By International Federation of Automatic Control, Heinz Unbehauen

ISBN-10: 0080334318

ISBN-13: 9780080334318

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D. thesis (1984). Instituttet for Kemiteknik. Technical University of Denmark, Denmark. , and Hallager, L. (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.

In both cases of increasing and decreasing dead time, the control scheme goes unstable. In Fig. 9, the dead time starts increasing, and the controller is able to maintain stable operation until an undetermined disturbance occurs at about 135 minutes. The prediction step is shorter than optimal, and the disturbance induces cyclic behavior which increases to saturation. In Fig. 10, the control loop manifests unstable tendencies by the end of 26 D. E. Clough and Seu Jung Park the dead time change period at 85 minutes, and by 100 minutes there is an oscillatory saturation condition.

Copyright © IFAC Adaptive Control of Chemical Processes, Frankfurt am Main, 1985 ADAPTIVE CONTROL OF A RECYCLE REACTOR G. E. Bortolotto and S. Bay j0rgensen Instituttet for Kemiteknik, Danmarks Tekniske H0jskole, 2800 Lyngby, Denmark Abstract. A MIMO self tuning controller (MIMOSC) with an explicit model structure is applied to control a fixed bed chemical reactor with recirculation of unconverted reactants. The dynamic behaviour of recycle reactors is more complex than that of reactors without recycle, due to the feedback introduced by the recirculation.

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

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