tarek moustafa1 chemical reaction engineering an introduction to industrial catalytic reactors tarek...
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Tarek Moustafa 1
Chemical Reaction Engineering
An Introduction to Industrial Catalytic Reactors
Tarek Moustafa, Ph.D.
November 2011
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Module objectives (TPO)
• To differentiate between various types of catalytic reactors
• To apply the design equations: material, energy and momentum balance equations on ideal and industrial catalytic reactors
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Introduction
• In most of chemical engineering job venues, a good understanding of industrial reactors is essential and important
• The reactors are the heart of most chemical processes and all technologies starts from the reaction part and accordingly the reactor
• Many types of industrial reactors are available depending on the reaction and the process involved
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General Classifications• Catalytic vs. non-catalytic Reactions
- Catalytic reactions are more dominant in chemical industry (especially organic)
- Catalytic reactions are more difficult to handle
• Homogeneous vs. Heterogeneous Catalysts
- Homogeneous catalysts are generally more active but a separation & recycle steps for the catalyst are essential
- Heterogeneous catalysts are most widely used
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Introduction
• Ultimate Objective:
Commercial Reactor– Design and Operate:
Successfully
• Typical Unfortunate News– Catalyst does not perform
well when scaled-up to commercial reactor
– Hot spot, temperature
runaway, explosion
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Phenomena in Commercial Reactors
• Transport Phenomena– Momentum Transfer– Heat Transfer– Mass Transfer
• Chemical Reactions– On Heterogeneous Catalyst
Surface
All Happens Simultaneously !
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Types/Configurations of catalytic reactors
• Fixed Bed Catalytic Reactors- Adiabatic single packed bed- Adiabatic beds in series with intermediate cooling or
heating- Multi-tubular fixed bed- Radial flow bed- Reverse flow bed- Auto-thermal reactors
• Fluidized Bed Reactors• Moving Bed Reactors• CSTR with jacket or coil (usually for liquid phase)
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Reactors’ Schematic
Single Adiabatic
bed
Adiabatic beds in series or staged
beds with intermediate
heating or cooling
Multitubular fixed bed
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Reactors’ Schematic
Radial flow bed
Reverse flow reactors
Auto-thermal reactors
TT0
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Important Phenomena & Considerations
• Adiabatic Packed Bed Catalytic Reactors- Simplest design- Used when reaction is associated with moderate heat
generation / consumption• Multi-tubular fixed bed
- Reaction is associated with high heat generation / consumption
• Radial flow bed- Pressure drop is critical
• Reverse flow bed- Used for endothermic reactions, to produce product and exothermic catalyst regeneration
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Ideal reactors
• CSTR (continuous stirred tank reactor)- Composition and temperature everywhere is the
same and equals that of the outlet- Infinite diffusion and sometimes called one point
reactor
• PFR (Plug flow reactor) - Composition and temperature changing from one point to another along the length of the reactor- No diffusion and flow is only due to bulk flow inside the reactor
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Non-isothermal continuous-flow stirred catalytic reactor
Process Feed
Cooling/Heating fluid inlet
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Non-isothermal continuous-flow stirred catalytic reactor – Design Equations
Q = Fout Cp (T – Tr) - FAo Cpo (To – Tr ) + FAo x HR
• Material Balance
W rA = FAo x
• Rate Law (in case of first order reaction)
rA = ko e-E/RT CA
• Energy Balance
Q = U A (T – Tc)
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Example 101 An isomerization reaction is taking place in a continuous stirred catalytic reactor: A BThe reaction is first order with respect to A and the rate can be expressed as: k = 16.96*1014 e-19400/T m3/kg cat h. It is desired to feed 800 kgmole per hour of pure liquid A to the reactor. If the reactor is operated adiabatically and the inlet temperature and concentration are 140°C and 10 gmol/l respectively. What is the volume required of the catalyst to achieve 20% conversion if the catalyst bulk density is 2 g/cm3. (Hr = 21 kcal/gmole,
Cp A = 32 cal/gmole K and Cp B = 36 cal/gmole K)
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Solution
Q = Fout Cp (T – Tr) - FAo Cpo (To – Tr ) + FAo x HR
• Material Balance
W rA = FAo x W rA = 800 * 0.2
• Energy Balance
• Rate Law
0 = 800*32.8*(T – 298) – 800*32*(413 – 298 ) - 800*0.2*21000
rA = ko e-E/RT CA = 16.96 1014 e-19400/538.2 *10(1-0.2)
= 0.377 kgmol/kgcat h
T = 538.2 K
W = 424.6 kg and V = 0.2123 m3
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Isothermal plug-flow catalytic reactor
• Compositions and possibly pressure are changing along the length of the reactor
• Rate is not constant inside the reactor, and is varying form one location to another
Fs 2
T, P2
Fs 1
T, P1
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Isothermal plug-flow catalytic reactor – Design Equations
• Material Balance
rA dW = FAo dx
• Rate Law
Could be power form or Langmuir-Hinshelwood kinetics
rA = ko e-E/RT CA /(1+KACA+KBCB)
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Non-isothermal plug-flow catalytic reactor
• Compositions, temperature and possibly pressure are changing along the length of the reactor
• Rate is not constant inside the reactor, and is varying form one location to another
Fs 2
T2, P2
Fs 1
T1, P1
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Non-isothermal plug-flow catalytic reactor – Design equations
F Cp dT + rA dW HRo - U A (T – Tc) = 0
• Material Balance
rA dW = FAo dx
• Rate Law (Langmuir-Hinshelwood kinetics)
rA = ko e-E/RT CA /(1+KACA+KBCB)
• Energy Balance
• Momentum Balance
dP/dL = - G (1-) [150(1- ) + 1.75 G]Dp 3 Dp
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References• Missen, R., Mims, C. and Saville, B., Introduction
to chemical reaction engineering and kinetics, Wiley (1999).
• Fogler, S., Elements of chemical reaction engineering, 4th ed., Prentice-Hall (2004).
• Froment, G.F. and K.B. Bishoff, “Chemical reactor analysis and design”, 2nd ed., Wiley (1990).