Advanced control of chemical processes (ADCHEM '94) : IFAC by D Bonvin; International Federation of Automatic Control

By D Bonvin; International Federation of Automatic Control

This ebook brings jointly the newest learn findings within the key zone of chemical approach keep watch over; together with dynamic modelling and simulation - modelling and version validation for program in linear and nonlinear model-based regulate: nonlinear model-based predictive regulate and optimization - to facilitate restricted real-time optimization of chemical methods; statistical regulate techniques - significant advancements within the statistical interpretation of measured info to steer destiny examine; knowledge-based v model-based control - the combination of theoretical facets of regulate and optimization idea with newer advancements in synthetic intelligence and laptop technology.

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27 5. 0 Figure 5 a : Simulated optimal control trajectory for distillate flow rate (kmol/h). 0 Figure Sb : Simulated optimal control trajectory for distillate composition for 1-butene (mole fraction). ; Problem specification for the optimal control (start-up) of the MTBE process Unit Mixer CSTR Mixer CSTR Distillation column Variable Component hold-up, kmol n, n, n, n. n, n, n, n. 1 2 Constraints < 100 kmol/b < 100 kmol/b > 100 kmol/b > 50 kmol/h It has been shown that an analysis of the model equations and their method of solution leads to the identification of similarities and differences among various forms of models and methods of solution.

From the above figures it can be noted that many of the desirable features in a dynamic simulator for design/control of chemical processes arc available in DYNSIM. The structure shown in Figure 2 is employed for on-line control based on fixed set-points or for optimal control (where the 26 The process flowsheet related to the production of methyl tertiary butyl ether (MTBE), earlier used by Perregaard et al. (1992) is used in this paper to illustrate the application of some of the integrated design/control features presented above.

Dashed line is Pl-controller and continuous line is predictive controller. ;) IFAC Advanced Control of Chemical Processes, Kyoto, Japan, 1994 DYNAMIC SIMULATION OF A MULTISTAGE REACTOR Yasuaki Yabuki*, Taketoshi Kajihara**, Chiye Kuwada***, Minoru Yoneda* and Masami Mori* • Yokkaichi Plant Engineering Department, Mitsubishi Kasei Corporation, Mie, Japan •• Yokkaichi Plant Research and Development Center, Mitsubishi Kasei Corporation, Mie, Japan *** Electronics Division, Mitsubishi Heavy Industries Ltd, Hiroshima, Japan Abstract.

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