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Sieve ColumnDesign
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Given: Ethanol-Water System
D = 300,000 L/day
XF= 0.10 by volume
XB= 0.01 % by volume
XD= azeotropic concentration
95.6 % ETOH - 4.4 % H20 by wt.
Operating Conditions:
25 oC and 1 atm
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Seive Column Design
TRAY
Tray Spacing, Tray thickness, Number ofholes, hole diameter, Pitch
COLUMN
Number of Equilibrium Stages andColumn Diameter
DOWNCOMER ASSEMBLY
Weir length, Weir height, DowncomerLength
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Data TOP BOTTOM
Pressure, (psia)
Temperature, (o
C)L (lb/cu. ft)
V (lb/cu. ft)
Internal reflux
Max vapor, Qv(lb/hr)
Max liquid, QL (lb/hr)
Max vapor, Qv(cu. ft/hr)
Max liquid, QL(cu. ft/hr)Max liquid, QL(gpm)
Surface Tension, (dynes/cm)
Tray Spacing, (ft.)
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XD= 0 8947
18.016kg
14.4kg
46.069kg
195.6kg
46.069kg
195.6kg
fraction)(molXDmolmol
mol
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Convert XF= 0.01 by vol. to by percent by mole
From Perrys (Table 2-28)H2O@ 25
oC = 997.045 kg/m3
From (Table 2-30)
))/1(1(
2
14
3C
CTEtOH
C
C
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Convert XF= 0.01 by vol. to by percent by mole
From Perrys (Table 2-28)H2O@ 25
oC = 997.045 kg/m3
From (Table 2-30)
))/1(1(
2
14
3C
CTEtOH
C
C
))92.513/15.2981(1(
2331.0
27627.0
648.1
EtOH
305082236.17
m
kmolEtOH
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kg
kmol
m
kg
m
kmol
m
kmol
XF
016.18
1045.99790.00508.1710.0
0508.1710.0
33
3
0331.0FX
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Convert XBinto mole fraction:
Since given is XB= 0.01% by volume- the fraction of ethanol in the bottoms
can be assumed to be negligible
Thus, assume the temperature in the
bottom plate can be assumed to be 100 oC- the boiling point of water at 1 atm
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From Table 2-28 of Perrys (p.2-91)
3
3
3100
7492.59
28.3
1
1
2.2365.9580
2
f t
lb
f t
m
kg
lb
m
kgCatOH
37492.59
f tlb
LV
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3
92.513
15.37311
100 4429.15
27627.0
648.12331.00
m
kmolCatetOH
kg
kmol
m
kg
m
kmol
m
kmol
XB
016.18
1365.9580001.014429.150001.0
4429.150001.0
33
3
5109035.2
xXB
Solving for XB
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Determination of Densities
Saturation temperature at azeotropic concentrationTsat= 78.10
oC
Interpolating from Table 2-256 of Perrys
Tsat= 273.15 + 78.10 = 351.25 K
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351.25 0.001 33505
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Determination of Densities
Saturation temperature at azeotropic concentrationTsat= 78.10
oC
Interpolating from Table 2-256 of Perrys
Tsat= 273.15 + 78.10 = 351.25 K
kg
mxVf
3
31033505.1
3
3
3 6985.462.2
28.3
11
f t
lb
kg
lb
f t
m
kg
mVF
LV
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Assuming that the gas phase behaves ideally,
manipulation of the ideal gas equation:
L
g
KKmol
atmL
atmmol
g
RT
MP
V
mVT 5881.0
15.3730821.0
1016.18
3
3 28.3
1
1
1000
1000
2.25881.0
f t
m
m
L
g
lb
L
gVT
30167.0
f t
lbVT
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3
3 28.31
11000
12.2
100014951.1
15.2731.780821.0
11150.43
f tm
mL
k glb
gk g
Lg
KKmol
atmL
atm
mol
g
RTMP
Vm
VB
VB
30932.0
f tlb
VB
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Data TOP BOTTOM
Pressure, psia
Temperature,o
CL lb/cu. ft
V lb/cu. ft
Internal reflux
Max vapor, lb/hr
Max liquid, lb/hr
Max vapor, cu. ft/hr
Max liquid, cu. ft/hrMax liquid, gpm
Surface Tension , dynes/cm
Tray Spacing, ft.
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,o
CL lb/cu. ft
V lb/cu. ft
Internal reflux
Max vapor, lb/hr
Max liquid, lb/hr
Max vapor, cu. ft/hr
Max liquid, cu. ft/hrMax liquid, gpm
Surface Tension , dynes/cm
Tray Spacing, ft.
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,o
C 78.1 100L lb/cu. ft
V lb/cu. ft
Internal reflux
Max vapor, lb/hr
Max liquid, lb/hr
Max vapor, cu. ft/hr
Max liquid, cu. ft/hrMax liquid, gpm
Surface Tension , dynes/cm
Tray Spacing, ft.
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,o
C 78.1 100L lb/cu. ft 46.6985 59.7491
V lb/cu. ft
Internal reflux
Max vapor, lb/hr
Max liquid, lb/hr
Max vapor, cu. ft/hr
Max liquid, cu. ft/hrMax liquid, gpm
Surface Tension , dynes/cm
Tray Spacing, ft.
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,o
C 78.1 100L lb/cu. ft 46.6985 59.7491
V lb/cu. ft 0.0932 0.0367
Internal reflux
Max vapor, lb/hr
Max liquid, lb/hr
Max vapor, cu. ft/hr
Max liquid, cu. ft/hrMax liquid, gpm
Surface Tension , dynes/cm
Tray Spacing, ft.
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MF= 0.0331(46.069) + (1 - 0.0381)(18.016)= 18.9446 g/mol
MD= 0.8947(46.069) + (1 - 0.8947)(18.016)= 43.1150 g/mol
MB= 2.9033x10-5
(46.069) + (1 - 2.9033x10-5
)= 18.0168 g/mol
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OMB: F = D + B
hr
day
kg
kmol
m
kg
L
m
day
L
hrday
kgmol
mkg
Lm
dayLD
24
1
016.18
1974.972
1000
1000,3008947.01
241
069.461036.749
10001000,3008947.0
3
3
3
3
Material Balances
hrlbmolD 095.550
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CMB: FXF= DXD+ BXB
5
109033.2095.550
8947.0095.5500331.0
xhr
lbmol
F
hr
lbmolF
hrlbmolB
hrlbmol
F
626.332,14
721.882,14
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Determination of L and V (McCabe-ThieleGraphical Method)
D
Lo
RD
min)50.105.1( DDactual RR
ESOL Eqn:
ND
Dn X
R
RY
1
1
1
D
D
R
X
Dn XV
DX
V
L
SSOL Eqn:
1n
Y
B
B
mB
B
R
X
XR
R 1
Bm XV
BX
V
L
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XF = 0.0331
77oF
q = 4
q - line
XD = 0.8947
F
Fvap
H
HH
q
33.1
3
4
1
q
qm
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XF = 0.0331
XD = 0.8947
ESOL for RDmin
70769.01min
min DD
RRESOLofslope
RDmin = 2.4211
2666.01
intmin
D
D
R
XESOLofy RDmin = 2.3551
RDmin,ave = 2.3881RDactual =
1.50(RDmin)
RDactual = 3.58215
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XF = 0.0331
XD = 0.8947
7993.01 Dactual
Dactualactual
RRESOLofslope
XB
N = 20
Feed Stage, NF= 17
2706.11
B
B
RRSSOLofslopeRB =3.6957
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58215.3D
LoRD
L = 3.58215D = 3.58215(550.095)
L = 1970.523 lbmol/hr
Balance over Top Plate:
V = L + D
V = 1970.523 + 550.095
V = 2520.618 lbmol/hr
V
L
V
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B
B
R
R 1
mm
mm
25.4
4.5Slope of SSOL, = 1.2706
RB= 3.6957 =B
V
332.626)3.6957(14,3.6957B V
V
VBL lbmol/hr67,301.712L
= 52,969.086 lbmol/hr
= 14,332.626 + 52,969.086
Balance Over Bottom Plate
V
L
V
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N = 20
Feed Stage = 17
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FLOW RATES FOR TOP PLATE
lb/hr84,959.11
1150.431970.523L
lbmol
lb
hr
lbmol
/sft0.50543600
1
6985.46
184,959.1 3
3
s
hr
lb
ft
hr
lb
gpm40.67min1
60
785412.3
1
283.3
10000.5054
3
3
s
L
gal
ft
L
s
ft
lb/hr5108,676.441150.43
2520.618V
lbmol
lb
hr
lbmol
/sft323.9053600
1
0932.0
15108,676.44
33
s
hr
lb
ft
hr
lb
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FLOW RATES FOR BOTTOM PLATE
lb/hr4851,212,561.1
0168.1867,301.712L lbmol
lb
hr
lbmol
/sft5.6373600
1
7492.59
14851,212,561. 3
3
s
hr
lb
f t
hr
lb
gpm453.591min1
60
785412.3
1
283.3
10005.637
3
3
s
L
gal
ft
L
s
ft
lb/hr86954,333.42
0168.18
52,969.086V
lbmol
lb
hr
lbmol
/sft7223.2323600
1
0167.0
186954,333.42 3
3
s
hr
lb
ft
hr
lb
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,o
C 78.1 100L lb/cu. ft 46.6985 59.7491
V lb/cu. ft 0.0932 0.0367
Internal reflux 3.58215 3.6957
Max vapor, lb/hr
Max liquid, lb/hr
Max vapor, cu. ft/hr
Max liquid, cu. ft/hrMax liquid, gpm
Surface Tension , dynes/cm
Tray Spacing, ft.
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,o
C 78.1 100L lb/cu. ft 46.6985 59.7491
V lb/cu. ft 0.0932 0.0367
Internal reflux 3.58215 3.6957
Max vapor, lb/hr 108,676.445 954,333.429
Max liquid, lb/hr
Max vapor, cu. ft/hr
Max liquid, cu. ft/hrMax liquid, gpm
Surface Tension , dynes/cm
Tray Spacing, ft.
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,o
C 78.1 100L lb/cu. ft 46.6985 59.7491
V lb/cu. ft 0.0932 0.0367
Internal reflux 3.58215 3.6957
Max vapor, lb/hr 108,676.445 954,333.429
Max liquid, lb/hr 84,959.1 1,212,561.5
Max vapor, cu. ft/hr
Max liquid, cu. ft/hrMax liquid, gpm
Surface Tension , dynes/cm
Tray Spacing, ft.
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,o
C 78.1 100L lb/cu. ft 46.6985 59.7491
V lb/cu. ft 0.0932 0.0367
Internal reflux 3.58215 3.6957
Max vapor, lb/hr 108,676.445 954,333.429
Max liquid, lb/hr 84,959.1 1,212,561.5
Max vapor, cu. ft/hr 323.905 7,225.232
Max liquid, cu. ft/hrMax liquid, gpm
Surface Tension , dynes/cm
Tray Spacing, ft.
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,o
C 78.1 100L lb/cu. ft 46.6985 59.7491
V lb/cu. ft 0.0932 0.0367
Internal reflux 3.58215 3.6957
Max vapor, lb/hr 108,676.445 954,333.429
Max liquid, lb/hr 84,959.1 1,212,561.5
Max vapor, cu. ft/hr 323.905 7,225.232
Max liquid, cu. ft/hr 0.5054 5.637Max liquid, gpm
Surface Tension , dynes/cm
Tray Spacing, ft.
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,o
C 78.1 100L lb/cu. ft 46.6985 59.7491
V lb/cu. ft 0.0932 0.0367
Internal reflux 3.58215 3.6957
Max vapor, lb/hr 108,676.445 954,333.429
Max liquid, lb/hr 84,959.1 1,212,561.5
Max vapor, cu. ft/hr 323.905 7,225.232
Max liquid, cu. ft/hr 0.5054 5.637Max liquid, gpm 40.67 453.5941
Surface Tension , dynes/cm
Tray Spacing, ft.
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For Surface Tension:
mmNm /40.71
At 100oC: mmNwater /91.58
mmN
mmN
etOH
water
/55.17
/32.59
894701244.0D
X
At 78.1oC:
105298756.02 OHX
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6277.3
1
log
log1
log
10
)0185.0)(32.59(2
0627.055.17
25.351
21.44
)0627.0)(8947.0()0185.0)(1053.0(
0627.08947.00185.01053.01010
3
2
32
1
2
w
w
x
w
w
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cm
dyne
xx
x
water
water
etOH
w
ww
w
w
9313.17
)55.17(9848.0)32.59(0152.0
9848.00152.01
0152.0
103567.2103567.2
103567.21
25.025.0
44
4
4
1
2
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,
o
C 78.1 100L lb/cu. ft 46.6985 59.7491
V lb/cu. ft 0.0932 0.0367
Internal reflux 3.58215 3.6957
Max vapor, lb/hr 10345.44 90840.23
Max liquid, lb/hr 8087.69 115420.53
Max vapor, cu. ft/hr 30.83 687.56
Max liquid, cu. ft/hr 0.0481 0.5366Max liquid, gpm 21.61 241.03
Surface Tension , dynes/cm 17.93 58.91
Tray Spacing, ft.
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Data TOP BOTTOM
Pressure, psia 14.7 14.7
Temperature,
o
C 78.1 100L lb/cu. ft 46.6985 59.7491
V lb/cu. ft 0.0932 0.0367
Internal reflux 3.58215 3.6957
Max vapor, lb/hr 10345.44 90840.23
Max liquid, lb/hr 8087.69 115420.53
Max vapor, cu. ft/hr 30.83 687.56
Max liquid, cu. ft/hr 0.0481 0.5366Max liquid, gpm 21.61 241.03
Surface Tension , dynes/cm 17.93 58.91
Tray Spacing, ft. 1.5 1.5
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TOWER DIAMETER
CALCULATIONS
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*Assuming a non-foaming system* Based on 80% flooding and the use of splash baffle
5.0
L
V
FV
LP
0349.06985.46
0932.0
445.108676
91.84959 5.0
0315.7492.59
0367.0
4286.954333
485.1212561 5.0
TOP PLATE BOTTOM PLATE
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From Figure 13.21 of Van Winkle,With a Tray Spacing of 1.5 ft
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0.275
0.280
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From Figure 13.12 of Van WinkleWith a Tray Spacing of 1.5ft
275.0CP
280.0CP 269.0
20
93.17275.0
,
8.0
,
corrC
corrC
P
P
348.020
91.58280.0
,
8.0
,
corrC
corrC
P
P
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For 100% flood,
fpsU
U
VN
VN
015.6
0932.0
0932.06985.46269.0
5.0
fpsU
U
VN
VN
047.14
0367.00367.07492.59348.0
5.0
5.0
V
VLCVN PU
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Computing for vapor flow net area ANfor 80 %of flood,
8.0VNV
NU
QA
ftsqAN 312.67
8.0015.6905.323
ftsqAN 231.643
8.0037.14
232.7223
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Assume Ad= 0.1A,Thus A = AN+ 2Ad= AN+ 0.2A
A = 67.312 + 0.2AA = 84.14 sq. ft.
A = 643.231 + 0.2AA = 804.039 sq. ft.
From
5.0
2 44
ADDA
D = 10.35 ft D = 31 ft
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Check the validity of the assumption from Table 14.2
Table 14.2 Recommended Limits: Tray and Column design
Perforated Trays
Column diameter
basis: % flood
Tray Spacing
Tray
Flow arrangementGeneral
med. diam. 6-12 ft
large diam. 12-24 ft
Tray layout
1-24ft
80-85% NF
70-75%
Fig. 13.21
12-36 in.Col. diam. 2.0-4.0ft; 12-18 in
Col. diam. 5.0-24 ft; 24-36 in
check: liquid backup, entrainment
(table 14.3)
Cross flow
DP
Multiple pass
Hole diam.: 1/81/2 in.Hole area: 6-15% col. Area
Spacing: pitch/hole diam., 2-4
tray thickness: 16 gage to in.
AssumedTray Spacingless thanminimum fora 10ftcolumn
Assumedwas 18in
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Check the validity of the assumption from Table 14.2
Change tray spacing to 36 inches (3ft)
Read Pc from Table 13.2
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0.48
0.49
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Check the validity of the assumption from Table 14.2
Change tray spacing to 36 inches (3 ft)
Read Pc from Table 13.2
Pc= 0.48
Following previously done calculations
D = 23.5 ft
Pc= 0.49
D = 7.5 ft
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Check for Percent Flood
AVN
V
AUQflood %
)51.10)(321.45)1.0(2321.45(
905.323%
flood
)525.24)(125.433)(1.0(2125.433(
232.7223%
flood
%85% flood %85% flood
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A = 45.321 ft2 A = 433.125 ft2
A = 0.1(A)
= 4.5321 ft2
AA= A2(0.1)A= 2 36.257 ft2
A = 0.1(A)
= 4.5321 ft2
AA= A2(0.1)A= 346.5 ft2
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D = 23.5 ft
D = 7.5 ft
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SEIVE TRAY
DESIGNCALCULATIONS
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dhtp
P
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Tray Spacing, Stray
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From Table 14.2, create a pre-assumedTray Layout
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Table 14.2 Recommended Limits: Tray and Column design
Perforated Trays
Column diameter
basis: % flood
Tray Spacing
Tray
Flow arrangement
General
med. diam. 6-12 ft
large diam. 12-24 ft
Tray layout
1-24ft
80-85% NF
70-75%
Fig. 13.21
12-36 in.
Col. diam. 2.0-4.0ft; 12-18 in
Col. diam. 5.0-24 ft; 24-36 in
check: liquid backup, entrainment
(table 14.3)
Cross flow
DP
Multiple pass
Hole diam.: 1/81/2 in.
Hole area: 6-15% col. Area
Spacing: pitch/hole diam., 2-4
tray thickness: 16 gage to in.
Hole clearance:
hole-tower wall, 1.5 in.
hole-weir, 2.0in., min
hole-apron, 2.0 in., min
Ave. dyanamic seal hds:
vacuum, 0.50.6 in.
atmospheric, 0.51.5 in.
pressure, 1.5-3.0 in.
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From Table 14.2, create a pre-assumed
Tray Layout
Top Plate Bottom Plate
Tray Spacing 3.0 ft 3.0 ft
PlateThickness, tp
0.25 in 0.25 in
Hole
Diameter, dh
0.50 in 0.50 in
P/dhPitch, P
4
2 in
4
2 in
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WEIR ANDDOWNCOMERASSEMBLY
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Weir (Outlet Weir)
Downcomer
Weir Height, hw
Weir length, lw
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Weir Length, lw
From Table 14.8, select hw= 3.0 in
Ad= 0.1A, 1.0A
Ad
From Table 14.10
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Check for ENTRAINMENT
From Tower Diameter calculations
PF= 0.0349 PF= 0.0315
From Figure 13-26 (Entrainment Correlation)
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0.165
0.160
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Check for ENTRAINMENT
From Tower Diameter calculations
PF= 0.0349 PF= 0.0315
From Figure 13-26 (Entrainment Correlation)
Entrainment , moles/moles of downflow = 0.160 = 0.0165
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5.2
w
Lw
l
QfF
5.2
w
L
l
Q
0946.25435.2
61.21
5.2
6931.1267.7
03.2415.2
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From Figure 13.7
With L/D = 0.7267
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L/D = 0.7267
1.020
1.022
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From Figure 13.7
Fw= 1.022 Fw= 1.020
67.0
48.0
w
L
wow l
Q
Fh
inh
h
ow
ow
35.012525.5
67.40)022.1(48.0
67.0
inh
h
ow
ow
82.012085.17
591.453)020.1(48.0
67.0
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h(equivalent surface tension head loss, in.)
hLdh
04.0
inh
h
0307.0
)50.0)(6985.46(
)93.17(04.0
inh
h
0789.0
)55.0)(7492.59(
)91.58(04.0
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ho(equivalent head loss through holes, in.)
2
186.0
o
h
L
vo
C
Uh
Uh= velocity of vapor through holes
h
vh
A
QU
Ah= total hole area
From Table 14.8, with
10Ah
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,
1.0A
Ah
2
2
6257.3
257.361.0
ftA
ftA
h
h
2
2
65.34
5.3461.0
f tA
ftA
h
h
fpsUh 46.20865.34232.7223
h
p
dt 50.0
50.0
25.0
50.050.0
25.0
89.34fps3.6257
323.905
hU
From Figure 13 18
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From Figure 13.18,
725.0oC
725.0oC
Solving for ho
2
186.0
o
h
L
vo
C
Uh
inh
h
o
o
64.5725.0
34.89
6985.46
0932.0186.0
2
inh
h
o
o
45.9725.0
46.208
7492.59
0367.0186.0
2
t
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1.0AA
h
50.050.0
25.0
in
in
d
t
h
p
0.50
0.725
From Figure 13 18
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From Figure 13.18,
725.0oC
725.0oC
Solving for ho
2
186.0
o
h
L
vo
C
Uh
inh
h
o
o
64.5725.0
34.89
6985.46
0932.0186.0
2
inh
h
o
o
45.9725.0
46.208
7492.59
0367.0186.0
2
(relative foam density)
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(relative foam density)
)( vaFf 5.0
)( vVAVA UF
UVA=vapor v eloci ty based on act ive area, fps
A
Q
A
QU v
A
v
VA8.0
93.8257.36
905.323VAU
87.205.346
232.7223VAU
5.0
)( vVAVA UF
727.2
)0932.0)(93.8( 5.0
VA
VA
F
F
0.4
)0367.0)(87.20( 5.0
VA
VA
F
F
From Figure 13 16
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From Figure 13.16
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0.56
0.55
From Figure 13 16
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From Figure 13.16
56.0
55.0
Solving for total pressure drop
hhhhH owwT )( 0
inH
H
T
T
5802.7
0307.064.5)35.00.3(56.0
inH
H
T
T
5917.11
789.045.9)82.00.3(55.0
WEEP POINT
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WEEP POINTCalculated (h
o+ h) > Theoretical (ho+ h)
(ho+ h)calc
6707.5)0307.064.5(
5289.9)0789.045.9(
(hw+ h
ow)
35.3)35.00.3(
82.3)82.00.3(
From Figure 13.22,
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0.53
0.55
WEEP POINT
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WEEP POINTCalculated (h
o+ h) > Theoretical (ho+ h)
(ho+ h
)
calc
6707.5)0307.064.5(
5289.9)0789.045.9(
(hw+ h
ow)
35.3)35.00.3(
82.3)82.00.3(
From Figure 13.22
53.0h(h o theo
55.0h(h o theo
LIQUID BACKUP IN DOWNCOMER
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LIQUID BACKUP IN DOWNCOMER
d
dowwTD hhhHH1
2
= liquid gradient, in.
hd= equivalent head loss in downcomer, in.
d= froth density in downcomer
2
10003.0
dm
L
d A
Q
h
Adm
= minimum area of liquid flow in downcomer assembly
AAP= (apron clearance)(l
w)
Assume Apron clearance of 1.5 in
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2691.0
)525.5(
12
1)5.1(
f tA
ft
in
ftinA
AP
AP
2136.2
)085.17(
12
1)5.1(
ftA
ft
in
f tinA
AP
AP
2
10003.0
dm
L
d A
Q
h
inh
h
d
d
4.01.0
)691.0(100
67.4003.0
2
inh
h
d
d
135.0
)136.2(100
591.453
03.0
2
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Assume: = 0.10 d= 0.5
Solving for HD
inH
H
D
D
99.10
5.0
10104.0
2
10.035.00.35802.7
inH
H
D
D
5967.15
5.0
1
135.02
10.0
82.00.35917.11
LIQUID RESIDENCE TIME IN DOWNCOMER
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LIQUID RESIDENCE TIME IN DOWNCOMER,
rateflowdowncomerofvolume
ssft
in
ft
inft 2126.8/5054.0
12
1
)99.10(5321.43
2
ssft
in
ftinft
987.9/637.5
12
1)5967.15(3125.43
3
2
L
Dd
QHA
SUMMARY
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TOP BOTTOM
Tower diameter 7.5 ft 23.5 ftTray spacing 3 ft 3 ft
Active area 36.257 ft2 346.5 ft2
Area of holes 3.6257 ft2 34.65 ft2
Area downcomer 4.5321 ft2 43.3125 ft2
Ah/A 0.08 0.08
Ad/A 0.1 0.1
Ah/AA 0.1 0.1
dh 0.5 in 0.5 in
lw 5.525 ft 17.085 fthw 3.0 in 3.0 in
Tray thickness 0.25 in 0.25 in
Downcomer clearance
SUMMARY
SUMMARY Z = 60 ft
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SUMMARY
N = 20
DISTILLATION COLUMN
NF= 17
DT= 7.5 ft
DB= 23.5 ft
TOTAL CONDENSER ANDPARTIAL REBOILER
Z = 60 ft
SUMMARY
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SUMMARY
TRAY LAYOUT
Stray = 3 ft
Top and Bottom Plates
dh = 0.50 in
tp = 0.25 in
P = 2 in
Number ofholes=
SUMMARY
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SUMMARY
DOWNCOMER ASSEMBLY
Top Plate
hw= 3 in
lw = 5.525 ft
R f
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References:
Barrientos, Melvin Buensalido.
Foust, Alan S., et al. Principles of Unit Operations. 2nded. Singapore:John wiley & Sons. 1980
McCabe, Warren L., et al. Unit Operations for Chemical Engineers. 7th
ed. USA: McGraw-Hill Inc. 2006.
Molina, Claudia Arabelle.
Perry, Robert H., and Don W. Green. Perrys Chemical EngineeringHandbook, 7thed. USA: McGraw-Hill, Inc. 1997.
Van Winkle, Matthew. Distillation.