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- A bank of 1000 one-in. schedule 40 tubes \( 1.79 \mathrm{~m} \) in length corresponds to \( 1.0 \mathrm{~m}^{3} \) \( \left(0.001 \mathrm{~m}^{3} /\right. \) tube \( =1.0 \mathrm{dm}^{3} / \) tube \( ) \) and gives \( 20 \% \) conversion. The heat-exchange fluid has a flow rate \( \dot{m}_{c} \) of \( 0.111 \mathrm{~mol} / \mathrm{s} \), with a heat capacity of \( 34.5 \mathrm{~J} / \mathrm{mol} \cdot \mathrm{K} \). Plot the conversion and temperature along the length of the reactor - Case 1 The reactor is operated adiabatically. - Case 2 Constant heat-exchange fluid temperature \( T_{a}=1250 \mathrm{~K} \) - Case 3 Co-current heat exchange with \( T_{a 0}=1250 \mathrm{~K} \) Additional information \[ \begin{array}{l} \mathrm{CH}_{3} \mathrm{COCH}_{3}(\mathrm{~A}): \mathrm{H}_{\mathrm{A}}^{\circ}\left(T_{\mathrm{R}}\right)=-216.67 \mathrm{~kJ} / \mathrm{mol}, C_{\mathrm{P}_{\mathrm{A}}}=163 \mathrm{~J} / \mathrm{mol} \cdot \mathrm{K} \\ \mathrm{CH}_{2} \mathrm{CO}(\mathrm{B}): \mathrm{H}_{\mathrm{B}}^{\circ}\left(T_{\mathrm{R}}\right)=-61.09 \mathrm{~kJ} / \mathrm{mol}, C_{\mathrm{P}_{\mathrm{B}}}=83 \mathrm{~J} / \mathrm{mol} \cdot \mathrm{K} \\ \mathrm{CH}_{4}(\mathrm{C}): \mathrm{H}_{\mathrm{C}}^{\circ}\left(T_{\mathrm{R}}\right)=-74.81 \mathrm{~kJ} / \mathrm{mol}, C_{\mathrm{P}_{\mathrm{C}}}=71 \mathrm{~J} / \mathrm{mol} \cdot \mathrm{K} \\ U a=110 \mathrm{~J} / \mathrm{s} \cdot \mathrm{m}^{3} \cdot \mathrm{K} \end{array} \]

          - A bank of 1000 one-in. schedule 40 tubes \( 1.79 \mathrm{~m} \) in length corresponds to \( 1.0 \mathrm{~m}^{3} \) \( \left(0.001 \mathrm{~m}^{3} /\right. \) tube \( =1.0 \mathrm{dm}^{3} / \) tube \( ) \) and gives \( 20 \% \) conversion. The heat-exchange fluid has a flow rate \( \dot{m}_{c} \) of \( 0.111 \mathrm{~mol} / \mathrm{s} \), with a heat capacity of \( 34.5 \mathrm{~J} / \mathrm{mol} \cdot \mathrm{K} \). Plot the conversion and temperature along the length of the reactor
- Case 1 The reactor is operated adiabatically.
- Case 2 Constant heat-exchange fluid temperature \( T_{a}=1250 \mathrm{~K} \)
- Case 3 Co-current heat exchange with \( T_{a 0}=1250 \mathrm{~K} \)
Additional information
\[
\begin{array}{l} 
\mathrm{CH}_{3} \mathrm{COCH}_{3}(\mathrm{~A}): \mathrm{H}_{\mathrm{A}}^{\circ}\left(T_{\mathrm{R}}\right)=-216.67 \mathrm{~kJ} / \mathrm{mol}, C_{\mathrm{P}_{\mathrm{A}}}=163 \mathrm{~J} / \mathrm{mol} \cdot \mathrm{K} \\
\mathrm{CH}_{2} \mathrm{CO}(\mathrm{B}): \mathrm{H}_{\mathrm{B}}^{\circ}\left(T_{\mathrm{R}}\right)=-61.09 \mathrm{~kJ} / \mathrm{mol}, C_{\mathrm{P}_{\mathrm{B}}}=83 \mathrm{~J} / \mathrm{mol} \cdot \mathrm{K} \\
\mathrm{CH}_{4}(\mathrm{C}): \mathrm{H}_{\mathrm{C}}^{\circ}\left(T_{\mathrm{R}}\right)=-74.81 \mathrm{~kJ} / \mathrm{mol}, C_{\mathrm{P}_{\mathrm{C}}}=71 \mathrm{~J} / \mathrm{mol} \cdot \mathrm{K} \\
U a=110 \mathrm{~J} / \mathrm{s} \cdot \mathrm{m}^{3} \cdot \mathrm{K}
\end{array}
\]

- A bank of 1000 one-in. schedule 40 tubes 1.79 m in length corresponds to 1.0 m^3 (0.001 m^3 /. tube =1.0 dm^3 / tube ) and gives 20 % conversion. The heat-exchange fluid has a flow rate ṁc of 0.111 mol / s, with a heat capacity of 34.5 J / mol·K. Plot the conversion and temperature along the length of the reactor
- Case 1 The reactor is operated adiabatically.
- Case 2 Constant heat-exchange fluid temperature Ta=1250 K
- Case 3 Co-current heat exchange with Ta 0=1250 K
Additional information

CH3COCH3( A): HA^∘(TR)=-216.67 kJ / mol, CPA=163 J / mol·K
CH2CO(B): HB^∘(TR)=-61.09 kJ / mol, CPB=83 J / mol·K
CH4(C): HC^∘(TR)=-74.81 kJ / mol, CPC=71 J / mol·K

U a=110 J / s·m^3·K

Added by Kushal L.

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