By International Federation of Automatic Control, Heinz Unbehauen

ISBN-10: 0080334318

ISBN-13: 9780080334318

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Extension of this work to multiple-input, multiple-output systems is also in progress. ACKNOWLEDGMENTS We gratefully acknowledge support of this research in the form of funds and equipment from E. I. , and an equipment donation from Kaye Instrument. Fig. 12. Performance of Adaptive Dead-Time Controller. Dead Time Ramps from 75 to 45 Seconds from 70 to 85 Minutes. These results show that the adaptive dead-time scheme was able to detect a shift in process dead time and adjust the control scheme prediction step accordingly.

1). Matrix Cl indicates that the noise is not expected to be white, but filtered through a first order filter. The experimental data were collected from the reactor around the following conditions (steady state values): Ti = 54 C C. g. the inlet and outlet temperatures of the reactor. The total flow rate could have been used as a control input, but it has some undesired characteristics. Firstly, it interacts with the pressures in different places of the process. Secondly, the inlet feed of Oxygen has to be adjusted accordingly to avoid that changes in the flow affect the inlet concentration.

1985). Sparse process modelling for robust multivariable adaptive chemical process control. 7'th IFAC/IF0RS Symposium on Identification and System Parameter Estimation. K. Preprints p. 391. total mass Φ oxygen enthalpy Fig. 1. Dynamic Quantity Interaction Diagram (DYQUID) for fixed bed reactor with a pseudo first order reaction with recirculation of unreacted reactant. 32 G. E. Bortolotto and S. Bay J0rgensen K: 1 ; " ··»—^i ' : · 7 Γ" Fig. 6. Open loop response to a step in the total mass flow rate.

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Adaptive Control of Chemical Processes 1985 by International Federation of Automatic Control, Heinz Unbehauen


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