Concentration PID Control

The objective of this case study is to use an existing dynamic model of a blending tank and develop a controller to maintain outlet concentration. A mixing tank has a liquid inlet stream and outlet stream. The tank is well mixed so the concentration is assumed to be the same throughout the reactor. The temperature is not important for this application.

A prior exercise involves starting with species and energy balance equations and deriving the dynamic concentration and temperature response. The derivation of the concentration response is provided below with a constant tank volume V of 100 m3 and an inlet flow rate `\dot V` of 100 m3/hr. A species balance is simulated with the accumulation, inlet, and outlet terms of the number of moles n of species A. The accumulation of A, d(nA)/dt, in a control volume is calculated by inlet, outlet, reaction generation, and reaction consumption rates.

$$\frac{dn_A}{dt} = \sum \dot n_{A_{in}} - \sum \dot n_{A_{out}} + \sum \dot n_{A_{gen}} - \sum \dot n_{A_{cons}}$$

The molar amount, nA is often measured as a concentration, cA. In this application there are no reaction terms so the species balance can be simplified.

$$\frac{dc_A V}{dt} = c_{A_{in}} \dot V_{in} - c_{A_{out}} \dot V_{out}$$

Exercise: Implement PID Control

Implement a PID controller that maintains the outlet concentration of A in the mixer by automatically adjusting the feed concentration. Assume that the concentration is continuously measured and that the controller should be designed to follow set point changes to 1.5 mol/L and then down to 1.0 mol/L. The maximum feed concentration is 2.0 mol/L and the minimum is 0.0 mol/L. Report the PID tuning parameters and show time plots of the dynamic response of the controller.

PID Solution

Step Response Code

import numpy as np
import matplotlib.pyplot as plt
from scipy.integrate import odeint

# define mixing model
def mixer(x,t,Tf,Caf):
    # Inputs (2):
    # Tf = Feed Temperature (K)
    # Caf = Feed Concentration (mol/m^3)
    # States (2):
    # Concentration of A (mol/m^3)
    Ca = x[0]
    # Parameters:
    # Volumetric Flowrate (m^3/hr)
    q = 100
    # Volume of CSTR (m^3)
    V = 100
    # Calculate concentration derivative
    dCadt = q/V*(Caf - Ca)
    return dCadt

# Initial Condition
Ca0 = 0.0
# Feed Temperature (K)
Tf = 300
# Feed Concentration (mol/m^3)
Caf = 1
# Time Interval (min)
t = np.linspace(0,10,100)

# Simulate mixer
Ca = odeint(mixer,Ca0,t,args=(Tf,Caf))

# Construct results and save data file
# Column 1 = time
# Column 2 = concentration
data = np.vstack((t,Ca.T)) # vertical stack
data = data.T             # transpose data

# Plot the results
plt.ylabel('Ca (mol/L)')
plt.xlabel('Time (hr)')