Chapter11 Lecture Notes 1
Transcript of Chapter11 Lecture Notes 1
Chemical Reaction Engineering
(S1.2012)Fogler Chapter 11
External Diffusion Effects on Heterogeneous Reactions
Gia Hung Pham
Catalysis reactor types
1. Two phase reactor
- Fixed bed reactor
- Fluidized bed reactor
2. Three phase reactor
- Slurry reactor
Fixed bed reactor
Lit.: Jens Hagen; Industrial Catalysis A Practical Approach; Wiley-VCH; 1999
Fluidised bed reactor
Gas
Gas
Solid catalyst
Reactor
Cyclone
Compare: Fixed bed and Fluidised bed reactor
1. Catalyst pellet size
Fixed bed reactor : large (Heat and mass transfer will influence the rate and product selectivity)
Fluidised bed reactor: small
2. Catalyst weight
Fixed bed reactor requires much more catalyst than fluidised bed reactor.
3. Temperature control
Fixed bed reactor: bad, non-isothermal operation and hot spots ruin the catalyst.
Fluidised bed reactor: very good (rapid mixing of solid)
4. Pressure drop
Fixed bed reactor: high
Fluidised bed reactor: low
5. Catalyst deactivation - regeneration
Fixed bed reactor: less advantages (not suitable)
Fluidised bed reactor: more advantages
6. Scale-up
Fixed bed reactor: easy
Fluidised bed reactor: difficult
Three phase reactor
Lit.: Jens Hagen; Industrial Catalysis A Practical Approach; Wiley-VCH; 1999
Notes: reaction rate units
smmolCkdt
dN
Vr A
AA
3/1
sgmolCkdt
dN
wr catA
AA /
1 ''
smmolCkdt
dN
Sr A
AA
2'''' /1
Chapter 11: External diffusion effects on heterogeneous reaction
Effective reaction rate constant
Two steps involve in the reaction (External mass transfer and surface reaction )
Catalyst pellet
1
4Gas
Boundary layer
δ
CAb
CAs
A
P
4
1
P
Reaction first-order
A P
External mass transfer
Fick’s law
with
- kc : Mass transfer coefficient (m/s)
- DAB : Diffusion coefficient (m2/s) (is a function of T and P)
- δ : Boundary layer thickness (m) (is unknown, depends on fluid velocity, particle diameter, viscosity, density, temperature….)
- JAZ: average molar flux from the bulk fluid to the surface (mol/m2.s)
AsAbcA
ABAz CCkdz
dCDJ
AB
c
Dk
Concentration
Positional coordinate
Gasδ Cat
CAb
CAs
Mass transfer rate
Surface reaction rate (first order reaction)
Determination of CAs
At steady state rMT = rs
)( AsAbcMTAZ CCkrJ
AsrS Ckr
AsrAsAbc CkCCk )(
rc
AbcAs
kk
CkC
Derive the effective reaction rate
keff
Rate limiting1. Mass transfer is faster than surface reaction rate
kc » kr we have kc + kr ≈ kc
keff = kr
2. Surface reaction is faster than mass transfer kr » kc we have kc + kr ≈ kr
keff = kc
Ab
rc
rceffA C
kk
kkr
,
,
Determination of kc by using correlation equation
Sherwood number
Flow over a sphere
Reynolds and Schmidt number
u : fluid flow velocity (m/s)
l : characteristic length (particle diameter) (m)
ν : kinematic viscosity (m2/s)
kc increases with increasing fluid velocity. (Why ?)
AB
c
D
lkSh
3/12/1Re6.02 ScSh
ABDSc
luRe
Frossling correlation
From Sherwood number and Frossling correlation equation
3/12/1Re6.02 ScD
lk
AB
c
l
D
D
luk AB
AB
c
3/12/1
6.02
Fluid velocity affects kc
Effect of fluid velocity on the effective reaction rate
reff
u
With mass transfer effect
Without mass transfer effect
Example: Rapid reaction on a catalyst surface
Determine the effective rate of reaction per unit surface area of catalyst.
l = dp = 1 cm
CAs = 0 mol/L
CAb = 1 mol/L
u = 0.1 m/s
ν = 0.5x10-6 m2/s
Catalyst pellet
1
4
Fluid
Boundary layer
δ
CAb
CAs
A
PP
Reaction first-order
A P
DAB = 10-10 m2/s
Solution
AsAbcMT CCkr
7.460Re6.02 3/12/1 ScD
dkSh
AB
pc
2000105.0
1.0()01.0(Re
126
1
sm
msmud p
500010
1051210
127
sm
sm
DSc
AB
161210
1061.401.0
7.46010
msm
sm
d
ShDk
p
ABc
CAb = 103 mol/m3
rMT = 4.61x10-6 m/s x (103 – 0) mol/m3 = 4.61x10-3 mol/m2s
This is the effective reaction rate.
smmolr effA
23''
, /106.4
Mass transfer-limited reaction in packed bed
Reaction A + B P
At steady state
z z+∆z
Mass balance for this slice
of the catalyst bed
0''
\\ zAarFF ccAzzAzzAz
Molar rate in
Molar rate out
Molar rate of accumulation
0''
\\ zAarFF ccAzzAzzAz
Rate of generation of A per unit
Catalytic surface area (mol/s.m2)
External surface area of catalyst per volume of
catalyst bed (m2/m3)
Pd
16
Particle diameter (m)
Porosity of the bed (-)
Cross-sectional area of tube (m2)
Dividing the above equation by Ac∆z and ∆z →0
δ
flow in tube: JAz<<BAz
01 ''
cA
Az
c
ardz
dF
A
cAzAzAzcAz ABJWAF
Molar flux of A (mol/m2s)
Molecular diffusive flux (mol/m2s)
Flux of A resulting from
Bulk flow (mol/m2s)
cAAzcAzcAz AUCBAWAF
superficial velocity (m/s) = constant
Cat
SurfaceCA
CAs
)(''
AsAcArA CCkWr
= 0
AccA Cak
dz
dCU
z
U
ak
C
C cc
A
A exp0
Axial concentration profile in the reactor
CA/CA0
1
z
Integrating with the limit, at z =0, CA = CA0
0
Determine the reactor length L necessary to achieve a conversion X
At z = L
z
U
akCkr cc
AcA exp0
''
Reaction rate along the length of the reactor
0
0
A
ALA
C
CCX
LU
ak
X
cc1
1ln
In class exercise
Tubular fixed bed reactor with spherical catalyst
External mass transfer control
Calculate final conversion X of the reaction A P
Additional information:
- Catalyst bed length L = 2 m
- Catalyst bed diameter dR = 6 cm
- Bed porosity φ = 0.5
- Catalyst sphere diameter dp = 3 mm
- Superficial gas velocity U = 3 m/s
- Sherwood number Sh = 60
- Diffusion coefficient DAB = 10-7 m2/s
Solution
- Reorganise the equation
- Calculate kc
- Calculate ac (specific surface area)
- Calculate kc ac L / U
- Calculate X