A distillation column can be described using several material and energy balance equations. Figure 4 shows a typical distillation column.
Tray distillation column.
The overall material balance can be found as follows:
where F, D, and W are the feed, distillate, and residue rates, respectively (kg/h).
The component material balance can be found as follows:
where xf, xd, and xw are the distillate compositions in the feed, distillate, and residue, respectively.
The overall heat balance can be found as follows:
where Qr and Qc are the reboiler duty and condenser duty, respectively, and hf, hd, and hw are the specific enthalpies (J/kg) for the feed, distillate, and residue, respectively.
Here, cp is the sensible heat (J/kg °C).
Here, V and L are the rates of the vapor at the top plate and liquid flow returning to the top plate (kg/h), respectively.
Here, λmix and λ steam are the latent heat of vaporization (J/kg) values for the overhead mixture and reboiler steam, respectively.
The material balance equations were presented in Eq. (10). The general equation for the heat transfer across a surface is as follows:
where Q, U, A, and ΔTm are the heat transfer per unit time (W), overall heat transfer coefficient (W/m2 °C), area of heat transfer (m2), and log mean temperature difference (°C), respectively. The log mean temperature difference was calculated using the following equation:
where T1 is the hot-fluid inlet temperature, T2 is the hot-fluid outlet temperature, t1 is the cold fluid inlet temperature, and t2 is the cold fluid outlet temperature.
The total energy required can be calculated from the following equation:
where W is the work done (J/kg), is the elevation difference between z1 and z2 (m); is the system pressure difference between P1 and P2 (N/m2); is the pressure drop due to friction, including miscellaneous losses and equipment losses (N/m2); is the liquid density (kg/m3); and g is the acceleration due to gravity (m/s2) [24]. Figure 5 shows the piping system.
Piping system.
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