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161 An analytical approach to modelling in distillation control
Abstracts
159 Nonlinear Multivarlabie Control of Product Properties In an Industrial Gas Phase Polyethylene Reactor K.B. McAuley, J.F. MacGregor, pp 173-178 A nonlinear model-based scheme is developed for product property control in industrial gas phase polyethylene reactors. The controller is designed for instantaneous melt index and density regulation over a range of products, and for control during grade changeovers. The nonlinear model-based feedback controller design is based upon global input/output linearization methods. Mismatch between the model and the process is removed using an extended Kalman filter. Through simulations on a complex mechanistic model of the process, it is shown that the controller performs well for both regulatory and servo-eontrol. The simplicity of the control algorithm makes it an excellent candidate for industrial application.
160 A Comparison of Strategies for the Control of a Polypropylene Reactor B. Lie, J.G. Balchen, pp 179-184 The paper discusses various structures for the control of the reactor in an industrial polypropene plant. The present structure uses single-loop PI controllers. In a suggested new structure, refluxed liquid is used to control the pressure while removed energy in the heat exchanger controls the accumulator liquid level. A multivariable PID controller is investigated, in addition to a decoupling structure. The different structures are compared with regard to set point tracking, disturbance rejection and suppression of varying process parameters. Overall, the multivariable PID controller yields the best result. The present structure may also give a satisfactory result if properly tuned.
161 An Analytical Approach to Modelling in Distillation Control T. Liider, G. Wozny, pp 185-192 This paper presents a second-order linear process model for a distillation column. It gives a steady-state exact representation of the column for any control configuration in the time and frequency domains, and preserves the physical significance of all parameters. Because of the low computational effort and the consistency of the modelling information it is an effective tool for control structure analysis and controller design. A systematic comparison with related work reveals the analytical strength of the approach. A comparison to simulation results shows very satisfactory reproduction of the column behaviour in the low- to midfrequency range as well as the high-frequency deficiencies of the model.
162 The Unique Challenges of Cryogenic Distillation Column Control for Integrated Coal Gasification Combined Cycle Applications D.M. Esple, J.A. Mandler, D. Miller, D. O'Connor, pp 193-199 The world's largest coal gasification plant for electricity generation is being built in Buggenum, The Netherlands and will be on-stream in 1993. A program of dynamic modelling, simulation, and control system design was undertaken at a very early stage in the plant design, prior to detailed equipment specification. This paper describes the approach taken to understand the dynamics of the proposed air separation unit under the expected load-
567 following conditions in order to verify the process design and to develop and optimise the control strategy. The work highlights the importance of incorporating control and operability considerations early during plant design.
163 Dynamics and Control of Unstable Distillation Columns E.W. Jacobsen, S. Skogestad, pp 201-206 The paper addresses the dynamics and control of distillation columns operated at open-loop unstable operating points. Ideal two-product distillation columns may have multiple steady states and right half plane poles. With reflux and boilup as independent variables the operating points become unstable if the internal flows are sufficiently large. An open-loop unstable operating point may be stabilized by use of one-point control, i.e., feedback control. If the control is insufficiently fight, the column may go into a stable limit cycle. With distillate flow and boilup as independent variables the operating points may also become unstable. The column may then also go into a stable limit cycle.
164 Relating the DRD Structure to Conventional Model Based Controllers J.B. Wailer, K.V. Waller, pp 207-212 A systematic way of constructing control structures, introduced in an earlier paper, has been investigated. A parametrization of a suggested static disturbance rejecting and decoupling structure (DRD) has enabled analysis of the structure in terms of other model-based controllers (such as IMC and Inferential Control). The analysis shows that in practice there will be a need for rel'ming the sla'ucture design by introducing suitable dynamics. Illustrative means of how to do this are presented.
165 Control Structures for a Sidestream Distillation Column Separating a Ternary Mixture A KoggersbOI, S.B. Jergensen, pp 213-218 The distillation under study is that of an impurity which accumulates on intermediate trays due to the thermodynamics of the ternary system. The resulting control problem is to minimize the sidestream flow (i.e. maximize main product recovery) while maintaining the two high-quality end products. This paper first investigates sensor selection with the goal of identifying the column states using relatively few sensors. Next, actuators are selected with the goal of obtaining a control problem of low sensitivity. A simple strategy for controlling the location of the maximum concenlration of the accumulating impurity is described and lowest control sensitivity is obtained for an (LV) type of control structure.
166 Selection of the Best Control Configuration for an Industrial Distillation Column D. Ariburnu, C. Ozgen, T. Gurkan, pp 219-224 The best regulatory control structure is determined for an industrial, multicomponent, high-purity ethylbenzene distillation column. Steady-state plant data and design information are utilized with a ste-dy-state model of the column. The column-model match is obtained by adjusting the column efficiency. Dynamic column behaviour is experimentally obtained by pulse and step testing. Steady-state rating programs are used to obtain the steady-state process and disturbance gain matrices of the control configurations. Steady-state control configuration selection methods are used. Single-end and dual composition control of the column is examined
159 Nonlinear Multivarlabie Control of Product Properties In an Industrial Gas Phase Polyethylene Reactor K.B. McAuley, J.F. MacGregor, pp 173-178 A nonlinear model-based scheme is developed for product property control in industrial gas phase polyethylene reactors. The controller is designed for instantaneous melt index and density regulation over a range of products, and for control during grade changeovers. The nonlinear model-based feedback controller design is based upon global input/output linearization methods. Mismatch between the model and the process is removed using an extended Kalman filter. Through simulations on a complex mechanistic model of the process, it is shown that the controller performs well for both regulatory and servo-eontrol. The simplicity of the control algorithm makes it an excellent candidate for industrial application.
160 A Comparison of Strategies for the Control of a Polypropylene Reactor B. Lie, J.G. Balchen, pp 179-184 The paper discusses various structures for the control of the reactor in an industrial polypropene plant. The present structure uses single-loop PI controllers. In a suggested new structure, refluxed liquid is used to control the pressure while removed energy in the heat exchanger controls the accumulator liquid level. A multivariable PID controller is investigated, in addition to a decoupling structure. The different structures are compared with regard to set point tracking, disturbance rejection and suppression of varying process parameters. Overall, the multivariable PID controller yields the best result. The present structure may also give a satisfactory result if properly tuned.
161 An Analytical Approach to Modelling in Distillation Control T. Liider, G. Wozny, pp 185-192 This paper presents a second-order linear process model for a distillation column. It gives a steady-state exact representation of the column for any control configuration in the time and frequency domains, and preserves the physical significance of all parameters. Because of the low computational effort and the consistency of the modelling information it is an effective tool for control structure analysis and controller design. A systematic comparison with related work reveals the analytical strength of the approach. A comparison to simulation results shows very satisfactory reproduction of the column behaviour in the low- to midfrequency range as well as the high-frequency deficiencies of the model.
162 The Unique Challenges of Cryogenic Distillation Column Control for Integrated Coal Gasification Combined Cycle Applications D.M. Esple, J.A. Mandler, D. Miller, D. O'Connor, pp 193-199 The world's largest coal gasification plant for electricity generation is being built in Buggenum, The Netherlands and will be on-stream in 1993. A program of dynamic modelling, simulation, and control system design was undertaken at a very early stage in the plant design, prior to detailed equipment specification. This paper describes the approach taken to understand the dynamics of the proposed air separation unit under the expected load-
567 following conditions in order to verify the process design and to develop and optimise the control strategy. The work highlights the importance of incorporating control and operability considerations early during plant design.
163 Dynamics and Control of Unstable Distillation Columns E.W. Jacobsen, S. Skogestad, pp 201-206 The paper addresses the dynamics and control of distillation columns operated at open-loop unstable operating points. Ideal two-product distillation columns may have multiple steady states and right half plane poles. With reflux and boilup as independent variables the operating points become unstable if the internal flows are sufficiently large. An open-loop unstable operating point may be stabilized by use of one-point control, i.e., feedback control. If the control is insufficiently fight, the column may go into a stable limit cycle. With distillate flow and boilup as independent variables the operating points may also become unstable. The column may then also go into a stable limit cycle.
164 Relating the DRD Structure to Conventional Model Based Controllers J.B. Wailer, K.V. Waller, pp 207-212 A systematic way of constructing control structures, introduced in an earlier paper, has been investigated. A parametrization of a suggested static disturbance rejecting and decoupling structure (DRD) has enabled analysis of the structure in terms of other model-based controllers (such as IMC and Inferential Control). The analysis shows that in practice there will be a need for rel'ming the sla'ucture design by introducing suitable dynamics. Illustrative means of how to do this are presented.
165 Control Structures for a Sidestream Distillation Column Separating a Ternary Mixture A KoggersbOI, S.B. Jergensen, pp 213-218 The distillation under study is that of an impurity which accumulates on intermediate trays due to the thermodynamics of the ternary system. The resulting control problem is to minimize the sidestream flow (i.e. maximize main product recovery) while maintaining the two high-quality end products. This paper first investigates sensor selection with the goal of identifying the column states using relatively few sensors. Next, actuators are selected with the goal of obtaining a control problem of low sensitivity. A simple strategy for controlling the location of the maximum concenlration of the accumulating impurity is described and lowest control sensitivity is obtained for an (LV) type of control structure.
166 Selection of the Best Control Configuration for an Industrial Distillation Column D. Ariburnu, C. Ozgen, T. Gurkan, pp 219-224 The best regulatory control structure is determined for an industrial, multicomponent, high-purity ethylbenzene distillation column. Steady-state plant data and design information are utilized with a ste-dy-state model of the column. The column-model match is obtained by adjusting the column efficiency. Dynamic column behaviour is experimentally obtained by pulse and step testing. Steady-state rating programs are used to obtain the steady-state process and disturbance gain matrices of the control configurations. Steady-state control configuration selection methods are used. Single-end and dual composition control of the column is examined