Epstein N., Grace J.R. Spouted and Spout-Fluid Beds: Fundamentals and Applications
Подождите немного. Документ загружается.
Liquid and liquid–gas spouting of solids 327
2. Fine particles can cause a change in the spout inlet boundary condition. With gas-
spouted systems the spout becomes unstable, bubble generation commences within
the spout, and solid circulation is impaired. However, with liquid-phase spouting of
fine particles, this instability manifests itself as a change in the inlet voidage. No
longer is the inlet voidage equal to 1, but rather is a value less than 1. Dense transport
is established throughout the spout, and P
ms
/P
mf
exceeds 0.785. Morgan et al.
20
characterized such fine particle systems as low A
f
systems when the values of this
dimensionless parameter are less than 0.002 and thus indicative of a low inlet orifice
momentum. In this regime, they found that a modified A
f
parameter correlated the
system dynamics better. Kim and Ha
21
studied the annulus flow of fine-particle water-
spouted systems and found that the axisymmetric model of flow, which assumes Darcy
flow in the annulus and uses the experimental spout–annulus interfacial condition,
predicts the annulus fluid streamlines well.
20.1.6 Bed expansion
With an increase in liquid flow rate, a bed’s spout and fountain expand, thereby increasing
the average bed voidage even though the annular voidage increases minimally. Kmiec
22
investigated overall bed expansion to the top of the fountain using glass spheres, silica
gel particles, ion-exchange resins, and sand spouted with water in an 88-mm-diameter
conical-cylindrical column with included cone angles of 30
◦
,60
◦
, and 180
◦
.Ona
logarithmic plot, the voidage versus liquid superficial velocity relationship exhibited
a change in slope at a voidage ≈0.85. Similar behavior has been reported by several
investigators of liquid fluidized systems (Di Felice
23
). The following correlations were
proposed by Kmiec
22
for low and- high-voidage regions:
For ε<0.85,
ε = 0.838 · Re
0.182
Ar
−0.0866
(H
0
/D)
−0.243
θ
−0.067
, (20.16)
where Re = d
p
Uρ/μ and Ar = d
p
3
ρ(ρ
p
− ρ)g/μ.Forε>0.85,
ε = 1.102U
0.0774
(H
0
/D)
−0.105
θ
−0.047
, (20.17)
with U in m/s. Eqs. (20.16) and (20.17) are valid for 3.5 < Re < 350, 2.1 ·10
3
< Ar <
2.6 ·10
6
,0.19< H
0
/D < 1.55, π/6 <θ<π radians, and 0.023 < U < 0.095 m/s.
Ishikura et al.
24
investigated the maximum bed expansion in liquid-spouted and flu-
idized beds undergoing upward piston movement under conditions in which U exceeds
the single particle terminal velocity.
20.1.7 Mass transfer
Had
ˇ
zismajlovi
´
cetal.
25
and Kim et al.
26
studied the liquid–solid mass transfer coefficients
in liquid spouted and spout-fluid beds of ion exchange resins. They found that the
traditional spouted bed is less effective than an equivalent fluidized bed. Such liquid
spout-fluid beds can be successfully used to treat liquids contaminated with suspended
328
ˇ
Zeljko B. Grbav
ˇ
ci
´
c, Howard Littman, and Morris H. Morgan III
solid particles, but the bed height should be significantly greater than H
m
to obtain
efficiency comparable with fluidized beds.
20.1.8 Spouting of binary mixtures and elutriation
Relatively little research has been done on liquid spouting of poly-disperse particle
systems. Ishikura and Nagashima
27
investigated the spouting of binary particle mixtures
with glass spheres of d
p
= 1.124 mm as the coarse particles and glass spheres of
diameters 233 and 474 μm as the finer component. The spouting fluids were water and
aqueous sucrose solution. The addition of a small amount of the finer particles to the
coarse ones produced a much lower minimum spouting velocity for the mixture than
that for the coarse particles alone. An increase in the liquid viscosity led to a decrease
of the minimum spouting velocity and hence the bed pressure drop. Ishikura et al.
28,29
also investigated the elutriation of the fine particles from a liquid spouted bed of binary
solids in conical-based cylindrical columns of 66 and 100 mm diameter. These results
were compared to similarly sized fluidized beds employing a perforated plate instead of
an inlet nozzle. The initial fines entrainment velocity, U
be
, was found to be smaller than
the free-settling terminal velocity of the fines, but larger than the velocity required to
entrain the same species from a liquid-fluidized bed. It was also found that U
be
decreased
with a reduction in freeboard height, making the particles more subject to elutriation. An
empirical correlation for the elutriation coefficient was strongly dependent on a modified
Froude number. Other variables – the column diameter, the initial total particle holdup,
initial fines mass fractions, and nozzle diameter – were found to have little effect on this
elutriation coefficient.
20.2 Liquid–gas spouting
Functionally, liquid–gas spouting systems are analogous to three-phase fluidization, and
thus many expressions used to predict the dynamics of the latter hold for the former.
Basically, two types of contactors have been investigated: contactors in which the gas
is a dispersed phase, including liquid–gas spouted beds with draft tube, and contactors
in which the liquid is a dispersed phase. The principal applications of these systems are
similar to those for three-phase fluidized beds.
20.2.1 Gas as a dispersed phase
20.2.1.1 Liquid–gas spouted and spout-fluid beds
Nishikawa et al.
30
studied gas absorption in a liquid–gas spouted bed by monitoring
oxygen dissolution into a copper-catalyzed sodium sulfite solution in a conical-based
cylindrical column of diameter 150 mm and length 1400 mm. Air and water were
introduced at the cone base through a nozzle whose diameter varied from 10 to 45 mm.
Glass spheres of diameters 1.01, 2.59, 3.10, and 4.87 mm were the solid particles. Bed
mass varied between 2 and 10 kg. For the largest solids mass loading, the estimated
Liquid and liquid–gas spouting of solids 329
H/D ratio was ∼3. Experiments conducted at gas and liquid superficial velocities of 4.7
and 3.8 cm/s, respectively, showed that particles smaller than 3 mm were not effective
because of channeling in the central portion of the bed. With particles larger than 3 mm,
the gas–liquid volumetric mass transfer coefficient was more than 1.75 times larger than
that of a column without particles because of efficient bubble breakage in both the spout
region and in the fluidized bed region above the spout.
Wang et al.
31
proposed the use of a three-phase spouted bed with large particles and a
downward annular liquid flow for gas–liquid reaction systems in which deposition and
adhesion on the nozzle or the reactor wall limited effectiveness. Large particles were
found to reduce fouling because of their high impact momentum. Glass beads of 10.5,
12.0, and 16.0 mm diameter were used as the solid phase. The column was 230 mm
in diameter and was equipped with a slotted conical base. Water in the column leaked
into a reservoir through the slots and was pumped back to the column for spouting the
glass particles through a 16-mm-diameter nozzle. Air was introduced through a ring-
type distributor equipped with six 8-mm-diameter gas injection tubes. Wang et al.
31
identified three characteristic flow regimes: a packed bed regime, a transition regime,
and a spouting regime. The experimental minimum liquid spouting velocity was found
to increase with increasing static bed height and to decrease slightly with increasing
gas velocity. The spout was effective for bubble breakup, whereas frequent collisions of
the particles with the reactor wall and the nozzles prevented fouling and promoted self-
cleaning. Gas holdup increases accompanied corresponding increases of the superficial
gas and liquid circulation velocities. Gas holdup varied between 0.1 and 0.5, depending
on bed operating conditions.
Anabtawi et al.
32,33
investigated liquid-phase mass transfer from the dispersed gas in
a three-phase spout-fluid bed at conditions above and below the minimum spout-fluid
values. They followed oxygen absorption in carboxymethylcellulose solutions under
varying rheological conditions. The gas-absorbing solution was introduced into the
surrounding annular section and the spouting air through a central nozzle. Spherical
glass particles of diameter 1.75 mm were the solids. These authors stated that the main
advantage of this contacting system was the enhanced mixing associated with a vigorous
circulatory motion caused by rising bubbles.
20.2.1.2 Liquid–gas spouted and spout-fluid beds with a draft tube
The gas–liquid–solid fluidized bed has emerged in recent years as one of the most
promising devices for three-phase operations.
34
A new design with a spouting orientation
incorporates a draft tube that is coaxially located inside the bed with a gas and liquid
injector under the draft tube. The draft tube promotes bulk circulation of gas, liquid, and
solids between the draft tube and annulus, thereby achieving intimate contacting between
phases (Figure 20.3). If there are no particles flowing in the draft tube, the system is,
in essence, an internal loop gas lift reactor. Fan et al.
34
conducted the most detailed
study of this type of contacting system. They identified flow regimes and studied an
array of variables: pressure profiles and pressure drops, b ubble penetration depth in the
annulus, overall gas holdup, apparent liquid circulation rate, and bubble size distribution
330
ˇ
Zeljko B. Grbav
ˇ
ci
´
c, Howard Littman, and Morris H. Morgan III
TO
RESERVOIR
COLUMN
DRAFT TUBE
PARTICLES
AIR
WATER
Figure 20.3. Liquid–gas spouted bed with a draft tube, adapted from Fan et al.
34
in both the draft tube and annulus. Three flow regimes were identified: a packed bed
mode, a fluidized bed mode, and a circulated bed mode. The circulated bed mode is
of particular interest, as this bed mode generates both high gas holdup and efficient
contacting between phases. The transition points between the respective regimes are a
complex function of particle size, particle density, and particle loading.
The overall gas holdup increases with an increase in either gas or liquid superficial
velocities. In all cases the overall gas holdup of a draft tube three-phase spouted bed is
significantly higher than that for the corresponding three-phase fluidized bed system.
Different hydrodynamic aspects of liquid–gas spouted and spout-fluid beds with a
draft tube have also been investigated by Karamanev et al.,
35
Hwang and Fan,
36
Vunjak-
Novakovi
´
c et al.,
37
Kundakovi
´
c et al.,
38
Cecen Erbil,
39
Nitta and Morgan,
40
Olivieri
et al.,
41
and Pironti et al.
42
20.2.2 Liquid as a dispersed phase
Fluidized bed contactors containing large, low-density spheres considerably improve
gas–liquid contacting in scrubbers, absorbers, distillation columns, and direct cooling
towers.
43
They operate at much higher gas and liquid rates before flooding than con-
ventional packed towers and have lower static bed heights. Lighter packing and higher
fluid flowrates also make them efficient low-pressure-drop contactors. Movable packing
Liquid and liquid–gas spouting of solids 331
GAS OUT
MIST
ELIMINATOR
LIQUID ENTRY
LIQUID
DISTRIBUTOR
PERFORATED
CONE
GAS ENTRYLIQUID OUT
H
0
= 243 mm
D = 194 mm
1.0 m
2.0 m
Figure 20.4. Three-phase spouted bed, adapted from Vukovi
´
cetal.
44
systems allow for the handling of gases and liquids containing particulate matter and
precipitates, and, for all practical purposes, clogging is eliminated. The highly turbu-
lent states induced in such contactors reveal transfer rates two orders of magnitude
higher than those in packed beds.
43
These fluidized bed contactors do possess certain
shortcomings – they tend to channel, and liquid backmixing makes true countercurrent
operation impossible. Vukovi
´
cetal.
44
developed a three-phase spouted bed contactor
in which the solid particles are spouted in a countercurrent flow of gas and liquid. A
schematic diagram of their system is shown in Figure 20.4. Hollow 10-mm-diameter
polyethylene spheres (ρ
p
= 320 kg/m
3
) were spouted in a 194-mm-diameter column.
A perforated 60
◦
conical section, 86 mm high, served both as a bed suppor t and water
drain. Air was introduced axially through a converging nozzle 30 mm in diameter, and
water was admitted through a distributor containing sixty 2-mm-diameter tubes.
Two general flow regimes were observed in this three-phase spouted bed contactor as
the gas flowrate was raised. In the higher-flowrate regime, the pressure drop, total liquid
holdup, and bed expansion all increased with gas flowrate. The “active” holdup, given
by the ratio of the measured bed pressure drop/pressure drop owing to the total weight
of the bed, rises rapidly in this flow rate regime and it is likely that interphase transfer
processes then occur at the highest rate. A spouted bed contactor with gas and liquid
mass flowrates of 2.18 and 1.88 kg/m
2
s, respectively, had similar pressure drop per unit
area of particle surface, total holdup per unit of operating bed volume, and “active”
holdup as a comparable fluidized bed contactor.
332
ˇ
Zeljko B. Grbav
ˇ
ci
´
c, Howard Littman, and Morris H. Morgan III
20.2.3 Processing in liquid–gas spouted beds
Several possible applications of liquid–gas spouted beds have been reported. Kecha-
giopoulos et al.
45
investigated a spouted bed reactor system for hydrogen production via
reforming of ethylene glycol, which served as a representative compound for aqueous
phase bio-oil. An olivine–nickel alloy was a suitable catalyst with high reforming activity,
excellent anticoking characteristics, and exceptional mechanical strength. Coke for ma-
tion, a major problem in most reforming processes, was drastically reduced because
of rapid and effective mixing of the hot solid particles and the cold reactants. Wright
and Raper
46
investigated fluidized and spouted beds for the biological filtration of gases
because of their high specific gas flowrate and vigorous mixing that facilitates enhanced
gas–biomass contacting. Switching from a conventional fluidized bed to a spouted bed
improved yields by 10 percent to 20 percent. Nieto et al.
47
and Tailleur
48
studied the
butene–isobutane alkylation reaction on a super-acid solid catalyst in a three-phase
spouted bed reactor. The main result was that the three-phase draft tube spouted bed
reactor improved both gas–solid contact and liquid mixing because of internal and exter-
nal recycling. Dabhade et al.
49
investigated the degradation of phenol by immobilized
Nocardia hydrocarbonoxydans (actinomycetes) on granular activated carbon in a gas–
liquid–solid three-phase spouted bed contactor. The effect of an array of variable flow
rates, influent concentrations, and solid loadings on phenol degradation was examined.
It was found that adsorption was dominant during the initial reaction phase, whereas
biodegradation dominated after adsorption equilibrium was reached. In general, higher
liquid flow rate increases shear between the spout and the annulus and enhances tur-
bulence; unfortunately, in biofilm reactors, this turbulence caused biomass detachment,
resulting in poor degradation of phenol. Elmaleh et al.
50
evaluated the oxygen transfer
characteristics of a high compact multiphase r eactor (HCMR) for wastewater treatment
employing cells immobilized on spouting particles. The high turbulence levels caused
significant particle–particle attrition, limited the biofilm thickness around the particles,
and lowered the biomass holdup. Even though biomass holdup was relatively low in
these HCMRs, they were effective low-energy and low-sludge-producing reactors.
Chapter-specific nomenclature
A
f
parameter defined by Eq. (20.8)
C
p
parameter defined by Eq. (20.4)
f
1
= 150[(1 − ε)
2
/ε
3
]μ/d
2
p
f
2
= 1.75[(1 − ε)/ε
3
]ρ/d
p
g(φ
s
) particle sphericity function
8
, g(φ
s
) = 1 for spherical particles
H
mSF
maximum spoutable bed height at the minimum spout-fluid condition, m
H
∗
lowest bed height for a one-dimensional model based on Eq. (20.3), m
U
a0
superficial fluid velocity at the inlet to the annulus (= V
a0
/A
a
), m/s
U
G
superficial gas velocity in three-phase bed, m/s
U
L
superficial liquid velocity in three-phase bed, m/s
Liquid and liquid–gas spouting of solids 333
U
s
superficial fluid velocity in the spout, m/s
U
T
terminal velocity of a single particle, m/s
V total fluid flow rate (= V
a0
+ V
n0
), m
3
/s
V
a0
inlet annulus flowrate, m
3
/s
V
mf
minimum fluidizing flow rate, m
3
/s
V
ms
minimum spouting flow rate, m
3
/s
V
mSF
total fluid flow rate at the minimum spout-fluid condition, m
3
/s
V
n0
fluid flow rate in spout inlet tube, m
3
/s
V
T
= U
T
·A,m
3
/s
X = 1/(1 + H/D)
Y = 1 − P
ms
/P
mf
Greek letters
ε
g
gas holdup in three-phase bed
θ
f
parameter defined by Eq. (20.5)
φ
s
sphericity
Subscripts
a in the annulus
mf minimum fluidization
ms minimum spouting
mSF minimum spout-fluid condition
References
1. K. B. Mathur and N. Epstein. Spouted Beds (New York: Academic Press, 1974).
2. A. Nagarkatti and A. Chatterjee. Pressure and flow characteristics of a gas phase spout-fluid
bed and the minimum spout-fluid condition. Can. J. Chem. Eng., 52 (1974), 185–195.
3. D. V. Vukovi
´
c, D
ˇ
z. E. Had
ˇ
zismajlovi
´
c,
ˇ
Z. B. Grbav
ˇ
ci
´
c, R. V. Gari
´
c, and H. Littman. Flow
regimes for spout-fluid beds. Can. J. Chem. Eng., 62 (1984), 825–829.
4. W. Sutanto, N. Epstein, and J. R. Grace. Hydrodynamics of spout-fluid beds. Powder Technol.,
44 (1985), 205–212.
5.
ˇ
Z. B. Grbav
ˇ
ci
´
c, D. V. Vukovi
´
c, F. K. Zdanski, and H. Littman. Fluid flow pattern, minimum
spouting velocity and pressure drop in spouted beds. Can. J. Chem. Eng., 54 (1976), 33–42.
6. T. Mamuro and H. Hattori. Flow pattern of fluid in spouted beds. J. Chem. Eng. Japan, 1
(1968), 1–5.
7. K. B. Mathur and P. E. Gishler. A technique for contacting gases with coarse solid particles.
AIChE J., 1 (1955), 157–164.
8. H. Littman and M. H. Morgan III. A general correlation for the minimum spouting velocity.
Can. J. Chem. Eng., 61(1983), 269–273.
9. S. Ergun. Fluid flow through packed columns. Chem. Eng. Progr., 48:2 (1952), 89–94.
334
ˇ
Zeljko B. Grbav
ˇ
ci
´
c, Howard Littman, and Morris H. Morgan III
10. H. Littman, D. V. Vukovi
´
c, F. K. Zdanski, and
ˇ
Z. B. Grbav
ˇ
ci
´
c. Pressure drop and flowrate
characteristics of liquid phase spout-fluid bed at the minimum spout-fluid flowrate. Can. J.
Chem. Eng., 52 (1974), 174–179.
11. H. Littman, D. V. Vukovi
´
c, F. K. Zdanski, and
ˇ
Z. B. Grbav
ˇ
ci
´
c. Basic relations for the liq-
uid phase spout-fluid bed at the minimum spout fluid flowrate. In Fluidization Technology,
Vo1. 1, ed. D. L. Keairns (New York: Hemisphere and McGraw-Hill, 1976), pp. 373–388.
12. R. Legros, S. Charbonneau, and R. C. Mayer. Prediction of minimum spouting velocities in
liquid-solids conical beds. In Fluidization VIII, ed. J. F. Large and C. Lagu
´
erie (New York:
Engineering Foundation, 1998), pp. 639–646.
13. G. A. Lefroy and J. F. Davidson. The mechanics of spouted beds. Trans. Instn. Chem. Engrs.,
47 (1969), T120–T128.
14. N. Epstein and S. Levine. Non-Darcy flow and pressure distribution in a spouted bed. In
Fluidization, ed. J. F. Davidson and D. L. Keairns (London: Cambridge University Press,
1978), pp. 98–103.
15. M. H. Morgan III and H. Littman. General relationships for the minimum spouting pres-
sure drop ratio P
ms
/P
mf
and the spout-annulus interfacial condition in spouted bed. In
Fluidization, ed. J. R. Grace and J. M. Matsen (New York: Plenum Press, 1980), pp. 287–
296.
16. H. Littman, M. H. Morgan III, D. V. Vukovi
´
c, F. K. Zdanski, and
ˇ
Z. B. Grbav
ˇ
ci
´
c. A theory for
predicting maximum spoutable bed height in spouted beds. Can. J. Chem. Eng., 55 (1977),
497–501.
17. H. Littman, M. H. Morgan III, D. V. Vukovi
´
c, F. K. Zdanski, and
ˇ
Z. B. Grbav
ˇ
ci
´
c. Prediction of
the maximum spoutable height and the average s pout to inlet tube diameter ratio in spouted
beds of spherical particles. Can. J. Chem. Eng., 57 (1979), 684–687.
18.
ˇ
Z. B. Grbav
ˇ
ci
´
c, D. V. Vukovi
´
c, D
ˇ
z. E. Had
ˇ
zismajlovi
´
c, R. V. Gari
´
c, and H. Littman. Prediction
of the maximum spoutable bed height in spout-fluid beds. Can. J. Chem. Eng., 69 (1991),
386–389.
19. H. Littman and S. J. Kim. The minimum spouting characteristics of small glass particles
spouted with water. In Fluidization V, ed. V. K. Ostergaard and A. Sorensen (New York:
Engineering Foundation, 1988), pp. 257–264.
20. M. H. Morgan III, H. Littman, and B. Sastri. Jet penetration and pressure drops in water
spouted beds of fine particles. Can. J. Chem. Eng., 66 (1988), 735–739.
21. S. J. Kim and J. H. Ha. Flow in the annulus of a water spouted bed of small glass particles at
minimum spouting. J. Chem. Eng. Japan, 19 (1986), 319–325.
22. A. Kmiec. Expansion of solid-liquid spouted beds. Chem. Eng. J., 10 (1975), 219–223.
23. R. Di Felice. Hydrodynamics of liquid fluidization. Chem. Eng. Sci., 50 (2005), 1213–1245.
24. T. Ishikura, I. Tanaka, and H. Shinohara. Length of particles bed in batch solid-liquid spouted
and fluidized systems – experimental study for the region of transport bed. J. Chem. Eng.
Japan, 12 (1979), 332–333.
25. D
ˇ
z. E. Had
ˇ
zismajlovi
´
c, D. V. Vukovi
´
c, F. K. Zdanski,
ˇ
Z. B. Grbav
ˇ
ci
´
c, and H. Littman. Mass
transfer in liquid spout-fluid beds of ion exchange resin. Chem.Eng.J., 12 (1979), 227–236.
26. S. J. Kim, C. Y. Chung, S. Y. Cho, and R. J. Chang. Mass transfer in liquid-fluidized and
spouted beds of ion exchange resin at low Reynolds number. Korean J. Chem. Eng., 8 (1991),
73–79.
27. T. Ishikura and H. Nagashima. Flow characteristics of liquid-spouted beds with binary mix-
tures of particles. Fukuoka Daigaku Kogaku Shuho, 64 (2000), 153–161.
Liquid and liquid–gas spouting of solids 335
28. T. Ishikura, I. Tanaka, and H. Shinohara. Elutriation of particles from a batch spouted bed in
solid-liquid system. J. Chem. Eng. Japan, 12 (1979), 148–151.
29. T. Ishikura. Behaviour and removal of fine particles in a liquid-solid spouted bed consisting
of binary mixtures. Can. J. Chem. Eng., 70 (1992), 880–886.
30. M. Nishikawa, K. Kosaka, and K. Hashimoto. Gas absor ption in gas-liquid or solid-gas-liquid
spouted vessel, 2nd Pacific Chemical Engineering Conference (PAChEC ’77), 2 (1977), 1389–
1396.
31. J. F. Wang, T. F. Wang, L. Z. Liu, and H. Chen. Hydrodynamic behavior of a three-phase
spouted bed with very large particles. Can. J. Chem. Eng., 81 (2003), 861–866.
32. M. Z. Anabtawi, N. Hilal, and A. E. Al Muftah. Volumetric mass transfer coefficient in
non-Newtonian fluids in spout fluid beds. Chem. Eng. Technol., 26 (2003), 759–764.
33. M. Z. Anabtawi, N. Hilal, A. E. Al Muftah, and M. C. Leaper. Non-Newtonian fluids in
spout-fluid beds: mass transfer coefficient at low Reynolds numbers. Partic. Sci. & Technol.,
22 (2004), 391–403.
34. L. S. Fan, S.-J. Hwang, and A. Matsuura. Hydrodynamic behavior of a draft tube gas-liquid-
solid spouted bed. Chem. Eng. Sci., 39 (1984), 1677–1688.
35. D. G. Karamanev, T. Nagamune, and I. Endo. Hydrodynamic and mass transfer study of a
G-S-fluid-solid draft tube spouted bed bioreactor. Chem. Eng. Sci., 47 (1992), 3581–3588.
36. S.-J. Hwang and L. S. Fan. Some design considerations of a draft tube gas-liquid-solid spouted
bed. Chem.Eng.J., 33 (1986), 49–56.
37. G. Vunjak-Novakovi
´
c, G. Jovanovi
´
c, Lj. Kundakovi
´
c, and B. Obradovi
´
c. Flow regimes and
liquid mixing in a fluidized bed bioreactor with an internal draft tube. In Fluidization VII,
ed. O. E. Potter and D. J. Nicklin (New York: Engineering Foundation, 1992), pp. 433–444.
38. Lj. Kundakovi
´
c, B. Obradovi
´
c, and G. Vunjak-Novakovi
´
c. Fluid dynamic studies of a three-
phase fluidized bed. J. Serbian Chem. Soc., 61 (1996), 297–310.
39. A. Cecen Erbil. Effect of the annulus aeration on annulus leakage and particle circulation in
a three-phase spout-fluid bed with a draft tube. Powder Technol., 162, (2006), 38–49.
40. B. V. Nitta and M. H. Morgan III. Particle circulation and liquid bypassing in three phase draft
tube spouted beds. Chem. Eng. Sci., 47 (1992), 3459–3466.
41. G. Olivieri, A. Marzocchella, and P. Salatino. Hydrodynamics and mass transfer in a lab-scale
three-phase internal loop airlift. Chem. Eng. J., 96 (2003), 45–54.
42. F. F. Pironti, V. R. Medina, R. Calvo, and A. E. Saez. Effect of draft tube position on the
hydrodynamics of a draft tube slurry bubble column. Chem. Eng. J. & Biochem. Eng. J
., 60
(1995), 155–160.
43. B. K. O’Neill, D. J. Nicklin, N. J. Morgan, and L . S. Leung. The hydrodynamics of gas-liquid
contacting in towers with fluidized packing. Can. J. Chem. Eng., 50 (1972), 595–601.
44. D. V. Vukovi
´
c, F. K. Zdanski, G. V. Vunjak,
ˇ
Z. B. Grbav
ˇ
ci
´
c, and H. Littman. Pressure drop,
bed expansion, and liquid holdup in a three phase spouted bed contactor. Can. J. Chem. Eng.,
52 (1974), 180–184.
45. P. N. Kechagiopoulos, S. S. Voutetakis, A. A. Lemonidou, and I. A.Vasalos. Sustainable
hydrogen production via reforming of ethylene glycol using a novel spouted bed reactor.
Catalysis Today, 127 (2007), 246–255.
46. P. C. Wright and J. A. Raper. Investigation into the viability of a liquid-film three-phase
spouted bed bio-filter. J. Chem. Technol. & Biotech., 73 (1998), 281–291.
47. O. Nieto, M. Nino, R. Martinez, and R. G. Tailleur. Simulation of a spouted bed reactor for
solid catalyst alkylation. Fuel, 86 (2007), 1313–1324.
336
ˇ
Zeljko B. Grbav
ˇ
ci
´
c, Howard Littman, and Morris H. Morgan III
48. R. G. Tailleur. Simulation of three-phase spouted bed reactor for solid catalyst alkylation.
Chem.Eng.&Proc., 47 (2008), 1384–1397.
49. M. A. Dabhade, M. B. Saidutta, and D. V. R. Murthy. Continuous phenol removal using
Nocardia hydrocarbonoxydans in spouted bed contactor: shock load study. African J. Biotech.,
8 (2009), 644–649.
50. S. Elmaleh, S. Papaconstantinou, G. M. Rios, and A. Grasmick. Organic carbon conversion
in a large-particle spouted bed. Chem.Eng.J., 34 (1987), B29–B34.