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0-169

 

This is to certify that the
thesis entitled
AN IIWESTIGATION OF HEAT
TRANSFER COEFFICIENTS FROM A
STEAM HEATED PLATEN

presented bg

James Myron Trebilcock

has been aceepted towards fulfillment
of the requirements for

M degree mMEfigineering

I

flay/@7449;

Major profe’ssor

Date September 14. 1950

 

 

 

 

 

 

‘ 'II'éfis’quN OF HEAT TRANSFER
NTS FROM A STEAM HEATED PLATEN

BY

James Hyron Trebilcock

A THESIS
Submitted to the School of Graduate Studies of Michigan
State College of Agriculture and Applied Science
in partial fulfillment of the requirements
for the degree of
IiélBTER OF 331514 GE

Department of Chemical Engineering

1950

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in also eifiloeaza to nflo no a. tiiyglh.wf tor his easintance

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in the mechanical aeyauts of thu investigation.

344600

IiiTRU DUCTION

(3) Definition of Drying

Drying in its broadest sense means the removal of a
liquid (especially water) from a solid, from a gas, or
even from another liquid. The chemical engineering unit
operation of drying, however, concerns itself “nly with
the removal of a liquid by vaporization from a eolid~
liquid mixture in which the solid forms the continuous
phase. This latter definition, of course, eliminates
dehumielfication, the dehydration of liquids, evaporation,
aietilliticn, filtration, crystallization, centrifuging,
and other more or less remotely related fields which might
fall unler the more general d finition of drying.
(b) Tyres of Eryers

Even when drying is considered in the more restricted
sense, it covers a wide variety of different types of equip-
ment. The type which is best suited to a particular ap-
plication degenis noon the che acteristics of he solid-
liquii system to be driel, and upon the require29nts of
the separation with regard to profiuct quality and economy.

Qne way of classifying dryers might be according to
whether the material being dried has a definite form,

such as sheet, thread, block, etc., or whether it in a

*9

ree flowing bulk material such as powier, crystals,
flakes, or grains.
Another classification is based on the way in which

vaporization is prolucefl. The so-caller direct iryers

employ a stream of air or gas, perhaps heated in an
external apparatus, to supply the heat and act as a
carrier for the vapor. The so-called indirect dryers use
no air or gas, but supply the heat through heat transfer
surface built into the apparatus. There are also dryers
which are a combination of direct and indirect action.
tome examples of oirect dryers are the tray and compart-
ment dryers, the Spray dryer, the th“ough cir ulotion
dryer and the tunnel dryer. Sons examples of indirect
dryers are the rotary shelf dryer, the screw conveyor
dryer, the aéitated pan dryer, the vscuue rotary dryer,
the indirect rotary dryer, sni the drum dryer.
(0) Scope of this investigation

This investigation concerns itself with the indirect
type of dryer when applies to free-flowing materials.
More particularly it relates to dryers of this tyye in
which the solid-liquid mixture is moved across the tested
surface mechanically. Dryers which fall it this category
incluce the rotary shelf cfiyer, the jacketed sores con-
veyor, the agitateu tan cryer, the vacuum rotary dryer,
and yerhsps the indirect rotary uryer.
(d) rue notary shelf dryer

The rotary shelf dryer consists of circular steel
plates fitted in a horizontal position inside a vortic.l
cylindrical shell. A rotatin5 contrul‘shsft turns urns
which carry diagonal plows. Material Eel continuously to

the center of the top plate is moves outward Dy tne plows

to successive concentric circles of material until it
drops through a slot onto the plate below. Here the plows
are oriented so as to move the material toward a slot in
the center of the plate. Usually about ten plates are
used. Vapors from the drying action move toward a vapor
pipe at the top while the dry solid comes out the bottom.
Each plate is constructed with interior channels with
steam between for heating.

Dryers of this type have been known for some time but
have not been promoted commercially. The name rotary
shelf dryer is the name given to them by Riegel. Thorpe
calls them rotating rabble dryers.

A great deal of interest has been shown recently in
the use of this type of dryer for desolventizing soybean
or cottonseed flakes after solvent extraction. Economies
over the use of Jacketed screw conveyors have been
claimed although data on either of these types of dryers
are badly lacking.

The investigation made here is particularly applicable
to this type of dryer the apparatus being constructed so
as to 06 as similar as possible to this type.

(e) The Jacketed Screw Conveyor

This type of dryer consists of a circular Jacketed
conveyor in which material is heated and dried as it is
conveyed. The conveying of the material is accomplished
by a revolving screw inside the conveyor and frequently

this screw is also heated. The heating medium degends

upon the temperature sensitivity of the material being
dried and may be hot water, steam, or a high-ten erature
heat transfer med um such as Dowtherm.

Since this dryer produces evaporation by moving a
eclii across a heatea surface coefficients should be of
the same order of negnitud as for the rotary shelf dryer
aha should be similarly affected by variables of velocity,
bed derth, anfi temperature difference. Eecause the jacketed
screw conveyor dryer isrmuhatuaof multiple units it is
perhaps not so well adapted to large installations as is
the rotary shelf dryer.

(f) The Agitated Ian Dryer

This type of dryer usually consists of a shallow
circular pan jacketei on the bottom and partway up the
sides for steam or other heating mediums. A central
vert'cal shaft supports an agitator to stir the material
in he pan and bring fresh material in contac with the
hot surface. The agitator can he designed to scrape the
inside surface or set to a very close clearance.

In many respects this dryer is similar to a rotary
shelf dryer but is Operated batchwise instead of contin-
uously. Similar coefficients would be exgected on these
two dryers as long as the same type of material is used
in both cases. However the agitated pan dryer has been
use: largely for the combined evaporation and drying of
slurries.

(S) The Vacuum Rotary Tryer

This type of dryer consists of a stationary cylind-
rical shell mounted horizontally in which a set of agitator
blades mounted on a revolvin3 central shaft stir and
a3itate the material being cried. Heat is furnishei by
circulatin; a suitable heating medium through a jacket
around the shell. The dryer is chn 391 throuih a manhole
at the too of tre shell and discharged through one or more
manholes at th.. bottom of the dryer.

The tumbling action in this type of dryer slould
help to re1ove any suyerheat from the heated solid. Heat
transfer is ob+ ained hoiever by moving the 30111 across
the heated surface as in the previous type. Like the
agitatel pan dryer it is designed_for batch Operation.

Like the Jacketes screw conveyor full use of the heat
transfer surface at the top of he cylinder is not ob-
taint-3 .

(h) The Indirect Rotary Dryer

Indirect rotary iryers consist of a rotating cylinder
inclined to the horizontil With material fei to one enfl
an; removed from the coyosite end. Dryinr however is
see omg-lishsd entirely iniirectly with heat bein3 conaucted
to the material through the metal shell or to see. Wet feed
1ay enter the dryer through a screw conveyor or gravity
chute. It passes through the dryer by virtue of the letters
31338 anl'rotation. The product aischarges from the dryer

hrOU311 periw1rsral ogiehin as in tie shell.

This erer Segonds upon gravity for agitation of the

of the solid. There is no positive means for forcing the
solid to move across the surface. When caking occurs
there is very little, if any of this type of action. The
investigation made here is therefore of little interest
in connection with this dryer.

(1) The Drum Dryer

This type of dryer consists of a revolving heated
metal drum. Drying is accomplished by applying a liquid
material, solution, slurry, or paste to the drum. The
drum conducts heat to the wet film to evaporate the water
during a partial revolution of the drum. The dry material
is scraped from the drum by a stationary knife.

The scraping action in this type of dryer is for
removing the solid only. The solid and the surface move
together and there is no motion of one relative to the
other. It is therefore not related to the work or this
thesis. '

(1) Advantages of Dryers Based on Moving Solids Across

a Heated Surface

Dryers in which solids are moved across a heated sur-
face may advantageously be used for one or more of the
following reasons.

(1) Like other indirect dryers all the heat goes
into the product or vapor. No heat is required for raising
the temperature of a carrier gas.

(2) Since no air is used organic solvents or solids

are not likely to produce eXplosions.

(3) The gentle agitation is not likely to produce
the large quantities of dust often formed in direct dryers.

(A) The equipment is conveniently raie vapor tight
allonir; operat101 under pressure or vacuum or recovery
of‘the vapors.

(S) If vapors are to be recovered t are is no diluting
air or gas stream.

(6) Continuous as well as baton .quipneht is con-
vi ntly constructed.

(7) West transfer coefficients may be quite good in
comparison with some other types of dryers. It was a

purpose of this investigation to determine if this is the

(h) frevious work

A survey of the literature for the past 15 years was
made by searching Chemical Abstracts. to applicable work
was fo'nd under the subjects drying apparatus, oriers,
rotary shelf driers, shelf driers, and indirect driers.
The Ghemical Engineers handbook gives data on vacuum
rotary dryers, jacketed screw conveyors, indirect rotary
dryers, and agitated pan dryers. The only data that was
applicable to this investigation was that on the agitated
pan dryer. coefficients from 5 to 75 3.t.u./hr. sq. ft. °r.
were quoted for those dryers but no mention was made of the
material dried, depth of bed or how the coefficients varied
with the different variables. Walker Lewis fichdams &
Gillilsnd and Badger & thabe give descriptions of some of

the different types of dryers but make no mention of

‘ t“, M ‘. . , 1, .4, W, .1 1
tneory or tiesign do .ta. nieqels Jheoical tacniher; ass: ribes
rotary sqolf dryers ens jacketed screw conveyors but gives
11:: .1.».:.r.:‘-"";-4.I’.iv.>‘r1 on; w 113’: to base the heat 1““.‘3162 for carer:

- .3 . . .0 J: ‘ y ,. .: - In I.
-so assign o- tosse oryers.

FFJi the reti:tl hei.t tra: -.?sr considerations it
ti;ht 3e ““1r”l°i that poor coefficients ould be obtained.
Between the surface and the htlk of the material there is
a stitiioa“" loyor of 3011‘. one tricknzeosciftfifltfiideue
ugon the fiistwsco tietwoen the sorfzce er. the glows. If
this solii acts as an eiioctivn nsulator, verr poor
coefficients should be obtained. In View of the use of
this type of equipment in tho pest and in vies: of the
current interest it would seer.3 that this is not the case.
The work of this thesis is sirected toward esteroining in
a quantitative way what sort of coefficients are obtain-

his.

mhe system of sand and water was on sen for the crying
material. This was decided u on because of its convenience
for run ard of the fewer uncontroll ei variab1.s presented
by this mixture. The san&-water mixture probably gives the
highest coefficients attainable with this apparatus with

lower ace efficients be in n; obtained with materials that

adsorb water or solvents.

APTARATUS

The initial problem of this investigation was to design
a piece of equipment that would assimilate as near as pos-
sible conditions in an industrial_rotary shelf dryer. It
was also paramount that this apparatus maintain constant
speeds of rotation under varying loads and that it be sturdy
and rugged enough to be available for further study.

The problem of obtaining a constant temperature plate
was solved when the Lukens Steel Company of Coatesville, Pa.
donated a Lukenweld Steam Tlaten to Michigan State College.
The plate was forty inches square and one and three-quar-
ters inches thick (Fig. 1). Because of its construction
and operation this type of plate is well suited for the
purpose of this investigation. The platen maintains a very
uniform heat distribution and is able to withstand high
steam pressures.

From this point a drawing of the equipment was made
(Fig. 2). The motor, speed reducer. 2-1 gear reducer,
regulator valve and steam trap were equipment of the Chem-
ical Engineering department at Michigan State. Using pul-
leys from motor to speed reducer it was seen that the ro-
tational velocities commonly used industrially could be
obtained.

The 2-1 gear reducer required a l l/h" vertical shaft
so the platen was sent to a local tool and die shop and a
hole was bored in the center of the plate 1 5/8“ diameter.
This hole was then hushed with a 1/8" thick steel bushing

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12

by freezing the bushing and pressing into the plate. The
bushing extended l/B" into the passages on either side of
the center land.

The main shaft driven by the 2—1 gear reducer extended
up through the platen and had 1/16" clearance. The shaft
was key driven by the large horizontal gear and a blind
flange 6" in diameter and 3/4" thick was welded to the top
end of the shaft to be attached by bolts to the plow arms.

The plow arms were constructed of 8“-ll.5§/ft. channel
iron. Two arms each 35 1/2" long were cut and connected
at right angles to each other with their flat faces to-
gather. These arms were held together by 3/4“ bolts that
extended through both plow arms and the blind flange on
the top of the main shaft.

The eight plows were constructed of 8"-ll.5§/Tt.
channel iron with one flange removed. The plows were con-
nected to the plow arms with 3/6" bolts. The four plows
that were attached to the bottom channel iron plow arm
were milled .220" shorter than the other four plows to give
all the plows the same clearance with the plate.

Four supports riding on 0.1. casters were constructed
for the ends of the plow arms to reduce the thrust on the
main shaft to a minimum. These supports were constructed
from 8"-ll.5#/ft. channel iron and 3 x 3 x 1/4“ angle iron.
The bolt holes connecting the channel and angle iron were
slotted to allow the clearance of the plows from the plate

to be varied. The c. I. casters were 2" diameter wheels with

a 7/8" face.

The speed reducer and the 2-1 gear reducer shafts
were connected by a flexible coupling and the motor and
speed reducer were belt driven by cone pulleys of 2,3 and
4 inch diameters.

When the drive unit was assembled it was moved under
the plate and shimmed so that the main shaft was perfectly
vertical and did not bear in the plate. A flat piece of
insulation l/2“ thick was then placed on the bottom side of
the plate to prevent the drive unit from becoming excessively
heated.

The next step was to build two retaining walls to
prevent the mixture from moving outside the drying bed.
This was done by soldering two circular sheets of 18 gauge
sheet metal to the plate. The inside well Just cleared
the leading edge of the innermost plows and was approx-
imately five inches high and 8 l/e” in diameter. This
wall also prevented any sand from getting in the hole
through which the main shaft turned. The outer circular
wall Just cleared the leading edge of the outermost plows
and was approximately five inches high and 30 1/2" in
diameter.

- The final step was that of piping the steam in and out
of the platen. One-half inch steel pipe was used.

In the original construction all plow angles were 45°.
when a trial run was made it was seen that the outermost
plows were not shearing the material and moving it inward.

Instead these plows were Just pushing the mixture in front

14

of them. It was obvious that these plows turning on the
larger radius were offering too much face to the oncoming
material. The angles were adjusted slightly and it was
found that when the plows were on 52° angles that they
exhibited a good plowing action. They also covered the
same bed area and over lapped each other slightly. The
final plow angles used were 45° for the inside plows with
1/2” overlap and 52° for the outside plows with a very
slight overlap.

The sand used for this investigation was the white
Ottawa sand from Ottawa. Illinois. This sand is of a
fairly fine grain size as can be seen from the included
sieve analysis. The sieve analysis was included to give
an idea of the size of the drying material and as was
mentioned before this substance probably gives the highest

coefficients obtainable with this apparatus.

ease 30.3 35 zoned;
fleece ”Eases? Seqsamaouosw

 

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Photograph showing plow
arms with plows attached

/7

18

1“ RC) CEDURE

The steam was turned on and adjusted to the correct
pressure for the particular run by means of the steam pres-
sure regulator valve. This was done some time before the
run started to assure the plate of being at a uniform tem-
perature. During the time that the plate was heating up
steam was bled through the cock at top of steam trap to
remove the air from the system.

The low pressure runs were made when the gauge regis-
tered on the first mark. The gauge had been previously
tested on a dead weight tester in the pressure range from
five to twenty pounds per square inch gauge. When the runs
were completed the gauge was tested at the very low pressures
by calibrating using a column of water. It was found that
the first mark on the gauge corresponded to a pressure of
1.63 pounds per square inch gauge and this is the reason for
the odd steam pressure for the low pressure run. During
all of the runs the barometer read approximately 7#0 mm of
Hg and this small correction was applied to the absolute
pressures and boiling points.

The sand and water mixture was made up by weight and
thoroughly mixed to assure a uniform composition of the
material to be dried. The final mixture was then weighed
as a check on the preceding weights and the temperature of
the mixture then taken. This was done by immersing a ther-
mometer into the mixture.

The motor was started and the apparatus checked to

make sure that the dryer was in Operating order. The time

*1

was then noted and the sand and water mixture was dumped on
the plate to commence the run.

Sampling was done at five minute intervals 1 ten sec-
onds. The sampling was done by means of a rectangular scOOp
approximately two inches deep by two inches wide by nine
inches long. This was used to obtain a representative
sample of the mixture across the drying bed. The samples
were taken Just after the mixture had been moved toward the
center of the bed by the outermost plows and were taken
parallel to the plow arms across the width of the bed. The
sample was then thorouahly mixed in the scoop and a repre-
sentative sample was taken from the scoop by selecting por-
tions from one end to the other with a spatula. These por-
tions were immediately placed in a dry weighed weiahing
bottle, covered and weighed on the analytical balance.

The remainder of the sample in the scoop being returned to
the drying bed.

After being weighed the uncovered weighing bottles
were placed in an electrically heated oven at 130°C. for
at least eight hours.

The preceding sampling procedure was continued at five
minute intervals until the material appeared practically
dry and then the time intervals were lengthened to ten
minutes until the material appeared as dry as it was peso
sible to obtain with the drying apparatus. This was easily
noted after some experience by observing the final moisture

content of some of the previous runs. In runs 19 and 21

20

ten minute intervals were used during the complete run due
to the longer drying times expected.

When all the sampling had been completed and the samples
dried in the oven for at least eight hours they were removed
and placed in a dessicator. After cooling they were weighed
and the per-cent moisture was then calculated.

The weighing bottles were then cleaned and the material
removed from the plate and another run was started exactly
as in the preceding manner using different variables of
rotation. bed depth or steam pressure.

In plotting the drying curves the initial moisture con-
tent was calculated from the amount of water added to the
original mixture. The sand that was used had been removed
from the drying bed for a short time and was almost per-
fectly bone dry. This method of calculating the moisture_
content of the original charge was used because the larger
weights reduced errors and also because it was difficult
to obtain a representative sample of the original mixture.
The difficulty encountered was when the original mix was
placed in the pail prior to placing on the drying bed the
more moist material was toward the bottom of the pail.

After the material had been placed on the bed the material
was thoroughly mixed and the sand-water mixture was con-
sistent. In all but the first few runs at 15 psig steam
pressure and 3/4" bed depth the initial moisture contents

are the same.

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23
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1.0
1.0

35

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F."

43 2J0

325 3:.

7 I
,2 r
.J 36.0
68.5

65

130 190

150 75 19.0

30 .5 07
u .5
3 0 a
q 3500

98.0

2:!
15
1 . 5
99.5

Run #1

Steam pressure-15 psig

RIM-3/4

Plow clearance from plate-l/lé"
80d depth—3/A"

Composition of drying mixture

Weight of dry sand (lbs.)
Weight of water added (lbs.)
Total weight (lbs.)

27 3/#
l 2
311

Initial temperature of mixture-83°F.

Time

in Sample
thine NO.
0

5 18
10 19
15 20
20 21
25 22
30 23
35 24
45 25
55 26

W1

21.#330
21.3150
20.9988
21.9413
19.9070
21.5698
20.5057
46.7351
49.3762

Bate: 7/15/50

We

33.7235
29.9660
28.83k6
28.7424
30.0503
30.3626
28.6751
5#.6471
58.5687

W3

12.2905
8.6510
7.8358
6.8011

10.1433
8.7928
8.1718
7.9120
9.1925

‘V

W4

32.6783
29.6042
28.637#
28.6430
30.0220
30.3352
28.67#6
54.6466
58.5680

w5

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11.38
8.50
0.18
2.52
1.#5

.28
.31
.006
.006
.008

Run 5",“ 2

Steam pressure~15 psig

Flow clearance from plate-l/lé“

Bed depth-3/4"

Composition of drying mixture

weight of dry sand (lbs.)
Weight of water added (lbs.)
Total weight (lbs.)

27 7/8
8

31 158

Initial temperature of mixture-98°F.

Time

in Sample
2-21 n. I-Eo .

0

5 10
10 11
15 12
2O 13
25 1#
35 15
45 16

w]-

19.4331
19.7382
22.3375
20.9357
21.3170
21.1210

Date; 7/15/;G

WE

24.3663
24.0152
23.168k
24.369A
22.9#18
24.7144
23.3538

“3

8.9332
4.2770
3.#528
2.0319
2.0051
3.3974
2.2328

24.0440
23.8680
23.1130
24.3594
22.9405
24.7137
24.3530

0!

D

.
hoist.

10.90
5.51
3.45
1.61

.89
.07
.02
.04

Run 33

Steam pressure-15 psig

a: 11-5

110w clearance from plate-l/lé"
see depth-3/4"

Composition of drying mixture
Weight of dry sand (103.) 28 1/4

weight of water added (lbs.) 3 1116
Total weight (lbs.) 31

Initial temperature of mixture-84°F.

Time

in Sample

0

5 2 19.5052 24.2700 4.7648
10 3 20.5524 25.3588' 4.8068
15 4 18.3110 22.6120 8.3010
20 5 18.8730 20.8740 2.0010
30 6 18.4208 21.h540 3.0332
40 7 19.3895 22.5051 3.1156
50 8 19.9685 22.7366 2.7681

“3‘93 7/15/50

81‘

23.9992
25.2098
22.5538
20.8730
21.4534
22.5049
22.7358

.2708

.1898

.0582
.0010
.0006
.0002
.0008

'0
U1

%

15:01 8 to o

9.88
5.68
3.11
1.35
.05
.02
.006
.03

Run #4

Steam pressure-8.5 psig
RfM-3/4

flow clearance from plate-l/l6"
Bed depth-3/4“

Composition of drying mixture

weight of dry sand (lbs.) 27 1/4
Weight of water added (lbs.) 1 2
Total weight (lbs.) 3

Initial temperature of mixture-llOOF.

Time

in Simple
Mine NO 0 W1 we W}

0

5 ' 20 20.9988 28.5143 7.5155
10 21 21.9413 30.62 8.6827
15 22 19.9070 28.4416 8.5346
20 23 21.5698 30.5076 8.9378
25 24 20.5037 30.3488 9.6451
30 25 46.7351 55.3848 8.6497
35 26 49.3762 56.4683 7.0921
40 27 20.9797 25.3226 4.3429
50 28 17.4224 21.8701 4.4477

Date: 7/16/50

W4

27.9310
30.1548
28.0760
30.2425
30.1552
55.3026
56.4666
25.3220
21.8694

W 5

.5833
.4692
.3655
.2550
01935
00822
.0017
00006
.0007

75
Moist.

11.40
7076
5.40
4.28
2097
1097

095
.02
.01
.02

Run #5

Steam pressure-8.5 psig

Rim-1.5

Elow clearance from plate-l/l6"

Bed depth-3/4"

Composition of drying mixture

Weight of dry sand (lbs.)
Weight of water added (lbs.)

Total weight

27 1/4

5.552%

Initial temperature of mixture-100° F.

Time

in Sample
N0.

8:111.

o

5
10
15
20
25
30
35
45

C081 O\U1 45W“)

18

W1

19.5052
20.5524
18.3110
18.8730
18.4208
19.3895
19.9685
21.4330

7/10/Su

“2

2707188.

28.7458
26.4612
26.9108
27.7622
25.9102
25.5960
26.8870

“3

8.2136
8.1934
8.1502
8.0378
9.3414
6.5207
5.6275
5.4540

W4

27.1491
28.3492
26.1837
26.7456
27.7005
25.9094
25.5952
26.8869

w5

.5697
.3966
.2775
.1652
.0617
.0008
.0008
.0001

M01580

11. 40
6. 93
4.84
3.40
2.06

.66
.01
.01
.002

Run £6

Steam pressure-8.5 peig

arm-3

Plow clearance from plate-l/l6"
Bed depth-5/4"

Composition of drying mixture
Weight of dry sand (lbs.)

Weight of water added (103.)
Total weight (lbs.)

27 1/4
1 2
30'375

Initial temperature of mixture-83°F.

Time

in Sample
161110 13.0 0 WI W2 W3

0

5 10 19.4331 31.8512 12.4181
10 11 19.7382 27.1564 7.4182
15 12 19.7156 29.8350 10.1194
20 13 22.3375 30.1485 7.8110
25 14 20.9367 26.1104 5.1737
50 15 21.3170 27.8802 6.5632
40 16 21.1210 25.6846 4.5636

* Sample spilled.

“3t3= 7/17/53

“4

30.9109

26.7981

29.5150

30.0407

26.1097
%

25.68A3
27.0070

“5

.9h03
.3583
.3200
.1078
.0007

.0004

%

M013to

11.40
7.58
4.83
3.16
1.38

.01
Q
.007
.007

Run 87

Steam pressure-1.63 p815

arm-3/4

Plow clearance from plate-l/lé"

Bed depth-3/4"

Composition of drying mixture

27 1/4

2 1§2
0

Initial temperature of mixture-79°F.

Weight of dry sand (lbs.)
Weight of water added (108.)
Total weight (103.)

3‘)

Time

in Sample
Min. No.. w1 w2 w}

0

5 23 21.5698 31.0100 9.4402
10 24 20.5057 30.1898 9.6861
15 25 46.7351 58.6402 11.9951
20 26 49.3762 60.7264 11.5502
25- 1 18.5225 26.4906 7.9683
50 2 19.5052 26.9562 7.4510
35 3 20.5524 28.9956 8.4412
40 4 18.5110 25.5528 7.2418
45 5 18.8730 26.4270 7.5540
50 6 18.4208 25.2534 7.0326
60 7 19.3895 26.2900 6.9305
70 8 19.9685 26.4900 4

* Samgle not needed for run.

Da'w-
'9’.

7/17/51)

W4

30.0864
29.5018
57.9413
60.2510
26.2264
26.7662
28.8716
25.5178
26.4122
25.4522
26.2880

“’5

.9236
.6880
.6961
.4754
.2642
. 1900
.1220
.0350
.0148
.0012

..0020

of

p
NOlSto

11.48
9.79
7.12
5.85
4.19
3032'
2.55
1.45

.48
.20
'.02
.03

Run 48

Steam pressure-1.63 psig

R1‘ 1‘51"]. 9 5

flow clearance from plate-l/lé"
Bed deyth‘j/z‘"

Comyosition of drying mixture

Weight of dry sand (108.) 27 3/8
Weight of water added (108.) 1 2
20011 901500 (108.) 30 3 4

Initial temperature of mixture-960?.

Time

in Sample
Fin. No . 1'11 W2 W3

0

5 12 19.7156 27.9558 8.2402
10 13 22.3375 33.3234 10.9859
15 14 20.9367 30.868 9.9316
20 15 21.3170 30.8666 9.5496
25 16 21.1210 9.9010 8.7800
30 17 21.7204 29.6376 7.9172
35 18 21.4330 30.9766 9.5436
40 19 21.3150 27.1946 5.8796
50 20 20.9938 29.2216 8.2223
60 21 21.9413 29.3500 7.4087

Date: 7/17/50

1'" 1+

27.3096
32.6664
30.4402
30.5845
29.7514
29.5648
30.9759
27.1945
29.2226
29.3500

\3’ 5

.6462
.6570
.4281
.2821
.1496
.0728
.0007
.0001
-.0010
.0000

%

1'1015t 0

11.40
7.85
5.98
4.32
2.96
1.70

.92
.007
.001

0.00

Run £9

Steafl pressure-1.63 p813
m-72-5

Plow clearrtince from plate 1/10

Bed depth-3/4”

f"

Composition of drying mixture

weight of dry Band (108.) 27 1/4
Weight of water added (105.) ”2_1 2
Total we151t (105.) 30 37

Initial temperature of mixture-87°F.

Time

in Sample
131 no 1‘10 0 “'1 V12 W3

0

5 2 19.5052 26.8566 7.3514
10 3 20.5524 31.5898 11.0374
15 4 18.3110 28.2922 9.9812
20 5 18.8730 26.9041 8.0311
25 6 18.4208 30.2176 1J.7958
30 7 19.3895 26.3574 6.9679
35 , 8 19.9505 27.3086 7.4201
45 9 18.6536 24.4723 5. 8187
55 10 1994331 21307300 I "0‘1969
1.13.133; 7/' 1.1! 71:";

W4

25-2240
30. 9642
27.9072
26.7314
30.1614
26.3572
27.3084
24.4722
26.7292

A
‘l

6-.

.6326
.6256
.3850
.1727
.0562
.0002
.0002
.0001
.0008

of
/J
Moist.

11.40

8.60
5.66
3.86
2.15
.48
.003
.003
.002
.01

Run #10

Steam pressure-15 p315

Rifl-B/A
flow clearance from plate-1/16"

Bed depth-l 1/4"

Composition of drying mixture

Weight of dry sand (lbs.)
Weight of water edged (1bs.)
Total weight (lbs.)

Initial temperature

Time
in
H1 11 o

0

5
10
15
20
£5
30
35
40
45
55

Sample
1st 0

KO CON! O\U" «PUN

10
11

W1

19.5052
20.5524
18.3110
18.8730
18.4208
19.3395
19.9555
18.6536
19.4331
19.7382

Date: 7,’18/f§il*

WE

25.9448
28.5920
27.1146
26.6302
26.5564
28.9544
27.4202
26.5920
25.5670

45 1/2
5 a 4

51. l/ w

of mixture-80°F.

‘i:
«I

0
\JJ ‘44

Q

0 I
"x
‘J

o

C.‘ (1‘, CA Ln 0*. O)'\‘. U \o \3
GHQChfiMOCDHJGHhCA

(‘PKO'N'JKC- bf-“ICQC-IP

[‘3 U1 (h 39 (h‘xl ‘31

W4

26.3995
28.1588
26.3779
26.4244
26.7268
23.6728
2?.4054
26.3534
25.5698

DSASB
.4352
.3575

rsr;
o (1)2

.1744
.1276
.‘816
.0145
.0386
“00028

.4
3::

'IO’ifit 0

11.20
7.33
5.39
4.06
3-25
2.14
1.71

.91
.17
.56

CCCCC

Run #11

Steam pressure-15 psig

BEM‘IIS

Flow clearance from plate-l/lé"
Bed depth~l 1/4"

Composition of drying mixture

Weight of firy sand (lbs.) 45 1/2
Weignt of water added (lbs.) 5 5/4
Total weight (lbs.) 51 173

Initial temperature of mixture-86°F.

Time

in Sawyle %
E1“. “00 W1 "2 H3 #4 W5 LOlSto
O 11.20

5 2 19.5052 30.0883 10.5831 29.3292 .7591 1.18
10 3 20.5524 28.6756 8.1232 28.2794 .3971 .88
15 4 18.3110 29.2094 10.6984 28.7908 .4186 3.84
20 5 18.8730 29.4346 10.5616 29.2054 .2292 2.17
25 6 18.6208 28.2752 9.8544 28.120 .1545 1.57
30 7 19.3095 26.7923 7.6028 26.7482 .0461 .60
55 8 19.9635 27.0896 7.1211 27.0686 .0010 .01
4O 9 18.6536 25.3374 4.6838 23.3364 .0010 .02
50 10 19.6331 24.1662 4.7331 24.1656 -.0006 .01

7" ' n f' I,~'_
L'JL'T): ‘/l ;‘./ ’,.J

Run #12

Steam pressure—15 p815

Rim-3

klow clearance from plate-1/16"

Bed depth-1 1/4“

Composition of drying mixture

weight of dry sand (lbs.)
weight of water added (lbe.)
Total weight (lbs.)

45 1/2

2%?

Initial temperature of mixture-1130?.

Time

in Sample
Mine NO 0
0

5 12
10 13
15 lk
20 15
25 16
30 17
40 18

w1

19.7156
22.3375
20.9367
21.3170
21.1210
21.7204
21.4330

Tu". t6 : 7/19// :5

W2

28.0840
30.9158
29.6686
28.4832
29.3818
27.3406
28.4335

1”}

8.3684
8.5783
8.7319
7.1062

8.2608

5.6202
7.0005

”2.

ii-
30.5392
29.4210
28.3672
29.3586
27.3398
28.4330

“5

e
.3766
.2746
.1160
.0232
.0008
.0005

Moist.
11.20

‘I'
4.39
2.84
1.62

.28

.01

.01

x1:w clearance from plate-1/16"
Ben'l o.e:th-1 1/4"

Composition of drying mixture

Weight of dry sand (lbs.) 45 1/2
Weight of water added (lbs.) 5 3 4
Total weight (lbs.)1l }

Initial temperature of mixture-1050?.

Time

in Sample

0

5 14 20.9367 .9726 9.0359
10 15 21.3170 31.2 {16 9.9546
15 16 21.1210 29.5660 8.4650
20 17 21.7204 30.3202 8.5998
25 18 21.4330 29.3698 7.9368
35 20 20.9988 20.3553 7.3565
40 21 21.9413 33. 5808 8.6395
45 22 19.9070 29.24% .3386
50 23 21.5698 27.6426 6.0728
55 24 20.5037 26.2042 5.7005
65 25 46.7351 54.8226 8.0875'

7/20/50

“4

29.2184
30.7159
29.2070
29. 9890
29.1105 4
2). 0006
23.2216
30.4660

29.1988

27.6420
26.2040
52.8242

W5

.7524
.5557
.5790
.3312
.2544
.2308
.1337
.1148
.0468
.0006
.0002
-00016

%
H0130.

11.20
8.35
5.53
4.48
3.85
3.34
2.71
1.82
1.33

.50
.01
.003

v.

Run 514

Steam pressure-8.5 p315
PIOW‘clearanoe from plate-l/l6"
Bed depthal 1/4“

Composition of drying mixture

Weight of dry sand (lbs.) 45 1/2
Height of water added (lbs.) 5 4
Total weight (1be.) 51 1 _

Initial temperature of mixture-81°F.

Time

in Sample
Lin. 1.00 W1 W2 113

0

5 2 19.5052 28.1470 8.6418
10 3 20.5524 27.4616 6.9092
15 4 18.3110 29.1360 10.8250
20 5 18.8730 26.4518 7.5768
25 6 16.4208 24.5778 6.1570
35 8 19.9685 23.6800 6.7115
40 9 15.6536 27.4076 6.7540
45 10 19.4531 25.1596 5.7265
55 11 19.7382 20.5946 6.9565

b“: 7/21 53

W4

27.4098
27.0236
28.6086
26.1601
24.4030
28.1746
27.3912
25.1588

25.6943

WS

.7372
.4380
.5274
.2917
.1748
.1930
.1120
.0164
.0008
.0005

%
Ioiat.

11.20
8.54
6.35
4.87
3.84
2.84
2.15
1.29

.19
.01
.01

Run 9

5

Steam pressure-8.5 9518

Rim-3

110w clearance from plate- 1/15u
Bed depth-l 1/4“

Gomyosition of drying mixture

I

Welhht Of dry sand (le.}
weight of water added (lbs.}
Total weight (lbs.}

45 1/:
51 l 4

Initial temperature of mixture-1080?.

Time
in
Min.

0

5
10
15
20
25
30
35
#0
50

Beta;

Sample

NO.

“1

22.3375
20.9257
21.3170
21.1210
21.7204
21.4330
21.3120
QOoSQCB
21.9h13

7/21/uc

29.5532
1 '- (\
29.5,:0

“3

11.8154
11.3603
12.,18:
10.:LL'3

7. ' LA-)
12.€LTF
8. 9800
8.5544
7963??

“4

33.2394
31.6358
33.0651;
31.1CQS
29.:52'
34.1. a .2.
30.2342
5'27

33:5 {CE}

W

.9135
.6612

n
.5562

02960
.1540
.0934
.0008
.0005
.0002

g
MOiSto

11.20
7.74
5.63
4.45
2.69
1.93

.73
.01
.01
.001

:31 ‘ut. of Cr
.'-"€.: ‘IAL C]? ..
m-« ‘3‘-
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fi‘
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H H
H Lug: {jg-x} CV1}! Pk“ m H

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1::
16
17

L.u1

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18.5123
l£.?C53
2%.).7-12'4
13.3110
1?.fi?}3
17.2383
1:933};
‘ ("2?
1.1. o'- 723;.)
1;.3331
22.3373
20.9357
21.31?0
21.1210
21.7204

rate: 37/21/50

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“'\ P" 71..“ 9-4 ‘| "1 F4 C)

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100:! FCC
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119': ‘; ‘u 1‘»
11.31;?
11-39'lh
lQ‘: L3
(rox);>13
9.14ng
90724?
9.7832
11.9000
6““..{3'12
6.9102

.,‘-‘,.‘-I :\
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-\_

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i“
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51.9616
3‘506466
55.2880
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a
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0.0.0...
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.0733
.0090
00032
.0012

Run #17

Steam pressure-1.63 p315

£1; :‘I-l o 5

flow clearance from plate-l/lé"
Bed depth-l 1/4"

omposiblon of drying mixture

flry Band (155.)1/2
15:94

51 173

Initial temperature of mixture-1030 r

Weight of
weight of water added (103.)
Total weight (lbs.)

Time

.1. n 53. 1918
min. 1.0 0 W1 We W3

0

5 11 19.7382 31.5434 11.L102
10 13 22.5575 33.6386 Ll.}011
15 14 :0.)3’7{ 32.3335 ll.w_09
2O 15 LL.:517O 32.6256 11.3066
25 16 Ll.1210 32.3295 L-.-0L5
30 1? 131.7204 30. 7198 3.“)!’
35 18 L1.i33 2?.773.L1. 402
40 19 231.3150 35.4!00 14.1050
45 20 20 .99:8 30.3532 9.3544
50 21 21.9413 33. 3198 11.3785
55 22 19.9070 31.2474 11.3404
60 23 21.5698 29.0132 7.4434
70 24 29.7602 9.2565

20.5037

* Samples spilled.
Date; 7/22/50

.1

1'... l 4

30.4334
39.0229
.9}. . -4428

30.4056 .

32.46442
5401) {.12
j V ‘32324

’33. 2700

31.2490
29.0278
29.6370

"'

3!
5

1.3290
0 JEN )2
.7723
.4567
.3112

."C90
.1208

w

Maicto

11.20

3.9
52

6.5

4.;4
3.46
2.72
1.87
1.29
9.44
9

i
‘I'

Steam pressure~l.6

4--

p315
ELP‘;
130w 013. 3303 from plate-l/lé"
.10 .L 4.1"? u}: .1 1/4"

Congcsiticn of dr"1r 3 mixture

Wti3ht of dry sand (lbs.) 45 1/2
1' t of water ai;ea (135.) . ‘
1L|131 ‘331 ~JAAtI (LbSC) i’l .L/‘l;

 

Initial targerature of mixture-73 ‘.

Tlma
in S-lfiule
2’21)?! 0 ‘XU 0 ‘71

G
S
h}

“’3

U" 0

1 18.5223 23.9036 10.3563
10 2 19.?332 28.30’3 9.3 986
lj 3 23.5524 23.3924 gov/DJ
20 4 13.5110 27.3410 8.:43w0
25' 5 l?.$750 25.2433 5 ‘(3U
50 6 13.4393 23.1734 9.“336
35 T 19.3;j5 25.9956 6.; 31
40 8 13.93QE 31.3376 11.w2yl
A?) 9 1:. (’les Eric'FBUl 90C":":'.J
Sj 10 ljo4331 97.6525 8.2295

o; ?l
.2134
I “‘c ‘U
.3514
.{JLS
01276
.0520
.0002
.0001

Run #19

S‘teo.m pressure-1. 63 p513

$1-105 '

;low clearance from plate-l/lé"
Eed depth-l 1/4“

Drying had covered
Composition of drying mixture
Weight of dry sand (lbs.) 45 1/2
Height of water added (lba.) g E64
Total weight (1be.)

Initial temperature of mixturo-BloF.

Time

in Sample f
Min. No. W1 W2 W3 WA H5 Moist.
0 11.20
10 1 18.5223 28.6502 10.1279 27.7602 .6900 8.78
20 2 19.5052 28.5294 8.3242 27.7082 .6212 7.05
30 3 20.5524 32.9105 12.3642 32.2575 .6290 5.10
40 4 18.3110 2” .7062 11.3952 29.3153 .5904 3.43
50 5 3.3730 9.0278 15.1543 31.3004 .2274 1.7}
60 6 l .fl208 Ju..g6‘ 12.2353 33.5590 .0375 .31
70 7 1?.3-7395 27.11/40 7. {24'} 27.11.40 .0000 0.00
so 8 13.3335 29.0500 9.0315 29.0510 -,oolo -.--

Date: 7/23/50

Run £20

Steam pressure-15 p513

1&1'3

llow clearance from ,ilate—B/S"
30" C3pT.h-l 1/4"

Comzaosition of drying nu ‘xture

Height 0: dry Band (leQ) 45 1/2
Weight of water addei (lbs.) _:~:/4
Total weight (lbs L1 1/4

Initial temperature of mixture-81° F.

Time

in Sample
1'1“! no. “1 W2 W3

0

5 9 18.6536 29.7056 11.0520
10 1019.4331 31.6224 12.1893
15 1119.73c2 31.6576 11.9194
2 1} 22.3375 33.3264 10.9839
25 14 20.9367 33.5930 12.6563
30 15 21.317 ’0 31.&860 lL.EGgO
35 16 -1.1210 50.2808 9 .1593
43 17 £1.7204 55.2514 11.531:

Saba; 7/24/TU

28.8100
313 9 57‘1“)
31.1706
--)-: o ()2 1.0

“4104

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.7484
.4870
.3054
.1766
.0106
.0000
“0001.157

Run #21

Steam prea3ure~15 p31

l"\

o- - a .
, _
"t; L- 4‘

39: degth-l 1/4"

Composition of drying mixture

#1-

L)

weight of dry sand (1bs.)

Weight of water addei

T0131 weight (lb9.)

{lbs.)

45 1/2
.35 ‘1.
51 1_h

Initial temperature or mixture-810?.

Time
in Sample
p113}. 330 0
O
10 9
20 10
30 11
4:) 13
50 14
60 15

Late: 7/2

4/

w1

18.6536
19.4331
19.?332
22.3375
21.3170

50

w2

29.9736
29.1542
3‘3 o 3.13:“
3/4. 370;.)
3J.;,-1
31.62£O

"3

11.3200
9.7211
10.?57?

12.333}

13.049 L
1:3ko 30

”I.

29.5530
29. 015?.
30.01.“
J'fo 530'2

3J.}n33
31.w'-v

.4206
.1390
.1T08
00.706
.0222

.0010

“013‘.

11.20

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1.113
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18‘,

19*
20

21

15

15

 

Initial
301 Temp. of
3/4 t}
3/4 9%
3/4 84
1/4 110
3/4 100
1/4 83
3/4 {9
3/4 96
3/4 67
1 1/4 80
1 1/4 86
1 1/4 115
1 1/4 105
1 1/4 31
1 1/4 108
l 1/4 75
1 1/4 103
1 l/4 78
1 1/# El
1 1/4 81
1 1/4 81

(if
(73"
‘u to!“

_
3H

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U1 U1 U‘

L31

49.0
53.7
70.1
5.5
79.#
96.8
23?.0
331.0
398.0
5A.5
73.0
80.5
77.5
91.0
110.0
2&&.0

341.0

_440.0

291.0

1862
2185

2640

1455

86.1 3270

42.2

1500

* Run to. 19 & 17 are the same except that the dryer 13
covered 111 Run :30. 1.9.

Note: All runs with the exception of No. 20 have a plow

clearance with the plate of 1/16"

53

0133233103

The drying curves are all consistent in so far as the
slower agitation runs requirei the longer drying times.

In some cases, for example in Fig. 7, it is seen that the
instantaneous drying rates of the slower agitation runs are
larger than those of the increased agitation runs during
the initial time intervals. This is noted where the

slopes of the curves are steeper and cross under the curves
for the faster agitated runs. This is the case in Fig. 7
where the curve at .75 r.p.m. shows a faster drying rate
during the first 10 or 12 minutes of the run than the other
runs at increased agitations. The reasons for this lie in
the initial temperature differences of the mixtures and
also by the fact that the worst source of inconsistencies
probably exists during the initial stages of the runs when
the charge is being heated up.

It may seem rather inconsistent that the overall
coefficients obtainei decrease with an increasing temp-
erature difference as shown in Fig. 13 e 14. It is believed
that this can be eXplained by the fact that in run no. 21-
Fis. 11, in which no agitation was used, it was noted that
the material on the tsp and bottom of the bed was dry while
the material in the center was still moist. Eventually
all the material became dry but the material on the top
and bottom of the bed were dry some tine before the material
in the middle. The material next to the plate would be

exyected to become dry first since it was in contact with

59

the hot surface. The material on top becoming dry sooner
than the material under it leads to the conclusion that
air currents were assisting the drying process. If this
was the case, the aptaratus was not entirely an indirect
dryer. This phenomenon was suspected before run he. 21
and that is the reason for run no. 19-Fig. 9. In this

run a cardboard box was placed over the drying apparatus
and it was seen that the drying time was increased as coma
pared to the same run with no cover in Fig. 8. while this
method of covering the dryer was not air tight it served
the purpose of protecting some of the surface from stray
air currents. This ran showed a somewhat lower coefficient
that the similar run no. 17 indicating that air currents
over the bed were helping to dry the mixture.

From the above observation it is seen that if steam
at atmospheric pressure were used giving a zero temperature
difference there would be some drying by the air currents
and the overall coefficients would be infinite. Since the
temperature difference in the runs using the low steam
pressure were small (50F.) this is believed to be the
reason for the extremely high coefficients obtained for
these runs. Of course the runs at the higher steam pres-
sures were all assisted by the air currents so the coef-
ficients obtained here will be higher than those in a
sealed rotary shelf dryer that is the common installation
industrially. I

The curves in Fig. 12 show an increase of overall

60

coefficients with increased rate of agitation and this is
as wouli be exyecteo. L1ue to hi3her a 3itation rates brin-3in3
more material in Contact with the hot surfsoe and breaking
up the mixtu re to allow the moisture to escape.

When the initial wet mixture was placefl on the drying

J

bed not all of the neat trans1el area was utili moi during
the initial sta3os of the run. since the sand was moist
it tended to a33lonzer.ate tO‘Vsner ansi wi.th a plow clearance
of o;-11y 1/13" the trailin3 space behind the glows was bars
of material. Eden tee next set of plows novel material
onto this space it left a bare sgnce in the say: manner and
so on.. This was the cise {Hitil the material became drier
ani tended to be sore 3m nular and free flowin3 anl then
there was a constant shallow layer under the plows and
also a sli: ht anount of material fell behind the plows.
This is not the case in the industrial installation where
the material moves in one direction across the plate but
in this case, due to the linitei equi3)sent, the mixture
was raked back and forth. In accounting for the slightly
increasei coefficients with greater bed depth it seems
possible that this unused area was different for the two
bed depths. It seems that with the 3r% ater bed degth that
there would be more of a tendency for the wet material to
fall behind the plows and utilise some of the space left
bare by the plows. Theoretically one would eXgGCt the
same coefficients for all bei 1e pths.

In run no. el-Fig. 11 in which no a3itstion was used

61

a longer drying time was required than in the similar runs
using agitation. he the drying time is increased the drying
rate falls off. This is because the insulating layer of dry
sand is becoming thicker as the material is drying. When
this layer of dry sand becomes thicker it offers more
resistance to the passage of heat and thereby reduces the
heat transferred to the moist material above the dry sand
layer. During the agitated runs this extreme decrease

in drying rate was not present. Also during the run with

no agitation it was noted when the run was completed that

a thin black scale had formed on the drying bed. The run
was only conducted for one hour and the scale was probably
not too serious although continued Operation would build

up the scale and reduce the heat transfer and thereby the
capacity. The absence of the scale is another distinct
advantage of using agitation while drying.

The curves of Fig. 15 show the expected increase of
heat transferred per unit area with an increase in tem-
perature difference.

In run no. 20-Fig. 10 in which the plow clearance was
increased to 3/8“ a higher heat transfer coefficient was
obtained. In this run all the heat transfer area was
utilized during the run and this probably accounts for the
higher coefficients. Since only one run was made at this
increased plow clearance as a matter of curiosity no valid
conclusions can be drawn due to the limited investigation.

As was mentioned before the outermost plow angle was

62

adjusted to 52° to obtain a suitable plowing action from
hese plows.
The temperature difference used throughout in the

calculations was the difference between the temperature of

which water vnyor was formed at the existing atmospheric
E'T‘OSSUI'B o
The bed area used in the calculations was the entire

area included between the two circular retaining walls.

63

GORGLUSIGNS

1. Heat transfer coefficients were obtained for the
drying of wet sand by plowing it across a heated surface.
For a variety or coniitions these coefficients ranged
upward from 49 Btu's/hr. transferred per square foot
of heated surface ger degree Fahrenheit temperature
difference between the surface and the boiling point of
be water.

2. It may be necessary to lower the above figure
somewhat when a correction is made for drying caused by
stray air currents.

. The rate of plowing was varied from 6 times per

\N

minute at any given point to 24 times per minute, the
coefficients being consistently greater at the higher
rates.

4. Bed c pths of 3/4“ and 1 1/4" were used, greater

coefficien s being noted at the greater depths.

(:0 O

5. Temperature differences ranging from J F. to 38 F.
were used. ruck higher coefficients were noted at the

lower differences. This may be due in pert to the effect

of air currents.

6. Que run in which the glow clearance was increased
from 1/15“ to 3/8" showed an increase rather than a decrease
in coefficient.

7.. For the same plowing action, the angle between the
plow edge and it’s path must be less for plows raking toward
thr center of the plate th.n for those raking toward the

periphery.

()4

77'7"“ ' Y :3 ;‘rftwvs a. n ”r59 £15— .‘2 "
tumq‘ --;;. blu_.2.iTlL-J'!.J ." .JA 1'

pr- “Or

CKTHQR can;

An love sti gaticr cor ducted in t? a some manner as this
one only o151051115 on air ti5ht s":to m would give more of
an iniicaticn of the heat trazasfer coefficients that could
be ex octel i; ustriclly. It would also show to t} act extent

51er coefficients at low temperature differences are due

2

F-
Ft-
*1—

tc air col“ r'onts.
The effect of bed depth and plow angle coulfl

atufliofl z-.ore ticrcuoulj. A different method of agitation

()

might :1}.3 be etucied such as a plow that would cover the
comilete be 1 .mxc just scrape the bottom thereby moving
the material over it and tumbling it behind the plow.

The effect of different drying materials such an
fibrous materials and those that adsorb Loioture en;. show
distinct falling rate periods could be investigated.

The effect of plowing the material continuous 91y in

one direction could be studied as Opposed to this method

of movint the material back and forth.
.J

65

CALGSLAIIGES
(l) Lrying bed area
'1

Diameter of outer retaining wall-30.56
Diameter of inner retaining well- 8.50"

_K_;Z:;5, (30.56)2 - (8.5)2 a 4.71 Sq. ft.
XA'4

(2) for cont moisture

loss. in wt. of sample x 100 = % moisture
sample wt.

(3) Sample calculation for Run $16 (Fig. 8)

Steam pressure~l.6} psig
mug/2+

Bed depth-1 1/4"

110w clearance from plate-l/IG“

Initial temperature of mixture-75°F

wt. of bone dry send-45.5 lbs.
fit. of water at start of run—5.75 lbs.

Time to cry mixture-7O minutes
Final moisture content of mixture-0.08%

51002 x Y a .08 Y = .0364 lbs. of water at end of run.
5. + X

5:7500
" 0072-64
3.7130 wt. of water removed in drying.

Meet required as sensible heat and boat of vaporization.
Sensible heat

Sensible heat of HeO Latent ht. of H20 of sand

q: 5.713o)<1)<211-757 + (5.7136><971> + (45.5)(.23)
(211-75)

q=7750 BTU/70 minutes

7750 are x 60 min. a 6650 BTU/hr.

70 min. 1 hr.
q=Unfit A3#.71 sq. ft. Temp. of 1.63 p315 steam=216°Fo
.At2216-211=5°F.

on g a 6680 a 284 eru/ hr. sq. ft. 0?.

fit EJIXS

The coefficients for all the runs were calculated in
the same manner as the above calculation.

NOMENCLATURE

weight of weighing bottle

weight of weighing bottle + sample

Sample weight (WQ-wl)

Weignt of weighing bottle + sample after drying
Height of water removed in drying (WE-uh)

Heat transferred to drying mixture, STU/hr.

everall heat transfer coefficient, BTU/hr. sq. ft. oF.
Area of crying bed, sq. ft.

Temperature difference between drying surface and

boiling point of the water, 0?.

aevolutions per minute of plow arms

(1)

(2)

(3)

(4)

’s
U7
V

67

BIBLIOGRKJHY

Perry, J. H. . Chemical Engineers' Fanflbook, revised
third edition, ncfiraw-hill Book Company. New
York (1950)

 

HcAiams, W. H.. Heat Transmission, EcGraw~Hill Book
Company, second edition, Rev York (1942)

Badger, W. L. a McCabe. W. L., Elements 9; Chemical
Engineering, second edition, Moiraw-Hill Book
Sonyany. New York (1936)

walker, Lewis. McAdams and Gilliland, Principles 9;
Chemical Engineering, third edition, MOGraw-
Hill Book Gomyany, new York (1937)

 

Riegel, E. R., Chemical machine . Reinhold Publishing
Company, flew York (TQEES

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