20-Bio-A2 Process Dynamics and Control · Undated paper
Question 3 of 8: Linear vs. Nonlinear-Valve Draining-Tank Dynamics
Nivaar worked solution (AI-drafted; not reviewed by a licensed engineer)
Notes on this paper
National Exams / EGBC — May 2019 — 04-Bio-A2 Process Dynamics and Control (the paper's own header line alternates between the codes "04-BIO-A2" and "04-BIO-A3" across pages; the subject line and content are unambiguously Process Dynamics and Control, so 04-Bio-A2 is used throughout). Three-hour open-book examination; any non-communicating calculator is permitted. The cover page states that only the first five questions in the answer book are marked, yet all eight problems are printed on the paper — all eight are solved below for completeness, since the full set is a study resource. Content spans the effect of a real zero on step-response overshoot, the Nyquist criterion for an open-loop-unstable process, a two-tank linear-vs-nonlinear-valve comparison, state-space-to-transfer-function conversion, Routh–Hurwitz stability with PI control of an unstable process, inverse Laplace transforms with time delay, Internal Model Control (IMC) design for a dead-time process, and Bode/gain-margin design.
Reference texts: D. E. Seborg, T. F. Edgar, D. A. Mellichamp & F. J. Doyle III, Process Dynamics and Control (4th ed., Wiley) — Laplace-domain modelling, transfer functions, Routh stability, Nyquist/Bode frequency response, and Internal Model Control design; G. Stephanopoulos, Chemical Process Control: An Introduction to Theory and Practice (Prentice Hall) — the Nyquist criterion for open-loop-unstable processes and dead-time systems. Standard control conventions (deviation variables; unity valve/sensor gain unless stated) are used throughout.
Problem 3: Linear vs. Nonlinear-Valve Draining-Tank Dynamics (20% total)
The paper's text is internally inconsistent between the two cases (it labels Case II's outlet an "exit pump" in one sentence while both the formula and the figure describe a valve, and it carries Case I's parameter $R=1$ into a paragraph nominally about Case II) — a wording inconsistency rather than a real ambiguity in the physics. The two formulas given are unambiguous and are used as the governing law for each case: Case I is the linear resistance $q=h/R$ with $R=1$; Case II is the valve law $q=K\sqrt{\Delta P/(\rho g)}$, which for a tank draining to atmosphere ($\Delta P=\rho g h$) reduces to the classic square-root valve law $q=K\sqrt{h}$, with $K$ fixed by the common initial condition $q_0=1\ \text{m}^3/\text{s}$ at $h_0=1\ \text{m}$.
Given. Two independent tanks, each cross-section $A=1\ \text{m}^2$, common initial steady state $h_0=1\ \text{m}$, $q_0=1\ \text{m}^3/\text{s}$; Case I outlet $q=h/R$, $R=1$; Case II outlet $q=K\sqrt{h}$ ($K$ from the IC); inlet flow steps $q_i:1\to2\ \text{m}^3/\text{s}$ at $t=0$.
Find. (a) $\delta H(s)/\delta Q_i(s)$ for each case; (b) $\delta h(t)$ for each case for the given inlet step.
Left: Case I, linear outlet resistance $R$. Right: Case II, nonlinear valve law linearized about the common initial steady state $h_0=1\ \text{m}$.
Approach. Write the unsteady mass balance $A\,dh/dt=q_i-q$ for each tank; Case I's outlet is already linear so the transfer function is exact, while Case II's outlet must first be Taylor-linearized about $h_0$ before Laplace-transforming; both reduce to a standard first-order lag, then apply the known step response with $M=\delta q_i=1\ \text{m}^3/\text{s}$.
(a) Case I transfer function. $A\dfrac{dh}{dt}=q_i-\dfrac{h}{R}\Rightarrow AR\dfrac{dh'}{dt}+h'=Rq_i'$, so with $A=R=1$: $$\boxed{\frac{H'(s)}{Q_i'(s)}=\frac{R}{ARs+1}=\frac{1}{s+1}\qquad(\tau_I=AR=1\ \text{s},\ K_I=R=1).}$$
(a) Case II: fix $K$, then linearize. From the IC, $q_0=K\sqrt{h_0}\Rightarrow K=q_0/\sqrt{h_0}=1/\sqrt1=1$. Linearizing $q=K\sqrt h$ about $h_0$: $\left.\dfrac{dq}{dh}\right|_{h_0}=\dfrac{K}{2\sqrt{h_0}}=\dfrac12=0.5$. The balance becomes $A\dfrac{dh'}{dt}=q_i'-0.5\,h'$, so $$\boxed{\frac{H'(s)}{Q_i'(s)}=\frac{1}{As+0.5}=\frac{2}{2s+1}\qquad(\tau_{II}=A/0.5=2\ \text{s},\ K_{II}=1/0.5=2).}$$
(b) Apply the standard first-order step response, $M=1\ \text{m}^3/\text{s}$ (the $1\to2\ \text{m}^3/\text{s}$ inlet step). $h'(t)=K M(1-e^{-t/\tau})$ for each case: $$\boxed{\delta h_I(t)=1-e^{-t}\ \text{m},\qquad \delta h_{II}(t)=2\left(1-e^{-t/2}\right)\ \text{m}\qquad(t\ \text{in s}).}$$
Sample values and a note on the linearization. At $t=1\ \text{s}$: $\delta h_I=0.632\ \text{m}$, $\delta h_{II}=0.443\ \text{m}$ (Case II starts slower, $\tau_{II}=2\tau_I$). As $t\to\infty$: $\delta h_I\to1\ \text{m}$ (new level $h=2\ \text{m}$, exact, since $q=h/R$ is already linear and $q_i=2=h/1\Rightarrow h=2$ exactly). $\delta h_{II}\to2\ \text{m}$ (linearized new level $h\approx3\ \text{m}$); the exact nonlinear new steady state solves $q_i=2=K\sqrt h=\sqrt h\Rightarrow h=4\ \text{m}$, i.e. $\delta h=3\ \text{m}$ — the linearized model under-predicts the true new level by $1\ \text{m}$ because the step ($\delta q_i/q_0=100\%$) is large relative to the point of linearization.
Result
Value
Case I: $\tau_I,K_I$
$1\ \text{s},\ 1$
Case II: $\tau_{II},K_{II}$
$2\ \text{s},\ 2$ (linearized)
$\delta h_I(t)$
$1-e^{-t}\ \text{m}$
$\delta h_{II}(t)$
$2(1-e^{-t/2})\ \text{m}$
Exact new level, Case II
$h=4\ \text{m}$ (linearized model predicts $h=3\ \text{m}$)