G1

G2
g1
g2
Gs
L2
L1
Ls
Li
y1
y2
x1
x2
X1, X2, Y1, Y2

molar flow rate of incoming gas

molar flow rate of outgoing gas
molar low rate of solubles in incoming gas
molar flow rate of solubles in outgoing gas
molar flow rate of insolubles in gas
molar flow rate of incoming liquid
molar lowrate of outgoing gas
molar flow rate of solubles in liquid
molar flow rate of inolubles in liquid
mole fraction of solute in incoming gas
mole farction of solute in outgoing gas
mole fraction of solute in outgoing liq
mole fraction of solute in incoming liquid
respective mole ratio

Data:
g1
G1
Gs
y1
Y1
y2
Y2
G2
g2
packing

0.001373913
12.72413793
12.72276402
0.000107977
0.000107989
1.07989E-06
1.07989E-06
12.72277776
1.37391E-05
pall rings

kmol/hr
kmol/hr
kmol/hr

kmol/hr
kmol/hr

l1
L1
Ls
x1
X1
x2
X2
L2
l2

Diameter of the column

Fp
92 /m
packing factor
a
130 m2/m3
surface area
FLG
0.116801854
take 4.2 mm/m water column pressure drop
from graph
KF
0.0042
K
0.00182952
Gw
0.501653707 kg/m2/s
G1
0.004559483 kg/s
A
0.009088905 m2
D
0.107574871 m
107.5748713 mm

m
no

1.234
y
Y
x
X
1 0.000107977 0.000108 8.75015E-05 8.75092E-05

L2, Ls, x2, X2

L1, Ls, x1, X1

1.2
66.66803
0
0.018
0.01833
0.01798
0.018309
66.66667
1.19864

kmol/hr
kmol/hr
kmol/hr

kmol/hr
kmol/hr

2
3
4
5
6
7
8
9
10

0.000215954
0.000323931
0.000431908
0.000539885
0.000647861
0.000755838
0.000863815
0.000971792
0.001079769

0.000216
0.000324
0.000432
0.00054
0.000648
0.000756
0.000865
0.000973
0.001081

0.000175003
0.000262505
0.000350006
0.000437508
0.000525009
0.000612511
0.000700012
0.000787514
0.000875015

0.000175034
0.000262574
0.000350129
0.000437699
0.000525285
0.000612886
0.000700503
0.000788135
0.000875782

0.0012
0.001
0.0008
Y 0.0006
0.0004
0.0002
0
0

0.0002

L2, Ls, x2, X2

G2, Gs, y2, Y2

L1, Ls, x1, X1

G1, Gs, y1, Y1

Equlibrium curve

0.0002

0.0004

0.0006
X

0.0008

0.001

G1
G2
g1
g2
Gs
L2
L1
Ls
y1
y2
x1
x2
X1, X2, Y1, Y2
Gw
Lw
A
D
P
ae
L
CaL
ReG
Z
Dl
Dg
aw
Data:
G1
g1
Gs
y1
Y1
y2
Y2
G2
g2

molar flow rate of incoming gas

molar flow rate of outgoing gas
molar low rate of solubles in incoming gas
molar flow rate of solubles in outgoing gas
molar flow rate of insolubles in gas
molar flow rate of incoming liquid
molar lowrate of outgoing gas
molar flow rate of insolubles in liquid
mole fraction of solute in incoming gas
mole farction of solute in outgoing gas
mole fraction of solute in outgoing liq
mole fraction of solute in incoming liquid
respective mole ratio
mass velocity of gas
mass velocity of liquid
area of column
diameter of column
operating pressure
efffective area for mass transfer
suraface tension liquid side
liquid capillary no.
(l*Lw/L/L)
gas reynolds no.
(6*Gw/a/g)
height of packing
m
liquid phase diffusion coefficient
gas phase diffusion coefficient
wetted surface of packing

12.26662074
0.001373913
12.26524682
0.000112004
0.000112017
3.3605E-05
3.36062E-05
12.26565901
0.000412188

kmol/hr
kmol/hr
kmol/hr

Flow rate of incoming gas

Flow rate of incoming liquids
HNO3 final concentration
NO2 absorbed

kmol/hr
kmol/hr
L2
l2
x2
X2
l1
L1
x1
X1

11.11111
0.4
0.036
0.037344
0.400962
11.11207
0.036083
0.037434

kmol/hr
kmol/hr

kmol/hr
kmol/hr

Gm
Lm
packing

12.26613987 m
11.11159197
pall rings

1.234

polypropylene

nominal size
no of elements
mass
surface area (a)
percent void space ()
packing factor (Fp)
MWR
liquid rate

38
13600
76
130
91
105
0.1
13

mm
/m3
kg/m3
m2/m3
/m
m3/m2/hr

Tower diameter
FLG
KF
K
P
Gw
G1 (mass)
A
D'
D
A

0.031210124
0.105
0.045738
6
2.252183636
0.098916667
0.043920338
0.23647645
0.5
0.196349541

ratio
liquid rate

13.15789474 if >10 than accept

4.553699012 same so accept

from figure 9.3

mmWC/m of packing
kg/m2/s
kg/s
m2
m
m
take

0.105 for 1150

from fig. 9.3

for pall rings

scrubbing of NO2 from air by water is liquid phase controlling problem

NTU
absorption with reaction
NOG
1.203860794
HTU
Lw
P
L
caL
ReG
Dl
Dg
T

1.264916392
101325
70
1.80702E-05
5618.753355
2.00E-09
1.53E-05
298

NTU
absorption with reaction
NOL
NOL
kg/m2/s
Pa
mN/m

m2/s
m2/s
K

pure water

C1
R
c

5.23 for d>12 mm

8314 J/Kmol/K
33 mN/m

trial
Takeuchi method
HOG
Z
l^0.5
Z^0.4
(caL*ReG)^0.392
ae
(R*T/a/Dg)
(Gw/a/g)^0.7
(g/g/Dg)^1/3
(a*d)^-2
KG
HG
HOG

method 2
HOG
z
Scg
f1
f2
f3
HG
HOG
z

trail

0.6
0.722316476
8.366600265
0.877992909
0.407932841
156.6576932
1.25E+09
120.2380994
1.006181959
0.040977561
2.08E-08
0.234808333
0.234808333

m
m

HOL
Z
ae
Re
Fr
We
XXX
aw
(l/l/g)^1/3
(Lw/aw/l)^2/3
(l/l/Dl)^-0.5
(a*d)^0.4
KL
HL
HOL

m2/m3

kmol/m2/s/Pa

cornell
0.08
0.096308864
1.018660764
1
1
1
0.291446798
0.291446798
0.350861374

HOL
z
phi
C
(l/l/Dl)^0.5
(Z/3.05)^0.15
HL
HOL
final

300
200
1
2

kmol/hr
lit/hr
M
M

L2, Ls, x2, X2

G2, Gs, y2, Y2

L1, Ls, x1, X1

G1, Gs, y1, Y1

g
l
MW air
MW water
MW NO2
l
g

1.187
1000
29.03
18
46
1
9.81
1
0.0185

kg.m3
kg/m3

cP
m/s
cP

tion with reaction

0.002314876
0.5

packing

pall rings

metal

nominal size
no of elements
mass
surface area (a)
percent void space ()
packing factor (Fp)
MWR
liquid rate

25
50100
88
205
90
170
0.1
20.5

mm
/m3
kg/m3
m2/m3
/m
m3/m2/hr

Tower diameter
FLG
KF
K
P
Gw
G1 (mass)
A
D'
D

0.031210124
0.105
0.045738
50
1.770002939
0.098916667
0.05588503
0.266749001
0.3

ratio
liquid rate

12 if >10 than accept

3.578775951 same so accept

from figure 9.3

mmWC/m of packing
kg/m2/s
kg/s
m2
m
m
take

from fig. 9.3

for pall rings

scrubbing of NO2 from air by water is liquid phase controlling problem

NTU
absorption with reaction
NOG
1.203860794
HTU
Lw
P
L
caL
ReG
Dl
Dg
T

0.012200094
101325
70
1.74287E-07
2800.268328
2.00E-09
1.53E-05
298

kg/m2/s
Pa
mN/m

m2/s
m2/s
K

pure water

C1
R
c

5.23 for d>12 mm

8314 J/Kmol/K
33 mN/m

trial
Takeuchi method
HOG
Z
l^0.5
Z^0.4
(caL*ReG)^0.392
ae
(R*T/a/Dg)
(Gw/a/g)^0.7
(g/g/Dg)^1/3
(a*d)^-2
KG
HG
HOG

0.6
0.722316476
8.366600265
0.877992909
0.050335941
30.48258271
7.90E+08
73.84717372
1.006181959
0.038072576
1.87E-08
1.05E+00
1.053938372

0.21
0.252810767
0.06
0.75
22.36067977
0.688294595
0.211153377
0.211153377

method 2
HOG
z
Scg
f1
f2
f3
HG
HOG

0.37
0.445428494
1.02E+00
1
1
1
4.153104901
4.268452666

0.254199272

0.6
0.3
222.635407 m2/m3
9.730126094
2.1203E-05
0.000175826
-0.31473013
35.10183986
46.71363513
10.90991315
0.04472136
1.894483292
0.000100915 kmol/m2/s/Pa
0.056300727
0.056300727

cornell

5.138622815

m
m

m2/m3

kmol/m2/s/Pa

from fig. 9.3

for pall rings

ng problem
NTU
absorption with reaction
NOL
0.002315
NOL
0.002315

trail

final

HOL
Z
ae
Re
Fr
We
XXX
aw
(l/l/g)^1/3
(Lw/aw/l)^2/3
(l/l/Dl)^-0.5
(a*d)^0.4
KL
HL
HOL

0.26046
0.000603
519.3203 m2/m3
0.059513
3.11E-09
1.04E-08
-0.04192
8.416043
46.71364
1.280865
0.044721
1.92255
1.2E-05
0.001954
0.001954

HOL
z
phi
C
(l/l/Dl)^0.5
(Z/3.05)^0.15
HL
HOL

0.247
0.000572
0.06
0.75
22.36068
0.276019
0.084676
0.084676

0.101939

G1
G2
g1
g2
Gs
L2
L1
Ls
y1
y2
x1
x2
X1, X2, Y1, Y2
Gw
Lw
A
D
P
ae
L
CaL
ReG
Z
Dl
Dg
aw
Gm
Lm
m
G
L

molar flow rate of incoming gas

molar flow rate of outgoing gas
molar low rate of solubles in incoming gas
molar flow rate of solubles in outgoing gas
molar flow rate of insolubles in gas
L2, Ls, x2, X2
molar flow rate of incoming liquid
molar lowrate of outgoing gas
molar flow rate of insolubles in liquid
mole fraction of solute in incoming gas
mole farction of solute in outgoing gas
mole fraction of solute in outgoing liq
mole fraction of solute in incoming liquid
respective mole ratio
mass velocity of gas
mass velocity of liquid
area of column
L1, Ls, x1, X1
diameter of column
operating pressure
efffective area for mass transfer
suraface tension liquid side
liquid capillary no.
(l*Lw/L/L)
gas reynolds no.
(6*Gw/a/g)
height of packing
m
liquid phase diffusion coefficient
gas phase diffusion coefficient
wetted surface of packing
average molar fow rate of gas
avergae molar flowrate of liquid
slope of quilibrium line
mass flow rate of gas
mass flow rate of liquid

Data:
Flow rate of incoming gas
Flow rate of incoming liquids
HNO3 final concentration
NO2 absorbed

300
1200
1
2

G1
g1
Gs
y1
Y1
y2
Y2
G2
g2

300
0.001373913
299.9986261
4.57971E-06
4.57973E-06
1.37392E-06
1.37392E-06
299.9990383
0.000412174

kmol/hr
kmol/hr
kmol/hr

L2
l2
x2
X2
l1
L1
x1
X1

66.66666667
2.4
0.036
0.037344398
2.400961739
66.66762841
0.036013907
0.037359363

kmol/hr
kmol/hr

kmol/hr
kmol/hr

kmol/hr
kmol/hr

kmol/hr
lit/hr
M
M

300 kmol/hr gas

removal nox is 70%

G2, Gs, y2, Y2

G1, Gs, y1, Y1

Gm
Lm
m

299.9995191 kmol/hr
66.66714754 kmol/hr
1.234 pv/pt

G
L

252.7379949 kg/hr
1200 kg/hr

Properties
g
l
MW air
MW water
MW NO2
l
g

g
packing

1.187
1000
29.03
18
46
1
9.81
1
0.0185
pall rings

kg/m3
kg/m3

gas density
liquid density

cP
m/s

liquid viscosity

cP

gas viscosity

metal

nominal size
no of elements
mass
surface area (a)
percent void space ()
packing factor (Fp)
MWR
liquid rate

16
214000
116
340
87
310
0.1
34

mm
/m3
kg/m3
m2/m3
/m
m3/m2/hr

Tower diameter
FLG
KF
K
P
Gw
G1 (mass)
A'
D'
D
A

0.163582209
0.12
0.052272
45
2.088316895
0.070204999
0.033617981
0.206890656
0.21
0.034636059

ratio
liquid rate

12.93066598 if >10 than accept

for pall rings
35.69518302 >
34 accept
34.64597401

from figure 9.3

mmWC/m of packing from fig. 9.3
kg/m2/s
kg/s
m2
m
m
take
m2

scrubbing of NO2 from air by water is liquid phase controlling problem

NTU
absorption with reaction
NOG

1.203968225

HTU
Gw
Lw
P
L
caL
ReG
Dl
Dg
T
C1
R
c

2.026933797
9.623881668
101325
70
0.000137484
1933.482159
2.00E-09
1.53E-05
298
5.23
8314
33

kg/m2/s
kg/m2/s
Pa
mN/m

pure water

m2/s
m2/s
K
for d>12 mm
J/Kmol/K
mN/m

Trial and Error

method 2
HOG

cornell
1.8

Calulation of HG
z'

Calculation for HL
2.167142804

Scg
f1
f2
f3
kappa
HG

1.018660764
1
1
1
60 for metal pall ring
0.049317

HOG
z'

1.802583198 m
2.170252893

z
take

3.617088155 m
3.75 m

phi
0.065 fig. 9.5
C
0.75 fig. 9.6
(l/l/Dl)^0.522.3607
(Z/3.05)^0.150.95003
HL
0.31574

Takeuchi method
HOG
Z

0.518 m
0.62365554 m

l^0.5
Z^0.4
(caL*ReG)^0.392
ae
(R*T/a/Dg)
(Gw/a/g)^0.7
(g/g/Dg)^1/3
(a*d)^-2
KG
HG

8.366600265
0.82790006
0.594894868
633.6536475 m2/m3
4.76E+08
834.1909441
0.044780555
0.03379109
1.38613E-08 kmol/m2/s/Pa
0.007821782

HOG
z

0.518220941 m
0.623921546

ReL
28.30553432
FrL
0.00321004
WeL
0.003891559
XXX
-0.50619314
aw
135.0527818
(l/l/g)^1/3
46.71363513
(Lw/aw/l)^2/3
17.18823015
(l/l/Dl)^-0.5
0.04472136
(a*d)^0.4 1.968972089
KL
0.000165239
HL
0.091914939

0.034636059 m2

A
nh
Lm
v
a
dp

distributor ias required for each 194 cm2 are

nh
Lm
v
a
dp

1.785363866
4
0.000333333
3
0.000111111
5.947080387
6

take
m3/s
m/s
m2
mm
mm

c/s area of column

no if ditributor
volumetric flowrate of liquid
solvent velocity in holes
c/s of liquid pipe
dia of pipe
void space

perforated pipe type distributor

dia of ring would be

0.105 m with 4 no of holes with 6 mm dia. seperated 90 deg apart

paking support design

hs
x

height of the riser

width of slot in riser

dc
210 mm

87 %
use cap type packing support

dr
n
dc

diameter fo riser
no of risers
inside diameter of the coulmn

ns
as
vw
nw
dw

no of slots per riser

total area of slots of riser
velocity of liquid thropugh weep hole
no of weeping holes
dia of weeping hole

nr

no of redistributor required

riser design
dr
35 mm
let, x
10
ns
5.497787144
6 take
minimum area required
minimum height of slot in riser (hs)
take
let, dw
vw
aw
nw

5
1
1.9635E-05
16.97652726
20

so, n

30133.37 mm2
71.74612 mm
80 mm

mm
m/s
m2
take

redistributor design
nr
1.5
take 1 at 1.75 m
use same as packing support.

use hold down plate above packings

use 12 mm sqaure aperture wire grid.

flowrate of liquid
ocity in holes

meter of the coulmn

of slots of riser
ns*n*h*x
liquid thropugh weep hole

tributor required

Data:
Flow rate of incoming gas
Flow rate of incoming liquids
HNO3 final concentration
NO2 absorbed

G1
g1
Gs
y1
Y1
y2
Y2
G2
g2

300
0.001373913
299.9986261
4.57971E-06
4.57973E-06
4.57973E-08
4.57973E-08
299.9986398
1.37391E-05

kmol/hr
kmol/hr
kmol/hr

L2
l2
x2
X2
l1
L1
x1
X1

66.66666667
2.4
0.036
0.037344398
2.401360174
66.66802684
0.036019668
0.037365563

kmol/hr
kmol/hr

Gm
Lm
m

299.9993199 kmol/hr
66.66734675 kmol/hr
1.234 pv/pt

G
L

252.7379949 kg/hr
1200 kg/hr

300
1200
1
2

kmol/hr
lit/hr
M
M

kmol/hr
kmol/hr

kmol/hr
kmol/hr

Properties
g
l
MW air
MW water
MW NO2
l
g

g
packing

1.187
1000
29.03
18
46
1
9.81
1
0.0185
pall rings

kg/m3
kg/m3

gas density
liquid density

cP
m/s

liquid viscosity

cP

gas viscosity

metal

300 kmol/hr gas

removal nox is 99%

nominal size
no of elements
mass
surface area (a)
percent void space ()
packing factor (Fp)
MWR
liquid rate

16
214000
116
340
87
310
0.1
34

mm
/m3
kg/m3
m2/m3
/m
m3/m2/hr

Tower diameter
FLG
KF
K
P
Gw
G1 (mass)
A'
D'
D
A

0.163582209
0.12
0.052272
45
2.088316895
0.070204999
0.033617981
0.206890656
0.21
0.034636059

from figure 9.3

mmWC/m of packing from fig. 9.3
kg/m2/s
kg/s
m2
m
m
take
m2

ratio
12.93066598 if >10 than accept
for pall rings
liquid rate 35.69518302 >
34 accept
34.64597401
scrubbing of NO2 from air by water is liquid phase controlling problem
NTU
absorption with reaction
NOG
4.605165606
HTU
Gw
Lw
P
L
caL
ReG
Dl
Dg
T
C1
R
c

2.026933797
9.623881668
101325
70
0.000137484
1933.482159
2.00E-09
1.53E-05
298
5.23
8314
33

Trial and Error

kg/m2/s
kg/m2/s
Pa
mN/m

pure water

m2/s
m2/s
K
for d>12 mm
J/Kmol/K
mN/m

method 2 cornell
HOG

2.31

Calulation of HG
z'
10.63793255
Scg
f1
f2
f3
kappa

1.018660764
1
1
1
60 for metal pall ring
HG
0.083372

HOG
z'

2.309200112 m
10.63424893

z
take

17.72374822 m
18 m

Calculation for HL
phi
0.065 fig. 9.5
C
0.75 fig. 9.6
(l/l/Dl)^0.522.36068
(Z/3.05)^0.151.206101
HL
0.400838

Data:
Flow rate of incoming gas
Flow rate of incoming liquids
HNO3 final concentration
NO2 absorbed

G1
g1
Gs
y1
Y1
y2
Y2
G2
g2

20.4443679
0.01373913
20.43062876
0.000672025
0.000672477
6.72477E-07
6.72478E-07
20.4306425
1.37391E-05

kmol/hr
kmol/hr
kmol/hr

L2
l2
x2
X2
l1
L1
x1
X1

55.55555556
2
0.036
0.037344398
2.013725391
55.56928095
0.036238104
0.037600682

kmol/hr
kmol/hr

Gm
Lm
m

20.4375052 kmol/hr
55.56241825 kmol/hr
1.234 pv/pt

G
L

500
1000
1
2

m3/hr
lit/hr
M
M

0.632 kg/hr

kmol/hr
kmol/hr

kmol/hr
kmol/hr

593.5 kg/hr
1000 kg/hr

Properties
g
l
MW air
MW water
MW NO2
l
g

g
packing

1.187
1000
29.03
18
46
1
9.81
1
0.0185
pall rings

kg/m3
kg/m3

gas density
liquid density

cP
m/s2

liquid viscosity

cP

gas viscosity

metal

500 m3/hr gas

removal nox is 99.9%

nominal size
no of elements
mass
surface area (a)
percent void space ()
packing factor (Fp)
MWR
liquid rate

25
50100
88
205
90
170
0.1
20.5

mm
/m3
kg/m3
m2/m3
/m

51.816 /ft

m3/m2/hr

Tower diameter
FLG
KF
PF
K
P
Gw
G1 (mass)
A'
D'
D
A

0.058050322
0.175
1.902418081
0.07623
60
2.285063969
0.164861111
0.072147263
0.303085381
0.32
0.080424772

No need of fig
Correlation found by datafit
KF = 1/(4.363+31.534*FLG+10.419*FLG^
PF = 0.12*Fp^0.7
P = (0.66^2)*PF

from figure 9.3

inchH2O/ft 158.5348 mmH2O/m
mmWC/m of packing from fig. 9.3
kg/m2/s
kg/s
m2
m
m
take
m2

ratio
12.12341525 if >10 than accept
liquid rate 13.86053966 >
12.43397993

FLG
KF
PF
K
P

for pall rings

accept

scrubbing of NO2 from air by water is liquid phase controlling problem

NTU
absorption with reaction
NOG
6.907083028
HTU
Lw
Dl
Dg

3.453883314 kg/m2/s
2.00E-09 m2/s
1.53E-05 m2/s

Trial and Error

method 2 cornell
HOG
0.224
z'
1.547186598
Calulation of HG

Calculation for HL

Scg

phi

1.018660764

0.065 fig. 9.5

0.05805
0.160548
1.902418
0.069935
69.05778

f1
f2
f3
kappa
HG

1
1
1
60 for metal pall ring
0.137583206

HOG
z'

0.273832453 m
1.891383485

z
take

3.152305809 m
3.3 m
Crosscheck:
Flg
Gw
K
KF
Flooding

0.05805
2.04988 Kg/m2/s
0.061346
0.17
0.600715

0.080424772 m2

distributor ias required for each 194 cm2 are

nh
Lm
v
a
dp

4.145606801
4
0.000277778
3
9.25926E-05
5.428916799
6

C
0.75 fig. 9.6
(l/l/Dl)^0.522.36068
(Z/3.05)^0.150.903205
HL
0.300173

take
m3/s
m/s
m2
mm
mm

A
nh
Lm
v
a
dp

c/s area of column

no if ditributor
volumetric flowrate of liquid
solvent velocity in holes
c/s of liquid pipe
dia of pipe
void space

perforated pipe type distributor

dia of ring would be

0.16 m with 4 no of holes with 6 mm dia. seperated 90 deg apart

paking support design

hs
x

height of the riser

width of slot in riser

dc
320 mm

90 %
use cap type packing support

dr
n
dc

diameter fo riser
no of risers
inside diameter of the coulmn

riser design
dr
53.33333333 mm
let, x
10
ns
8.37758041
7 take
minimum area required
minimum height of slot in riser (hs)
take
let, dw
vw
aw
nw

5
1
1.9635E-05
14.14710605
20

so, n

ns
as
vw
nw
dw

no of slots per riser

total area of slots of riser
velocity of liquid thropugh weep hole
no of weeping holes
dia of weeping hole

nr

no of redistributor required

72382.29 mm2
147.719 mm
90 mm

mm
m/s
m2
take

redistributor design
nr
1.64
take 1 at 1.25 m
use same as packing support.
use hold down plate above packings
use 12 mm sqaure aperture wire grid.

n found by datafit
63+31.534*FLG+10.419*FLG^2)

inchH2O/ft 158.5348 mmH2O/m

mmWC/m of packing

flowrate of liquid
ocity in holes

meter of the coulmn

of slots of riser
ns*n*h*x
liquid thropugh weep hole

tributor required