Question

For the homogeneous autocatalytic reaction A + B → B + B, where
–rA = k*C**A**C**B*, aconversion rate
of A of X = 0.44. The velocity constant is k =
*10**-3* *m**3* / (mol s).
The feed stream of 0.1 *m**3* / s contains A with
*C**A0* = 90 mol / *m**3*
and B with CB0 = 10 mol / *m**3*. It is considered
whichreactor configuration that will be most suitable

1.1

The reaction must take place in a flow reactor. Set up the
stoichiometric table and find *C**A* and
*C**B* asfunction of *C**A0* and X.

Answer #1

The stoichiometric table is given as

Consider a plug flow reactor with a reversible isothermal
gas-phase reaction:
A + B <--> C
The reactor feed consists of a mixture of 50% A and 50% B. The
reaction rate is: (-rA) =
k1*CA*CB -
k2*CC2 The inlet temperature is
500 K and the total pressure is 200 kPa. The volumetric feed flow
rate is 10 m3/s. The rate constants have a values of:
k1 = 0.1 m3/(mol*s) and k2 = 0,05
m3/(mol*s).
a) Calculate the conversion of...

Task # 3
the first order reaction A → B, with –rA = kCA, takes place in a
liquid phase in a CSTR reactor witha volume of 10 l. The velocity
constant k equals 2.5 min-1
CA=0.0672 mol/L
3.2
There is an operating accident where the feed flow with A is
interrupted and the concentration of A drops to 0 inreactor. How
long will it take for the feed to resume (ν0 = 0.12 l / s, CA0 =
0.3mol...

A liquid phase reaction A+B --> C+D is to be carried out in
an isothermal and well mixed batch reactor. The initial moles of A
and B are both 0.1 mole. The rate of destruction of A is
given by –rA = k*CA*CB, with k
= 6.0 L/ (mol*min). Calculate the amount of
time (in minutes) that the reaction must proceed within a 10 L
reactor in order to achieve a final concentration of A of 0.001
mol/L. Please express your answer to...

The elementary irreversible organic liquid-phase reaction, A + B
→ C, is carried out in a flow reactor. An equal molar feed in A and
B enters at 27 oC, and the volumetric flow rate is 2 L/s. The feed
concentration is CA0 = 0.1 mol/L. a) Calculate the PFR and CSTR
volumes necessary to achieve 85% conversion when the reaction is
carried out adiabatically. b) What is the maximum inlet temperature
one could have so that the boiling point...

A packed bed reactor has the reaction A --> B occurring. The
rate law is –rA = kCA where k = 15 L/g-min. The superficial gas
velocity is 4.8 kg/m2-s with a density of 0.45 kg/m3 and a
viscosity of 3.9x10-5 kg/m-s. The porosity, catalyst density, and
particle diameter are, respectively, 0.45, 2.2 g/cm3 and 0.255 cm.
The cross sectional area of the reactor is 12 cm2. The inlet
pressure is 100 kPa. Calculate the conversion ‘X’ when the catalyst...

Consider the CSTR with first order reaction and the process
parameters and variables are given by: The process parameters and
variables are defined as: CA0 = feed concentration = 2.7 mol/L. Cp
= heat capacity of the reactor feed and product (1000 cal/kg*K) =
Cv. E/R = normalized activation energy (20,000 K). F = mass feed
rate and product rate (10 kg/s). k0 = rate constant (1.97×10^24
1/s). Q = heat addition rate (initially 700,000 cal/s). T0 = feed
temperature...

The elementary liquid phase reaction takes place in an adiabatic
flow reactor.
? + ? → ?
An equimolar feed in A and B enters at 300K, and the volumetric
flow rate is 2 dm3
/s and CA0= 100
mol/m3
.
a) Calculate the PFR and CSTR volumes to achieve 75 %
conversion.
b) If the outlet temperature of the reactor is 550 K, for complete
conversion, calculate the inlet temperature
of CSTR.
HA°(273 K) = - 20 kcal/mol, HB°...

A+2B --> C
-ra=kCaCb^2
Where k-0.01 s1(gmoLt 500c)
CA-concentration of A. gmolL CB-concentration of B, gmol/L.
100 gmol are feeded and assume that all gases behave as ideal.
Calculate the time needed to produce product containing 1 1.8% B in
batch reactor operating at 500°C and a constant pressure of 10 atm.
The reactor containing 40%A, 40%B and 20% inert.

Problem 1 Consider the liquid phase reaction A à products
accelerated by a homogeneous catalyst dissolved in the solution.
The observed rate data follows the form:
-r=k1Ca/(1+K2Ca+K3(Ca^2))
You are asked to recommend either a steady CSTR or steady PFR.
Your reactor must reduce the feed composition of 0.6 mole/liter
down to 0.3 mole/liter in the effluent. • Create a plot of ordinate
1/(-rA) vs. abscissa CA. Use the data below. Use sufficient
resolution in your plot to get a smooth...

The irreversible gas-phase non-elementary reaction A + 2B
---> C takes place in an isothermal (227 C) constant-volume
batch reactor. The initial feed to the reactor consists of 40 mol%
A and 60 mol% B at a total pressure of 10 atm. Measurements of the
rate of reaction as a function of conversion yielded the following
results:
-rA (mol dm^-3 s^-1) x (1x10^8)
0.010
0.005
0.002
0.001
XA
0.0
0.2
0.4
0.6
Calculate the time required to achieve a conversion...

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