STUPIDSID
1(a)
Write short note on Shrinking core model and Progressive conversion model
5 M
1(b)
What is significance of hatta number in Fluid Fluid reactions?
5 M
1(c)
Explain Segregation model
5 M
1(d)
Determine the pore volume and catalyst particle porosity for the sample of activated silica from following data:
Mass of catalyst sample placed in chamber = 101.5 gm.
Volume of Helium displaced by sample = 45.1 cm3
Volume of Mercury displaced by sample = 82.7 cm3
Mass of catalyst sample placed in chamber = 101.5 gm.
Volume of Helium displaced by sample = 45.1 cm3
Volume of Mercury displaced by sample = 82.7 cm3
5 M
2(a)
It is proposed to remoce CO2 from air by countercurrent contact with water at 25°C.
i) Find the resistance of the gas and liquid films for this operation?
ii) Suggest the simplest form of equation for tower design.
iii) For this absorption operation, would you except reaction with absorption to be helpful? If so, why?
Data: For Co2 between air and water,
kg=0.80 mol/(h.m3.Pa)
Kl=25 hr-1
H=3000(Pa.m3)/mol
i) Find the resistance of the gas and liquid films for this operation?
ii) Suggest the simplest form of equation for tower design.
iii) For this absorption operation, would you except reaction with absorption to be helpful? If so, why?
Data: For Co2 between air and water,
kg=0.80 mol/(h.m3.Pa)
Kl=25 hr-1
H=3000(Pa.m3)/mol
10 M
2(b)
For the gas-liquid reaction of the type
A(gorl) + bB(I) &rarr
A(gorl) + bB(I) &rarr
10 M
3(a)
Derive the conversion time expression for the case of Chemical reaction controlling ina gas non catalytic reaction.
10 M
3(b)
An ore of uniform size complete size particles is to be roasted in a fluidized bed reactor. The time required for complete conversion of solid particles is 20 min and the mean residence time of particles in the bed is 48 min. The solids remain unchanged in size during reaction. Calculate the fraction of the original ore remaining unconverted assuming:
i) The chemical reaction step to be rate controlling.
ii) The ash diffusion step to be rate controlling.
i) The chemical reaction step to be rate controlling.
ii) The ash diffusion step to be rate controlling.
10 M
4
A tracer with number of dividing baffles is to be used to carry out the reaction A → R with -rA = kCA, k=0.25 min-1
The results of a pulse tracer test are given below
a) Plot C(t), E(t) and F(t) curves.
b) Calculate mean residence time.
c) Find the conversion excepted in the tank-in-series model and how many tanks in series would you suggest to model this reactor.
d) calculate conversion assuming Mixed Flow reactor
The results of a pulse tracer test are given below
| t, min | 0 | 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10 | 12 | 14 |
|
Tracer output Concentration (mg/l) |
0 | 1 | 5 | 8 | 10 | 8 | 6 | 4 | 3 | 2.2 | 1.5 | 0.6 | 0 |
a) Plot C(t), E(t) and F(t) curves.
b) Calculate mean residence time.
c) Find the conversion excepted in the tank-in-series model and how many tanks in series would you suggest to model this reactor.
d) calculate conversion assuming Mixed Flow reactor
20 M
5
Ethanol can be produced by catalytic vapor phase hydration of ethylene at 135 atm and 573 K.
C2H4 + H2O ⇌ C2H5OH
A + B ⇌ R
The rate expression for this reaction is \[-r'=\dfrac{0.018 k_Ak_B(P_AP_B-P_R/K)}{(1+k_AP_A+k_BP_B)^2},\dfrac{mol}{(gm \ catalyst \ h)}\]
Where kA = kB = 0.003
The equilibrium constant is given by,
RT 1nK = 30 T - 9730 where R = 1.987 cal/(mol.K)
The total feed rate to a PFR is 10 kg/h with equimolar amounts of ethylene and steam. Find the weight of catalyst needed to achieve 20% conversion of ethylene.
C2H4 + H2O ⇌ C2H5OH
A + B ⇌ R
The rate expression for this reaction is \[-r'=\dfrac{0.018 k_Ak_B(P_AP_B-P_R/K)}{(1+k_AP_A+k_BP_B)^2},\dfrac{mol}{(gm \ catalyst \ h)}\]
Where kA = kB = 0.003
The equilibrium constant is given by,
RT 1nK = 30 T - 9730 where R = 1.987 cal/(mol.K)
The total feed rate to a PFR is 10 kg/h with equimolar amounts of ethylene and steam. Find the weight of catalyst needed to achieve 20% conversion of ethylene.
20 M
Write short note on any two:
6(a)
Tanks in series Model
10 M
6(b)
Slurry Reactor
10 M
6(c)
Fluidized Bed Reactor
10 M
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