Page 1 of 3
Name
Reg No
APJ ABDUL KALAM TECHNOLOGICAL UNIVERSITY
07 THRISSUR CLUSTER
SECOND SEMESTER M.TECH. DEGREE EXAMINATION APR 2017
Chemical Engineering
Process Control
07 CH 6102
ADVANCED CHEMICAL REACTION ENGINEERING
Time 3 hours Max.Marks: 60
Answer all six questions. Part of each question is compulsory.
Answer either part or part of each question
Q.no. Module 1 Marks
1a Show that equal sized mixed flow reactors in series are equivalent to a plug
flow reactor?
4
Answer b or c
b How will you test the kinetics of autocatalytic reactions? 5
c An aqueous feed of A and B (400 L/min, 100 mmol 200 mmol is to be
converted to product in a PFR. The kinetics of reaction is represented by
200CACBmol lmin .Find the volume of reactor needed for
99.9% conversion of A to product.
5
Q.no. Module 2 Marks
2a Explain in detail the causes of non ideality? 4
Answer b or c
b Explain axial dispersion model? 5
c Draw the temperature-conversion plots for irreversible, reversible exothermic
and reversible endothermic reactions? Write a note on reactor stability?
5
Q.no. Module 3 Marks
3a For the reaction A B X A.X A.X ,C.X X
Develop rate expression if surface reaction is the rate controlling step.
4
Answer b or c
Page 2 of 3
b Define internal effectiveness factor? What is its significance?
5
c Derive the expression for Thiele modulus? 5
Q.no. Module 4 Marks
4a
Explain the mechanism of catalyst deactivation.
4
Answer b or c
b What is meant by fluidized bed? Briefly explain its features and discuss the
different types of fluidized beds.
5
c The catalytic decomposition of reactant → is studied in a packed bed
reactor filled with 2.4 mm pellets and using a very high recycle rate of product
gases (assume mixed flow). The results of a long-time run and additional data
are given below.
hr) 0 2 4 6
XA 0.75 0.64 0.52 0.39
De 5×10-10 m3/m cat. s ρs 1500 kg/m3 cat 4000 kg s/m3
Find the kinetics of reaction and deactivation, both in the diffusion-free and in
the strong pore diffusion resistance regime.
5
Q.no. Module 5
Marks
5a Outline the applications of different kinds of reactors used for solid catalysed
Gas-liquid reactions.
5
Answer b or c
b Derive the performance equations for different flow patterns of contacting
phases for gas-liquid reaction taking place on the surface of solid catalyst in
which the liquid component is in excess.
7
c Aqueous acetone (CB0 1000 mol/m3 liq, 10-4 m3 liq/s) and hydrogen
atm, 0.04 m3 gas/s, HA 36845 Pa m3 liq/mol) are fed to the bottom of a
long slender column m high, 0.1 m2 cross section) packed with porous
Raney nickel catalyst dp 5×10-3 m catalyst, ρs 4500 kg/m3 catalyst, fs
0.6, De=8×10-10m3 liq/m catalyst. and kept at 14oC. At these conditions
acetone is hydrogenated to propanol according to the reaction
7
Page 3 of 3


→



with rate given by
′ ′

and 􀝇′=2.35×10-3m3liq.(mol)1/2/kgs(m3liq)1/2. What will be
the conversion of acetone in this unit?
Q.no. Module 6
Marks
6a What are the factors to be considered for selecting a contactor for fluid-fluid
reactions?
5
Answer b or c
b Derive the expression to find the volume of reactor for plug flow gas/plug flow
liquid with straight mass transfer (for both concentrate and dilute systems) for
the reaction
→
7
c Gaseous A absorbs and reacts with B in liquid according to
→
in a packed bed under conditions where
kAga =0.1 mol/hr. m2 of reactor.Pa fl=0.01 m3liq/m3 reactor;
DAl=DBl=10-6m2/hr kAla 100 m3 liq/m3 reactor. hr; a 100 m2/m3 reactor
HA 105 Pa.m3 liq/mol; 10 m3 liq/mol.hr. At a point in the reactor where pA
100Pa and CB 100mol/m3 liquid.
Calculate the rate of reaction in mol/hr. m3 reactor.
Locate the major resistance to reaction
Determine the behaviour in the liquid film
7