# Neglect Level Control at Your Peril

## Neglect Level Control at Your Peril -- This first article in a four-part series examines reset mode tuning issues.

**Figure 2 **illustrates the response in level to an upset to the material balance. When the material balance is closed (imbalance is zero), vessel level is constant. In **Figure 2,** this is the case prior to time 0. At that point the discharge valve opening is reduced by 10%, which decreases discharge flow and causes level to increase.

All examples we'll discuss pertain to a straight-walled vessel containing a constant density liquid, hence the ramp has a constant slope as in Figure 2. We'll express the level as a percentage of the level measurement span. The response in **Figure 2** is for a 12,000-L vessel. The average flow through the vessel is 200 L/min, giving a residence time of 60 min or 1 hr.

A simple characterization of a level process relies on two parameters whose value can be readily obtained from the response in **Figure 2**:

*Process gain, K _{F}*. This is the effect of a 10% change in the controller output on the slope of the ramp. From

**Figure 2**, a 10% reduction in the controller output causes the slope of the ramp to change from zero to 0.49%/min. So:

*K _{F}* = (0.49 %/min)/10% = 0.049 (%/min)/%

A decrease leads to an increase in level, so the process is reverse acting.

*Process lag, θ*. The material balance suggests the ramp should commence immediately, as indicated by the dashed line in **Figure 2**. Instead, the slope changes gradually from zero to 0.49 %/min. By the time the slope reaches 0.49 %/min, the actual response lags by 0.4 min.

The process lag shown by the ramp in** Figure 2** includes the following:

*Control valve lag*. A digital system can change its output by 10% very quickly but all final control elements exhibit some lag in responding to a change in their input signal. Rarely are the response characteristics of the final control element well known.

*Measurement device lag*. This depends on the measurement technology employed and, sometimes, on how the device is installed. Rarely is this lag quantified.

*Smoothing of the process variable*. When smoothing is applied either within the measurement device or the control system, quantitative values are available. However, with some level measurement technologies, smoothing can be applied externally.

The lag observed in **Figure 2 **is roughly the sum of these lags. The combined effect often is approximated by a transportation lag or dead time. In the simple approximations of the dynamics of a level process, the process lag θ is considered to be entirely transportation lag.

Unfortunately, for many level loops, conducting a test such as in **Figure 2** is impractical due to the presence of noise on the measured level value and variability in the feed flow to the vessel.

Testing procedures are available to determine *K _{F}* and θ in face of both measurement noise and flow upsets. One approach is to use a pseudo-random binary signal (PRBS) for the output to the control element. Model predictive control technology relies on such tests to find process characteristics. However, such tests are long-duration (days) and difficult to justify for level control applications.

**TUNING EQUATIONS**

When a proportional-integral (PI) controller is used, the relationships between the tuning coefficients and the process characteristics are:

*Controller gain, K _{C}*: inversely proportional to the process gain

*K*; inversely proportional to the lag θ.

_{F}*Reset time*, *T _{I}*: not affected by

*K*; directly proportional to θ.

_{F}Especially for large tanks with long residence times, tuning equations often suggest unreasonably large values for *K _{C}*. Most tuning relationships link the product

*K*(the loop gain) to the process dynamics. The large value for K

_{F}K_{C}_{C}results from two factors:

1. For responsive processes, the tuning equations suggest a large value for

*K*. For a vessel with a residence time of 1 hr, a lag of 0.4 min is trivial.

_{F}K_{C}2. For large vessels, the process sensitivity

*K*is small.

_{F}Using the Ziegler-Nichols tuning equations, the suggested values for the tuning coefficients are:

*K _{C}*= 1/(

*K*θ) = 0.9/{[0.049 (%/min)/%] × (0.4 min)} = 46 %/%

_{F}*T _{I}*= 3.33 θ = 3.33 × (0.4 min) = 1.33 min

The performance objective for the Ziegler-Nichols tuning equations is a response with a quarter decay ratio, which usually provides a rapid response to a disturbance. **Figure 3 **presents the response to a 10-min 50-L/min increase in one feed for the level process in **Figure 1**. These tuning coefficients maintain the vessel level very close to its set point — the maximum level deviation is approximately 0.2%. The response period, *P*, is 2.7 min. Also note the feed flow change is translated quickly into a discharge flow change.

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