By J. G. Balchen, E. D. Gilles, K. V. Waller, J. B. Rawlings
As well as the 3 major topics: chemical reactors, distillation columns, and batch methods this quantity additionally addresses a few of the new tendencies in dynamics and keep an eye on method similar to version dependent predictive regulate, new equipment for id of dynamic types, nonlinear keep watch over thought and the applying of neural networks to identity and keep an eye on. presents an invaluable reference resource of the key advances within the box.
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Extra resources for Dynamics and Control of Chemical Reactors, Distillation Columns and Batch Processes. Selected Papers from the 3rd IFAC Symposium, Maryland, USA, 26–29 April 1992
Example text
1987) . , Shinskey, 1984) , and it may not correlate very well with the product composition. g . , Luy ben, 1973, Kister, 1990) . 2) However, the most sen sitive temperature location may move. To avoid this problem Luyben (1971) suggested to use a weighted average of many temperatures. Johnson ( 1 984) im plemented this on a deethanizer, a demethanizer and a C2-splitter and Whitehead and Parnis { 1987) on a C2-splitter. Bozenhardt ( 1988), Marquardt ( 1 988) and Wozny et al. ( 1 989) suggest various methods for locating the temperature front using multiple mea surements.
M. and Morari, M . , Shell Process Control Work matica, 1 , 3 1-53. shop, Butterworth. Rosenbrock, H . H . A. and Laflamme, D. ( 1 990), "Advanced con distillation columns and heat exchangers. An historical and critical review" , Trans. Instn. Chem. Engrs. , 40, trols improve performance of two-shell, dualpressure col 376-384. umn" , Oil & Gas Journal, 88, 60-63. Rovaglio, M. and Doherty, M . A. L. (1990), erogeneous azeotropic distillation columns" , AIChE Jour "Control of vapor recompression distillation columns" , nal, 36, 39-52.
Lear et al. (1989) consider optimizing control using single loops. Indus- trial applications of Dynamic Matrix Control (DMC) are presented by Hokanson et al. ( 1 989) for the com bined level and composition control in the top part of demethanizer column, and by Tran and Cutler ( 1989) for supervisory control of benzene and toluene towers. 5 Control o f the column a s a 5 problem x 5 scheme or as a simple estimator). 4) Fast setpoint changes in compositions are difficult to make. An alternative procedure which may solve all of the above problems is to use a composition estimator based on all available measurements.