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£1?PAR$NT VISO OSIT
OF
FLUIDIZD SOLIDS BY
ROTATING CYLINDER VISO CETER
by
HAROLD HUFPMAN SCOTT
submitted to
OREGON STATE COLLEGE
in partial fulfillment of
the requirements for the
degree of
MASTER OF SCIENCE
June 1948
ìJ'PROVED:
Redacted for Privacy
-
Head of Department c
Chemia1 Engineering
In Charge oD Major
Redacted for Privacy
Chairman of Søbool Ga4uate Comrnittes
Redacted for Privacy
Dean o
Gradutte
¿3
A
OWLEDGMLN T
The author wishes to express appreciation
for the helpful suggestions offered by Professor
Walton and Professor Schulein. The author
also indebted to Professor Sheely, of the Industrial Arta Department, for his patience and
diligence in constructing the apparatus.
is
UF CONTEN
hflL
Page
Introduction
.
.
.
.
.
.
.
.
.
blate:rials
.
.
.
Apparatus
.
.
.
a
a
a
e
a
a
a
Technique
.
.
.
.
.
.
.
.
.
.
Calibration
Results
.
D isouss ion
.
a
..
e.
.
.
a
o
a
s
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.
a
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i
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a
3
4
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,
a
a
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,
ea
17
a
e
a
28
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COf101USiOflSae...aa...a'.a
Bibliography
a
a
e
a
a
13
32
a
e
e
a
s
s
e
a
a
34
s
e
s
a
s
s
a
a
a
35
a
a
e
a
s
a
a
a
a
36
Appendix
Sample Calculations
Data
e
a
a
s
a
e
s
LIJT
Oi'
FIGURES
Pase
Figure
i
Diagram of Apparatus
2
Pbotograh of Appara tue
3
Photograph of Apparatus
4
Viscometer Calibration
.
.
,
.
,
.
5
,
8
3
9
,
,
.
,
15
.
18
Efeots
of Bentity on Catalyst
Viscosity on Baia of Direct
Comparison to Glycerol
5
S
Filtrol
.
.
.
.
.
.
.
.
.
.
.
19
Catalyst Shear Stress - Shear
Rate Relationship
'sØ
7
Filtrol
8
Catalyst3A
9
Generalized Calibration Curve
.
''s
s
-
S
.
S
s
.
.
20
21
24
Effect of Density on Catalyst
Viscosity on Basis of
Turbulent flow
10
1].
'iltrol
Catalyst3A
............
28
2?
APPÁRNT VISCOSITY OF
FLUfl)IZED SOLIDS BY
ROTATING CYLINDER VISO C4E[R
INThOLUCTI ON
(3, p1-2) pothted out the lack of Information generally available concerning the proportleß of cornRynnin
merciai fluidized solid catalysts. More specifically, in
his attempts to correlate his data by means of exIstIng
fluid flow ecjuatlons (3, p.U-l2), he Indicated the need
of an independent evaluation of the "apparent viscosity"
of the flowing material. This work was carried out In the
hope of filling this need and enriching the general fund
of information concerning fluidized solids.
The fluidized solid under ctonsideratlon here Is
true fluid. It is an aerated mass of finely divided
particles, which, superficially at least, behaves in
manner similar to a true fluid. Because it is not a
not a
solid
a
true
reason to believe that its proper-
fluid, there is little
ties can be expressed with validity
by the same terms
properties of a true fluid. However,
If modifications of existing flow equations are to be us-
which describe the
od
to
desoribe the behavior of this material,
venient to use the terms
it is
con-
"apparent density" and "apparent
viscosity".
following variables are believed by the author to
have a possible effect on the apparent viscosity of a fluThe
idized solid:
2
1.
The shape, size, and moisture content of the solid
particles.
2.
The "apparent density" of the aerated mass.
3.
The chemical composition, temperature, pressure and
humidity ot the
aerating gas.
This investigation was limited to variables one and
two; using two different
powdered
solids
and using air as
the aerating gas.
In selecting the method of measuring the apparent
viscosity, consideration bad to be given to the approxi-
mate range in which the viscosity might fall.
The direc-
tor of this research indicated that be had reason to be-
lieve that the viscosity was in the neighborhood of that
of a light petroleum neutral oil.
It appeared that a ro-
tating cylinder type viscometer might be built which would
adequately cover
the
indicated range.
Such
a
viscometer
was designed and constructed.
Because the fluidized solid is not a true
there was some doubt as to whether the
fluid,
"a: pparent
ity", as measured by a "true" viscometer,
viscos-
was the same as
the "apparent viscosity" indicated in the previously men-
tioned fluid flow correlations.
However, it was hoped
that the measured quantity would at least be proportional
to the quantity desired.
3
)AÄTERIALS
The two solids used in these experiments were com-
mercial ;owdered cateiysts, both o
aluminum si1ioìtes.
currin
hioh are
hy1rtd
One is produced from a naturally oc-
substance and sold under the trade name "Filtro].".
The other is ?rOduOOd synthetie&].ly under the de3ignation
"Catalyt 3A".
Both catalysts have been ground to about
the same decree of fineness; that is, about 90% through
100 mesh
nd 25% below 20 microns.
In spite of the faot that the two catalysts
eire
of
similar chemical composition and the particles approxi-
mately the same size, they have
appearance and "feel".
a
different physical
The Filtro]. looks and feels much
like ordinary flour, while the Catalyst 3A has a flaky
appearance and feels gritty.
4
APPA Rh TUS
The viscometer used here was basically a Stormer
type Instrument.
However, the peculiar nature of the
"fluid" under consideration dictated some dearture from
the conventional
The
design.
apparatu? ag finally used is diagramed schematic-
ally in Figure 1.
It consIsted, essentially,
of a cylin-
drical fluidizing chamber In which a "rotating" cylinder
was concentrically suspended.
fabricated from a
The fluidizing chamber was
clear plastic and
mounted
vertically;
air being supplied troia the bottom through a short, conical section.
t
the junction between the conical section
and the tube, a perforated
retaining plate
was
installed.
This plate served the dual purpose of supporting
the cata-
lyst bed and admitting air uniformly throughout the cross
section of the tube.
A cast iron cover plate was fitted
into the top of the plastic cylinder.
to
support the
This plate served
bearing housing, and center it with resIn order to
Imot to the outer cylinder.
present
minimum
disturbance to the airflow through the chamber, the rotating cylinder was made as
ends.
a
hollow shell, open on both
This was accomplished by fitting a spoked wheel In
the top of a brass tube and
drive shaft.
connecting
the "hub" to the
The spoke connection can be seen in Figure
2.
PULLEY
BEARING HOUSING
4 AIR EXITS TO
DIAGRAM
COMPRESSED
AIR LINE
0F
APPARATUS
TO
COLLECTING BAGS
H.H.
Scott
August 1947
BRASS
SHAFT
II
WEB CONNECTION
TO CYLINDER
IV'
-g
'NYLON
THREAD
ROTATING
BRASS CYLINDER
WATER MANOMETER
I
I
'FALLING
J
WEIGHT
AUXILLiAR AIR
FRrM 3OMPRESSOR
LUCITE
Ci'LINDER
TO COMPRESSED
AIR
FITTING ON
BEARING HOUSING
CLEAN OUT
STD
I
PIPE
1ORIFICE
PHIMARY AIR
FROM
TO
BLOWER
FIRST
FLOOR LEVEL
ND FLOOR LEVEL
Y
Figure 1
cl'
Fiurc
2
Photograph of Apparatus
Air exits from the apparatus were provided by drilling and tapping four symmetrically placed holes in the
cover plate.
The air was led troni these exits into col-
lecting bags through four 1-1/2 inch standard street eus.
Figure 2 shows one of these collecting bags in place.
The bearing housing was made in a tubular form from
Duraluminum alloy.
A ball bearing assembly was fitted in
either end of the tube.
The housing was secured concen-
trically to the cover plate by means of a flange.
A
shoulder on the drive shaft transmitted all of the end
thrust to the upper bearing, the bottom one acting only as
a low
friction alignment device.
Both bearings were lub-
ricated with kerosene.
In order to keep the catalyst out of the bearings, a
small amount of high pressure air was admitted to the
ing.
Ìious-
Thus there was a continuous flow of air away from
both bearings.
This was very effective in prevtnting
changes In bearing friction due to infiltration of the abrasive catalyst dust.
The rotating cylinder was actuated by means of a fal-
ling weight; the linkage being provided by the light
weight nylon thread wound on a pulley secured to the top
of the drive shaft.
The dimensions of critical parts of the apparatus are
tabulated as follows:
[;]
Inside diameter of plastic cylinder
.
.
.
8.58 inches
Length of plastic cylinder
.
.
.
19.12 inches
.
.
.
5.97 inches
0.062 Inches
Outside diameter
.
.
.
.
of brass cylinder
Thickness of brass cylinder
.
.
.
.
.
.
.
Length of brass cylinder
.
.
.
.
.
.
.
.
.
.
.
Distance from top of retaining plate
to bottom of brass cylinder . . . .
Distance from top of retaining plate
to top of brass cy1der
.
.
.
.
.
Distance from top of retaining plate
to bottom of cover plate (approz.)
Diameter of pulley
.
.
.
.
.
.
.
.
.
10.0
inches
4.0
inches
.
14.0
inches
.
.
19.
inches
.
.
2.12 inches
The whole apparatus was set up on the second floor of
the laboratory
and arranged so that
could be dropped to
the first floor.
the actuating weight
The weight traveled
approximately eight feet before timing was
begun, and the
timing interval was eight feet.
Certain limitations and failures of the apparatus
will receive attention in later sections of this paper.
Figure 3
Photograph or Apparatus
io
TECHNIQUE
Betore proceeding further
that
a rough
it
should be pointed out
operational classification has evolved in the
Operation at low super-
field ot fluid oataiyst technique.
tidal
air velocities
(below
2 ft/sec)
"dense phase" operation (2, p.429).
Ix
has been termed
this case the
bed
of particles is set Into violent motion, but stili retains
a
definite surface. On the
violently boiling liquid.
whole
it
looks very much like
other type cf operation
(encountered in pneurtic conveying) occurs when the air
velocity is raised to the point where the definite sura
The
face disappears and the particles are carried along with
This
the aerating gas.
has been termed "lean phase"
oper-
ation (2, p.429).
The work done
tiere has been confined to dense phase
operation.
In order to start a series of runs, 10 or 12 pounds
of catalyst were placed in the fluidizing chamber; the
cover plate with
the rotating cylinder was then set in
place. After applying high pressure air to the bearing
housing, the blower was
started and the flow adjusted so
that the desired bed height was obtained.
At
times
it
was
necessary to break the bed loose with high pressure air,
then switch over to the blower.
11
When the bed appeared to be completely fluldized, the
nianometer (air flow) reading and average height of the bed
were noted.
The
aotuìtin
weight was then released.
over the
fell approximately 16 That, and was timed
ita tall by means or a stop watch.
eight feet o
aoilItated
Ing jrooedure was
by
lust
The tim-
the use ot two mirrors
placed so that the weight could be ohservec
the timing mark:ers.
It
it
e.s
Qassed
4fter each run the air was shut off
and the collecting haga weighed, in order to estimate the
loss.
The data collected were:
niiìaoxaeter
reading, height
of bed in fluidizing chamber, original weight of catalyst
in chamber, loss to the bags, mass of actuating weight,
and the time for the weight to fall eight fest.
To
added of
compensate for bearing
sufficient
tion of the
inner
every opportunity
friction,
a
tare weight
was
magnitude to maintain continuous rota-
cylinder in air.
arid
This was checked at
only ones did it deviate appreciably
from its normal value of 16.8 grams.
eriodical checks
indicated that the weight was fai-
ling at constant velocity.
It
might
be said at this time that one of the most
serious fauit3 in the design of the apparatus
plate irnmersion of the rotating cylinder wa
jible.
was
that
o-
never pos-
This made the estimation of the catalyst bed
height doubly important.
4ot only did this
fziotor enter
12
Into the calculation of the apparent density, but more Im-
portant, lt determined the effective length of the cylin-
der, thus introducing complications in calibration. And
unfortunately, because of the rapid fluctuations of the
"boiling" surface, this was probably the least accurate of
all the data taken.
13
CALIBRA TI ON
Because of its ¡eculiar design, this visoometer was
not an "absolute" instrument, hence calculation of viscosity directly from the data was not feasible.
meter was therefore calibrated by means
eous glycerol solutions.
of
The visco-
standard aqu-
For convenience in selecting the
proper range of values, the calibration was
postponed
un-
til after most of the runs were made.
Under conditions
of'
viscous flow in a given ideal vis-
cometer, the viscosity is directly proportional to the mass
of the falling weight and inversely proportional to the re-
sultant constant
velocity attained
by
the weight. Ronce
ratio was used here as the basis for comparing the
the
catalyst data to the standard solutions.
Grains.
V
The
M
-
eigb.t in
Velocity of weight - Ft/sec.
actual calibration procedure
was as
follows:
A solution was made up to approximately the desired
concentration,
means of
and
its specific gravity
a Westphal balance.
With
determined by
this specific gravity,
the viscosity was determined from interpolation curves
previously prepared from data in Lange's Handbook (i, p.
1275 and 1563).
The viscometer was filled with
the glycerol solution
so as to obtain complete immersion of the rotating cylinder.
The
ratio was thon determined
with three different
14
actuating weights.
With every solution employed, this
procedure was repeated for five different liquid levels,
ranging rrom
tali.
coverage of cylinder (10 inches) to a
partial coverage of four inches.
Throughout the calibration, changes
in
liquid
temper-
ature were carefully recorded.
It
was immediately
evident that
the .- ratio increased
appreciably with increased shear rate. This behavior added
complications and rocuired some explanation.
At the time
(This point will be discussed further in succeeding sec-
tions.) it appeared that this increase could be reason-
ably attributed to an increase in bearing friction with
inorease( velocity.
On this basj.s it was believed that the best and sat-
est procedure would be to compare the catalyst and the
glycerol only at identical shear rates. The only method
found for accomplishing this wid, proved rather awkward
and laboriou8. The original calibration data were used to
prepare families of curves (a separate family for each
viscosity) showing the variation of the . ratio with the
mass of the falling weight. From these curves, were iade
faiailies (a family for each weight employed) showing the
variation, at constant viscosities, of
tiori of
cylinder covered.
ratio with frac-
Completion of these curves per-
mitted the preparation of the final calibration curves.
Figure 4 shows the curve for the lO gram weight. It
15
32
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CALIBRATION
z'
--
H.Scott Aug1947
/t
-___
____ -----
4
00
40
120
RATIO
- GM SEC/FT
Figure 4
160
80
L3
is typical of the others which were prepared for 50,
130, 150, and 200 gram weights.
100,
The nonconformance of the
"full coverage" curve was evident in every oase.
This was
attributed to the turbulence caused by the spokes in the
connection of the cylinder to the shaft.
It Is apparent that in order to make use of these celi-
bration curves, three items from the catalyst data were essential:
the mass of the weight, the coverage of the
tating cylinder, and the v-ratio.
ro-
It the weight used In
the particular case was 120 grams, the 120 gram calibration
curve would be selected.
Entering this curve with the
ratio and the coverage, the viscosity was determined.
Fur-
ther, since the mass, M, has been specified, the compar-
ison of the catalyst to glycerol must have been made at
identical velocities.
17
RESULTS
The resilts of this work were not entirely satisfac-
Apparent viscosities were first determined directly
tory.
from celibration curves, of the type shown in Figure 4
(sample calculations are shown in Appendix).
Figures 5 and 6 show the apparent viscosity as a tuno-
tion of apparent density.
The points were so badly scat-
tered that it was difficult to draw any definite conclusions.
However, in the case of Catalyst 3A at least, there
seemed to be some justification for concluding that over
the range covered, apparent viscosity was independent of
apparent density.
On this assumption, Figures 7 and 8
were prepared.
Here shear rate is shown as a function of applied
shearing stress.
Because of the wide variation In cylin-
der coverage, it was necessary to reduce the applied force
to a unit cylinder height.
The dotted lines on either
side of the curves show the shape of the corresponding gly-
oerol curves.
Again, the points were very scatterecL How-
ever, for both catalysts, the best line through the points
extrapolated readily to the origin and complied fairly
well with the shape of the glycerol curves.
During the calibration, the failure of the
remain
4
ratio to
constant with the increased shear rate, was attri-
buted to a progressive
increase in dynamic bearing friction.
EFFECT 0F DENSITY
i-
ON
(I)
w
FLUID CATALYST VISCOSITY
(f,
i
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Aug 1947
H H Scott
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FILT RO L
20
22
24
26
h
APPARENT DENSITY-
28
30
32
34
LBS/FT3
Q,
Figure 5
50
_________________
.
_________________
.
°
EFFECT 0F DENSITY
---
ON
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----
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--
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FLUID CATALYST VISCOSITY
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Scott
Aug.
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APPARENT DENSITY-
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30
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Figure 6
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CATALYST SHEAR
STRESS-SHEAR RATE
RELATIONSHIP
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H.H.Scott
DOTTED LINES INDICATE
GLYCEROL SOLUTIONS
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-
______________
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4.0
8.0
2.0
6.0
UNIT SHEAR STRESS- GMS/
Figure?
20.0
INCH OF CYLINDER
24.0
COVERED
28.0
32.0
2.0
o
w
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16
I-
-
(f
°
CATALYST SHEAR
H
STRESS-SHEARRATE
----
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Aug.
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DOTTED LINES INDICATE
GLYCEROL SOLUTIONS
1/'
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5.0
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15.0
20.0
UNIT SHEAR STRESS
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FIgure 8
25.0
30.0
OF CYLINDER COVERED
35.0
40.0
2
'
Howcyer, consideration of the Reynolds number involved,
(computed on the basis of a mean hydraulic radius) indicates that operation was well into the turbulent flow
re-
Hence, lt la probable that the major cause for the
gion.
variation of the
+ratio
was turbulence, not dynariic fric-
ti on.
In the turbulent flow region, the velocity attained
by the falling weight is no longer
i
cile
function cf
the £iES6 of the weight and the viscosity or the fluid. Furt-
ther, it is no longer independent of the density of the
flowing iuterìal.
Under these conditions, determination
of viscosity by direct ocxnarison coula not be valid, if,
as in this case, there was a difference in density between
the calibrating fluid and the fluid measured.
more general relationship was therefore sought
whiCh would permit use of data taken in the turbulent flow
region.
The method suggested by Squires and Dockendorft (4, p.
295) was mocilfied slightly and used in this case.
2hèi
nethod is based on a modified "friction factor-Reynolds
number" plot which is used as a generalized calibration
curve for a specific visoometer.
tor, f1, was defined as, t
=
nunther, he', 'was defined as, he' :
where:
'oroe applied - Grams.
'i
=
Density
-Gmsoc.
specific friction taoand a specific Reynolds
.
::
Revolutions of cylinder/minute.
R
p
=
Viscosity
-
Centipoises.
In the :x'esent case
sini1r groups were defined as
follows:
Specific friction factor,
'
Specific Reynolds number, Re'
Vhere:
S = Shearing stress- Oma/inoh of cylinder covered.
L
=
Density- Gius/oc.
:
Linear velocity cf actuating weight- Feet/sec.
Viscosity - Centipoises.
Confornixig to these definitio.s tbrouhout, va1u08 of
Re' and f' were
cloulted from
plotted in Figure
the oalbration data and
ci.
in the viscous flow region, visooity is prcportional
Therefore,
indGpenderit of density.
to S/L, end
in a
plot such as Figure 9, the viscous jortion would be represented by
a
straight line with a slope of xdnus 45°. At
the transition to turbulent flow, the curve would st&rt to
flatten out.
The curves shown in i'igure
flatter than the Indicated minus 45°.
ci
are obviously
It is therefore ap-
parent that the entire calibration was carried out in a
region of turbulent flow.
To determine visoositio
iro.
this curve, a friction
factor, f', was calculated for each of the oatalyat runs.
Entering the calibration curve with the friction factor and
100
tLI1f
90
i
,
80
--
70
60
-
-
-
-
-
---
-
,;
-
-
GENERAUZED
CALIBRATION
_:
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-
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-
CURVE
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50
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---- T
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Cylinder Coverage
-
4.0
u-
550
o
Rez
u-
520
LJ
fi
ci
-
L
L
7.0
90
VISCOSITY- CENTIPOISES
OAU ir.
-nreiv
-
I
-
S
U)
-
---
i
I
I
0.0 05
L
LINEAR VELOCITY 0F ACTUATING WEIGHT-
S
SHEAR
0.007
STRESS
001
-
FT/
SEC
GRAMS/INCH 0F CYLINDER COVERED
0.02
003
-
004
SPECIFIC REYNOLDS NUMBER-Re'
-
FIgure
9
006
0.08
01
02
25
the cylinder coverage, the Reynolds number, Re', was de-
termined.
and L known, viscosity wa
ith
from the Reyoid
viscosities
s
a
number.
?iures
calculated
lo ind 11 show the3e
function of apparent density.
It will be notod that the points are somewhat more
scattered, but since the general level of both patterns
has been raised, the percentage deviation froi the mean
line has actually been reduced slightly.
The Filtrol line
(Figure io) now apptars to be definitely independent of
dezsity over the range covered, and bas
mately 44 contipoises.
a
value of
appi-
About 70% of the points lie with-
in plus or minus five centipoises of this line.
The gen-
eral shape of the 3A pattern (Figure 11) is the sane as In
Figure 6, but the average value has been raised to approxi-
mately 29 centipoises.
About 60% of the points fall with-
in plus or minus five centipolsea of this value.
U)
w
U)
o
QI.-
z
w
o
>-
F(I)
o
o
(J)
i-
z
lii
QQ-
18
20
22
24
26
APPARENT DENSITY-
28
30
32
34
LBS/FT3
D.,
Figure 10
_/
(1)4
w
o
T
:
Q-
:
-
I-
z
---
I
w
t___.000
i
-
o
-
>-3
J_
-----------
DH-o-
FU)
o
>
____
-
.
,
o
F-2
z
w
FrrrT
a:
-
I_U
I
L....
'J
1
r
'JI
o
o
Jo
Q
oO----O-1
.
L)
U)
___o
S
-
.
L)
o
TTr ____
:t
H:
'J)
o
-------
-
o
o_______ __________
____ ____
-
-
-
o
o
o
H
o
C
-o
-----
------
O
--------
-
flhJITY
I_
L..'
s..FI
I
I
ON
£1-
a-
CATALYST VISCOSITY
3A -
b
H.H. Scott
20
CORRECTED FOR
TURBULENT FLOW
Aug. 1947
22
CATALYST
26
28
APPARENT DENSITY- LBS/FT3
24
Figure 11
30
32
34
2L
DISCUSSION
!rìu'ouhout this work, consistency of the data has
been poor.
This would indicate
iare expriet.tal
errors
or the operation of some unconsidered vuriable, or both.
While no attent was made to control the temperature
and humidity of the aerati
air, these variables did
ohan8e a;reciably throujhout the course of the runs, without any detectable effect.
The largest obvious source of experimoital error was
undoubtedly failure to
of the catalyst bed.
ro;erly estiiate the average height
Considering the
raid fluctuations
of the Tboiling" surface it is doubtful that the average
height was estimated closer than the nearest one half inch.
This, in a typical case, could be sufficient to cause an
error of five to ton percent in the calculated viscosity.
Errors in timing tha Thllixig weight are considered in most
oases to be below two peroent.
However, since time was
squared in the friction factor, f', timing errors were pro-
bably important in a nuaber of oese.
The two errors mentioned probably account for most of
the scattering.
But it can hardly be supposed that they
can account for the xuinerous points which are both very
high end very low.
The following is tendered as
explanation for these extrere peinte.
velocities,
(high densitIes) there is
½t
e
possible
very low air
narked tendency
29
tor the air to wash out "ohannels" In the catalyst bed.
Thus, once the3e chaxinels are established, most o
is by passed and most ot the
bed
the air
renains untluidized.
As
the air velocity is increased the tendency to channel is
reduced, a1tbouh it is probably nover entirely eliminated.
It is entirely possible that some undetected channeling
occured occasionally, such that j,art of the catalyst adja-
cent to the cylinder remained unfluidized. The unfluid**
izad portion, being relatively immobile , could act as an
effective brake on the cylinder, thus giving an apparently
high viscosity. On the other hand, if the nature of the
channeling was such that a large fraction of the cylinder
was adjacent to an abnormally "lean" mixture of
catalyst, the result would
If
equipment of
and
be an apparently low viscosity.
this type is to
be used
work, redesign so as to obtain complete
in
future
immersion of the
rotating cylinder is suggested. Also if the explanation
just presented is valid, consideration should be given to
the possibility of designing a superior air intake mani-
fold.
The reliability of the absolute magnitudes of apparent viscosities of fluidized solids determined in a rotat-
'
It
was noted during operation that before air
was admitted to the bed, the rotating cylinder
was quite effectively "frozen". Admission of
even a small amount of air (it channeling was
avoided) rendered the bed "fluid" and "unlocked"
the oylinder.
3D
Ing cylinder vlsooxaeter is Questionable.
The
o1lowing
points in this connection are ottered tor consideration:
1.
There is no way to account tor the possible "slip" ot
the cylinder past the particles immediately adjacent to
the cylinder.
It such slippage occurs,
it would have the
effect of giving a lower than correct viscosity.
2.
It appcars that for proper fluldizatlon, a reasonably
large annulus (perhaps not cuite so large as was used here)
between the concentric cylinders is necessary.
The result-
ant etfect on the Reynolds number is such that lt Is dit:tioult to avoid operation in the turbulent flow region.
In this region, of course, the visconieter is less 3onsItIve
to viscosity.
3.
Since operation will probably be in the turbulent re-
gion, it does not appear that direct coriparison to the
calibrating fluid could be valid.
On the other hand,
the
correction for turbulent flow is based on the assumption
that the catalyst is exhibiting the properties of a true
fluid.
In view of the foregoing statements, rather than attempt measurements of absolute viscosities, perhaps future
woric
with a rotating cylinder visoometer might be more pro-
titabY directed toward extension
of the upper and lower
portIons of the curves shown In Figures
7
and 8.
The shape
t
of a complete curve
of'
this kinc
should prove helpful in
understandinß the differences between fluidized solid
systema and true fluid systems.
32
CONCLUSI ONS
One:
A visoorneter of the type used in this investigation
can (with alterations suggested in text) be used with sorne
measure of success for determining relative values of apparent viscosities of fluidized solids.
Its reliability
as an absolute instrument is questiGnable.
Two:
The author believes that by careful control of con-
ditions, a rotating cylinder viscometer can be used to develop complete relationships between
shearing stress and
relationships could, perhaps, permit classification of fluidized
solid systems into one of the common rheologloal types.
shearing rate for fluidized solid systems.
It the lines shown in Figures
Three:
'1
Such
and 8 can be con-
sidered to represent the points, the fluid catalysts, Filtrol and 3A, act like true fluids in that the viscosity is
substantially independent of shearing rate,
over
the range
studied.
Four:
Filtrol
Five:
Over the range studied, the arparent viscosities of
trid
Catalyst 3A ere independent of apparent density.
The apparent viscosity of Filtrol is considerably
higher than that of Catalyst 3A.
The
values of viscosity
obtained by direct comparison to the calibreting fluid
about 22 and 12 centipoises respectively.
The values
are
33
computed on the
basis of
turbulent flow are about 44 and 29
centipoises reseotively. The latter are considered by the
author to be more nearly correct.
Handbook cf chemistry.
Handbook publishers inc., 1946.
1.
Lange, N. A.
2.
Parent,
3.
Rynning, D. F.
.
D., Yagol
L,
Sandusky, Ohio,
1767p.
and Steiner, C. S.
Fluidiz-
Ing processes, basic observations from laboratory
equipment. Chemical engineering progress, vol.
43, no.8, p.429-436. Aug.1947.
dered
Flow
catalysts.
characteristics of commercial
A thesis submitted to Oregon
pow-
State College, June 1947. 4 p.33.
4. Squires, L. and Dookendorff, R. L. Extending the useful rne of concentric cylinder visconieters. Industrial and engineering chemistry, analytical
editIon, vol.8 p.295-297 Jan.1938.
35
SAMI'LE CALCU LATI ONS
Critical Dimensions of Apparatus:
Inside diameter of fluidizing chamber - 8.562 inches
Distance from retaining plate to bottom of rotating
cylinder - 4.00 inches
Original Data from Run No. 22
Catalyst 3Á:
-
Initial weight of catalyst
9.55 Lbs.
Loss to bags during ran
stiinated bed height
z
0.11 Lbs.
=
9'75 Inches
Actuating weight, M,
= 120
Gma.
Time to fall 8 ft.
= 7.0
Seconds
Calculation of Viscosity by Direct Comparison to the
Glyoerol Solutions:
Average weight of oatelyst during run
0.11
9.5
1b.
Volume occupied by catalyst
??i(8.562J2(9.75)
1144)
(12)
-
O.Z2b ft.3
Apparent density of catalyst
-
0.325
9.7b - 4.00 :
575
Velocity, V, attLixied by
:
M
yratio
z
QQ
=
1.14
-
inches
flliu
1.14 ft/eec.
-
120
-
29.2 lbs/ft3
Coverage of rotating cylinder
::
-
gi sec/ft.
weight
-
-"J
ratio = 105
Entering Figure 4 with
gin
sec/ft and
5.7e inches, the viscosity is es-
cylinder coverage
timated as 12.eì ccratipoiaes1
Calculation of
Run on Basis of Turbulent Flow:
Sanie
Unit Shear Stress, S,
20.9 gins/inch of crl1nder covered
S =
Linear velocity of falling weight, L, is
previous calculation
L
ssrte
-
1.14 ft/sec
=
Density of ceta1yst,
____
=
Friction Factor,
0.469 gnia/oc
f'
= -
eL
(20.9)
(O.46C) (1.14)2
f'
Fron Figure 9, Re'
=
(0.46)(1.l4)
(0.0181
34 3
0.0181
2ì.3 eentijoises
s
V in
Oil
:un
Avg. Wt.
During
LTo.
:un-Lbs.
l-6
7
8
9
10
11
12
13
14
15
16
1'7
18
19
20
21
22
23
24
25
26
27
28
29
30
31
32
Est. Bed
Height
Inches
DATA FOR CATALYST 3A
Basis o Direct Comparison
Apparent
Density3
Lbs/Ft
1reliminary Orienttion Runs
20.2
14.
9.4
9.0
8.9
8.85
8.75
8.73
8.67
8.63
8.55
8.46
8.28
6.84
9.73
9.64
9.59
9.50
9.41
9.35
9.30
9.21
i.12
9.05
9.03
9.03
9.0
8.95
11.5
11.5
8.25
11.25
8.0
11.0
8.5
10.5
11.0
11.0
10.0
10.0
--10.0
9.75
10.5
11.5
10.2
10.7
9.0
9.75
8.5
9.0
9.1
10.5
23.5
23.2
32.2
23.4
32.7
23.7
30.4
24.4
23.1
22.6
20.5
29.2
--28.7
29.2
26.9
24.4
27.3
25.8
30.4
27.8
31.9
30.1
29.7
25.o
CY1imIer
Coverage
Inches
Actuating
Weight
Grams
10.
7.5
100
100
---
10E)
4.25
7.25
4.0
100
100
100
100
50
50
7.0
4.5
6.5
7.0
7.0
6.0
6.0
-6.0
5.75
6.5
7.5
6.2
6.'?
0
5.75
4.5
5.0
5.1
6.5
0
50
50
100
--120
120
100
100
100
100
120
120
120
120
120
120
Tie
to M
Fall 8 t Y
Gmsec/Ft
Secon.s
9.].
8.3
13.4
6.9
8.15
6.7
7.0
11.3
15.1
15.2
15.3
15.3
15.3
--6.8
7.0
11.2
9.0
8.1
8.6
6.0
6.4
6.5
10.5
6.0
6.7
114
103.8
---86.2
102
83.7
87.5
70.6
94.4
95.0
95.6
77.0
----
102
105
140
112.5
101.5
107.5
9'.0
96.0
97.5
157.5
90.0
1C0
Apparent
VIscosity
Ceritipoises
6.0
10.3
13.4
10.2
13.0
6.3
13.5
17.1
15.6
15.8
11.9
11.1
12.6
29.8
12.9
12.7
13.4
8.8
9.4
14.7
8.3
8.7
Avg.
Run
33
Z4
35
36
317
38
39
40
it.
Est. Bed
Apparent
Density3
Lbs/Ft
Cylinder
Coverage
Inches
Actuating
Weight
7.0
6.0
8.75
5.2
6.0
4.0
4.75
5.b
6.0
10
8.0
8.1
24.3
22.0
20.1
26.9
23.9
29.1
2G.0
21.3
29.6
30.7
27.9
29.0
26.2
30.5
28.9
28.b
24.8
33.2
32.2
35.5
29.6
29.4
23.3
29.7
29.0
7.5
14.0
11.75
11.75
30.9
24.8
28.8
28.7
During
Run-Lbs.
Height
Inches
8.90
8.80
8.52
8.25
7.98
7.77
11.0
12.0
12.75
9.2
10.0
8,0
7.J9
8.
6.175
9.5
10.0
9.6
10.o
10.0
11.0
9.4
9.9
4].
9.8'?
42
43
44
45
46
9.82
9.7b
9.67
9.62
47
48
49
50
51
52
53
54
55
56
9.52
9.49
9.43
9.41
9.40
9.38
9.36
9.30
8.95
7.92
57
58
59
'7.83
9.5'l
60
sea
7.74
11.54
61
62
11.31
11.25
10.0
11,4
8S5
8.75
8.4
9.5
9,5
U.5
n- -
.6
6,5
6.0
?0
5.4
5.9
6.0
7.4
4.5
4.75
4.4
5.5
5.5
7.5
4.0
4.1
n-
3.5
10.0
7.75
7.75
Grains
120
120
100
100
100
100
100
150
150
130
130
130
130
130
10
130
130
130
130
130
130
130
150
150
___
150
200
200
200
Time to
M Ratio
Fall 8 Ft V'
Seconds Gri3eo/Ft
6.5
7.3
8.3
7.4
8.6
7.5
8.2
7.9
6.3
9.1
7.1
7.5
6.75
7.3
5.9
6.2
6.8
5.6
5.9
12.4
6.2
5.7
7.8
6.0
5.3
se e
4.?
6.0
10.8
6.3
97.5
109.7
124.5
92.5
107.5
93.8
102.j
98.9
118
171
115.3
122
110
118.5
Apparent
Viscosity
Centipolses
7,0
11.2
12.3
15.7
18,5
19.2
14.0
13.0
42.5
12.7
17.5
94
14.4
9b.9
10].
110.5
91.0
9b.9
202
101
92.6
126.8
112.5
99.4
n-
88.1
150
270
157.5
8.?
8.8
10.0
11,5
10.6
13.?
23.7
13.6
11.0
8.5
15.1
Avg.
Run
No.
63
64
65
66
67
lit.
During
Run-Lbs.
10.23
9.70
9.24
9.0
8.8
Est. Bed
Height
Inches
11.0
10.5
10.0
9.0
10.0
Apparent
Density
Lbs/Ft3
2'1.9
2?.?
2?.?
30.0
26.4
Cylinder
Coverage
Inches
7.0
6.5
6.0
5.0
6.0
Actuating
Weight
Grams
200
200
200
200
200
Time to
M
FaI]. 8 Ft Y
Seconds Cmsec/Ft
5.6
5.6
Apparent
Viscosity
Centipoises
12.2
14.2
6.8
7.7
140
140
105
192.5
4.7
1).?.5
9.0
4.2
DATA POR PILTROL
On Basis of Direct Corjaon
Run
kvg. Wt.
ist. Bed
During
HeIght
inches
RuLbs.
88
69
70
71
92
73
74
'75
76
7?
78
79
80
81
82
83
84
65
86
87
68
69
90
91
92
93
94
U8
11.40
fl3
11.32
11.26
11.22
11.10
10.96
1O.?8
10.60
11.8
11.59
11.55
11.48
11.42
11.40
11.38
11.30
11.20
11.09
10.92
10.63
10.42
10.33
10.27
10.10
9.60
13.0
10.5
11.2$
10.5
10.0
9.0
12.0
10.0
12.0
9.75
12.0
10.5
11.75
11.0
11.0
10.5
11.25
11.0
12.0
U.S
13.75
14.00
12.00
11.00
10.50
12.00
12.50
Apparent
Density
Lbs/Pt3
Cylinder
Coverage
Inches
2.9
9O
2.6
60.3
32.4
33.8
37.4
27.8
32.9
26.9
32.6
29.5
33.1
29.5
31.3
31.1
32.6
30.3
30.8
28.0
28.9
23.8
22.8
26.4
28.1
29.4
25.2
23.0
8.5
7.25
6.5
6.0
LO
8.0
5,0
6.0
5.75
8.0
8.5
7.75
7.0
7.0
8.5
7.25
7.0
8.0
75
9.75
10.0
8.0
7.0
8.5
8.0
8.5
Actuating
Weight
grains
OO
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
to M
Ratio
Pa13. 8 Pt V
Seconds UnSeo/Ft
Time
7
?eO
7.9
9.0
e.
7.0
9.4
7,8
9.5
8.4
8.9
8.0
9.3
8.3
7.9
7.1
'7.9
7.6
8.1
7.8
8.8
8.?
7.2
7.8
8.8
8.3
8.0
167.5
131.1
148.1
169
167
131.1
176
142.5
178
120
16?
150
174.5
156
148
133
148
142.5
152
142.5
165
163
135
146
127.5
156
150
Apparent
Gentipoissa
13.8
164
19.9
36.5
39.3
26.4
28.4
25.0
29.6
15.1
24.0
25.4
29.8
25.0
21.1
17.2
19.8
18.8
18.].
18.7
16.8
12.6
12.5
20.2
15.0
19.8
16.0
to
Run
1 o.
J
Avg. Wt.
Est. Bed
Dtiring
fleight
Run-Lbs.
Inohea
Apparent
Density3
LbsJFt_
95
96
11.80
12.5
28.3
1L55
125
2'?.?
9'?
11.34
i5,5
25.2
1.5
22.2
26.4
25.9
24.0
31.b
20.9
98
99
loo
101
102
103
104
10513
9.67
9.50
9.20
ê..c'5
7.5
11.0
.11,0
11,5
8.5
10.75
Cylinder
Goverage
Inches
8.5
8.5
9.5
e_e
9.5
7.0
70
?5
4,5
6,75
Actuating
Weight
_z,ams
100
100
100
___
100
100
100
100
100
100
Tinie
to
tio
Fall 8 Ft
SOOOfld8
GmSec/Ft
Apparent
Viscosity
Cnt1po1aes
12.0
12.4
12.4
150
155
155
23.3
65.3
11.9
11.9
10.6
11.2
7.8
8.9
149
149
132.5
140
97.5
111
19.4
30.8
22.4
23.3
17.9
14.5
l.5
Roçresent unsuccessful attempts to fluidiz a third cita1yst
o
Avg. Wt.
ist. Bed
During
Run-Lbs.
Height
Inches
139
140
141
142
10.9?
10.68
10.73
143
144
145
146
147
148
149
150
151
152
153
154
155
156
157
158
10.48
10.39
10.29
10.16
10.03
9.81
9.47
9.04
10,0
12.0
12.2
11,0
11.5
11.0
11.75
10,2
11.0
11.25
10.75
Run
!22
159
180
161
182
163
164
165
188
167
168
1058
8.].
10.83
10.60
10.37
10.1
9.86
10.84
10.64
10.48
10.09
9.81
9.75
9.4
9.16
8.96
8.84
9.95
9.85
1O.
10.5
13.0
13.0
9.25
12.5
10.0
11.0
10.9
13.0
12.2
10.5
11.75
11.50
11.50
10.0
12.0
11.5
11.25
Apparent
Density
Lbs/Ft3
Cylinder
Coverage
Inches
Actuating
Weight
Grams
32.9
27.2
26.4
28.8
27.4
28.3
26.2
29.9
27.4
26.2
26.4
25.8
22.9
25.0
24.4
33.6
24.2
29.6
29.5
29.3
24.2
24.7
28.0
24.9
24.5
23.9
28.9
21.6
26.0
26.3
6.0
8,0
100
100
100
100
100
100
100
100
100
100
100
loo
100
93
93
93
93
93
93
93
93
93
113
100
8.2
7.0
7.5
7.0
7.75
6.2
7.0
7.25
6.75
6e5
6.5
9.0
9.0
5.25
8.5
6.0
7.0
6.9
9.0
8.25
6.5
7.75
7.5
7.5
6.0
8,0
7.5
7.25
100
100
120
120
120
120
Time to
Fall 4 Ft V
Seconds GmSec/Ft
5.15
5.6
5.64
5.5
5.4
5.5
5,54
4.88
5.30
5.30
5.30
4.90
4.80
8.4
8.0
o,15
6,0
5.3
5.6
5.85
6.8
6.35
4.68
5.0
5.7
5.75
4.5
4,83
4.8
5.35
Apxent
Viscosity
Contlpoises
129
140
141
137.5
135
28.8
20.9
20.6
24.8
137.5
138.5
122
132.5
132.5
132.5
122.5
120
149
24.8
21.6
21.7
22.4
21.2
1.40
120
140
123
130
136
158
147.5
137
125
142.5
144
135
145
144
160.5
21.].
24.
20.1
19.0
21.1
18.0
27.2
19.4
23.0
21.2
24.4
24.4
23.3
23.8
16.4
24.5
25.2
28.2
17.0
18.0
25,5
Avg. Wt.
Est. Bed
No.
During
Run-Lbs.
Reight
Inches
Apparent
Density3
Lbs/Ft
Cylinder
Coverage
Inches
Actuating
Weight
Grams
169
170
171
172
9.75
9.5?
9.19
8.95
8.5
30.0
22.1
22.0
22.4
19.2
5.75
9.0
8.5
8.0
8.5
120
120
173
9.75
13.0
12.5
12.0
12.5
Run
120
120
120
Time to M
Fall 4 Ft V Ratio
Seconds GmSec/Ft
5.15
5.4
5.54
4.75
4.82
154
162
185
142.5
145
Apparent
Viscosity
Centipoies
23.0
26.?
19.0
18.3
RECALCULATION OF 3A DATA
O
Basis of Turbul3nt Flow
s
.ctuatir
Run
eight
çkmø.
7
8
g
lo
u
:1.2
15
14
15
le
l'F
18
19
20
21
22
23
24
25
26
27
28
29
30
100
100
loo
loo
100
ioo
100
50
50
50
50
50
100
100
120
120
130
100
100
100
120
120
120
120
Shear
8tr388
Cylinder Gms/Iioh
Coverage Cylinder
Inches Coverc
10
'7.5
--4.25
7.25
4.0
7.0
4.5
6.5
7.0
7.0
6.0
5.0
--8.0
5.75
6.5
7.5
6.2
6.7
5.0
5.7
4.5
5.0
10
13.35
--23.5
13.8
25.0
14.3
11.1
7.'?
17.15
7,1
8.34
----20.0
20.9
15.4
13.3
16.1
14.9
24.0
20.9
26.7
L
Linear
Velocity
of Wt.
Ft/Sec
0.88
0.964
--1.16
0.981
1.19
1.14
0.530
0.526
0.522
0.65
0.524
--1.10
1.14
0.715
0.89
0.988
0.93
1.33
1.25
1.23
0.762
Re'
r'
to
-
Appareit
Densit
Lbs/Pt
in
Z
From
Curvo
;oises
24.8
2G.3
GmsJo.
p
20.2
23.5
23.2
32.2
23.4
32.7
23.7
30.4
24.4
23.1
22.6
20.5
29.2
0.324
0.377
39.9
38.1
--33.8
38.1
33.6
28,9
45.5
70.0
89.7
72.3
60.0
---
0.0115
0.0138
28.7
29.2
26.9
24.4
27.3
25.8
30.4
27.8
31.9
30.1
0.481
O.46?
0.431
0.392
0.436
0.414
0.486
0.446
0.512
31.1
34.3
69.8
42.8
37.7
41.6
27.8
0.0208
0.0181
0.00575
0.0116
0.0151
0.0128
0.0266
0.0224
0.0192
--
0.515
O.5?8
0,825
0.381
0.488
0.392
0.371
0.363
0.32e
---
j
30
34.4
Cetìti.-
---
0.0199
0.0139
0.0208
0.0223
0.0124
0.0058
0.00564
0.00534
0.00745
30.1
2G.5
30.0
19.5
217.8
35.8
34.7
35.5
28.7
---
26.2
29.5
53.7
30.1
28.6
30.5
24.4
24.9
32.8
s
At,tua-
Run
31
32
33
34
35
3f)
37
38
39
40
41
42
43
44
45
46
47
48
49
50
51
52
53
54
55
56
57
56
ting
YVeiht
Cylinder
______
Inche9
120
120
120
120
120
100
100
100
100
100
150
150
130
130
130
130
130
130
130
130
130
130
130
130
130
150
150
150
Coverat
5.1
6.5
7.0
8.0
8.?5
5.2
6.0
4.0
4.75
5.5
6.0
5.8
6.5
6.0
7.0
54
5.9
5.0
7.4
4.5
4.75
4.4
5.5
5.5
7.5
4.0
4.1
---
She r
Stress
Gms/Inch
Cylinder
Covered
23.5
18.5
17.2
15.0
13.7
19.2
16.17
25
21
18.2
25
26.8
20
21.?
18.6
24.1
22.0
21.7
17.6
28.9
27.4
29.6
23.8
23.8
17.3
3'7.5
36.6
---
L
Linear
Velocity
of Wt.
FtJ3e,
1.33
1.19
1.23
1.10
0.965
1.08
0.931
1.07
0.976
1.015
1.27
O.t8
1.12?
1.06?
1.185
1.095
1.356
1.29
1.1??
1.43
1.355
--1.29
1.405
1.02
1.332
1.51
---
(o
Re'
f'
L
Apparent
Density
Lbs/Tt3
29.7
25.6
24.
22.0
20.1
26.9
23.9
29.1
26.0
21.3
29.6
30.7
27.9
29.0
26.2
30.5
28.9
28.5
24.8
33.2
32.2
33.5
29.6
29.4
23.3
29.4
29.0
-
Troni
rve
Gins/cc.
0.47?
0.411
0.39
0.352
0.323
0.431
0.384
0.467
0.417
0.342
0.475
0.493
0.448
0.485
0.421
0.490
0.464
0.458
0.398
0.533
0.517
e-0.475
0.472
0.374
0.476
0.465
27.8
31.?
29.2
35.2
45.5
38.1
5Q.1
48.?
52.9
31.6
32.6
70.3
35,2
41.0
31.4
41.0
25.8
28.5
31.9
26.6
28.8
--
29.9
25.3
44.4
44.3
34.6
0.0267
0.0195
0.0219
0.0153
0.0099
0.0157
0.00975
0.0121
0.0096
0.0098
0.0195
0.0075
0.0164
0.0134
0.0193
0.0139
0.0269
0.0243
0.0188
0.030
0.0256
-e0.023
0.0305
0.0108
0.0131
0.0195
in
Con tiSOS
23.8
25.1
21.9
2.3
31.5
29.?
38.?
41.2
4.4
38.2
30.9
57.9
30.8
37.4
25.9
38.6
21.8
24.3
25.2
25.4
27.2
---.
26.?
21.8
35.3
48.5
36.0
s
Run
No.
59
60
61
62
63
64
65
66
87
Actuating
Weight
Shear
Stress
Oms.
Cylinder
Coverage
Inches
150
200
200
200
200
200
200
200
200
3.5
10.0
7.75
7.75
7.0
8.5
8.0
5.0
6.0
Gins/Inch
Cylinder
Covered
Linear
Velocity
of' Wt
FtJSep
20
1.70
1.33
25.8
25.8
28.6
30.8
33.3
40.0
33.3
1.27
1.43
1.43
1.905
--1.7
42.9
r'
L
----
Apparent
Density
Lbs/Ft3
Oms/co.
30.9
24.8
28.8
28.7
27.9
27.7
27.7
30.0
26.4
0.496
0.398
--0,461
0.448
0.445
0.445
--0.424
S
-
Re'
A
p
=
FrODi
Conti-
L
Curve
poises
29.9
28.4
0.0255
0.020
32.8
26.5
34.8
31.2
33.9
20.6
--27.2
0.0161
0.0195
0.0174
0.0434
36.5
32.8
36.6
19.6
---
0.0262
27.5
RECALCULATION OF FILThOL DATA
Basis ot Turbul,nt Flow
s
Stress
Run
Wt
Gs.
68
6g
70
71
'72
73
474
75
'76
7'?
78
79
80
81
82
83
84
85
86
8?
88
89
90
91
92
93
200
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
150
Cylinder
Coverage
Inches
9.0
6.5
7.25
6.5
6.0
5.0
6.0
6.0
8.0
5.75
8.0
6.5
7.75
7.0
7.0
6.5
7.25
7.0
8.0
7.5
9.75
10.0
8.0
7.0
6.5
8.0
Appliect
Grns/Inoh
çoverge
222
23»].
2O?
23e].
25.0
30
1SO?5
2.0
18.75
26.1
18.75
23.1
19.35
21.4
21.1
23.1
20.7
21.4
18.75
20.0
15.4
15.0
18.75
21.4
23.1
18.75
L
Linear
Velocity
of Wt.
Ft/Sec
l.l
1.14
1.013
0.89
0.90
1.14
0.851
1.052
0.842
1.25
0.90
1.0
0.86
0.964
1.01
1.13
1.01
1.052
0.988
1.052
0.91
0.92
1.11
1.025
1.175
0.964
°
Deneity
Lbs/Ft
26.9
32.6
30.3
32.4
33.8
37.4
27.8
32.9
26.9
32.6
29.5
33.1
29.5
31.3
31.1
32.8
30.3
30.8
28.0
28.9
23.8
22.8
26.4
28.1
29.4
25.2
i'
'
Densit
Gms/Cm'
S
:
,"-
pojp
_______
0.431
0.524
0.486
0.520
0.543
0.80
0.446
0.528
0.431
0.524
0.474
0.531
0.474
0.503
0.50
0.524
0.486
0.495
0.45
0.464
0.382
0.366
0.424
0.451
0.472
0.405
Viscosity
Conti-
35.4
34.0
41.4
56.0
56.9
38.5
57.9
4e.?
61.2
51.9
48.9
43.5
55.3
45.9
41.9
34.6
41.6
39.1
42.?
39.0
48.7
48.4
35.9
45.1
35.4
49.9
0.0137
0.0174
0.0123
0.0081
0.0061
0.0154
0.0071
0.0126
0.00548
0.0204
0.0092
0.0118
0.00767
0.0105
0.0121
0.0169
0.0121
0.0134
0.0113
0.0132
O.U085
0.0083
0.0149
0.0108
0.0163
0.0089
37.5
34.3
40.0
57.1
50.3
44.4
53.5
44.1
56.1
32.1
46.4
45
53.1
46.1
41.7
35
40.6
38.8
39.4
37.0
41.0
40.6
31.5
42.8
34.0
43.9
C-'
s
Mees
or
Ru.n
t
!2..
y4
95
98
97
go
99
loo
101
102
103
104
:1:38
139
140
141
142
14.3
144
145
146
147
148
149
150
ibi
152
153
154
mo
iCjO
100
100
i oo
100
i.00
100
lO(
lOO
100
Coerege
Stress
ppi1e
Gnw/Inoh
Inobes
Coyerae
Cylinder
8.5
8.5
8.5
9.5
17.65
1].7
11.75
10.6
-- a
L
Linear
Velociti
of Wt.
FtISeo
1.0
0.668
O.45
0.545
a
9.5
7.0
7,0
7.5
10.5
14.3
O.72
O.72
143
45
13.3
22.2
0.755
0.715
1.025
6,95
148
090
.Ç
Re'
f'
Density
S
Densit;
Gíns/Cm
Lbs/It'-'
_______ _____ ______
23.0
28.3
27.7
25.2
ee
22.2
28.4
25.9
24.0
31.6
20.9
0.369
0.455
0.445
0.403
..
.
.e
O.53
0.424
0.416
0.385
0.508
0.336
,Á-
47.8
58.2
53.5
62.2
ee
65.2
74.?
80.2
67.5
41.8
59.9
Represent unsuocesstui. attempts to fluidize a third catalyst.
100
6.0
16.?
0.776
32.9
0.529
52.4
100
8.0
12.5
27.2
0.714
0.436
5.3
8.2
100
12.2
O.'FlO
26.4
0.424
57.1
100
7.0
14.3
0.727
28.8
0.462
58.5
7.
100
13.3
27.4
0.74
0.44
55.2
100
7.0
14.3
0.727
28.3
O.44o
60.8
'1.75
100
l.9
0.72
26.2
0.421
58.?
6.2
100
18.15
0.82
29.9
0.480
50.1
100
7.0
14.3
0.?5b
27.4
0.44
57.1
100
7.25
13.8
0.755
25.2
0.421
5'7.4
100
6.75
14.8
0?55
26.4
0.424
61.1
100
8.5
15.4
0.818
25.8
0.415
55.7
100
8.5
lb.4
22.?
60.7
0.634
L.365
93
9.0
10.3
0.645
Eb.0
0.401
6b.6
93
9.0
10.3
0.686
24.4
0.392
59.1
5.25
93
17.7
0.776
33.6
0.54
54.5
Viscosity
Conti-
roisea_
0.0093
3.7
O.O385
44.3
47.5
48.?
0.03605
0.0059
.s
.
O.O55
0.0051
0.0370
0.0058
0.0143
0.00715
0.00918
0.00738
0.00719
0.00730
0.00775
0.00692
0.0070
0.003
0.00753
0.0074
0.00693
0.00312
C.00712
0.00564
0.00653
0.00905
a
43.1
55.3
4z,.O
47.5
3.4
42.3
44.8
42.2
41.9
46.0
42.0
48.8
43.5
41.0
44.1
43.0
48.2
41.'?
42.8
44.5
40.1
46.3
s
Mass
of
Run
g
1b5
156
15'?
158
159
160
181
162
163
164
165
167
168
169
170
171
172
173
Wt
Gms
93
93
93
93
93
93
93
100
100
100
120
120
120
120
120
120
120
120
120
Cylinder
Coverage
Incthes
8.5
6.0
7.0
6.9
9.0
8.25
6.5
7.75
7.5
7.5
6.0
8.0
7.5
7.25
5.75
9.0
8.5
8.0
8.5
Stress
Applied
Gm/Inoh
ÇçeraKe
10.9
15.5
13.3
13.5
10.3
11.3
14.3
12.9
13.35
13.35
20.
15.0
16.0
16.8
20.9
13.3
14.1
15.0
14.1
L
Linear
Velocity
of Wt.
Ft/Seq
0.668
0.755
0.715
0.885
0.588
0.63
0.824
0.80
0.702
0.895
0.89
0.829
0.835
0.748
0.776
0.74
C.722
0.842
0.83
(o
DensltL
Den8it
Lbs/Ft
Grns/Cm°
24.2
29.6
29.5
29.3
24.2
24.7
28.0
24.9
24.5
23.9
26.9
21.6
26.0
26.3
30.0
22.1
22.0
22.4
19.2
0.389
0.475
0.474
0.470
0.389
0.397
0.450
0.40
0.393
0.384
0.431
C.34?
0.417
0.422
0.481
0.355
C.353
0.380
0.308
Re'
f'
-
-/-
_______
63.1
57.2
55.0
61.2
76.8
71.7
46.9
50.4
68.9
72.1
58.5
63.0
55.1
70.0
72.0
88.2
76.5
58.8
66.5
0.00609
0.00803
0.0080
0.00683
0.00455
0.00515
0.0105
0.00867
0.00565
0.00525
0.00777
0.00625
0.0078
0.0055
0.00575
0.00532
0.00485
0.0089
0.00585
,AA
Viscosity
Centi
poises
42.8
44.7
42.4
47.1
50.3
48.5
35.3
37.0
45
50.8
49.3
46.0
44.5
56.5
49.4
54.9
44.0
45.3
AL1BRATIUN DATA
Soin.
Temp.
of
Tie to
Fall 8 Ft
seconds
Actuting
Viscosity
Ceatiroises
Weight
Gais
Depth of
Glycerol
olution
inobes
Cove rage
or
Rotsting
Cylinder
Inc h es
y =
Linear
Velocity
of
ct.%t.
ìatio
it'
V
GSec
Ft
Ft/See
C'
Solution
72
72
'72
72
92
?2
72
72
72
72
72
72
72
72
71.'?
7],'?
71.?
71.?
71.7
71.?
j.
- Spec.
19.6
19.6
19.6
19.6
19.6
l9.0
l'p/o
150
loO
loo
8.9
11.6
10.1
7.8
:iso
.
o.
C'
-
1.1797
9.6
9.8
9.1
8.1
1170
19.6
19.6
19.6
19.6
19.6
29.9
29.9
29.9
29.9
29.9
29.9
29.9
29.9
Gray.
150
150
lÇì.G
Solution
71.7
71.?
o.
)70
150
120
100
120
'1.0
)(:C
75
.-,
opec.
100
150
200
100
200
150
250
150
6.6
7.8
9.0
6.6
20°
r'
145
10.8
9.0
13.8
7.2
10.1
6.2
8.8
14.0
14.0
14.0
i3.0
13.0
13.0
11.0
11.0
11.0
9.5
9.5
9.5
8.0
8.0
= 1.1923
14.0
14.0
14.0
13.0
13.0
13.0
11.0
11.0
t.fr
Gly ,erol =
10.0
10.0
101.0
9.0
9.0
9.0
7,0
7.0
?,o
5.5
5.5
5.5
4.0
4.0
Wt.
10.0
j.o.o
10.0
9.0
9.0
9.0
7.0
7.0
69.44
0.834
180
0.816
184
0.880
193
0.988
17
0.900
167
0.690
145
0.792
126
1.027
148
1.142
149
1.212
124
1.026
117
0.389
113
1.212
99.0
1.068
93.6
Glycerol = 74.05
0.549
0.741
0.889
0.580
1.111
0.785
1.29
0.9].
182
25
172
180
191
194
165
*0
Coverage
M
Soin.
Temp.
of
Vi800sity
Centipoises
Actuating
Weight
Oms
Depth of
Glycerol
Solution
Inches
Time to
Fall 8 Ft
Seconds
of
Rotating
Cylinder
Inches
V
Linear
Velocity
otAct.Wt
Ft/Sec
tb0
QrnSec
Ft
Solution No. 2 (Continued)
71.7
71.?
71.7
71.7
71.7
71.7
71.7
29.9
29.9
29.9
299
29.9
29.9
29.9
ibO
100
150
170
100
120
150
11.4
10.2
49.5
49.5
49.5
49.5
49.5
49.5
49.5
49.5
49.1
47.5
47.5
47.3
47.3
47.3
46.8
46.8
150
150
100
100
200
200
200
100
150
100
150
200
100
150
200
100
9.5
9.5
9.5
8.0
8.0
8.0
?i
r4
8.4
7.5
6.5
Solution No, 3 - Spec. Gray.
64.8
64.8
64.8
64.8
C4.8
64.8
64.8
64.8
65.0
66.1
oo.i
66.2
66.2
66.2
66.5
66.5
11.0
Ç
C
1.2002
6,8
8
8,9
9.2
s.4
5.4
5.1
8.5
6.2
141.0
'1.2
11.0
11.0
11.0
5,3
4.2
6.2
4.5
3.7
5.1
14.0
14.0
14.0
14.0
14.0
13.0
13.0
L.0
95
9.5
9.5
8.0
7.0
b.5
b.5
b.:,
4.0
4.0
4.0
0.701
0.785
1.013
1.08
0.953
1.067
1.27
t.%:G1yeero1
10.0
10.0
10.0
10.0
10.0
10.0
9.0
9.0
9.0
7.0
7.0
7.0
5.5
5.5
4.0
O.6U
0.811
0.450
0,435
O"/4l
0?4i
0.785
0.471
0.645
0.556
0.755
0.953
0.845
0.890
1.08
0.785
l42.
127.5
148
157.5
105
112.5
118
77.0
245
245
222
230
269
269
255
212,
232.
180
198.5
210
155
168.5
185
129
ci,
o
M
Soin.
Temp.
F
Viscosity
Centipoise
Time to
laU 4 Ft
Depth of
1yoero1
Solution
Coverage
ot
Rotating
y11nder
V :
Linear
Veloolty
_SeQofld8
Jnches
Jnohes
It/Seo
:
Actuating
Weight
Gma
V
orot. Wt
Rati
Gse
Lt
Solution No. 3 (Cont1nuo)
66.5
66.5
46.8
46.8
Solution No. 4
69.2
69.2
69.2
69.2
69.2
69.2
69.0
69.0
62.0
69.0
69.0
62.0
69.0
69.0
69.0
69.0
69.0
69.0
89.0
69.0
69.0
69.0
9.65
9.&ç
9.6
9.65
9.85
9.65
9.'70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
150
200
3.8
3.1
- Spec. Gray.
100
100
150
153
200
200
200
150
150
100
100
100
100
150
150
120
120
100
100
120
120
20C
5.15
5.25
.95
4.00
3.32
.30
3.62
p.95
3.5
3.58
4.40
4.52
3.95
4.00
3.10
3.10
3.62
3.62
3.58
3.58
3.19
3.02
E.O
8.0
1.i49'7
1.
14
14
14
14
14
13
13
13
13
13
13
1].
11
1].
U
U
11
9.5
9.5
9.5
9.5
4.0
4.0
Nt.%
1.O5
1.29
G1yoeo1
10.0
10.0
10.0
10.0
10.0
10.0
9.0
9.0
9.0
9.0
9.0
9.0
7.0
7.0
7.0
7.0
7.0
7.0
5.5
5.5
5.5
5.5
142.5
155.0
58.51.
O.77&
129
0.761
1.012
1.00
1.205
1.213
1.325
1.355
1.142
1.117
0.910
0.885
1.012
3.00
1.29
1.29
1.104
1.104
1.118
1.118
1.253
1.322
131.2
148
150
156
155
151
147.5
131.5
134.2
110
113
98.9
100
116.5
116.5
108.5
108.5
89.5
89.5
95.8
90.8
(JI
M =
Soin.
F
Viscosity
Centiioises
Actuating
Woigìt
Gni
Time to
Fall 4 Pt
Seconds
Depth ot
Glycerol
Solution
Inob.ee
Coverage
of
Rotating
Cylinder
Inohea
V
Linear
Velocity
otAct.Wt
It/Seo
M &tio
V
Gin$eo
Solution No. 4 (Continued)
69.0
69.0
6S.0
69.0
69.0
69.0
69.0
o1ution No. 5
68.0
63.0
68.0
88.0
68.0
68.0
68.0
68.0
88.0
68.0
66.0
68.0
68.0
68.rO
68.0
68.0
68.0
150
150
--100
100
120
120
9.70
9.70
9.70
9.70
9.70
9.70
9.70
12.8
12.8
12.8
12.8
12.3
12.8
12.8
12.8
12.8
12.8
12.8
12.8
12.8
12.6
12.8
12.8
12.8
-
29
95
----
--8.0
8.0
8.0
8.0
3.19
3.11
2.73
2.98
3p80. Gray.
100
100
150
150
200
200
200
200
150
10
100
100
170
110
150
150
100
.5
2.8
20
5.4
b.6
4.4
4.38
3.60
3.78
3.3
3.2
3.82
3.70
4.8
4.95
3.0
3.0
3.4
3.3
4.29
1.1603
14.0
14.0
14.0
14.0
14.0
14.0
13.0
13.0
13.0
13.0
13.0
13.0
11.0
11.0
11.0
11.0
11.0
5.5
5.5
--4.0
4.0
4.0
4.0
1.38
1.43
--1.253
1.287
1.485
1.342
wt.% Glycerol
10
10
10
10
10
10
9
9
9
9
9
9
7
7
7
7
7
108.8
105.0
79.9
'77.7
82.0
894
61.3
0.746
0.715
0.910
0.914
1.112
1.06
1.21
1.25
1.048
1.08
0.834
0.809
1.33o
1.28
1.178
1.211
0.934
135
140
165
164
180
189
165
160
143
139
120
124
127.5
132.3
127.5
124
10?
M
Soin,
Temp.
°F
Viscosity
Oentipoizes
=
Actuating
Weight
Ums
Time to
Fall 4 Ft
Seconds
Depth o
Glycerol
Solution
Inobes
Coverage
V
of
flotating
Linear
Velocity
afAot.Wt
Ft/8eo
Cylinder
Inches_
:
M Ratio
V
Gmea
________
Solution No, 5 (Continued)
880
88,0
68,0
68.0
u8.0
68.0
68.0
12,8
l28
12.8
12.0
12.8
12.8
12,3
loo
100
100
150
150
120
120
4,35
3.89
3.80
2.5
3.1
34
3.43
11,0
0.45
9.45
3.45
3,45
9,45
9.45
7
b45
5.45
.45
5.45
45
45
0,920
1,03
1.053
1.355
1,29
1.18
1.167
108,7
97
95
111
118
102
103
01
aiCALCULATION OF CALIBRATION DATA
On Basis Of Turbulent Flow
s
Coverage
Viscosity
Centipoises
Actuating
Weight
solution AO.
Gins
i -
19.6
19.6
19.6
19.6
19.6
19.6
19.6
19.6
19.6
19.6
19.6
oiut1on Nc. E
170
150
100
100
150
170
150
120
100
120
100
29.9
29.9
29.9
29.9
29.9
29.9
29.9
29.9
29.9
of
ff
= 1.1?.7 Gins/ce.
9.0
9.0
9.0
7.0
7.0
7.0
5.5
.5
5.5
4.0
4.0
-
1.19L3 Gins/ce.
100
9.0
9.0
9.0
200
150
250
150
100
100
150
170
100
7.0
7.0
7.0
5.5
5.5
5.5
4.0
L
3hoar Atress
Gms/Inøh
Cylinder
overod
Linear
L
Velocity
Ft/Aee _______
Glycerol =
18.9
16.7
11.1
14.3
21.4
24.3
27.3
21.8
16.2
30.0
25.0
0.968
0.900
0.690
0.792
1.027
1.142
1.212
1.026
0.889
1.c12
1.068
wt.% Glycerol 11.1
22.2
16.7
35.7
21.4
14.3
18.2
27.3
30.9
25.0
Re'
0.580
1.111
0.785
1.29
O.10
u.?01
0.785
1.013
1.080
0.953
f'
3
_______
69.44
O.OS4
0.0541
0,0414
0.0476
0.0617
0.0685
0.078
0.0616
16.4
17.b
19.8
19.35
17.2
15.8
0.054
O.O79
17.6
19.6
17.3
0.0641
1.6
74.05
0.0231
---
27.7
0.0313
0.0514
0.0362
0.0280
0.0313
0.0403
0.043
0.0379
22.8
18.0
21.7
24.4
24.9
22.3
29.2
23.2
Coverage
_,4
ViscosltI
Centjpolses
otuating
Weight
Gma
L
s
of
Shear Stress
Rotating
Cylinder
Inches
Gins/Inch
Cylinder
Covered
Re'
f'
Linear
Velocity
Ft/Sec
,"
1.087
1.27
0.0425
0.0506
22.15
19.5
0.0191
0.01145
0.01405
0.0191
0.0242
0.0166
0.0226
0.0277
0.0201
0.0270
0.0331
30.0
41.6
33.4
38.5
31.3
26.3
36.4
28.7
26.0
33.8
26.2
25.0
0.157
0.1605
0.1352
0.1322
0.1078
0.1048
0.120
11.0
10.52
11.1
11.62
11.6?
12.32
12.14
soittien Jo, 2 (Contintiod)
29.9
29.9
3.20
ibO
Solution No. 3 49.5
49.5
49.1
47.5
4p1.5
4173
4r/.3
47.3
46.8
468
46.8
46.8
200
100
10
100
150
200
100
150
200
100
150
200
Solution No. 4 9.70
200
9.70
200
9.70
9.70
9.70
9.70
9.70
150
150
100
100
100
4.0
4.0
1.2002 Gma/co.
9.0
9.0
9.0
7.0
'70
7.0
5.5
5.5
5.5
4.0
4.0
4.0
- 1.1497 Gins/co.
9.0
9.0
9.0
9.0
9.0
9.0
7.0
30.0
3'7.5
Wt.% Glycerol
22.2
11].
16.7
14.3
21.43
28.6
18.2
27.3
36.4
25.0
37.5
50.0
??.O
0.785
0.471
0.645
0.556
0.755
0.953
0.645
0.89
1.08
0.785
1.052
1.29
O.O15'Th
Wt.% Glycerol - 58.51
22.2
22.2
18.7
16.7
11.1
11.1
14.3
1.325
1.355
1.142
1.117
0.91
0.885
1.012
UI
J»
-,
Viscosity
Cantipoises
Actuating
Weight
Gma
Coverage
of
Rotating
Cylinder
Inches
S
Shear Stroas
Gas/Inch
Cylinder
Covered
L
Linear
Velocity
FtíSep
Re'
f'
S
,,u
______
Solution No. 4 (ContInued)
9.70
9.70
g.7o
9.,,
9.90
9.?O
9.70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
9.70
100
150
150
120
120
loo
100
120
120
150
150
100
100
120
120
o1ution No. 5 -
12.8
12.8
12.8
12.8
12.8
12.8
12.8
12.8
12.8
200
200
150
150
100
100
170
170
150
7.0
7.0
'7.0
7.0
?.O
5.5
5.5
5.5
5.5
5.5
5.5
4.0
4.0
4.0
4.0
- 1.1603 Gins/co.
9.0
9.0
9.0
90
9.0
9.0
7.0
7.0
7.0
17.5
21.4
21.4
1?.15
1T.15
18.2
18.2
21.8
21.8
27.3
1.00
2.29
.29
1.104
].104
1.118
3.118
1.253
1.322
1.38
2'7.3
143
25.0
25.0
30.0
30.0
1.253
].287
1.465
1.342
0.1185
0.153
0.153
0.131
0.131
0.1324
0.1324
0.1485
0.1566
0.1635
0.1694
0.1485
0,152
0.1735
0.159
12.42
11.2
11.2
12.22
12.22
12.6?
12.6?
12.05
10.85
12.45
11.60
13.84
13.12
12.15
14.45
0.1097
0.1132
0.095
0.0979
0.0755
0.0733
0.121
0.1165
0.1068
12.5
11.7
13.1
12.4
13.78
14.62
11.72
12.68
13.3
Wt.% Glycerol = 61.3
22.2
22.2
16.?
16.7
11.1
11.1
24.3
24.3
21.4
1.21
1.25
1.048
1.08
0.834
0.809
1.335
1.285
1.178
//tÁ
Aotuatjn
Viscosity
CentIpo1se
Wtght
Gms
Coverage
of
Rotating
Cylinder
Inohes
S
Shear Stress
i/Inch
L
Re
L
f'
'
Cr1inder
Covered
Linear
Veloolty
Ft/Sec
_______
21.4
14.3
14.3
18.35
18.35
27.5
27.5
22.0
22.0
30.0
30.0
37.5
37.5
25.0
25.0
1.211
3.934
0.928
1.03
1.083
1.355
1.29
1.18
1.16?
1.33
1.38
1.685
1.54
1.25
1h25
0.110
0.0846
0.0835
0.0934
0.0955
0.123
0.117
0.137
0.1058
0.1213
0.128
0.152
0.140
0.114
0.1145
E
___
,
______
Solution No. 5 (ContInued)
12.8
12,8
12,8
12.6
12.6
12.8
12,8
12.8
12.?
12,7
12,?
12?
12.?
12.7
12.7
150
loo
loo
loo
100
150
150
120
120
120
120
150
150
100
100
7.0
7.0
7.0
5.45
5.45
5.45
5.45
b.45
5.45
1.0
'1.0
1.0
1.0
4..0
1.0
12.6
14.1
14.55
14.9
14.25
12.9
14.25
13.3
l4.S2
13.56
11.7
13.8
13.6
13.7