This example shows how to implement gain-scheduled control in a Simulink® model using a family of PID controllers. The PID controllers are tuned for a series of steady-state operating points of the plant, which is highly nonlinear.
This example builds on the work done in Design Family of PID Controllers for Multiple Operating Points. In that
example, the continuous stirred tank reactor (CSTR) plant model is linearized at
steady-state operating points that have output concentrations C = 2, 3,
..., 8, 9. The nonlinearity in the CSTR plant yields different linearized dynamics at
different output concentrations. The example uses the
to generate and tune a separate PID controller for each output concentration.
You can expect each controller to perform well in a small operating range around its corresponding output concentration. This example shows how to use the PID Controller block to implement all of these controllers in a gain-scheduled configuration. In such a configuration, the PID gains change as the output concentration changes. This configuration ensures good PID control at any output concentration within the operating range of the control system.
Begin with the controllers generated in Design Family of PID Controllers for Multiple Operating Points. If these
controllers are not already in the MATLAB® workspace, load them from the data file
This operation puts two variables in the MATLAB workspace,
Controllers contains eight
pid models, each tuned for one output concentration in the vector
To implement these controllers in a gain-scheduled configuration, create lookup tables
that associate each output concentration with the corresponding set of PID gains. The
PIDGainSchedCSTRExampleModel contains such lookup
tables, configured to provide gain-scheduled control for the CSTR plant. Open this
In this model, the PID Controller block is configured to have external input ports for the PID coefficients. Using external inputs allows the coefficients to vary as the output concentration varies. Open the block to examine the configuration.
Setting the Source parameter to
external enables the input ports for the coefficients.
The model uses a 1-D Lookup Table block for each of the PID
coefficients. In general, for gain-scheduled PID control, use your scheduling variable as
the lookup-table input, and the corresponding controller coefficient values as the output.
In this example, the CSTR plant output concentration is the lookup table input, and the
output is the PID coefficient corresponding to that concentration. To see how the lookup
tables are configured, open the
P Lookup Table block.
The Table data parameter contains the array of proportional
coefficients for each controller,
Controllers.Kp. (For more information
about the properties of the
pid models in the
Controllers array, see
pid.) Each entry in this array corresponds to an entry in the array
C that is entered in the Breakpoints 1
parameter. For concentration values that fall between entries in
P Lookup Table block performs linear interpolation to determine the
value of the proportional coefficient. To set up lookup tables for the integral and
derivative coefficients, configure the
I Lookup Table and
Lookup Table blocks using
Controllers.Kd, respectively. For this example, this configuration is
already done in the model.
pid models in the
express the derivative filter coefficient as a time constant,
Controllers.Tf (see the
pid reference page for more information). However, the PID
Controller block expresses the derivative filter coefficient as the inverse
N. Therefore, the
N Lookup Table block
must be configured to use the inverse of each value in
N Lookup Table block to see the configuration.
Simulate the model. The
Concentration Setpoint block is configured
to step through a sequence of setpoints that spans the operating range between
= 2 and
C = 9 (shown in yellow on the scope). The
simulation shows that the gain-scheduled configuration achieves good setpoint tracking
across this range (pink on the scope).
As was shown in Design Family of PID Controllers for Multiple Operating Points, the CSTR
plant is unstable in the operating range between
C = 4 and
7. The gain-scheduled PID controllers stabilize the plant and yield good
setpoint tracking through the entire unstable region. To fully validate the control design
against the nonlinear plant, apply a variety of setpoint test sequences that test the
tracking performance for steps of different sizes and directions across the operating
range. You can also compare the performance against a design without gain scheduling, by
setting all entries in the
Controllers array equal.