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126
236
THS

 

AN INVESTIGATION OF THE EFFECT

OF VISCOSITY UPON THE PLATE
EFFICIENCY IN A BUBBLE-TRAY TOWER

Thmis for the Degree a! M. S.
MICHIGAN STATE COLLEGE

Robert Asa Smi‘I-h
I949

 

 

 

 

 

 

 

 

 

AN INVESTIGATICH CF THE EFFECT OF
VISCOSITY UPON THE PLATE EFFICIENCY
IR A BUBBLE-TRAY TOHER

By
Robert Asa Smith

A THESIS
Submitted to the School of Graduate Studies of Eichigan
State College of Agriculture and Apylied Science

in partial fulfillment of the requirements
for the degree of

MASTER OF SCIEECE
Department of Chemical Engineering
1949

ACKKOHLEDGEHEE

The author is deeply appreciative of the valuable
advice and guidance of Professor Jc W. Donnell. Appreciea
tion is also expressed to Dr. C. M. Casper for his advice,
and to ur. W. B. Clippingcr for his assistance in the
mechanical aspects of the problem.

TABLE OF COHTENTS

HISTORY
EQUIEEEHT
PROCEDURE
DAIA
DISCUSSION
COECLUSIOHS
CALCULATIONS
HOEEECLATURE
BIBLIOGRAPL

Page

HISTORY

In 1943 Brickemer and Bradford presented a correlau
ticn.beteeen viscosity and plate efficiency in the‘grgnz
sections 9.3 the American Institute 3; ghemicel Engineered”
They pointed out that the tray efficiency of fractionating
columns is a function of many things. Some of these are
temperature, pressure, tray design, column.loed, physical
prcperties of the liquid. etc. When all other things are
constant, such as in columns of similar design or for similar
purposes, the efficiency may then.be a function of the physic-
al properties of the liquid.

It is obvious that the efficiency would not be a func-
tion of Just any one physical property, but of many. It is
desired in this problem, then, to study the effect of liquid
viscosity upon the efficiency of a bubble-tray tower. AA
water solution of a soluble cellulose gun was metered on to
the top tray of the tower. The effect of the gum use to vary
the liquid viscosity in the tower. By analyzing various
liquid end vapor samples from the tower. the efficiencies

and viseosities were determined.

The results obtained by Drickamer and Bradford were
drawn from test date on 54 refinery fractionating columns
and dealt wholly with hydrocarbons. They checked their re-
sulting curve against data on 80 commercial columns taken

from the literature. The literature data used was also from

hydrocarbon columns, except for four points. Two of these

2

points were Beer Stills. one an hectic Acid-deter tower,
and the othur on average :f five tests on commercial Alcohol»

tater t were.

Their results ere shown in figures (1) and (e). The
curve is of the form
3 n 0.17 - 0.616.10510 (zrhq

for efficiencies (E) of frecticneting colunns using hydrocuro

halter and Sherwoed have also deelt slightly with
this problem.(10) Qhoy suggested e general equation for
nurphrec efficiencies for gas absorption, tching into account
the effect of viscosity. They no une thet
Although it is highly probable that the indivio
duel 36s and liquid film coefficients are diff-
erent functions of viscosity, the present dets
con be correlated fairly well by assuming both
liquid end 598 film coefficients to be inversely
preportionel to viscosity to the 0.68 poser.
Their equation is
where
[3.9 h]- __

{3-50 I o.svo/n¢ei a 0.68 "0.33

Efficien ice estimated by this equation u re s.nsrinr
of Sufi different iron the experiments. results. The storage
deviation use 32%. The equation severed values of EEV from
0.0095 to 0.75. n from 0.70 to 22. n1 from 1.05 to 1.8". gee

rates from 0.70 to 3.4 pound mole per hour per square inch of

PERCENT TRAY EFFICIENCY

 

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.05 .l .2

.J .5 l 2

FEED STOCK AVERAGE MOLAL V|$COSUTY |N CENT|PO|5E5

PERCENT TRAY EFFICIENCY

 

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.05 .\ .2
FEED stocK AVERAGE

.3 .5 l 2
MOLAL VISCOSITY 1N CENTthSES

slot area. and He from 0.0013 to 8.0.

maxim-":2

The problem hora involved was attacked in o different
manner. Formerly many airfarent egotoms. typos no& 91263
of columns. troy designs, out conoitions were mood. flora
conaitions wo;e maiotninod as constant as toooltlo with only

the liqula viscosity as a vorioblo factor.

Th.r fore. to maintain these oooflitione, a oififile die.
tillotion column.was uood to gather all the data. The coluon
was an ox orlmvo'al loborotory fiiotillotion molt of 24 bubble-
trays. It is a portion of the cor oucnt oVoilvblo in the
Uoit Operations Laboratory of the Dogortmout of Chemical
Engineering at Eichigsn State College. Tkia colum3.woa don
Bianca for use for either boteh or continoouo froctionotion.
It was fitted with oam;1ing tops for liquid and.vo;or on

cash troy.

Who oyatom £thono1-§otor woo chosen due to the largo
amount of information nvviloblo'obout equilibrium curves,
floasity-concrntrotion curves, otc.. oné for the oooe and

inexgonoo of obtaining the comyonooto.

The major problem'with this method thou. was one of
Varying ona controlling the voriotion of tho viooofiity. The
problem was thrcomo by the uoe of a WfltLr soluble cellulooe

gum which greatly increases the viscosity of watgr when ifl.

even very allute solutions. Solutions of this cellulose
gas were motored into the top of tho bubble-troy column Eur»
fine agoration. Ia this manner the viscooity 0f the liquid
throughout the column could to filtoroa to a Eroaotorminoi

degree.

The bubble-tray column sod was on eagerlmoutol
laboratoz; aiotillntion unit. tyyo A-a. built t3.tho Vulcan
C0936: and Suyyly Comgnny of Cincinmoti. Colo. The column
shell was fobricatofl from 9" SIS cop;cr §-po. It ore for-
nished with 24 bubble-cop treya opooad on 6" ccntors. Er h
troy had two three inch Vuloan groomed bubble-cop osooabllos.
(See Figure 4). Zach troy and vofior 33309 woo fitted with

a 3/8 inch globe valve and union to facilitste snmgling.

-3otom necessary to food the vioooua solution

into the to? of the column was not a resolar port of the column,
but was conotructod oogoeimlly for that use. (Sea-Figures 5
on& é) Essentially it was oimgly a pressurized tank with .
alght gloss cod o olug Volvo to allow the solution to flow

on to tho top trn* or the column.

A small rofrig rated coil was uooa to take the liquid
and vapor Bangles directly from the column» (Plates 81, 32
aod 23 only); $313 somfilinc device was fabricated from six
foot of 1/8“ 603.0! toting formed in a coil inside of a three
quort stool can. The upgor ena of the coil woo brazed to

the mole half of a 3/8" "1on. The lower end or the tubing

11:1111 into tie iest tubes t1: t were used ta t: Le the
1119193. “uring 196111111 the 01:1 115 5111111111 by crunhefi
ice and 11.tcr. 11 n1lluatr1.ticn of t? 1 81111113 aggarmtus

11 11111 11 Figure V. For 1111113 :11 ice 1119 left cut of

the c11t11102.

The 11111 111 of the 1111111 were flat r1inad at room

11131111111 using a chain1111tic wentlusl b W1 111.

$11 V1111111131 cf the liquid 6113111 111 bottDm
profiucts were determinea by 18115 1 $1111 Kimble C-GGG v13»
111111111 of the Cstirld 1111. T16 111101111191 1111 1111-
111111 to 3'19 1r minus 011.1111 1 115111 ceatigrméa in 1
ccn1t11t tang: 1111 re untur'bfi The viaeas meter 11d b1 1h
are 11111 11 Figure 8. The bmth was 111tca by two 150 watfi
knife homters centrGLlca b; a 00110 Eczhatinsky Thermoa
regul1tar. A vfiriable 81111 stirrer assured a uniform temp

111111.116 1111;111:311 c at the bath.

Th 11111111t111 1113111111 were diatillod water
951 61131 1111101. T111 V1111 1113 11 the 111111 in fine tower
was varied using 311111111 cf 11111113 018. or Cellulmse G11,
15,7336 C: Cal-700E. (2)

’H

I 3.:- .
)

[Ima- " saga.“ '~ egaup

Figure 3.

Kodel A-2 Exgerimental Distillation Unit
previous to the installation of the sampling

valves and insulation.

 

 

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Figure 6. CM) feeding
system, showing the storage‘

tank and pressure source.

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. > ‘

Figure 7. Sampling
apparatus. showing the valves.

union: and cooling coil.

 

 

Figure 8. Viecoeimeter, showing the stirrer, heaters

and controller.

Photograrhy by Ruby,
(clear and Author.

IRiCSBULE

It was previaus 13 stEf tafl thtt tEe a; stem neceasarg
to feed the CEO solutiona 1333 the t3' of the towEr was
net 3 r gal r 1:3: t of the t330r uiHit but 333 tag 3 3333013 -
13 far this varo :3. The C"C eel: aticns 3Ecre fed into the
toner thrc" h 3h3t w33 ier.crly a 33’3”".Etcr 3611. This
3011 was 13 the 73333 83306 abeve tfie tsp (Eétiw .) tray and
aircctlJ telan the rcflax 13133. It 333 felt 3333 t! e efh
fact a: the refl u: liquid flowing down ever tfie CEO solution
3330 t 6 p031 of linuié b03135 the weir we 315 C333 9 Eddbnti‘l¢

13‘ 30 crfcct 313135.

A be 316 of $33. 3383 35 32 ex €02. 333 333a 33 3
33033330 auurcc for the feaéing 339303. The 33333336 13

the $603133 t33}: 33a }:c;t tetEpen 5 3: Ed ? pcic.

The 31603 aldwet r teca atock W a aixefi in ELc kettle
to 3 cor re.Er*tion of 33;i 34m 'cly 53 6 33301. by weight.
The 931331033 were t3 orcuEhlJ rifle“ t3 100130313 ti: n tc so-

aure ufliffirmity of tha feed:

A yrwblem tExnt 533 £53113 c'ufica a 33 333 3513, W a thrt
53 d1 calving the pauerad CL . It 365 fleeiEGd t3 use 8313»
tiona 6:! 0.753 and 0.1W5% C2 :0 33 fead. 301331033 of thesa
concemtr3tione have viscositiea or 35;rsxfimntoly 20 and 6
centiysise reageeEively. 330m th C”” ~03Eflcr 33:.3 3M ed to
watar, a vErg gelatiaeua film immeflinto 3 formed around 013333
of th. nofzfier. vary :30 atly decreasing th rate or caluticno

The prabicm was 3:1335 by 610313 3L51 C t: :e ccr3ectE m..nt

14

of €33 ta 80 pounds a! water while the salutiGnEW3s bcisg
agitfitefi with a C~4 Lightnin' 3133?. F33t3-fivo minutcs sf

mixing resulted in 3 ch3r uniform aelufiiant

The calumn 333 brcught to cgcrftins egailibriam by
allowing it to Operate unficr 3 $1333 33% of cemflitiens far
at least 30 minutes. baring 3313 333133, £005 r330 333
3305303 rate were £1333. 3nd 311 the athar 0 33131328 3336
allcwcd ta 333333 themselves 33003313313. The distillate
anfl Lotficm prciucta 3033 refi'clefl 333133 this yartion of tfle
run. Equilibrium 093333135 cafifiitifins 3330 said to exist
in the tower when in-cnming 33d out-53133 streams remained
essentially 6&38t3nt in qu33it; 333 Quality 33E: 3 pcriod 3f
tiac. The visible effects of equilihréum were inaicated by
cvnst33t 331398 of 3333m preseure. feed tangerafiure, $363.
reflur, and graduct meter 33331333. 333 3 33333333 3100301

ccmcentration in tie graduct 3333335.

When the £333: 3030303 the csnaition where it 333
09333313; 33 equilibrium. the CED aelutian.wna metcroa into
the toy plate. It 333313 be 3331331333 at this yoint that
£333 tmat time farward 3 3131333 mmsunt ct ogcr3ting tim
r633 med; 311 of the 8333133 h3fl to be -3hen befare the
anyyly 3f CEO 333 fecfl mtock was $336, fir the r0861VLr tfinhs

were Iillefi.

As the SIB aalution.waa startad 1333 the top of tha

031333, the 33001333 £3333 3333 13013305 from the 333310 30

 

15

tAA.t the egguLA AA AA lAA5ar recircuiatiAA. AAA flaw A? 033
salution.was regulnted to the desired rate AAA held at A

ASA At Vfilue. TAG W A ling ¥.'tA AA5AA LAAA tAA tawer A5A£n
came to equilibrium tr A tAA Affect- of tie CNS, unurLll

ALOut 20 AinutAAo

SAAglefi sf £0 Al. AAAA AAAAA Off erA each tray inta
seven inch tc-et t ibes La.w~ AA ccelefi Aamylin5 0311. {AA
the last three AA As a aligAt vacuum was usvd to syecé the

fir.uinr of samfilea. The Bagglea were taken in the orAer
321. A33. 333. 333. $33. T. B. and Fa Gauge, meter, and
ccna c-AA ta resaizv 5'9 Were trken Ana the BAA AlAA staggca.
TAG tewcr Ara left in operfitien far a aAart gerisd cf time

be clcnr it somewhat of viAco A Pul”°i Ans.

Befsze t:w t0? Jer cogld be Aacfl far anothvr run it
had to be claw Ad of all tAAv iAcAAa mafiarial¢ MA was sac»
canzilnficd b; QAAL iA* AAA V$39Wu3 buttvbg gACtht 51A mtAe
receivers into the kAttle. Acre it WAS AAA tea with clAAcd
steam AA thvt the Alcohal 3A1 Artcr A A boiled a: flLtcv A3
a Viaccua Aaficr sciatica. Ants WAS diacaréed and the achAAl

AAA water reused.

The snmyle concAAArAAiona flnfi viaccsities were den
tcrn‘nba in t? A AAAAAA described an page 36 CI DAAielA. A: -
beam and A11;1AAA. (3) DAAA far tAA Alcohol-water density.

teA,AAA1AAoncA1centrutian Acteruin¢tiua v*A AtkLn frsm 439

A: the Chemical Eflgincerg‘ AAAAAAAA‘AJ “err". (6)

    

15

D“:- '3

The followqu scetian 18 ccmyceea 0f the latcratoyy
data taken in the procesa of the exyeriucnt. Eh data may
be rowthy diviaea into two pnrfifl. Cue consista of special

observations $35 the other 19 n rnal tower o:crati:.al data.

The first psrt at the an a 13 far the stanflardizaticn
of the Catwala £539 Vificcaimctcr and the aquaticn far its
use. and an investigation of the effect of CED camcen‘ration

upon the liquid density and viscesity.

The secand yart. or marmal tower operaticnal aafia,
lists several things. -hese include: csncentrntion or GEE
feed aciutiun. rate af 030 food into thc toner, tamer rota.

meter retainga, and liquid and vagcr samgle grapertios.

l7

Standariization cf Cstwnld scesinetcr u"*"" dis-

unit-1%)

tilled water at 35.0 fies. C. (Kimble Viscosimctcr size 0—290)

10 ea. Witt? atmpne

time 9083

9.83
9.83
9.86 average tiue 9.05 800.

The visconi*v 0: water at 25.0 deg. C. 18 .8927 centipciae.

v5
The dcnaity 18 .9971.

Eta equntlun for uae with the visccsimetgr was flea

velopea as follows:

ul g dig; g‘ g gt
'5- gift 3 g 0‘ ii L "I. . ‘J‘ mm
a ;.-: :3

u 3' 03??? 6t

'1’" s " ..
.dv 3.90)

   

u 3 .09105_dt

where
n.18 viscosity in centipoiee
d 15 the fieneity cf tha fluid

t is the time 0f efflux in aeccnfle.

18

Investigati n of c£1cct of C13 ctnc at: tion
neon,aensity ana viscoaity.
9/l5/49

 

Ecight Front. Density Ecmycrfiture Density Euro Enter at

.13 £05. C. Cor1;toc 31 deg. C.
1 .60975 .9995 3305 1.0C0 .9933
2 .061873 :9983 81.3 .998’ 9983
3 .5003 7 9938 21.9 .9913 9993
‘ QC( £3468 :J9L 7 20.9 09987 :JQBZ
5 .030w11 .9937 21.1 .9937 .9933
6 .OCCll? .9977 31.3 .9979 983
7 .060659 .3930 $1.3 c9951 09933

9/19/49

8 .C1G 1.0606 33. 1.0015 .9982
9 .CO.:--O .9‘ ' 85.3 .9993 .9993
.COESO .998 83.6 0.999 .9983
.COlCO .9931 33.0 9339 9933
.090530 .9930 33; :9983 .9983
f1u°r 9991 33. .9984 .9 8?
:06800 :9983 2 .3 .9983 3932

19

All of the viscosities were determined at a bath temperature

or 85 deg. c. The viscosities are in centipoiss and time in

Viscosity 1.12

Viscosity .82

 

seconds.
Sample 2: Samgle a Sample 123
time 93.0 timc 40.4 time 25.93
89.5 40.8 25.94
87.0 59.8 26.15
85.5 40.2
84.0 ,
value value value
used 84.0 used 40.5 used 25.96
Viscosity 7.4 Viscosity 2.56 Viscosityz.28
89.23219 51 3519.210 3: 53121210 35;
time 15.89 time 9.45 time 6.63
15.40 9.29 6.60
15.00 9.56 6.62
12.68 9.58 '"'m“
12.7: 9c55
12.6 '
value value value
used 12.70 used 9.55 used 6.62

Viscosity .58

Samgls 1 38.111210 8 Samgle 3
time 6980 time 74:2 time 55.2
6.84 74.0 52.6
6.85 7460 53.5
6083 L. 5305
6.80 '**"'

value " '” value value
used 6.82 used 74.0 used. 55.1

Iiscosity .60

Viscosity 6.53

K

Viscosity 4.63

Sample 10

time 40. 5
40.7
40.3

value
13.566. 4005
Viscosity 3.57

Bangle 13

time 704:3
7.42

7.42

value
used

Viscosity .65

Sample 11
time 21.84

21.84
21.86

value
used 21.85
Viscosity 1.93

Sump le 15....

time 60 02
5.97
6.06
6.01

value
used 6.01

Viscosity .53

Sample 12

time 9.12
9.00
9.13
9.18
9.18

value
used 9.12

Viscosity .80

Run Bumber l

0.75% 0E0 solution

Rate of CEO feed

81

8/1/49

Steam condensate

242% at 7312
12331.? 815 6318w

 

 

 

“time ”fall use in 54 min.
6332 0"
6:48 6%” Rotsmetcr readings
Diameter of CEO iced Feca 11.3
Reflux 3.8
tank is 12%". Product 2.?
Scmgle‘gyoperticg
Sample Density Temperature 8t. Frost. Eel. Erect. H01.Frgct.
. deg. C. WW,A16’ Ale. ‘ Co «
321 .9648 26.5 .205 .092
x32 .9664 26.5 .195 .087
y22 09393 25.5 0356 01775 '0417
223 .9584 26.5 0243 0114
yzz 09029 26.5 6525 0302 .460
T .8890 26.5 .587 .358
B .9971 26.5 .000 .000

Viscosity Determinations

303. deg. Co 3650
Beth temp. 85.0
Time or efflux
seconds 15:25
15.15
15.51
15.25
15.28
15.21
Value used 15.24
V180081tf 1030
centipo as

84.5
83.5
10.08
10.12

10.05
10.04

10.07
0.85

A“ 4...

Run.fiumber 2

0.75% CEO solution
steam to column at 77 psig.
Feed liquid to column at 78 deg. C.

Rate of CEO feed

258%

 

an.

'1.

22

8/8/49

n X

Steam condensate

at 6:14
101% at 5:12

bra.

 

 

time fell Rotsmeter readings
5.43 0" Feed 11.4
6:05 7.5“ Reflux 4.3
. PTOdUCt 2.85
Diameter of CEO feed tank
18 13.5"
Ssmgle Epoperties
Sample Density Temperature Wt. Erect. M51. Erect. Mol.Frect.
w flag. 0. , 8100 A10. AlCd*
’21 .9574 33.0 V .231 .105
-122 .9840 23.0 .061 6025
yea .9520 33.0 .264 .123 .213
£23 .9768 33.0 .106 .043
y25 09848 53.0 0402 6208 .302
.9196 33.0 .421 .221
.9945 33.0 .003 .002
F .9835 33-0 .053 3026
Viscosity Determinations
Sample B
B.P. deg. C. 93.0 89.5 100.0
Bath temp. 92.0 88.5 98.0
Time of efflux
seconds 101.86 21‘08 25097
101.48 20.95 25.70
20.84 25.38
25.33
25.18
25.15
Value used 101.67 20.96 25.16
Viscosity
centipoiee 8.82 1.81 2.19

Run.Number 3

0.75% 080 solution
steam to column at 55 psig.

Feed liquid to column at 80 deg. 0.

Rate of CMC feed

23
8/11/49

Steam condensate

224# st 5:08.5
93% at 4302.5
1325 in 1:06 hrs.

 

 

 

 

time fell Rotemeter readings
4330 FBBd 9.5
5304 Reflux 3.5
Product 2.6
Diameter of CEO feed tank
is 12.5”
Somgle_ggogertie§
Sample Density Temperature 8t. Front. 201. Erect. 301.Frsc1
4 deg. Q__ Ale. Ale. “f ‘ Alc.
321 .9713 27.5 .157 .068
x22 .9888 27.5 .042 .017
yea .9663 27 .192 .094 .150
:23 .9694 27.5 .170 .074
yzz 09575 2705 9250 .116 0393
.9298 27.5 .398 .206
.9973 27.5 .000 .000
.9897 27.5 .097 .0145
Viscosity Determinations
Sample :22 x23 B
30?. deg. c. 95.0 8700 100.0
Bath temp. 94.0 8600 9900
Time of efflux
in seconds 82.58 23.22 28.00
77.02 23.24 27.92
74.82 23.05 27.63
74.38 22.82 27.57
25.20 27012
26.90
Value used 74.61 23.11 26.90
Viscosity
centipoise 6.47 1.95 2.35

Run.Humber 4

0.75% 020 solution 0
Feed liquid to column et 81 C.

Rate of CEO Feed

time 1211
4:14 0"
4:52.5 8.5”

Diameter of OMB feed tank
is 12.5"

24

8/17/49

Steam condensate

241# at 4051
:94# at 5358

 

147# in 1:15 hrs.

Rotemeter readings

Feed

Reflux
Product

Sample Properties

9.9
3.3

2.5

 

Sample Density Temperature Wt. Erect. Kol.Freet. Ebl.Frogt.
f deg. 0;» _Alc. K Ale. ‘A423
yzl .9687 26.0 .181 .079
322 .9692 26.0 .176 .077
322 .9682 26.0 .184 .0815
x23 .9869 26.0 .057 .023
ya:5 .9559 26.0 .266 .126
T4 .9343 26.0 .382 .194
F .9904 26.0 .055 .014
B .9980 26.5 .000 .000

Remark: Sample 325 taken before 3:23

Viscosity Determinations

Sample X28
B. P. deg. C: 8505
Bath temp. 85.5
Time of efflux
in seconds 12.62
12.74
12.72
12.65
Value used 12.68
Viscosity
oentipoise 1.09

x25

95.5
92.5

74.30
70.00
71.80
69.04
68.45

68.45

5.70

100
98.5

33090
33.54
33.02
32.88
52.73
53045
33.46

2.84

Run Number 5

0.75% 020 solution
Steam to column at 79 p
Feed to column at 80 0

Rate of 020 feed

8/19/49

25

Steam condensate

1908 at 5:20
112; at 4:41

78% in 39 min.

 

 

 

time fell
‘ ' Rotemctcr readings
4:36 0".
5:17 8%" Feed 10.3
Reflux 3.2
Diameter of 020 feed tank Product 2.9
is 12.5"
Sample Properties
Sample Density Temperature Wt.Frect. Ebl.Fract. Mbl.Fr§ot.
w, deg. Co A109 Ale. A130 7
y21 .9702 23.0 .169 .074
‘ X22 09897 26.0 0039 0015
y22 .9644 23.0 .220 .099 .142
$25 .9613 2605 0229 0104
I ‘ .9882 26.5 .361 .181
.9976 26.0 .000 .000
.9885 23.5 .051 .205
Viscosity Determinations
Sample :2. x23 B
B. P. deg. C. 95.5 85.0 100
Both temp. 9405 8400 98
Time of efflux
in seconds 43.22 9.81 15.57
41.73 9.65 15.22
41.14 9.68 15.00
40.56 9.63 14.70
40.26 14.71
40.02 14.65
Value used 40.02 9.65 14.69
Viscosity in
centipoise 3.48 0.82 1.28

Run.Humber 6
0.75% 080 solution
Steam to column at 70 psig.
Feed liquid to column at 79° 0.

Rate of 020 feed

time fall
3:48 0‘
4:04 7“

Diameter of 020 feed tank is 12.5"

26
8/23/49
Steam Condensate

156# at 4:11
109% at 3:47
47% in 324

Rotametor readings

Feed 10.4
RBflux 305
Product 3.9

Sample Properties

Sample Density Temperature Wt.Fract.

Mol.Fract. Mol.Fract.

 

A _Mdeg. C. Ale. Alc:_ Ale.
ygl .9393 24.5
yzg .9429 25.0
r .9237 25.0 .436 .232
B .9986 25.0 .000 .000
8 .9878 25.0 .052 .021

Remarks: Bun only partially completed.

.1 .1.

Viscosity Determinations

Sample B

3.?- deg. C. 100.0

Bath temp. 9800

Time of efflux in

seconds 14.80

14.80
14.57
14050

Value used 14.50

Viscosity in centi-
poise 1.266

Ran out of CEO at 4:04.

Run Number 7

27

8/25/09

0.375% 020 solution. Steam condensate

Steam to column at 70 psig.

 

Feed liquid to column at 72° C. 2425 at 1:15
7 130% at 12:17
Riggeof 020 ggig 1128 in :58 min.
12:14 0" Rotameter Readings
1312 9962"
FEQd 10-1
Diameter of CEO feed tank is 12.5” Reflux 3.8
Product 0.1

Somolg Preperties

Sample Density Temperature 9t.Fract. Mbl.Fract. 201.Fr§ctfi

 

 

deg. C. A10. A100 #4 ‘10::
y21 09194 2805 .445 0338
X22 .9603 30.0 c224 .102
yz2 .9069 28.5 .500 .282 .443
X23 .9445 2905 .317 0153
£23 .8764 2805 C635 .403 0408
.9033 29.0 .514 .293
B .9966 50.0 .000 .000
.9855 30.0 .057 .023
Viscosity Determinations
Sample :22 :23 B
BOP. deg. C. 85.0 83.0 10000
Bath temp. 84.0 82.0 98.5
Sims of efflux in
seconds 34.42 33.73 15.94
34.33 33.60 15.75
34.05 33.68 15.33
34.04 14.10
14.06
14.10
14.10
Value used 34.04 33.63 14.10
Viscosity in
centipoisc 2.89 2.81 1.26

Run Number 8

0.375% 030 solution
steam to column at 80 psig.
Feed liquid to column at 77° 0.

Rate of 020 feed

28

8/26/49
Steam condensate

185% at 5:28
1092 at 4:52

 

 

 

3 3 .
time fall 76. in z 6 min
Rotemeter readings
4:49 0"
5:17 10" Feed 10.4
RBflux 3.6
Diameter of CEO feed tank is 12.5" Product 2.3
Ssmole Eroyerties
Sample Density Temperature wt.Freot. H01.Froot. E01.Fre3t{
M deg. C. Ale. Ale. Ale. 1
x22 .9812 25.0 .095 .042
yzz 09433 24.0 .333 0164 .297
123 .9748 25.2 0139 .059
yzz 59250 24.0 0454 0231 '355
.8939 23.8 .575 .347
.9982 25.0 .000 .000
.9907 24.6 .036 .0145
Viscosity Determinations
smpla $22 X23 B
BOP. deg. C. 9100 88.5 100.0
Bath temp. 9000 87.5 9800
Time of efflux
in seconds 43.20 41.33 18.32
43.32 41.28 18.38
43.22 01.22 18.28
43.10 41.36 18.38
41.20 18.28
Value used 43.21 41.28 18.33
Viscosity in
08Ht1p0183 3975 3055 1060

Run Rumber 9

0.375% 030 solution

steam to column at 90 psig.O
Feed liquid to column at 78 0.

8/30/49
Steam condensate

199% at 531205

 

29

 

 

95% at 4:20;:
34863190: cm fifi 104.4é in :52.5 min.
4220.5 0" Rotemeter readings
5:11 7"
Feed 10.0
Diameter of 020 food tonk is 12.5" Reflux 3.7
Product 2.8
Somglc Progerties
Sample Density Temperature Wt. Frost. 301.22eet. moi. Fr etfi
- ‘9 deg} 06 A100 Alec filfilOOE 3
yZl .9658 19.0 .222 .100
$22 .9604 21.5 .253 0133
ygg .9620 20.0 .248 .114 .470
:23 .9850 21.4 .077 .031
ygs 09515 20.0 5313 0153 .248
.9097 20.6 .517 .295
.9988 21.3 .000 .000
.9895 21.5 .047 .019
Viscosity Determinations
Sample :22 x25 B
30?: deg. C: 3405 92.5 100.0
Beth temp. 83.5 91.5 98.5
Time of efflux
in seconds 7.90 23.76 13.77
7.96 23.10 13.68
8.00 22.97 13.47
8.08 22.80 13.37
7.91 22.96 13.39
7.91 22.98 13.34
8.00 13.37
Value used 7.97 22.93 13.37
Viscosity in
centipoiss .676 1.98 1.17

 

.......

......

30

Run.Bumber 10

0.00% CEO solution
Steam to column at 85 psig.
Feed to column at 80 deg. C.

9/2/49
Steam condensate

194% at 5:07
115% at 4‘29

 

 

 

 

Rate of CEO feed 79% in :38 min.
time fell
Rotometor reafiings
4:28 0"
5:04 7.5" Feed 10.65
Reflux 3.20
Diameter of CEO feed tank is 12.5" Product 3.35
Ssmole Properties
Sample Density Temperature Wt.Fract. MOl.Froct. Mbl.Frant.
A“ deg. 0. Ala. 3119. 1.13.7 g
’21 $9475 2108 .529 0161
222 .9374 24.0 .374 0189
yzz .9380 22.2 0378 0‘925 0521
3523 09549 2405 .277 0130
yzs .9274 22.1 .430 0288 9542
.9276 22.1 .429 .228
.9979 24.1 .000 .000
.9880 24.3 .046 .018
Viscosity Determinations
Sample X33 223 B
BoPd deg. c. 82.5 34.0 10000
Beth temp. 81.5 83.0 9888
Time of efflux in
seconds 8.22 8.38 8.82
8.08 8.40 4.77
8.02 8.50 5.90
8.00 8.38 3.82
8.04 8.45 8.83
Value used 8.04 8.42 8.83
Viscosity in
centipoise .666 .711 .770

Run Humber 11

No 080 solution used

Steam to column at 80 psig.

 

9/5/49

Rotnmetcr readings

 

 

Feed liquid to column at 78° C. Feed 10.7
Reflux 3.55
Product 2.80
Samgle Properties
Sample Density Temperature Wt.Frect. Ebl.Frsct. HOl.Fre2t.
# deg. Co .Alc.‘*_ A100 Ale. 5
321 08950 2105 0587 .357
x23 .8958 21.8 .572 .343
yzg .9103 21.0 .513 .293 '..510
323 .9333 22.0 .401 .207
323 09020 2102 I548 0322 .531
T .9017 21.5 .549 .323
.9973 22.1 .004 .001
.9894 22.4 .047 .019
Viscosity Determinations
Sample x22 x23 B
B. PO deg. C. 8006 8200 9900
Beth temp. 79.5 81.0 98.0
-Time of efflux
in seconds 8.60 8.28 7.01
8.71 8.13 7.10
8.55 0.16 6.96
8.55 8.10 7.05
Value used 8.55 8.13 7.02
Viscositi in
centipc so .677 .671 .613

Run.fiumber 12
0.75% CEO solution

Steam to column at 100 psig
Feed liquid to column at 80

Rate of 025 feed

5c].

 

()3
CU

9/9/49
Steam condensate
222% at 5:53

88% at 4:50
x f n. 8

 

 

time fell
Rotsmeter readings
5326.5 0"
5:51 6587" FGBd 1006
. Reflux 3.6
Diameter of CEO feed tank is 12.5" Product 2.75
Sample Properties
Sample Density Temperature Wt.Frect. lbl.Froct. 851.3ract;
v_ a w p deg. 0. Ala. Ale. fidlc.‘ j
321 .9590 25.0 I188 .085
332 09870 2500 1060 0024
$22 .9538 2500 9224 0102 5205
X23 .9859 25.2 .064 0026 0218
yaz 09543, 23.0 .287 .13.
$9073 2306 1511 0290
.9976 24-3 COCO .000
.9892 24.0 .046 .018
Viscosity Determinations
Sample x22 x2
Ba Po deg. Ct 93.5 93.5 100
Bath temp. 92.5 92.5 98.0
Time of efflux'
in seconds 12.12 80.4 9.03
12.12 79.1 9.06
12.16 76.7 9.00
12.03 72.6 9.02
70.8
71.4
Value used 12.11 71.6 9.03
Viscosity in
centipoise 1.05 6.2 .789

 

f '1-
(,3

9/13/49
Steam Coneenoete

195? at 334%
' . It
llfif at figug

7;: in we min.
Retemetor

food

Ram 00:11:01? 1:;

0.3?5fi CED solution
Steam to col’fin at 80 03169_ .
Feed liouid to colleen at 73° c.

Rete of 030 food

tfire fell

2:50 0”

3326 11.5"

roeéinca

10.7

Reilux 3.1
Diameter of 030 food tank 13 12.5" lroouot 0.1

EFfiQle Eregertieg

 

Beagle Density Temperature Lt.Froet. Hol.Feoot. Eo1.Fréo§.
A D l _ fiegp C.* 116.;y w ‘_Alo. Alo.rv

:31 .ovoe 31.7 .650 .422

”Le .eveo ea. .ce- .437

333 0&533 31.3 .690 .éefi .61&

£33 .oee a... .657 .453

323 08631 3107 c7175 c4985 063'

T .ovee .7.5 .625 .403

e .3071‘ 2o.o .000 .03

F .9911 2o.0 .038 .012

Remarkc:

Viecoeity Determinations

v.—

f

Steam euyply dragged to £5 poig. flaringrun.

Samole :33 x33 B
B. P. 56$: C; 89:4 00.0 100

fiflth tfififlo

Time of efflux in

fifieflnfifi

anue need

Viecoeity'in
centipoiee

V9.0

8051
3‘73
8.73
3.73
8.73

$674

79.0

8.78
o.vo
3.75
8.72
3.72

.669

93.0

15.67
15.65
15.69
15.64
15.66

1037

Run.fiumbcr 14

.0?5w 03:0 eclution

steam to column at 100 pa 3.
Food liCuil to co luau at 80° 0.
I :nte of 0:0 feed

ӎ
{a

9/36/49
Seern 60W1MB t0
hail n4.- 4' 0&1?“ ‘6
“233”“? :?IU

17.5" at 4:05

 

 

 

time fell
37:: b“ Dior wetcr of co ndeaeetc tank
3:06 1” 12 18.75"
8:07 2"
3:10 3“ Dieeetor of CEO fend took 18
3:32 4" 13.5"
3:30 5"
3:34 6” Rotumotcr renalnga
2:38 '7"
3151 8" Fe 10.4
Eefl‘fi 3.8
Broéuet .05
.gggglg Profortiee
Semgle Density Tomyoreture fit. ~ect. Hol.Froet. Lol.ET*gt.
“WV GQEc Cc £180 £10. AA 110. w
331 .9001 3 .0 5&3 .317
3,-2 0.1375 2602 .965 .133
322 .3701 34.8 1673 cééé .518
:LL .9313 ' :3 .o .376 .191.
W
325 .8620 25-1 .?Cl .4775 .521
T .9019 36.9 .53 305
B .9979 37.6 .030 .00
F .986? 2?.2 .055 .GLL
Viscoeity Determinations
BQPc deg. C. 83.5 8205 100-0
39 th tCEHQ 01.5 01.5 9300
Time of of"1ux la
seconds loo. 168 "0.:1
140.5 177 E e :7
17395 $3.?3
39.18
I) V")
1:90; 0
L3.13
370'3
37‘90
37072
Value need 144 173 27.01
Vleceoity in '
06flfi130186 11093 léclfi 39%3

Run Number 15
0.75% 0E0 solution

Steam to column at 90 p815.

Feed liquid to column.ut 82° 0.

Rate of OMB feed

35

Steam condensate

3.9” at 11:09
19.5" at 12:08

 

 

 

time fall
‘IITUZ 0 Diameter of condensate
11:11 1.0 tank is 18.75"
11:14 2.1 Diameter of CEO feed tank
11:25 8.0 13 12.5"
' 11:27.5 4:00
11:53 5.3 Rotumeter readings
11:38 6.4 Feed 9.7
1133905 700 Reflux 3.1
11:40 8.1 Product 2.85
11:43.5 9.0
11348 1000
Sum31§_Propertiea
Sample Density Temperature Wt.Fract. Ebl.Fract. 801.3ract.
deg. C. WAlOa A10. A193?
’21 .9792 22.3 .114 .047
122 09875 23.0 .058 1023
yea .9554 2208 .213 .096 0205
:23 .9764 22.9 .152 .056
323 . .9585 23.0 .260 .121 .345
T .9482 28.0 .321 .156
B .9I92 22.9 .000 .000
F .9846 23.0 .076 .081
Viscosity Determinations
Sample x22 x23 B
B! P. deg. C. 9305 8805 100.0
Bath temp. 92.5 87.5 98.5
Time of effluz
in seconds 24.92 27.22 23.85
24.68 27.80 25.94
24.64 27.40 28.93
24.78 27.40 83.80
Value used 24.70 27.40 23.88
Viscosity in f
can'tiPOiae 2014 2036 2.09

Run Numb er 16

0.75% CEO solution
steam to column at 85 p818.

36
9/29/49

Rotumeter readings

 

 

 

Feed liquid to column at 88 deg. 0. Feed 10.5
Rate of CHO feed Reflux 3.3
time fall Product 8.7
$313.5 ob
8:14.5 1.0 Diameter of CEO feed
8:16 2.0 tank is 12.5"
5317.5 3.0
5320.5 400
3827 500
3:33 500
3333 7.5
Sumgle Progerties
Sample Density Temperétufe Wt.Fract. Mbl.Fract. HOl.FractX
__ A deg. 0. Ala. Ale. Alc.* .
yzl 09779 24.0 9120 .050
122 .9844 29.1 0056 0027
322 .9758 26.8 .127 .053 .22
:23 .9702 29.1 .160 .069
y23 .9698 26.5 .171 .074 .580
T .9502 27.2 .295 .1505
.9979 27.8 .058 .015
.9896 27.1 .058 .015
Viscosity Determinations
Sample x22 :23 B
By P. deg. C. 9300 8705 10090
Bath temp. 92.0 86.5 98.5
Time or efflux
in seconds 31-20 18.73 28.04
81.13 18.47 27.98
51.80 18.89 27.95
18.48 27.75
18.44 27.81
Value used. 31.21 18.45 27.84
Viscomtg 2-65 1'55 p.42

37

TABLE I
SUEEARY 0F DAEA

.L

-22nd trgg 23rd tray .- Over-all Bottoms ;
Run Efficiency Viscosity Efficiency Viscosity Efficiency Viscositdf

____'_‘ w

@QQGGPNNP

F' Pd 5* F! .4 5- +4
at tn 9- c: to F’ c:

0.26
0.17
0.20
0.01
0.27

0.22
0.19
0.04
0.09
«0.28
0.16
0.23
0.68
0.86

0.017

1.30
8.82
6.47
1.09
5.48

2.89
2.73
0.68
0.67
0.68
1.05
0.67
11.98
2.14
2.65

0.44
0.47
0.10
0.58
0.10

0.56
0.85
0.29
0.10
0.22
0.29
0.20
0.44
0.10

0.076

0.85
1.81
1.95
5.70
0.82

2.81
5.55
1.99
0.71
0.67
6.20
0.67
14.16
2.86
1.58

0.292

0.208
0.250
0.208
0.208
0.292
0.292
0.375
0.208
0.208
0.208
0.208
0.624
0.292
0.292
0.208

F

A-vv-v v~ .

'7‘... F--.“ ....7...J_—...._._. “—7, .44 -————.—

._ -.. , .—.7

..7. -7.- _ 7

 

-7.. ”h u. ,
--7-L—.

.-,,...

 

 

i.“ .—7 _____‘7-

 

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7 . . _ _ ,
7 , . 7 . , 7 . V . , V 7 1
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7. _ .71 F . 7 m . . . . . . 1 ~ 4., a . . ,
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. . 7 . . * . ~ 7 1
.77 7 17Il1~n77 7 .7 . 707.I 77. 7V, . I 77 77 ... “I. .1 77777. 17-717.- 7|. #71777. I . it 777777 0.! .._77 I§7III77o7 II: 77 77,» 7I|7 I- g . II 7 -0777 7705. 11c ax -9777 I7I . .l. 7 . I. L . . 77 77 777M
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u . . . . . 7. _ r . 7.7.7... 7.. — . 1 7 7... __ _
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777|17 Iv-7 II .7710 77 ‘7! >7 7 1770...! .I77 '11 I If? u I 70 - ‘m II. II- 7777 [771.11] I051 .117 Il7r-| o OI. .| I] OI. 71.?II7III77 .77... 77.472-067.771? l VI..I¢'(I |I 7 .7IIL.I..II77'A c17I-707 . J. . .f a 06.7.": I 777777. IIP‘7II‘7 . . r 7.77 III 7 .1? -7021. v
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- If} " -
I
a .-— 773.4» -I...
D
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n
LIZ.
k -7
7......

.. x s 7 .t. .7 ’f k 7 . . h f. . .
. . \ .Q \\ . V 7...: \‘pl‘. ‘ O .
4 f I. . \- ch*« ‘ 7 — f \.IH7 b‘lr... v.

41
DISCUSSION

It is important to note that the efficiency of this
tower is unusually low, while it is often possible to easily
reach 95% efficiency with connercial towers of this and
other systems. With this tower the average over-ell of»
ficiency was aphroximotely 25%. Similar results have been

shown by other hereons using the tower in the past.

Naturally one can only postulate upon the reasons
for these low efficiencies, for there may be many. The
seemingly most obvious reason is the small amount of vapor
specs between plates. The individual trays in the column
are spaced on six inch centers. Such a distance is recosnized
as being very near the minimum. it such a distance a Very
significant amount of entrainment may result at the higher
vapor velocities, reaucing the overoell efficiency.

The high ratio of toner wall surface area to the tray
ores and vapor space may also add some explanation to the ef-
ficiency figures. A column of small diameter such as this
one may have the coefficient of heat transfer between liquid
and vapor reduces because of the liquid collection upon the
cello It is understood that the transfer occurs, not only
between vapor bubbles and liquid on the trey, but also boo
tween the vapor and liquid droplets in the vapor space. A
lengthy discussion might result over which is controlling.

If a portion of the liquid droPlets collect upon the tower

42

wall in the form of a film. the transfer surface area is re-

duced, resulting in a decrease in the transfer coefficient

and over-all efficiency.

Other conditions, such as the small number of bubble-
caps per tray, may also contribute to the trend of efficiency

figures.

It must be understood, therefore, that any conclusions
drawn from this experimental data of this problem should be
taken in a relative sense with regard to other towers and

systems, rather than in the absolute.

Figure 4 is a drawing of one of the bubble-trays cepied
from the company prints. It illustrates the lay-out ot’the
bubble-caps. weirs, down spout, and sampling ports. It is
difficult to explain the variation in individual tray cf.
fieiencies except perhaps by the close location of the camp-
ling ports to the bubble-caps. It might conceivably cause a
local concentration change if the liquid is depleted near
one side of a cap. i change in concentration of the sample
con cause an error in the calculation of the theoretical one

richment and the resulting plate efficiency.

The results of the problem are shown in Table I.
Figure 12 illustrates in graphic form the ovor-all tray ef-
ficiency versus liquid viscosity. Over the range of viscosity

studied here. there is no apparent correlation between liquid

viscosity and bubble tray efficiency.

43

The data observed here is plotted over the curve of
Drickamer and Bradford in figure 13. The two do not agree.
Drickamer and Bradford include in their original data only
one point at a viscosity of greater than 0.5 centipoise.

It is logical to have some doubt of the validity of the cor—
relation in the region from 0.5 to 1.5 centipoise. Their
correlation would indicate an efficiency of near 30% for towers
with a liquid viscosity near that of water. and correspond-
ingly lower for higher viscosities. While not true for

this particular tower, it is known that many commercial al~
cohol-water towers Operate at much higher efficiencies. and

the results of the present work indicate that the efficiency
does not necessarily decrease with increasing viscosity

over the range observed.

Figures 15 and 16 illustrate the effect of CEB conn
centration upon the solution density and viscosity. It was
discovered after extensive duplicate calculations that cor-
recting the solution concentrations for any change in density
due to the slight amounts of GTE had a negligible effect upon
the resulting efficiency figures.

It was necessary to determine the liquid viscosity
at a temperature slightly below the actual boiling point.
If any boiling had actually occurred during the determination
it would have caused considerable error. For simplicity,

the boiling point was determined from the concentration, and

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45

CURVE ‘ DQ/CKA/V/EQ 5 BQADFO-QD

PO/NT-S' AUTHOQ

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

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47

‘e temperature of one degree Centigrade less used. Figure
17, taken from the Hercules pamphlet, indicates that at higher
temperatures then is little change in viscosity with temp-

ereture, so the author feels the action Justified. (3)

The method used in calculating the efficiency was e
modification of the Sorel method. (9) This method was chosen
because of its greater accuracy ov r the Eco be-Thiele, for
the effect of the added CEO and the changes in latent heat
may be included. In the modified Sorel method the effect
of the difference between actual and theoretical feed coupes-
itione may also be corrected. The basic equations or the motu

ified Serel method are shown below. (See Figure 14).

A material balance around the top of the column and

the nil plate: yields

Vnsona   ‘D‘O (1)

and
We I... one. i x.» (a)

then
in ' xnll onllfl_, J lab (3)

 

 

and: 13.0 5:111 It 9‘0

esw-e’; (53

vn I},

A materiel balance around the bottom of the column
and the mth plate yields

 

 

 

      
   

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10000

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TEMVERATURE,'C.

50

By the same reasoning as in (3)

arm a x 0mg. . In“ (5)
am " ‘ W

Y : 011111 I- Iv}? 5

In 52%;... 7:. t )

faking a heat balance around the toy plate

Equation (1) may be written for the top of the column

and for the top plate
vt4~1.=ot(D-o _ (8)

Also for the top glete

Vt-l Vt.1

Another important equation around the complete tower 1:.

w a F I C - D (10)
and around the condenser

vtzorxn (11)

It was necessary to modify equation (5) for use on

the f~1 trey'when the actual feed comyoeition differed from
the theoretical.

3m 1: 553. 015112 I If? - W (13)
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v I II III J I 1 I I (I I..! II OII III» I I II II I '. I I o l I-.! II b II‘II’III III] "I III I II I I... IIVIIAI I; II II I I. I I 'II I) {It al IIIIIIIII HII I I II. I}... IYJKiIIIII II N I III 1 It I. IIlIIII- DOvIl IIII
. I . . I . r I
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w I J! I I. .. < . .\v m
N _ r . a I . . . n I I . \I I I . .
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. . .I/ . . . . . ‘I‘ . .
_ x, . ,. _ . . _ IIIIIILII "
. , I. H V V . . I ‘b‘k . I
II.” L '14 [ V r .I r In. On? I I , III I .u,
. . . _ _ I ..I m
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y o
) f n . '1 ‘1: I0 I .0 If I\ I . VI! . 3. ‘ .
r q . n4. . .IJ ML ... « ... .. . . W! M. . I 4. \II . . . . . . . J . .1». . I
r. a. . — a» Ir- 4 n. J If 1 I. ‘ (I OI h
. a. 3 It \«A 4 . I . I? w . . .... . of. .p, J .. .. J. . If. . .I ...I
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.I 4.. d 3» . a. _ ,.w 3 .1: .r 2. A7 I V r... ..., 4... f
I I I1 .I I I 4 f. IsI t I I 9 . .0 ..IIIII. I I III I I §II IIIII‘ . I I 0.1 I v? 3.91.10: l\ I I I h} I I t‘ft I i I V . ..... . . I- I I III II II I
. L Jo}: . A ow fCI — VWI. 1” «‘I v I 1.“ I” . _ k \ Jo.“ .. w‘, “a fi .
I I e Iv. . w .J. 2p s a . I . I: I .
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u a In. . _ x \. . I S ~ I‘.‘ ... ‘ o .9 \. . _ I I
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. I. I H F: \M 1‘ .n x \ . . I ..I “II _. , . . _ .. I b
w I p . . . . g . . W . . . .
..I I I . I I. I I If} It I I 0 I I I I I I I. I II I III V II t I IIT a ..l I'IIITI I I I II I I II III I II 1.1I II ) I I II I I.
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52

COfiCLUSIOflS

0n the basic of the experimental and theoretical work

done, the author believes the following conclusions may be

drawn:

1.

3.

4.

There is no definite correlation between the efficiency
and liquid viscosity of a bubblegtroy tower in the
viscosity range from 0.6 to 3.0 centipoieeI

The correlation of Driekemer and Bradford is in error

I in their higher viscosity range if it is to be used

as a general correlation covering ell types of systems.
There are many things which have a for greater effect
upon the tray efficiency than the liquid viscosity.
Some of these ere, elot area, bubble-cop design, Icir
design. downspout design, trey diameter, and vapor and
liquid rates.

There are several improvements which would lessen the
difficulty and increase the accuracy of future work
with this tower. Some of these improvements include:
thermometers in the feed, reflux, and product rote-
metcre, and condensers. a large diameter vapor connec«
tion between the kettle and column, and rotemeter celi-

brotion in the lower flow ranges.

53
CALCULATIOHS

Sample calculation of run number 3.

Basis . 1 minute

Hurphree Efficiencies ~

E22 3 5' 2 "" y21 8 0084 “‘ .0675

y - ygl .150 , .0575
L116 "' 0084“ g 0.104
.393 a 0084

8 O. 200

 

E25 *fifaz “<¥g§_
g
V25 - fee

The following calculations, along with all the others.
were 00mgleted in tabular form. Since the actual calcula-
tions are very lengthy. the complete calculations from only
Run H05 3 will be given.- A.condensat10n of the Kore important.
figures 0: the rest of the runs will be given at the end of r“
the calculations.

Run H0. 8
E01 tract. EtOH in feed 0.0145
M01 fractn EtOH in distillate 0.206
Reflux-u 0r (Corrected) (See ref. 8) 0.281 351.
Product - D " " 0.073 gal.
Feed a F " " 0.49 gal.
Spec. Gravity of 0B 0.905

" u “ F 0.990

" W n n .950.
Weight of OR .11 #
Weight Of F 4004 f
Weight of D . 0.555%
wt. tract. EtCH in OR . 0.398

Wt. EtOH inOR 0.8405

Wt. water in OR
K018 EtOH in OR
Mole water in OR
Total mole of OR

Wt. front. 131501! in F
Wt; E1303 in F

Wt. water in F

Hole EtOH in F

H013 water in F
Total mole of F

Wt. EtOH in D
Wt. water in D
Mole EtOH in D
E013 water in D
Total mole of D

Wt. water in 0
E015 water in C

F plus C
W a F J G a D

Vt 8 OR ‘ D
Total heat of vapor . H

Total heat or liquid - h
Het heat of vapor wlfln

1.27 #

0.182 mole

0.0705 mole
0.088? mole °:_QR

0.037

0.149 #

3.89 #

0.00525 mole
00216 3018
0.2193 moleflorgl

0.225 #

0.340 #

0.00489 mol!
0.01888 mole
0.02577 mole of D

0.641 #
9.0362flpole of 0

0.2555 mola
0.231? mole of W

9.1125_mols or 7%

20815 Btu
5000 Btu
17776 Btu in BE

2000 Btu 1n_gt

3

0.0248

0.0145

For purposes of

55

Tabular form of Sorel calculations

calculation Ifi was arbitrarily taken as 0.001

 

 

 

 

 

 

Estimates H b. ”H at vn or 715
let est. yt-l 3 .10 20758 2965 17795 2000 0.1123
2nd est. yt-l : .071 20758 2986 17752 2000 0.1127
let est. yt-z : .05 20715 5028 17690 2000 0.1151
[R h HH' Ht 75
let est. yf-1 a .035 20705 5072 17655 2000 0.1154
H h HE: Ht 7m
lfit GBtc y:_5 3 0007 20674 3201 17473 2000 0.1145
let est. yf,4 a .005 20670 5210 17460 2000 0.1146
3 a x. " onll
“ E [5" " K a (19) (D)

M ' x511 * °m¢2

7h

2 e 3511 ‘ omll

m

 

vn

u f: (
Q ( )mF)

S I (Kw) (W)

m

56

 

 

 

 

 

 

 

1. 0521 = ,

C Vhfc D Vth-D J K ya x;
0.0502 0.1458 0.0255 0.1247 0.0275 0.0455 0.0711 0.0002
0.0362 0.1489 0.0338 0.1251 0.0275 0.0436 0.0711 0.0083
0.0562 0.1495 0.0255 0.1255 0.0092 0.0254 0.0526 0.0002

omll' . w

W vmxc' 3” Q 3 5’n ;n*
0.2517 0.3541 0.0071 0.0380 0.0020 0.033 0.0041

W Omll Z 3 3n I;
0.2317 0.3457 0.0245 0.00203 0.0233 0.0030
0.2317 0.3462 0.0110 0.00202 0.0090 0.0014
0.2317 .3465 0.00423 0.00202 0.0030 0.0003

less than
0.001
A Therefore, in the third run. the Sorel method requires

seven theoretical
f“1. 1’2 8.110. f4.
theoretical trey.

culctione.
calculations is six.

trays.

Since the retailer or the tower acts as one

These trays are t, t-l, t~2 a 1.

tray 1.4 ie not counted in the efficiency cola

The theoretical number of trays used in the efficiency

Eaver‘all 0 6/24 C 0'250
Viscosity of bottoms . 2.55 centinoiee

 

 

 

15-5 11
0.0105 0.4
0.q
0.6
0.q
0..
0.0120 0.d
0.0005 0.0
0.0120 0.c
0.:
0.c
0.6
0.c
0.0043 0.c
0.0004 0.(
0.0070 0.:

O.(

58

coup-ow

58

NOEEHCLATURE

bottoms procuct

mole of CHE solution

liquid density. gmz’cc

mole of distillate

efficiency

murphree point vapor efficiency

feed tray

mole of feed

molal heat content of liquid

effective liquid depth. inches

molel heat content of vapor

Henry's low coolticient, #mola/ft.3 atm.

net heat of vapor above liquid cf its boiling point
mole of overflow from the nth tray

total Pressure, atmospheres

time of efflux through the viscosimeter, seconds
distillate sample

viscosity, centipoise

mole of vapor

bubble-cop slot width. inches

mole of bottoms Product

composition of liquid from the nth trc‘, moi fraction
composition of vapor from the nth trey, moi fraction

theoretical composition of vogor in equilibrium with
the liquid on the nth trey, moi fraction

. v...

uni.

a c

.r.. .
r

r

.Mv.

 

FD

 

(1)

(2)

(4)

(5)

(6)

(7)

(8)

(9)

(10)

60

BIBLIOGRAPHY

Corey, J. 3. and Lewis. W. K., Studies in Distillation,
Industrial and Begineering hemigiiy, V01. 24.
882-883 (1932)

Cellulose Products Department. Hercules CHC Cellulose
Gum, Form 500-87 Fm lu49, ficrcEIes Powier Com-
pany, Wilmington, Delaware. ‘

 

 

Daniels, Esthews and Williams. Exyerimentol Ph sicol
Chemistr McGrsw~Eill Book Companyifiré.‘eu1tion,
flew YorE 1941).

Dricksmer, H. G. and Bradford. J. R., Overall Plate
Efficienc* of Commercial Itdrocorfion Cqumns‘gg
a T E'

<unc lon.5T $iscooif . 'rsnsuctions of £58
thadcon IfiETiEufe of Shemicel Enrineers. Vol. 39,
319 (1943):

 

 

Kuong. Brown and white. The Enthel Comgosition Die, .m
for the Svotem Ethano-Je er. filetroleum Refiner,
0 O ‘11. O. 0

Perry, John H.. Chemical Engineers' Handbook. 2nd edition.
EcGrsw-Hill Book Company. Hewaork (1941). .

Robinson. 0. S. and Gillilend. E. R.. The Elements £2
Fractional Distillotion. EbGrao33IEr7353E"Uompsny.
flew Y E ll

 

Era eiifion, or 959)
Rotemeter Correction Factor Nomorre h for Liouids, Fischer
and Porter Company;5B e n o. 60. fififfioro. Pa.

Walkes, Lewis.‘Hcidsms end Gillilend, Principles of
Chemical En ineeri.1, let. edition. KcGrawzfiill
Book Company, eew ork (1923).

   
 

 

Walter. J. F. and Sherwood, T. K.. Gas Absorption i

Bubble-Cog Column. IndustrisI"Enfl"Enginecring
Cfiemistry, 701. 53, 493 (1943).

.2

V'- ‘2..-
. -..,

S

w

o

Uh -wrr- ...

- O

I -..-

l.

H.

6

'.
3‘
I.-.
g.
t.
i
g
I
i
F
g.
3
f

-
‘-

6-
.
l.‘

0"?qu «*1ny

 

 

 

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