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高等輸送二 — 質傳
Lecture 8Forced convection
郭修伯 助理教授
Forced convection
• Forced convection– The flow is determined by factors other than
diffusion, factors like pressure gradients and wetted area
– exist whether or not diffusion occurs
• Analyzing tools– simple physical models– elaborate analytical mathematics
The film theory (for interfacial mass transfer)
• Assuming a stagnant film exists near interface, a solute present at high dilution is slowly diffusing across this film.
• At steady-state:
p1
c1iGas Bulk liquid
c1
z = 0 z = l
Liquid film)( 111 cckN i or
1101011 ccl
DjnN izz
l
Dk
D
klnumberSherwood
D
klnumberSherwood
tcoefficiendiffusion
lengthsticcharacteritcoefficientransfermassnumberSherwood
))((
?
)( svariablesystemotherflengthsticcharacteri
factorcorrectionlengthsticcharacteri
tcoefficiendiffusiontcoefficientransfermass
Example
Carbon dioxide is being scrubbed out of a gas using water flowing through a packed bed of 1 cm Berl saddles. The carbon dioxide is absorbed at a rate of 2.3 x 10-6 mol/cm2 sec. The carbon dioxide is present at a partial pressure of 10 atm, the Henry’s law coefficient H is 600 atm, and the diffusion coefficient of carbon dioxide in water is 1.9 x 10-5 cm2/sec. Find the film thickness.
The interfacial concentration:
1
111 c
cHHxp i
10 atm 600 atm
1/18 mol/cm3
9.3 x 10-4 mol/cm3
)( 111 cckN i Mass transfer k = 2.5 x 10-3 cm/sec
cmk
Dl 0076.0 typical order: 10-2 cm
Penetration theory (Higbie, 1935)
• The falling film is very thick. In the z direction, diffusion is much more important than convection, and in the x direction, diffusion is much less important then convection.
• Flux at the interface:
)( 11max
01011 ccxDvjnN izz
dxdynWL
N z
L W
010 01
1 )(2 11
max1 ccL
DvN i
The flux averaged over x is:
p1
c1iGas Bulk liquid
c1
z = 0 z =
)( 111 cckN i
)(2 11max
1 ccLDvN i
LDvk
max2
Dk
2/1
max
2/14
D
Lv
D
kL
max0
3
2vv
2/102/16
D
Lv
D
kL
Sherwood number Peclet number
2/12/102/16
D
v
v
Lv
D
kL
Reynolds number Schmidt number
Surface-renewal theory (Dankwerts, 1951)
• It consists of two regions: – Interfacial region: mass transfer occurs by penetration
theory.
– Renewal region: constantly exchanged with new elements from a second bulk region.
The length of time that small fluid elements spend in the interfacial region is the key.
Residence time distribution
p1
c1iGas
Bulk liquid
c1
z = 0
In the interfacial region, the flux is that for diffusion into a infinite slab:
)( 1101 cct
Dn iz
Residence time distribution
0
1)( dttE
The probability that a given surface element will be at the surface for time t E(t)dt =
The fraction of surface elements remaining at time t :
t
t dttEe )(/
The residence time distribution of surface element :
/
)(te
tE
The average flux is:
)()( 110101 ccD
dtntEN iz
Dk Dk
Comparison of the three theories
• The film theory
• The penetration theory
• The surface-renewal theory
Dk Dk
LDvk
max2 Dk
l
Dk Dk lunknown :
maxv
Lunknown
:unknown
Contact time
Film thickness
Surface residence time
Boundary layer theory
• A more complete description of mass transfer• Based on parallel with earlier studies of fluid
mechanics and heat transfer
laminar region
turbulent region • The sharp-edged plate made of a sparingly soluble solute is immersed in a rapid flowing solvent.• A boundary layer is formed.• The boundary layer is usually defined as the locus of distance over which 99% of the disruptive effect occurs.• When the flow pattern develops, the solute dissolves off the plate.
turbulent region
Layers caused by flow and by mass transfer
• The distance that the solute penetrates produces a new concentration boundary layer c , but this layer is not the same as that observed for flow . The two layers influence each other.
• When the dissolving solute is only sparingly soluble, the boundary layer caused by the flow is unaffected.
Assuming flow varies as a power series in the boundary layer thickness
find c ?
Find the boundary layer for flow first:
Assuming the fluid flowing parallel to the flat plate follows:
...33
2210 yayayaavx
The boundary conditions are:
0,0,02
2
y
vvy x
xThe fluid sticks to the plate.The plate is solid and the stress on it is constant.
Far from the plate, the plate has no effect.0,, 0
y
vvvy x
x
0,, 0
y
vvvy x
x
3
0 2
1
2
3
yy
v
vx
turbulent region
Mass balance on the control volume of the width W, the thickness x and the height l:
lyyyxx
l
xx
l
x xWvdyvWdyvW
000
)0(~0
Dividing Wxx 0
l
xy dyvdx
dv
0
x-momentum balance gives:
)()0(0 00
00xWxWvvdyvvWdyvvW y
xx
l
xxx
l
xx
Dividing Wxx 0
y
l
x vvdyvdx
d 0
0
20
0
00 )( dyvvv
dx
d
y
vxxy
x
0
00 )( dyvvv
dx
d
y
vxxy
x
3
0 2
1
2
3
yy
v
vx
013
140
vdx
d
0,0 x
2/102/1
13
280
vx
x
We have now and use to find vx.3
0 2
1
2
3
yy
v
vx
How about c ?
Find the boundary layer for concentration:
Assuming the concentration profile parallel to the flat plate follows:
...33
22101 yayayaac
The boundary conditions are:
0,,021
2
11
y
cccy i
The concentration and flux are constant at the plate.
Far from the plate, the plate has no effect.0,0, 11
y
ccy
0,, 101
y
cvcy c
3
1
1
2
1
2
31
cci
yy
c
c
turbulent region
Mass balance on the control volume of the width W, the thickness x and the height l:
)0(0 010 10 1 lyyxx
l
xx
l
x xWNdyvWcdyvWc
Dividing Wxx 0
l
xy dyvcdx
dnN
0 1011
c
dyvcdx
d
y
cD xy
0 101
3
1
1
2
1
2
31
cci
yy
c
c
2/102/1
13
280
vx
x
3
0 2
1
2
3
yy
v
vx
D
dx
dx cc
33
3
4 c
D
dx
dx cc
33
3
4
0,0 cx
Dc
3
2/102/1
13
280
vx
x
3/12/1
064.4
D
vxxc
Schmidt number:
D
Mass transfer coefficient?
)( 111 cckN i
01
011
yy y
cDnN
3
1
1
2
1
2
31
cci
yy
c
c
c
iDcN
2
3 11
Similar to film theory
3/12/1
01
1 323.0
D
vxx
DcN i
3/12/1
0323.0
D
vxD
kx
3/12/1
0323.0
D
vxD
kx
Averaged over length L
3/12/1
0646.0
D
vxD
Lk
• Valid for a flat plate when the boundary layer is laminar (I.e., Re < 300,000)
• ,between the prediction of the film theory and the penetration/surface-renewal theories.
3/2Dk
Water flows at 10 cm/sec over a sharp-edged plate of benzoic acid. The dissolution of benzoic acid is diffusion-controlled, with a diffusion coefficient of 1.0 x 10-5 cm2/sec. Find (a) the distance at which the laminar boundary layer ends, (b) the thickness of the flow and concentration boundary layers at that point, and (c) the local mass transfer coefficients at the leading edge and at the position of transition, as well as the average mass transfer coefficient over this length.
(a) the length before the turbulent region begins:
000,300
sec01.0
sec101 30
cmg
cmcm
gxvx
x = 300 cm
2/102/1
13
280
vx
x
x = 300 cmcm5.2
Dc
3
cmc 25.0
3/12/1
0323.0
D
vxD
kxsec/109.5 5 cmk
Graetz-Nusselt problem
• Mass transfer across the walls of a pipe containing fluid in laminar flow.
• Find the dissolution rate as a function of quantities like Reynolds and Schmidt numbers
Flow conditions Diffusion conditions
zr
Sparing soluble solute
Fixed solute concentration at the wall of a short tube
zr
Mass balance for the solute in a constant-density fluid on a washer-shaped region:
Solute accumulation by convection
Solute accumulation by diffusion
Solute accumulation =
z
cv
z
c
r
cr
rrD z
121
211
0
z
c
R
rv
r
cr
rr
D
1
201 120
z
c
R
rv
r
cr
rr
D
1
201 120
rRs
z
c
R
sv
s
cD
10
21
2 40
0,,0
,0,0
0,,0
1
11
1
csz
ccsz
csallz
i
34
3
11
d
i
ecc
3/10
9
4
DRz
vs
incomplete gamma function
How to find the mass transfer coefficient?
)( 111 cckN i
RrRr r
cDnN
1
11
)0(
34
94
1
3/10
1
icDRzv
DN
3/10
9
4
34
DRz
vDk
Averaged over length L:3/13/13/103/1
34
3
L
d
D
v
v
dv
D
dk
Sherwood
1.62
Reynolds
Schmidt
diameter length
Water is flowing at 6.1 cm/sec through a pipe of 2.3 cm in diameter. The walls of a 14-cm section of this pipe are made of benzoic acid, whose diffusion coefficient in water is 1.0 x 10-5 cm2/sec. Find the average mass transfer coefficient over this section.
3/13/13/103/1
34
3
L
d
D
v
v
dv
D
dk
3/13/1
25
3/13/1
25 14
3.2
sec/101
sec)/1.6)(3.2(
34
3
sec/100.1
3.2
cm
v
v
cmcm
cm
cmk
sec/103.4 4 cmk Check before ending the question!
21001400Re Laminar flow?
cmRpenetratedhasdiffusioncmv
DLs 15.1)(01.0
40
Short pipe?
OK!
Concentrated solutions
• In most application, correlations for dilute solutions can also be applied to concentrated solutions.
• In a few cases, k is a function of the driving force:
11 ckN ),,( 1cScRefk
11 ckN ),( ScRefk
2211111
01111
)(
)(
NVNVccck
vccckN
ii
ii
mass transfer coefficient for rapid mass transfer ? dilute system
p1
c1i
Gas
Bulk liquid
c1
z = 0 z = l
A mass balance on a thin film shell z thick shows that the total flux is a constant:
dz
dn10
221111
01
11
nVnVcdz
dcD
vcdz
dcDn
11
11
,
,0
cclz
ccz i
Dlv
i
e
vnc
vnc 0
01
1
01
1
0111
0
011
10 vccc
e
vnN ii
Dlvz
...
)(12
)(
21
20
20
0
00
k
v
k
vkk
The relation between the dilute mass transfer coefficient k0 and the concentrated mass transfer coefficient k.
or
10
0
0
0
0
kv
e
kv
k
k
Benzene is evaporating from a flat porous plate into pure flowing air. Using the film theory, find N1/k0c1i and k/k0 as a function of the concentration of benzene at the surface of the plate.
The benzene evaporates off the plate into air flowing parallel to the plate : 02 n
221111
01
11
nVnVcdz
dcD
vcdz
dcDn
11
cV
cnv 10
i
z cc
c
l
DcnN
1011 ln
In dilute solution: )0( 1,1 id cl
DN
)1ln(1
111
01
iii
xxck
N
)1ln(1
111
1
10
10
0
00
10
0 ii
i
ckN
kv
xx
x
e
ckN
e
kv
k
k
Summary of forced convection
• Table 13.6-1• all predictions cluster around experimentally
observed values• In most cases. Sh Re1/2 and Sc1/3
• Recommend: film and penetration theories