1991-8-i-a-cre

The reaction of \(A\) and \(B\) produces the desired product \(R\) as well as the unwanted product \(S\). What level of reactant concentrations (high, medium, low) should we use for the following reaction scheme in order to maximize the conversion of
\(A\) to \(R\).

Reaction scheme: \[ \begin {align*} A + B \rightarrow R \qquad & r_{1} = k_{1}C_{A}C_{B}^{2} \\

A \rightarrow S \qquad \qquad & r_{2} = k_{2}C_{A} \end {align*} \]

- low \(C_{A}\), low \(C_{B}\)
- high \(C_{B}\), any \(C_{A}\)
- high \(C_{A}\), low \(C_{B}\)
- high \(C_{A}\), any \(C_{B}\)

1993-13-b-cre

For multiple reactions \[ \begin {align*} 2A &\rightarrow R \\

2R &\rightarrow S \end {align*} \] the number of moles of \(S\) present when the number of moles of \(A\) and \(R\) are 0.3 and 0.5 respectively (Initially 2 moles of \(A\) are
only present) are

- 0.125
- 0.175
- 0.535
- 0.350

1994-1-r-cre

To maximize the formation of \(R\) in the simultaneous reactions \[ \begin {align*} A + B \rightarrow R & r_{R} = 2C_{A}^{0.5}C_{B}^{2} \\

A + B \rightarrow S & r_{S} = 1.4C_{A}C_{B} \end {align*} \] we should have

- low \(C_{A}\), low \(C_{B}\)
- low \(C_{A}\), high \(C_{B}\)
- high \(C_{A}\), low \(C_{B}\)
- high \(C_{A}\), high \(C_{B}\)

2000-1-20-cre

For the liquid phase parallel reactions

\[ \begin {align*} A &\rightarrow R& r_R &= k_1C_A^2;& E_1 &= 80 \text { kJ/mol} \\

A &\rightarrow S& r_S &= k_2C_A;& E_2 &= 120 \text { kJ/mol} \end {align*} \]

the desired product is \(R\). A higher selectivity of \(R\) will be achieved if the reaction is conducted at

- low temperature in a CSTR
- high temperature in a CSTR
- low temperature in a PFR
- high temperature in a PFR

2003-19-cre

For a series of reactions \(A \stackrel {k_1}{\longrightarrow } B \stackrel {k_2}{\longrightarrow } C\) having \(k_1 \ll k_2\), the reaction system can be approximated as

- \(A \stackrel {k_1}{\longrightarrow } B\)
- \(A \stackrel {k_2}{\longrightarrow } B\)
- \(A \stackrel {k_2}{\longrightarrow } C\)
- \(A \stackrel {k_1}{\longrightarrow } C\)

2011-22-cre

Reactant \(R\) forms three products \(X\), \(Y\), and \(Z\) irreversibly, as shown below.

- high temperature, high concentration of \(R\)
- high temperature, low concentration of \(R\)
- low temperature, high concentration of \(R\)
- low temperature, low concentration of \(R\)

2012-20-cre

Consider the reaction scheme shown below \[ A \xrightarrow {k_1} B \xrightarrow {k_2} C \] Both the reactions are first-order. The activation energies for \(k_1\) and \(k_2\) are 80 and 20 kJ/mol, respectively. To maximize the yield of \(B\), it is preferable to use

- CSTR and high temperature
- PFR and high temperature
- CSTR and low temperature
- PFR and low temperature

2016-15-cre

The variations of the concentrations (\(C_A\), \(C_R\) and \(C_S\)) for three species (\(A\), \(R\) and \(S\)) with time, in an isothermal homogeneous batch reactor are shown in the figure below.

1989-17-ii-cre

Consider the following reaction: \[ \begin {align*} A + B &\stackrel {1}{\longrightarrow } P \text { (desired)} \\

A + B &\stackrel {2}{\longrightarrow } Q \text { (undesired)} \end {align*} \] \(r_1=100\exp (-3000/T)C_AC_B^{0.5}\)

\(r_2=10\exp (-2000/T)C_A^{0.5}C_B\)

The selectivity is defined as the moles of \(P\) produced per mole of \(Q\) produced. In a perfectly mixed tank reactor operated under steady state, in order to maximize the selectivity:

(a) should the inlet concentration of the reactant \(A\) be high or low?

{#1}

(b) should the inlet concentration of the reactant \(B\) be high or low?

{#2}

(c) should the temperature of the reactor be high or low?

{#3}

Explain briefly.

1999-16-cre

Two parallel first order reactions \(A \stackrel {k_1}{\longrightarrow } B\) and \(A \stackrel {k_2}{\longrightarrow } C\) are taking place in liquid phase in a well mixed batch reactor. After 60 min of operation, 80% of \(A\) has reacted awhile 2 moles
of \(B\) per mole of \(C\) was detected in the reactor. Calculate the rate constants \(k_1\) and \(k_2\) for the two reactions. Assume that no \(B\) and \(C\) were initially present in the reactor.

(i) \(k_1\) = ____________min\(^{-1}\).

{#1}

(ii) \(k_2\) = ____________min\(^{-1}\).

{#2}

2008-71-72-73-cre

Methane and steam are fed to a reactor in molar ratio 1 : 2. The following reactions take place,

\[ \begin {eqnarray*} \text {CH}_4\text {(g)} + 2\text {H}_2\text {O}\text {(g)} &\rightarrow &\text {CO}_2\text {(g)} + 4\text {H}_2\text {(g)} \\ \text {CH}_4\text {(g)} + \text {H}_2\text {O}\text {(g)} &\rightarrow & \text {CO}\text
{(g)} + 3\text {H}_2\text {(g)} \end {eqnarray*} \]

where CO_{2} is the desired product, CO is the undesired product and H_{2} is a byproduct. The exit stream has the following composition

Species | CH_{4} |
H_{2}O |
CO_{2} |
H_{2} |
CO |
---|---|---|---|---|---|

Mole % | 4.35 | 10.88 | 15.21 | 67.39 | 2.17 |

(i) The selectivity for desired product relative to undesired product is

{#1}

(ii) The fractional yield of CO_{2} is (where fractional yield is defined as the ratio of moles of the desired product formed to the moles that would have been formed if there were no side reactions and the limiting reactant had reacted completely)

{#2}

(iii) The fractional conversion of methane is

{#3}

2002-2-13-cre

In the hydrodealkylation of toluene to benzene, the following reactions occur

\[ \begin {eqnarray*} \text {C}_7\text {H}_8 + \text {H}_2 &\rightarrow & \text {C}_6\text {H}_6 + \text {CH}_4 \\ 2\text {C}_6\text {H}_6 &\rightleftharpoons & \text {C}_{12}\text {H}_{10} + \text {H}_2 \end {eqnarray*} \]

Toluene and hydrogen are fed to a reactor in a molar ratio 1:5. 80% of the toluene gets converted and the selectivity of benzene (defined as moles of benzene formed/ moles of toluene converted) is 90%. The fractional conversion of hydrogen is

- 0.16
- 0.144
- 0.152
- 0.136

2006-53-cre

Consider the following elementary reaction network

- constant at low temperature
- constant at high temperature
- increasing
- decreasing

2007-54-cre

The following liquid phase reaction is taking place in an isothermal CSTR

\[ \begin {eqnarray*} & & A \xrightarrow {k_1} B \xrightarrow {k_2} C \\ & & 2 A \xrightarrow {k_3} D \end {eqnarray*} \]

Reaction mechanism is same as the stoichiometry given above. Given: \(k_1=1\) min^{-1}; \(k_2=1\) min^{-1}; \(k_3=0.5\) litre/(mol.min); \(C_{A0}=10\) mol/litre, \(C_{B0}=0\) mol/litre and \(C_B = 1\) mol/litre, the solution for \(F/V\)
(flow rate/reactor volume in min^{-1}) yields

- 6.7
- 4.44 and 0.225
- 2 and 4/3
- 8

2007-59-cre

Determine the level of \(C_{A0}\) (high, low, intermediate), temperature profile (high, low, increasing, decreasing), which will favor the formation of the desired product indicated in the reaction scheme given below.

\[\begin{aligned} & A \xrightarrow{1} R \xrightarrow{3} S_{\text{desired}} \\ & A \xrightarrow{2} U\end{aligned}\]

\(n_1\) | \(E_1 \qquad\) | \(n_2\) | \(E_2 \qquad\) | \(n_3\) | \(E_3\) |

2 | 25 | 1 | 35 | 3 | 45 |

- High \(C_{A0}\), increasing \(T\) , plug flow reactor
- Low \(C_{A0}\), increasing \(T\) , plug flow reactor
- High \(C_{A0}\), decreasing \(T\) , mixed flow reactor
- High \(C_{A0}\), decreasing \(T\) , plug flow reactor

2008-56-cre

The elementary liquid phase series parallel reaction scheme

\[ \begin {eqnarray*} & & A \rightarrow B \rightarrow C \\ & & A \rightarrow R \end {eqnarray*} \]

is to be carried out in an isothermal CSTR. The rate laws are given by

\[ \begin {eqnarray*} r_R &=& k’ C_A \\ r_B &=& k C_A - k C_B \end {eqnarray*} \]

Feed is pure \(A\). The space time of the CSTR which results in the maximum exit concentration of \(B\) is given by

- \(\displaystyle \frac {1}{\sqrt {k?k’}}\)
- \(\displaystyle \frac {1}{\sqrt {k’ (k+k’)}}\)
- \(\displaystyle \frac {1}{(k+k’)}\)
- \(\displaystyle \frac {1}{\sqrt {k (k+k’)}}\)

1997-23-cre

The liquid phase parallel reactions \[\begin {align*} A &\rightarrow R; \qquad r_R = k_1C_A; \qquad k_1 = 0.3 \text { s\(^{-1}\)} \\

A &\rightarrow S; \qquad r_S = k_2; \qquad k_2 = 0.3 \text { kmol/(m\(^3\).s)} \end {align*} \] is conducted
in an isothermal plug flow reactor. The inlet concentration of \(A\) is 2.0 kmol/m\(^3\). No products are present in the feed. If conversion of \(A\) is 80%, then determine the exit concentration of \(R\) (in kmol/m\(^3\)).

1988-7-a-ii-cre

Consider the reactions \(A\rightarrow B\) and \(A\rightarrow C\), in an isothermal batch reactor. If the orders of the reaction differ, a low concentration of \(A\) favours the reaction of ––––- order.

1992-18-c-cre

Consider the set of elementary reactions: \[ \begin {align*} A &\stackrel {k_1}{\rightarrow } B \\

A + B &\stackrel {k_2}{\rightarrow } C \\

A + D &\stackrel {k_3}{\rightarrow } 2E \end {align*} \] At time \(t=0\), a batch reactor
is filled with a mixture of \(A\) and \(D\). What is the relation between the concentrations of \(B\) and \(D\) after a time \(t\)?

2003-71-72-cre

The following gas phase reactions are carried out isothermally in a CSTR

\( \begin {eqnarray*} A \rightarrow 2 R \quad & & r_1 = k_1P_A \quad k_1 = 20 \text { mol/(s.m$^3$.bar)} \\ A \rightarrow 3 S \quad & & r_2 = k_2P_A \quad k_2 = 40 \text { mol/(s.m$^3$.bar)} \end {eqnarray*} \)

total pressure = 1 bar; \(F_{A0}\) = 1 mol/s; feed is pure \(A\)

(i) What is the maximum possible value of \(F_R\) (mol/s)?

{#1}

(ii) The volume of a CSTR required for a fractional conversion of \(A\) equal to 0.3 due to the first reaction is

{#2}

2007-74-75-cre

The following liquid phase reaction is taking place in an isothermal batch reactor \[ A \xrightarrow {k_1 (\text {first order}) } B \xrightarrow {k_2 (\text {zero order}) } C \] Feed concentration = 1 mol/litre.

(i) The time at which the concentration of \(B\) will reach its maximum value is given by

{#1}

(ii) The time at which the concentration of \(B\) will become zero is given by the following equation:

{#2}

2013-50-51-cre

Liquid reactant \(A\) decomposes as follows

\[ \begin {align*} A \rightarrow R \qquad r_R &= k_1C_A^2 \qquad k_1 =0.5 \text { m$^3$/mol.s} \\ A \rightarrow S \qquad r_S &= k_2C_A \qquad k_2 = 1 \text { s$^{-1}$} \end {align*} \]

An aqueous feed of composition \(C_{A0} = 30\) mol/m^{3}, \(C_{R0} = 2\) mol/m^{3}, and \(C_{S0}= 1\) mol/m^{3} enters a CSTR in which the above reactions occur. Assume isothermal and steady state conditions.

(i) If the conversion of \(A\) is 80%, the concentration of \(R\) in the exit stream in mol/m^{3}, to the nearest integer, is ____________

{#1}

(ii) What is the % conversion of \(A\), to the nearest integer, so that the concentration of \(S\) in the exit stream is 11.8 mol/m^{3}? ____________

{#2}

Last Modified on: 01-May-2024

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