PSRI30yr anniversary lecture on Scaling Law and Agglomeration Issues in Fluidization Technology
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Transcript of PSRI30yr anniversary lecture on Scaling Law and Agglomeration Issues in Fluidization Technology
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Scaling and Agglomeration
in Fluid Beds
Masayuki Horio
Tokyo Univ. of Agri. and Tech.
Koganei, Tokyo
Congratulations! PSRI’s 30yrs Anniversary
Scaling and Agglomeration
in Fluid Beds
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25 min from Shinjuku
A best place to escape & concentrate
Koganei ?
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Livsville FBC
(FW)
AFBCs
w/ EPDC
Yubari 40t/d gasifier
w/ MHI-EPDC
Battelle’s MSFBC
w/ Mitsui
Some
Background 350MWePFBC
w/ IHI
Yubari de-H2S for
gasifier
w/ IHI-EPDC
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Soft Sphere Model with Cohesive Interactions
Normal and tangential component of F collision
and F wall
Surface/bridge force
Rupture joint h c
Attractive force F c
No tension joint
Normal elasticity k n
Normal dumping h n
Tangential dumping h t
k t Tangential elasticity
Friction slider m SAFIRE is an extended Tsuji-Tanaka model
developed by TUAT Horio group
SAFIRE (Horio et al.,1998~)
(Non-linear spring)
t
t n t x
x F F m = n t F F m >
dt dx
x k F n n n n n h - D =
dt dx
x k F t t t t t h - D = n t F F m
km g = h 2 ( )
( ) 2 2
2
ln ln
p + = g
e e
w/wo Tangential Lubrication
w/wo Normal Lubrication
Numerical simulation era coming
soon?
What is it providing us?
DEM (discrete element method) or
DPM (distinct particle method) Demo
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Plan of my Talk
1. Introduction
Nature of suspensions/beds and the effect
of Walls that we design
2. Scaling Issues
Derivations and validations
3. Agglomerating Fluidization
Progresses in Binderless Agglomeration
Plan of my Talk
1. Introduction
Nature of suspensions/beds and the effect
of Walls that we design
2. Scaling Issues
Derivations and validations
3. Agglomerating Fluidization
Progresses in Binderless Agglomeration
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Fluidlike
nature of
suspension:
no need of
walls but
appreciated
the wall
Plant
design:
trying to get
most out of
the wall
effect
Fluidization
science: high
potential in
developing the
knowledge on
suspension
nature
Confusions
in
definitions
etc.
Phenomenology and Design
Nature and Art (wall effect)
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Particle-Particle interactions created by
Particle-Fluid interactions
(Photo by Prof. Joseph) Nature
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Particle clustering simulated by Prof. Tsuji
Nature
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Particle clustering observed by laser sheet
method (Tsukada & Horio)
Gs=0.018kg/m2s, u0=0.67m/s, Dt=200mm
Nature
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Particle clustering in denser
suspensions observed by
internal picturing (Kuroki &
Horio)
Gs=0.21kg/m2s 0.70kg/m2s 1.2kg/m2s
Nature
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A set of three
laser sheets
Gas flow
A cup shaped cluster;
to the 3D structure of
suspensions (Kroki &
Horio) Nature
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Particle clusters moving to the wall
(Kuroki & Horio (‘94))
Gs=0.22 kg/m2s, u0=0.58m/s, z=1150mm Wall
Effect
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Particle clusters viewed by a horizontal laser
sheet (Tsukada, Ito & Horio)
Gs=0.019 kg/m2s, u0=0.74m/s, z=740mm
Nature
Wall Effect
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Scanning Laser Sheet
technique and 3D images
(Ito-Horio) Nature
Wall Effect
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A phase diagram of particle
suspensions (w/ Dr. Hirama data by Horio)
Fast fluidized beds = super-
critical state of G/S systems
Nature
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Hydrodynamics
Particle
behavior
Chemistry
Mechanisms
&
Kinetics
Heat &
Mass
transfer
Good performance
Hydrodynamics
Particle
behavior
Chemistry
Mechanisms
&
Kinetics
Heat &
Mass
transfer
Good performance
Hydrodynamics
Particle
behavior
Heat &
Mass
Hydrodynamics
Particle
behavior
Heat &
Mass
Transfer
Good performance
Chemistry
Mechanis
ms &
Kinetics
Scale-up issues
?
Boundary
Conditions
+ Nature
Good performance
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Three Previous Approaches
to the Scaling Law
1. Dimensional analysis
Fitzgerald (1982)
2. Dimensionless parameters in
differential equations which do not contain Dt as an explicit parameter
Glicksman (1982?, 84……)
3. Integrated relationships,
phenomenology and correlations
Horio et al. (1982, 84, 86) Note: Differential Eqs., boundary conditions and
integration gives solutions !
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m times
A simple thought experiment (‘82)
ub=[gDb]1/2
ub= ubo [gDb
o]1/2
ubb=u0-umf
bshould remain same
Dt=mDto
Dt=Dto
ub [ gmDbo]1/2
= m 1/2 ubo
Dbo
Db=mDbo
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Thought Expmt:
Dc/Db=(b+2)/(b-1)
Db: Bubble diam.
Dc: Cloud diam.
b= ub/(umf/mf)
umf/mf
ub=[gDb]1/2
umf/mf
ub=[gDb]1/2
umf/mf
ub=[gDb]1/2
xm
Gas flow in emulsion phase
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1) For Geldart Group B powders, the bubble
fraction, bubble size distribution, solids
circulation and mixing can be made similar
among different scale models if the following
condition is satisfied:
U U m U Umf mf0 0- = - ( )
2) Fluidization behavior of Group A powders,
both bubble distribution and interstitial gas flow
can be made similar if Equation (96b) is
satisfied, in addition to Equation (98).
U m Umf mf=
Horio’s Scaling Law
o
May allow to use
the same solids!
(96b)
(98)
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Horio’s Scaling Law and previous bubble correlations
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11
2 1 12
1 2
- =-
- - -
C A
p C AC
T C
sl C slu
u u** **
** **
,
** ,
/
( )( ) ( ) (60)
CFB: Area fraction of annulus Extended Capes model by Horio et al. (‘89)
usl: gas-solid slip velocity
Suffix C: core
Horio’sScaling Law
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Equation of continuity for gas:
tu+ =( ) 0 (1)
Equation of motion for gas:
( )
f f
u
tu u g p R+
= - - (2)
Equation of continuity for solid particles:
( )
( )11 0
-+ - =
tv (3)
Equation of motion for solids:
( ) ( )
p p s
tg p R P1 1 1- +
= - - - + +
vv v( ) ( )
(4)
where R denotes
R u M
D u
Dtf= - + -
-
( ) ( )
( )v
v1
(5)
with
β=( ) ( ) / p f T
ng u- - -1 1
(mf ≪≦ 1, Richardson and Zaki, 1954 ) (6a)
β=
1 150 1175
2
- -+ -
m
s p s p
fd d
u( )
. v
(≪1, Ergun, 1952 ) (6b)
Anderson-Jackson (’66) model
What happens if
we start from
the governing
equations ?
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f
p p
u
t u u
gl
U p
l
U u
U
÷ ÷ + +
+ + -
÷
÷ =
$
$ ( $ $ ) $ $ $ $ $
0 2
0
0
0
0 v
v (86)
( ) $
$ ( $ $ ) $ $ $ 1 0 0
0
0
0
2
0
0
0
2
0
0
-
÷ +
÷
-
÷ -
÷
÷ =
U
t
U l
U
U u
p v
v v v +
v
gl
U v
v
U v
0 2
(87)
where
$ / ( / ), $ / , $ / , $ / t t l U u u U p p U p
0 0 0 0
2 v v v and $ l .
Dimensionless expressions
The representative length should be the plant
scale.
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NO!
Remember: We are using same
molecules!
Scaling law should tell us in what
scale level and how much we can
sacrifice the similarity: Plant scale flow
pattern?; bubble/cluster scale?; particle scale?.
Are you trying to
make everything
similar?
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When f /p≪1,
$ $ ( $ $) + - =pl
Uu
p
0
0v
= -( ) /1 p Tg u (mf≪≦1)
= -( ) /1 mf p mfg U (mf≦≪1)
l
U
gl
U
U
up T0 0
2
0 1= -( ) (mf≪≦1)
l
U
gl
U
U
Up mf
mf
0 0
2
0 1= -( ) (mf≦≪1)
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The flow field in a unit of length scale l, which is
geometrically similar to a reference unit (denoted by
superscript °), can be made similar, if the following four
conditions are satisfied:
l U l U/ /0
2
0
2= (91)
U u U uT T0 0/ /= (mf≪? ≦1) (92a)
U U U Umf mf0 0/ /= (mf ≦ ≪1) (92b)
v v0 0 0 0/ /U U= (93)
f p f p/ /= (94)
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U U m0 0 0 0/ = =v / v (95)
u m uT T= (mf≪? ≦1) (96a)
U m Umf mf= (mf≦≪? ) (96b)
d
dm
p
p
p f
p f
=-
-
1 4
1 2
/
/
m
m (Ar≦104)
d
dm
p
p
p f
p f
f
f
=
-
-
(105≦Ar)
(97a)
(97b)
Ret=Ar/18 (Ar<104), Remf=Ar/1650 (Ar<1.9x104)
o
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As noted above, the judgment of the dominant
mechanism can be done based on the Archimedes
number Ar. The guideline of Glicksman (1988),
Rep<4
i.e. for the viscosity-dominant regime, can be
disregarded if fluidizing gas velocity U0 is
considered as not being related to the criterion for
particle size selection. In other words, Equations
(97) can be used regardless of the fluidizing gas
velocity.
Prof. Glicksman’s guideline ?
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Experimental Validation
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Properties of particles
Glass beads dp umf(obsd) umf(Wen-
Yu)
Particles mm m/s m/s
GB376 376 0.112 0.112
GB305 305 0.074 0.075
GB236 236 0.046 0.045
Experimental
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Experimental Validation for
Bubbling Bed
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Experimental Validation for Bubbling Bed
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Solid tracer concentration for the same
dimensionless time
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Straight column
Straight column
l/Dt=1/15
Tapered column
Straight column
l/Dt=2/15
Tapered column
l/Dt=1/15
Tapered column
l/Dt=2/15
radial position [-]
radial position [-] PE pellet concentration [%]
PE pellet
concentration [%]
Transient response
t*=t/[Dt/g]1/2
t*=16.2 ; ○: bed A Dt=0.6m,
▽:bed B Dt=0.3m, △:bed C Dt=0.15m
Validation of scaling
law
Radial and axial PE
pellet distribution
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Experimental Validation for
CFBs
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Experimental results from CFBs A&B
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Similarity in Gsmax vs gas velocity
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Similarity in Pressure distribution
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Similarity in Phase Transition
Characteristics
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Similarity in Pressure fluctuation
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Similarity in Mesoscale flow structure
lcl: cluster length Voidage in cluster
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Scaling
Experiments
Reactor Model
PLAN & IDEAS REAL PLANT
Experiments
using the same
materials and
conditions as
expected for the
real plant
Reaction,Heat
& mass
transfer,
distributor
elements etc.
Hydrodynamics,
Erosion etc.
Key points:
Reduce risks
but save
money &
time
Scale down
the imagined
plant and
organize
sure tests
down up CFD
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■Introduction ◇ Agglomerating Fluidization ◇ Previous thoughts and models ◇ Why binderless granulation? ■ Characteristics of PSG and PSG granules ◇ Granules appearance, structure, strength, size and density, operating factors, scale effect ◇ Co-agglomeration and coating ■ Model predictions ■ Applications ◇ Hard metal cutting tool manufacturing ◇ Dry Particle Inhalation ■ Concluding remarks
Agglomerating Fluidization
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“Agglomerating Fluidization”
“Agglomerating fluidization is a common mode of fluidization popular in beds of Geldart group C powders, spray granulation, coating or polymerization, metal powder processing at elevated temperatures and combustion or gasification with sticky ash or sorbent particles. However, in such a variety of cases their differences are only in types of cohesiveness, their order of magnitude, the rate of development and the elastic/plastic characteristics of necks between particles. Once interaction forces are properly expressed, it should be possible to mechanistically describe any different kinds of agglomerating fluidization.”
Iwadate and Horio, Fluidization IX, Durango (1998)
Cited by Prof. J.C. Chen of Lehigh U. for a quiz at 10th
ceremony of Fluidization X, Beijin, May 2001.
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Def
luid
izat
ion v
eloci
ty [
m/s
] Ash Agglomeration and
Defluidization; ’80s’ experience
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Iron particle growth by sintering
Experimental data from self nucleation tests
Wt pct
first cycle
Size, mesh
US std
+20
-20+30
-30+40
-40
Starter
bed
18.2
45.1
36.7
Final
bed
32.1
33.6
18.3
16.0
Final
bed less
oversize
49.4
27.0
23.6
Wt pct
second cycle
Wt pct
third cycle
Starter
beda
55.6
30.0
14.4
Final
bed
42.3
38.1
12.5
7.1
Final
bed less
oversize
66.0
21.7
12.3
Starter
bedb
67.0
22.0
11.0
Final
bed
44.6
36.2
10.1
9.1
Final
bed less
oversize
65.4
18.2
16.4
1500F 87% reduction 1600F 87% reduction
Starting
cast shot
Fines
taken up
Langston and Stephens (1960)
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Puzzling
Umf
increase
for fine
powders Data by Sugihara(1966)
and
correlation by Jimbo (1966)
[ Along with their efforts for
establishing Soc. Powder
Tech. Japan]
u m
f
[cm
/se
c]
dp mm]
um
f [cm
/se
c]
CaCO3
3 d 18 m 3 d 18 m u mf = d p
2
+ n2 F pm p
g( - f ) u mf = d p
2
+ n2 F pm p
g( p - ) f
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Chronology of Group C issues
1961 Davidson’s Bubble
1966 Jimbo, Sugihara’s umf issue left a question at least to Japanese
1973 Geldart’s Powder classification and ‘Group C’ for cohesive ones
197X Donsi-Massimila(75), Masters-Rietema(77): Cohesion force and fluidized bed behavior
1985 Chaouki et al., Group C fluidization and agglomerate size (da) prediction
1987 Kono et al.: Measurement of force acting on particles
1988 Morooka et al.: Energy balance model for da
1990 Pacek-Nienow: Fine & dense hardmetal powder fluidization
1991 Campbell-Wang: Particle pressure in a FB
1992 Nishii et al.: Pressure Swing Granulation
1993 Tsuji, Kawaguchi & Tanaka: DEM for Fluidized Bed
1998 Mikami, Kamiya & Horio: Numerical simulation of agglomerating FB (SAFIRE)
Iwadate-Horio: Particle pressure / Force balance model to predict da
Green letters: fundamentals
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Liquid Bridge formation (SAFIRE model)
droplet
Very slow liquid layer flow
liquid bridge
small
contact angle
large
contact angle
particle collision
particle collision
liquid bridge
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6 7 8 9 10
1 2 3 4 5
(a) Dry particles
u0=1.2m/s, dp=1.0mm, p=2650kg/m3
(b) Wet particles (water: 0.54wt%)
Fluidized bed behavior of dry and wet particles
(SAFIRE simulation, Mikami et al., 1998)
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Uematsu, Uchida and Zhang (1994)
(a) (b)
50mm 50mm
(a) before binder removal (b) after binder removal
Trace of original granules in alumina compacts
before and after binder removal
Spray Granulation: Pre Granulation is needed to avoid
dusting, sticking to walls & non-stoichiometric charging
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Potential of binderless
granulation (1)
Agglomeration: Reduces troubles associated with cohesiveness of
fines (dusting, sticking & poor chemical accuracy);
Increases uniformity of chemical composition of
product granules by decreasing segregation;
Binders: So far necessary to agglomerate but
Provide unnecessary strength to products;
Leave unwanted binder-originated species even
after the de-binder-ing operation;
Binderless ? Yes, because-------
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Because It gives weak products;
--Many processes do not need too much strength.--
Contamination-free;
Weaker granules provide higher green densities,
higher composition uniformity and not severe
defluidization;
Possible to granulate hydrophorbic powders / water
sensitive powders;
Well controlled granulation by Pressure Swing
Granulation (PSG; Dalton Ltd. / Fuji Paudal);
Probably possible to make layered structure.
Applications Dry ceramic process, Powder metallurgy, Drugs etc.
Potential of binderless
granulation (2)
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Characteristics of PSG and
its product granules
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Pressure Swing Granulation: PSG
Nishii et al., U.S. Patent No. 5124100 (1992)
Nishii, Itoh, Kawakami,Horio, Powd. Tech., 74, 1 (1993)
(a) apparatus (b) operation
time[s] 0 7200
15s 1s ② Compaction
interval
① Fluidization
interval
② Compaction
interval ① Fluidization
interval
0.108m
0.41m
Bag filter
Gas tank
Compressor
Compressor
Wall Effect
Group C
powder
Nature
+
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Typical examples of PSG
granules
Al2O3 Lactose
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PSG granules: weak but strong enough!
Change in PSD of PSG granules in realistic
conditions
PSG
granules
from ZnO
dp=0.57mm
slide
gate
after
1st fall
2nd fall
3rd fall
Particle size [10-6m]
C
um
ula
tive w
eig
ht [%
]
50
0m
m
original
PSG
granules
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0 10 20 30 40 500
20
40
60
80
100
dp,sv [mm]
No. 2 7.48
Primary particle size [mm]
Cu
mu
lati
ve
siz
e d
istr
ibu
tio
n [
v%
]
Fig. 4 Size distributions of primary particles
No. 3 4.95
No. 4 4.79
No. 5 4.14
No. 6 3.71
No. 7 2.58
PSG from lactose
Original powders of Lactose (Takano et al. (2001))
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1mm
1mm
No. 2
1mm
No. 4
1mm1mm
No. 3
1mm
No. 5 No. 7No. 6
Fig. 6 Microphotographs of PSG granules of lactosePSG from
lactose
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#16-1 #16-1#30-1 #30-1
#16-2#16-2#30-2#30-2
#16-1#30-1 #16-2#30-2
500mm
ZnO
Structure of PSG granules Granules split by a needle show a core/shell structure.
(Horio et al., Fluidization X (2001))
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E
Superficial gas velocity [m/s]
Me
dia
n d
iam
ete
r [m
1
0-6
]
0.1 150
1.0
1000
500
0.5
Effect of fluidizing gas
velocity on da
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Bu
lk d
en
sity o
f g
ran
ule
s [kg
/m3]
Maximum pressure difference for compaction [Pa104]
0.6
1.0
0.8
1.2
2.0 6.0 4.0 0
Factors affecting PSG
granule density
w=0.4kg
0.2kg
with gas velocity, solids charge
and compaction
chamber pressure
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-
DQ 500 series
DQ labo
ρ(bulk)=3710kg/m3
angle of repose=34º
DQ200
ρ(bulk)=3800kg/m3
angle of repose=33º
DQ350
ρ(bulk)=3760kg/m3
angle of repose=35º
Scale up
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compaction and attrition
bed expansion
bubbling
fines‘ entrainement
air (in bubbling period)
pulse (in reverse flow period)
① ②
cake
filter cleaning & reverse flow period:
Cakes and fines are returned to the bed cleaning-up the filter, and
bed is compacted promoting agglomerates’ growth and consolidation.
bubbling period:
Bed expansion de-agglomerates and compaction, attrition and solids revolution make grains spherical.
Fines are separated and re compacted on the filter.
①
②
What happens in
PSG?
distributor
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Numerical simulation of agglomerating fluidization
Iwadate-Horio (Fluidization IX, 1998)
Ha=0.39x10-19 J, dp=1mm, p=30 kg/m3
Ha=4.0x10-19 J
0.0546m
Gas velocity: linear increase from 0-0.25 m/s within t=0.1s, holding for 0.039s and linear decrease within 1.011s
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Authors External force/energy
Ekinetic =mumf /22
shearElaminer =3pmumfda2
Fpp
Fcoh,rup
FGa
v=umf
expansion
Chaouki et al.
Morooka et al.
Iwadate-Horio
Cohesion force/energy
p6
FGa = da
ag
3
Fexp =pDbag(-Ps)da
2
2nk
exp = - Ps
Fcoh,rup =24
2
Hada(1-a)
Model
FGa = Fpp
bubble
Fpp =16
2
hwdp1+[ hw
8p Hr
2 3 ]
Comments
Esplit =hw(1-a)da
2
32
adp
2
Esplit
Etotal
Etotal=(Ekin+Elam) =Esplit
Etotal=(Ekin+Elam)
Fexp = Fcoh,rup
No bubblehydrodynamiceffects included.
If 3mumf <hw(1-a)
/(32pdpa),negative da isobtained.
Force balance
Energy balance
Force balance
gravity force≒drag forcevan der Waals forcebetween primary particles
laminar shear + kinetic forceenergy required tobreak an agglomerate
bed expansion force cohesive rupture force
No bubblehydrodynamiceffects included.
Bed expansionforce caused bybubbles isequated withcohesive ruptureforce.
Comparison of previous model concepts
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1E-6 3E-6 1E-5 3E-5 1E-4 3E-4 1E-3 3E-3
1E-10
1E-9
1E-8
1E-7
1E-6
1E-5
1E-4
A
B
F coh,rup = H a d a (1- a )
24 2
F exp = 2n k
p D b a g(-Ps)d a 2 ^
stable point
fluidized
unstable point
easy to
defluidize
(a) example force balance and
two solutions
log d a [m]
log
F[N
]
1E-6 3E-6 1E-5 3E-5 1E-4 3E-4 1E-3 3E-3
1E-10
1E-9
1E-8
1E-7
1E-6
1E-5
1E-4
C
saddle point
(b) Limiting size of agglomerates
log d a [m]
log
F[N
]
The critical condition
Force balance of I-H model (Powder Technol., 1988)
and the critical solution
defluidization due to u0=umfa
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Fig. 2 Fracture tensile strength mesurement by a micro compression testing machine
0 50 100 150 2000
0.5
1
1.5
2
2.5
3Ff
Displacement [mm]
Lo
ad
[m
Pa]
Ff
A : Elastic and plastic
deformation
B : Elastic brittle fracture
C :Plastic deformation
(a) Example of fracture tensile strength mesurement
(b) Types of mesurements
Ff
Ff
Grain compression test
and typical force
displacement responses
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0.01 0.03 0.1 0.3 1 3 10 30 100 10
20 30
50
100
200 300
500
1,000
Iwadate-Horio Chaouki et al.
Morooka et al.
u 0 =0.5m/s
0.3 0.5 1 2 3 5 10
20
50
100
200
500
1,000
2,000
5,000
u 0 =0.5m/s Morooka et al.
IHM
Chaouki et al.
0.01 0.03 0.1 0.3 1 3 10
20
50
100
200
500
1,000
2,000
u 0 [m/s]
0.01 0.03 0.1 0.3 1 3 0.005
0.01
0.02
0.03
0.05
0.1
Morooka et al.
IHM
Chaouki et al.
u 0 =u mf
bubbling bed
fixed bed
da [m
m]
da [m
m]
da [m
m]
Da [m
m]
(a) Effect of primary particle size
(b) Effect of Hamaker const.
(c) Effect of u0
dp [mm]
Ha [J]
(IHM)
Comparison of model
performances
Bubble size
Iwadate-Horio (1998)
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1 10 100 1000 100001E-7
1E-6
1E-5
1E-4
1E-3
h=0
.057
7
1 10 100 1000 100001E-7
1E-6
1E-5
1E-4
1E-3
1 10 100 1000 100001E-7
1E-6
1E-5
1E-4
1E-3
1 10 100 1000 100001E-7
1E-6
1E-5
1E-4
1E-3
No. 7
dobs=373mm
dcalc=667mm
Fexp
Fcoh,rup
da[mm]
No. 6
Fexp
Fcoh,rup
dobs=607mmdcalc=726mm
da[mm]
No. 4
dobs=677mm
dcalc=621mm
Fexp
Fcoh,rup
da[mm]
F[N
]
da[mm]
No. 5
Fexp
Fcoh,rup
dobs=788mmdcalc=723mm
Fig. 13 Agglomerate size determination (PSG:2hr, pre-sieving by 16mesh)
F[N
]
F[N
]
F[N
]
F[N
]
h=1
h=1
hcr
i=0.
0390
h=1
h=1
h=1
hcr
i=0.
0808
hcr
i=0.
152
=hcr
=hcr
=hcr
=hcr
Agglomerate size determination by I-H
model (Takano et al. Powd. Tech.,accepted,2001; Lactose;
PSG:2hrs, presieving by 16 mesh)
Fe
xp
an
d F
co
h,r
up
[N
]
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Comparison of model predictions with observed data
d a,
ca
lc [m
]
0E+0
2E-4
4E-4
6E-4
8E-4
1E-3
1.2E-3
1.4E-3
0E+0
2E-4
4E-4
6E-4
8E-4
1E-3
1.2E-3
1.4E-3
Lactose
ZnO
L:E=7:3
L:E=1:1
L:E=3:7
d a,obs [m]
Model (IHM)
works !
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Possibility of size control by
surface modification
by
vacuum drying, CH2OH or
NH4OH adsoption
Nishii and Horio (1996)
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Me
dia
n d
iam
ete
r [
10
-
6m
]
Absorption time [h]
500
Me
dia
n d
iam
ete
r [
10
-
6m
]
300
400
500
293K,
4kPa
0 3 6 9 12
Me
dia
n d
iam
ete
r [
10
-6m
]
300
400
200
573K,
13.3kPa
0 3 6 9 12 Absorption time
[h]
Absorption time [h]
400
500
600
293K,
4kPa
0 3 6 9 12
Absorption time [h]
300
400
500
Med
ian
dia
mete
r [
10
-6m
]
573K,
13.3kPa
0 3 6 9 12
(a) C2H5OH (b) NH4OH
Mean size of PSG granules from TiO2 (0.27x10-6m) after heat treatment and surface modification
heat treatment:at p<13.3Pa
523K, for 6 hrs
adsorption:
bed= 150x10mm
in a 0.03m3 vacuum
dryer
PSG: charge=0.0333 kg
u0=0.55 m/s RH: 40-
50%
fluidiz.:15 s comp.: 1 s
total cycles=450
adsorption at:
p(adsorbate):
Nishii & Horio (Fluidization VIII, 1996)
Notes: At 573K all
hydroxyl groups
on TiO2 are
eliminated
(Morimoto, et al.,
Bull. Chem. Soc.
JPN, 21, 41(1988).
Highest heat of
immersion at 573K
(Wade &
Hackerman, Adv.
Chem. Ser., 43, 222,
(1964))
No effect: desorbed
during PSG
No effect ??
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Applications
Hard metal and Pharmaceutical
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Agglomerate 1
Powder 1 Powder 3 Powder 2
Agglomerate 2 Agglomerate 3
feed compositions
powd. dp(WC) WC Co wax*
x10-6m %wt %wt %wt
1 1.5 93.0 7.0 0.5
2 6.0 85.0 15.0 0.5
3 9.0 77.0 23.0 0.5
dp(cobalt)=1.3-1.5x10-6m
*) Tmp(wax)=330K
preparation: 1. grinding 2.5hr 2. vacuum drying PSG: Dt=44mm charge=150g u0=0.548 m/s P(TANK)=0.157 MPa total cylces=64
Hard Metal Application
SEM images of feeds and
product granules
Nishii et al., JJSocPPM(1994)
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Application to hard metal industry (Nishii et al., JJSPPM(1994))
Improved strength of sintered
bodies
PSG
method
convent-
ional
method
T
ransvers
e r
uptu
re s
trength
[N
/mm
2]
Co content [wt%] Co content [wt%]
PSG
method
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Co-agglomeration
of lactose and ethensamide
O
H
H
HO
O
CH2OH
H
OHH
OHH
OH
H
OHH
OHH
OHH
CH2OH
・H2O
C-NH2
O
OCH2CH3
Lactose Ethenzamide
CH3
O
OH
HN
C
Acetaminophen
Molecular structures
![Page 79: PSRI30yr anniversary lecture on Scaling Law and Agglomeration Issues in Fluidization Technology](https://reader033.fdocument.pub/reader033/viewer/2022052506/557c843ed8b42ab0788b4b22/html5/thumbnails/79.jpg)
top: PSG granules; second line: surface of agglomerate
(SEM)
Co-agglomeration of lactose
and ethensamide
L : E=1 : 0
500mm
L : E=0 : 1
500mm
L : E=3 : 7
500mm
L : E=1 : 1
500mm
L : E=7 : 3
500mm
10mm
L : E=0 : 1
10mm
L : E=3 : 7
10mm
L : E=1 : 1
10mm
L : E=7 : 3
10mm
L : E=1 : 0
L : E=1 : 0
500mm
L : E=0 : 1
500mm
L : E=3 : 7
500mm
L : E=1 : 1
500mm
L : E=7 : 3
500mm
10mm
L : E=0 : 1
10mm
L : E=3 : 7
10mm
L : E=1 : 1
10mm
L : E=7 : 3
L : E=0 : 1
500mm
L : E=3 : 7
500mm
L : E=1 : 1
500mm
L : E=7 : 3
500mm
10mm
L : E=0 : 1
10mm
L : E=3 : 7
10mm
L : E=1 : 1
10mm
L : E=7 : 3
10mm
L : E=1 : 0
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0 20 40 60 80 1000
20
40
60
80
1001000mm
500mm
250mm
Co
nc
en
tra
tio
n o
f E
the
nza
mid
e
in P
rod
uc
t G
ran
ule
s [
%]
Average Mass Concentration of Ethenzamide in Feed [%]
Granule Sample : 10mg
Chemical Uniformity of PSG
granules
UV
absorbance:
300nm
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Fra
ctu
re t
en
sile s
tre
ss
[k
N/m
]2
Ethenzamide Content of Mass Charged Powder [%]
0 1 2 3 4 5 60
10
20
30
40
50
60
70
0 30 50 70 100
Ethenzamide
Fracture Tensile Stress of Granules
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stage0:>11 m m
stage1:7-11 m m
stage2:4.7-7 m m
stage3:3.3-4.7 m m
stage4:2.1-3.3 m m
stage5:1.1-2.1 m m
stage6:0.65-1.1 m m
stage7:0.43-0.65 m m
Filter:<0.43 m m
air chamber
Cascade Impactor
ejector
pump 28.3L/min
compressor 28.3L/min
throat
differented pressure sensor
1.2mm
2.5L
capsule No.2 HPMC
vacuum
Preliminary test of DPI application of PSG
granules Takano, Nishii & Horio (2000)
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Agglomerate size [mm]
Cu
mu
lati
ve
un
der
siz
e[-
]
0 0.2 0.4 0.6 0.8 1 1.2 1.4 0
0.5
1
Ethen 100%
450M 50%
450M 25%
450M 75%
450M 87.5% 450M 81.25%
325M 75%
325M 62.5%
Application of PSG granules
to DPI ?
0 80 160
50
100
Cu
mu
lati
ve
siz
e d
istr
ibu
tio
n [
%]
Primary particle diameter [mm
Lactose(450M) d p = 11.9 m m
Ethenzamide
Lactose (325M) d p =54.7 m m
Ethenzamide (Jet milled) p=1.94mm
p=18.4mm
Size distributions of PSG
granules for a DPI test
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(42-32mesh)
0
5
10
15
20
25
30 F
racti
on
[%
] E=100
E/325M=75/25
E/325M=62.5/37.5
E/450M=75/25
E/450M=50/50
E/450M=25/75
Deagglomeration and dispersion
of PSGgranules Takano, Nishii & Horio (2000)
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0
5
10
15
20
25
30
35 F
racti
on
[%
] E=100
E/325M=75/25
E/325M=62.5/37.5
E/450M=75/25
E/450M=50/50
E/450M=25/75
Dispersion of PSG granules
by Fujisawa’s E-haler (42-
32mesh)
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Concluding remarks
Knowing the nature of both
suspension and suspension-
wall interactions and
governing them to get good
products should be the role
of fluidization engineers.