Download PDF by Piotr Tatjewski: Advanced control of industrial processes : structures and

By Piotr Tatjewski

"Advanced keep watch over of business approaches offers the suggestions and algorithms of complicated commercial method keep watch over and online optimisation in the framework of a multilayer constitution. quite basic unconstrained nonlinear fuzzy keep watch over algorithms and linear predictive regulate legislation are coated, as are extra concerned limited and nonlinear version predictive keep watch over (MPC) algorithms and online set-point Read more...

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Extra resources for Advanced control of industrial processes : structures and algorithms

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Let us observe that in this case the necessary information sent from the optimization unit to the subordinate controllers are optimal values of the set-points cf and yrd , although all elements of the vector c = (cf , cd ) are decision variables of the constrained optimization problem. However, transmission of the remaining part, cd , to the constraint controller may also be needed, as only the whole information defines the new optimal steady-state process operating point. In particular, when using a predictive constraint controller the case dim cd > dim y d may happen and be reasonable – then the predictive controller should know optimal steady-state value of cd to operate optimally (the case will be addressed in Chapter 4).

The inflow to the reactor is a stream of component A with a flow Fig. 5. 1 rate FA [kg/min] and a temperature TA [K]. Two reactions take place in the 1 1 ] and rC [ min ], respectively. The tank: A → B → C with reaction rates rB [ min first reaction is endothermic and the second one is exothermic. The mixture is heated by a heating medium flowing through a pipe heat exchanger located in the bottom part of the reactor. The flow rate of the heating medium Fh and the product outflow rate from the reactor F can be controlled by appropriate valves.

11). 11). 12d) were positioned is not incidental. , F and Fh or FA , TA and Thin , respectively. , without over-filling or excessive emptying of the tank and without exceeding the admissible temperature. 4 Process Modeling in a Multilayer Structure 19 Fig. 6. 6 presents the reactor together with direct control loops of level and temperature. The set-point values for these direct control loops, in the terminology of Fig. , W (t) = Wm T (t) = T sp (t) where particularly the former of these equalities can be relatively accurately enforced (fast stabilization of the level by manipulating the outflow rate F ).

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