglomeration of alumina powder is sensitized to the moisture level in the bed, automation is accomplished in the process of the present invention by monitoring moisture level and controlling the population of seeds in the bed.

In practicing the process of the present invention with a fluidized bed granulator, the entrainment of fine particles in the bed requires the installation of additional equipment to recover these fine particles.

A relatively high pressure drop across the fluidized bed requires a compressor sufficient to overcome the pressure drop through the fluidized bed.

The process of the present invention including a pretreatment step for cold granulation in a fluidized bed agglomerating step has produced granules having a high total pore volume (0.7-0.863 cm.sup.3 /g), high macropore volume (>0.3 cm.sup.2 /g) low packed bulk density (0.51 g/cm.sup.3 or 32 lb/ft.sup.3), high surface area (320-425 m.sup.2 /g), good crushing strength (1-6.99 MPa), and wide pore volume distribution.

A rehydratable alumina constituting a median particle size of 7 microns was processed in accordance with the present invention, and the properties of the granules produced (FBG-4) were compared with two other types of agglomeration techniques based on the use of alumina having a median particle size of 5 microns. The two other types of agglomeration techniques were tumbling drum and immiscible fluid or "oil drop." The results of the property comparison are shown in Table I.

The fluidized bed granules produced in accordance with the present invention have much lower packed bulk density than granules formed in the tumbling drum and compared favorably to oil drop balls in total pore volume, packed bulk density, and strength.

Mercury pore volume distributions for the three samples shown in Table I are depicted in FIG. 3. The granules produced in accordance with the present invention identified as FBG-4 had a much wider size distribution than that of the oil drop balls and had a larger macropore distribution (over 1,000 Angstroms).

Alumina granules were agglomerated in a fluidized bed, were aged, and were activated. Properties of the granules are shown in Table II.

Sample FBG-1 was prepared using 1 micron alumina as the starting material, while the rest used 7 micron alumina. Sample FBG-4 was pretreated using precooled 7 micron alumina powder and water at 5.degree. C. and granulated at room temperature. The rest were pretreated and granulated at room temperature.

As can be seen in Table II, the properties of the cold-pretreated granules (FBG-4) are significantly different from the room temperature-pretreated granules (FBG-3). The FBG-4 has much higher total pore volume (0.831 cm.sup.3 /g) than that of FBG-3 (0.609 cm.sup.3 /g). As a result, FBG-4 has lower mercury bulk density (0.863 vs. 1.063 g/cm.sup.3) and higher porosity (71.7% vs. 64.7%). Surface areas for these two samples are almost identical (333 vs. 326 m.sup.2 /g) despite the difference in the pore volume. Packed bulk density for FBG-4 (0.51 g/cm.sup.3) is smaller than that of FBG-3 (0.65 g/cm.sup.3), presumably due to low Hg bulk density and more uniform size of granules.

Comparison of the mercury pore size distributions for these samples is shown in FIG. 4. Higher pore volume for FBG-4 is attributable to the creation of macropores at 1-10 micron size range.

In Table II, the crushing strength of FBG-4 (6.99 MPa) is slightly better than that of FBG-3 (6.58 MPa) in spite of a lower density. The strength of granules is inversely proportional to the effective diameter of the secondary particles (the aggregated particles of the original CP particles after pretreatment). The pretreatment at low temperatures retards rehydration reactions. Therefore, the size of secondary particles is smaller for FBG-4 than for FBG-3 and consequently FBG-4 granules have slightly higher strength. Also, the analyses for FBG-3 show that fluidized bed granules have low abrasion loss (0.56% ) and relatively high crushing resistance (90.11%).

The effects of the particle size of CP powder on the properties of the final granules can be seen by comparing sample FBG-1 with FBG-3. Granules of CP-1 (FBG-1) have significantly lower density and higher surface area than that of CP-7 (FBG-3). The total pore volume is higher for FBG-1, and the majority of pores for CP-1 granules are concentrated at the lower range of pore sizes. It was believed from observation during the experimental procedure that the strength of CP-1 granules was higher than that of CP-7 granules, though no crushing strength results are available for CP-1 granules. Mercury pore size distributions for those two samples are also shown in FIG. 4.

While the invention has been described in terms of preferred embodiments, the claims appended hereto are intended to encompass all embodiments which fall within the spirit of the invention.