A simple distillation column is designed to separate an ideal binary mixture to specified distillate and bottoms purities at a given column pressure. If RR$_{\min}$ is the minimum reflux ratio for this separation, select the statement that is NOT CORRECT with regard to the variation in the total annualized cost (TAC) of the column with reflux ratio (RR).
In the design of a distillation column, the reflux ratio (RR) strongly influences both capital cost and operating cost, which together determine the total annualized cost (TAC). As RR increases, the vapor and liquid traffic inside the column increases, leading to larger column diameter and higher energy usage in the reboiler and condenser. Thus, extremely high RR values increase TAC due to higher operating costs. Conversely, when RR approaches RR$_{\min}$, the number of theoretical stages increases sharply, causing a steep rise in the capital cost of the column.
Step 1: Behaviour near RR$_{\min}$
As RR → RR$_{\min}$ from above, the number of stages approaches infinity. This drastically increases column height and capital cost. Therefore, TAC increases sharply near RR$_{\min}$. Hence, option (B) is correct.
Step 2: TAC at intermediate RR
Between RR$_{\min}$ and very high RR, there exists an optimum RR at which TAC is minimized. Option (A) correctly states that TAC has a minimum.
Step 3: TAC at high RR
For RR >> RR$_{\min}$, the column requires a large boil-up rate, increasing utility consumption. This makes TAC rise again, so (D) is correct.
Step 4: Identifying the NOT CORRECT statement
Option (C) states that the "sharpest decrease in TAC occurs as RR approaches RR$_{\min}$ from above," which is incorrect because TAC increases sharply in that region, not decreases. Therefore, (C) is the NOT CORRECT option.
Consider the process in the figure. The liquid-phase elementary reactions \[ A + B \rightarrow P -r_{B1} = k_1 x_A x_B \] \[ P + B \rightarrow S -r_{B2} = k_2 x_P x_B \] \[ S + A \rightarrow 2P -r_{S3} = k_3 x_S x_A \] occur in the continuous stirred tank reactor (CSTR). All fresh feeds, exit streams and recycle streams are pure. At steady state, the net generation of the undesired product $S$ in the CSTR is zero. Let $q = x_A/x_B$ in the reactor. For 90% single-pass conversion of $B$ and fixed product rate, determine the value of $q$ that minimizes the sum of the molar flow rates of the A and S recycle streams (rounded to one decimal place).

Consider a process with transfer function: \[ G_p = \frac{2e^{-s}}{(5s + 1)^2} \] A first-order plus dead time (FOPDT) model is to be fitted to the unit step process reaction curve (PRC) by applying the maximum slope method. Let \( \tau_m \) and \( \theta_m \) denote the time constant and dead time, respectively, of the fitted FOPDT model. The value of \( \frac{\tau_m}{\theta_m} \) is __________ (rounded off to 2 decimal places).
Given: For \( G = \frac{1}{(\tau s + 1)^2} \), the unit step output response is: \[ y(t) = 1 - \left(1 + \frac{t}{\tau}\right)e^{-t/\tau} \] The first and second derivatives of \( y(t) \) are: \[ \frac{dy(t)}{dt} = \frac{t}{\tau^2} e^{-t/\tau} \] \[ \frac{d^2y(t)}{dt^2} = \frac{1}{\tau^2} \left(1 - \frac{t}{\tau}\right) e^{-t/\tau} \]
Choose the transfer function that best fits the output response to a unit step input change shown in the figure:

An electrical wire of 2 mm diameter and 5 m length is insulated with a plastic layer of thickness 2 mm and thermal conductivity \( k = 0.1 \) W/(m·K). It is exposed to ambient air at 30°C. For a current of 5 A, the potential drop across the wire is 2 V. The air-side heat transfer coefficient is 20 W/(m²·K). Neglecting the thermal resistance of the wire, the steady-state temperature at the wire-insulation interface __________°C (rounded off to 1 decimal place).

GIVEN:
Kinematic viscosity: \( \nu = 1.0 \times 10^{-6} \, {m}^2/{s} \)
Prandtl number: \( {Pr} = 7.01 \)
Velocity boundary layer thickness: \[ \delta_H = \frac{4.91 x}{\sqrt{x \nu}} \]
The first-order irreversible liquid phase reaction \(A \to B\) occurs inside a constant volume \(V\) isothermal CSTR with the initial steady-state conditions shown in the figure. The gain, in kmol/m³·h, of the transfer function relating the reactor effluent \(A\) concentration \(c_A\) to the inlet flow rate \(F\) is:
