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Surge Tank Control Using Discrete Control Set MPC

This example shows how to use a linear MPC controller with both continuous- and discrete-set control actions to control the level of a surge tank in Simulink®.

Overview

Many petrochemical processes include surge capacity to insulate downstream operations from upsets in upstream flows. This example considers a liquid surge tank supplied by two pumps.

  • Pump 1 is variable-speed and can deliver a flow rate between 0 and 100 L/min. The rate of change of the flow rate is limited to 50 L/min per minute.

  • Pump 2 is on-off and delivers 100 L/min when it is on.

This system also has a continuously adjustable valve that regulates the tank discharge to accommodate a downstream process.

mdl = 'ReservoirMPC';
open_system(mdl)

The control objective is to use the two pumps (manipulated variables) to maintain the tank volume at its setpoint when the discharge valve introduces a disturbance to the surge tank (measured disturbance).

When downstream demand is constant, pump 1 controls the surge tank level, ideally keeping it near 50%. When a disturbance occurs, both pumps can go into action to maintain the tank volume between 25% and 75% during the transient time. When downstream demand is high, however, Pump 2 must turn on.

In summary, the MPC controller manages the two pumps such that:

  • The tank level stays near 50% when demand is constant.

  • The tank level stays within the ideal range when Pump 2 turns on and off. Rapid Pump 2 on-off cycling is undesirable.

Create Linear Plant from Nonlinear Surge Tank Model

In the Simulink model, the surge tank model is in the Reservoir subsystem. It implements the following equations.

  • dV/dt = Qin - Qout, where V is the tank volume between 0 and 100 (percent)

  • Qin = Q1 + Q2, the sum of the two pump flow rates (L/min)

  • Qout = 0.2*sqrt(2)*X*sqrt(V), the discharge rate (L/min)

  • X, the discharge valve, which can open between 0 and 100 (percent)

The plant starts running at its nominal steady-state operating point: pump 1 runs at 70 L/min, pump 2 is off, the discharge valve is at 35%, and the tank volume is at 50%. Create a linear model of the tank at this operating point. This model has three inputs: the manipulated variables Q1 and Q2, and the measured disturbance|X|.

plant = ss(-0.7,[1 1 -2],1,[0 0 0]);
plant = setmpcsignals(plant,'MV',[1 2],'MD',3);

Design MPC Controller with Continuous and Discrete Control Actions

Create a linear MPC controller with a sample time of one second, default prediction and control horizons, and default cost function weights.

Ts = 1;
MPCobj = mpc(plant,Ts);
-->The "PredictionHorizon" property of "mpc" object is empty. Trying PredictionHorizon = 10.
-->The "ControlHorizon" property of the "mpc" object is empty. Assuming 2.
-->The "Weights.ManipulatedVariables" property of "mpc" object is empty. Assuming default 0.00000.
-->The "Weights.ManipulatedVariablesRate" property of "mpc" object is empty. Assuming default 0.10000.
-->The "Weights.OutputVariables" property of "mpc" object is empty. Assuming default 1.00000.

Set the nominal values for the controller to match the steady-state operating point.

MPCobj.Model.Nominal.U = [70; 0; 35];
MPCobj.Model.Nominal.Y = 50;
MPCobj.Model.Nominal.X = 50;
MPCobj.Model.Nominal.DX = 0;

Choose the MVRate weights such that the controller adjusts pump 1 in preference to pump 2. That is, the controller penalizes pump 2 adjustments less than pump 1 adjustments.

MPCobj.Weights.MVrate = [0.1 0.2];

Specify safety bounds on the continuous input and output signals.

MPCobj.OV.Min = 0;
MPCobj.OV.Max = 100;
MPCobj.MV(1).Min = 0;
MPCobj.MV(1).Max = 100;
MPCobj.MV(1).RateMin = -50;
MPCobj.MV(1).RateMax = 50;

Since pump 2 has two discrete settings (0 and 100 L/min), specify a discrete set in the Type property of this controller. Depending on your application, the Type property can also be binary or integer.

MPCobj.MV(2).Type = [0 100];

Simulate Closed-Loop Response with Discharge Disturbance

The simulation begins at the nominal condition. At t = 5, the discharge rate ramps up until pump 1 is at its full capacity and pump 2 must turn on. Pump 2 turns on at t = 12. Pump 1 must then decrease as rapidly as possible to keep the level in bounds, then establish a new steady-state operating point. At t = 60, the discharge begins to ramp down to the nominal state. The MPC controller keeps the volume within the ideal range, and pump 2 does not exhibit rapid cycling.

sim(mdl)
open_system([mdl '/Volume'])
-->Converting model to discrete time.
-->Assuming output disturbance added to measured output channel #1 is integrated white noise.
-->The "Model.Noise" property of the "mpc" object is empty. Assuming white noise on each measured output channel.

ans = 

  Simulink.SimulationOutput:
                   tout: [106x1 double] 

     SimulationMetadata: [1x1 Simulink.SimulationMetadata] 
           ErrorMessage: [0x0 char] 

The following figure shows the flow rates from two pumps.

open_system([mdl '/Pumps'])

As expected, the MPC controller turns pump 2 on and off.
bdclose(mdl) % close simulink model.

See Also

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