Assessment and Future Directions of Nonlinear Model Predictive ...

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A Minimum-Time Optimal Recharging Controller 451where x is the tank temperature or pressure, the partials are the sensitivities,σx,P 2 Cis the estimate using the pressure measurement variance σP 2 C, σx,u 2 is theestimate using the control variance σu 2, F α is the F statistic at a confidencelevel α, λ is a tuning parameter to account for measurement noise and normalvariation in the inlet line pressure, and F > F α implies σx,P 2 C>σx,u 2 [9]. Ifthe variance estimated from the inlet line pressure measurement exceeds thatestimated from the control, the constraint control is terminated to a fail-safeoperation. This operation can either shut off the gas flow completely, where thetank pressure could then be determined by the inlet line pressure sensor, or canreduce the gas flow to a predetermined minimum safe value.5 ExampleThe control strategy is illustrated using a nitrogen–helium gas mixture. Wechoose this system because the sign of the Joule-Thompson coefficient is differentfor each component; negative for helium and positive for nitrogen. Thereare also significant differences in the intermolecular potentials leading to largedeviations from ideal behavior. The coefficients in Eqs. 2–3 are affine functionsof temperature taken from [10]. We consider a 1/4 He/N 2 gas blend in a 100lit storage tank where the component source pressures are both 175 bar, theambient temperature is 300 K, and the initial tank pressure is 10 bar. Figure 3presents the predicted tank temperature profiles for a series of flow rates whichclearly demonstrate the nonideal behavior and path independence of the tankstate. The predicted pressure profiles behave in a similar manner.3635345 mol/min10 mol/min20 mol/min50 mol/minTank Temperature (C)333231302928270 10 20 30 40 50 60 70 80 90 100 110Time (min)Fig. 3. Predicted tank temperature profiles
452 K.R. Muske, A.E. Witmer, and R.D. WeinsteinFlow Rate (mol/min) - Pressure (bar/4)252423222120191817161514131211109876543210control trajectory (mol/min)pressure profile (bar/4)0 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24Time (min)Fig. 4. Control trajectory and simulated tank pressure profile393Target Final Moles Terminal Constraint (mol)3923913903893883873863850 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23Time (min)Fig. 5. Target final moles of gas in the tankWe consider a desired value of n ⋆ D = 400 mol and a maximum operatingconstraint of PDmax = 100 bar for the tank pressure. At this pressure constraint,only 385 moles of gas can be stored in the tank assuming no thermodynamiclosses. Therefore, the maximum tank pressure is the most limiting constraintin this example. The inlet line pressure is simulated using an ideal gas nozzleflow equation with energy loss. The maximum gas flow rate is 25 mol/min. Thesample period is one minute. Figure 4 presents the dynamic constraint controltrajectory u(k) determined from Eq. 27 and the actual tank pressure. The first
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Lecture Notesin Control and Informa
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Series Advisory BoardF. Allgöwer,
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ContentsFoundations and History of
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ContentsIXRobustness, Robust Design
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ContentsXIHybrid NMPC Control of a
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Nonlinear Model Predictive Control:
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Hybrid MPC: Open-Minded but Not Eas
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Hybrid MPC: Open-Minded but Not Eas
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22 S.E. Tuna et al.this says that i
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24 S.E. Tuna et al.In particular, f
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26 S.E. Tuna et al.W N (f(x, ¯κ N
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28 S.E. Tuna et al.where ᾱ := max
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30 S.E. Tuna et al.21.521.5µ=51
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32 S.E. Tuna et al.obstacle and gra
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34 S.E. Tuna et al.[19] C. Prieur.
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36 É. Gyurkovics and A.M. Elaiw[8]
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38 É. Gyurkovics and A.M. ElaiwWe
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40 É. Gyurkovics and A.M. ElaiwWe
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Conditions for MPC Based Stabilizat
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A Computationally Efficient Schedul
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The Potential of Interpolation for
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The Potential of Interpolation 65De
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The Potential of Interpolation 67Al
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The Potential of Interpolation 693.
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The Potential of Interpolation 71Pr
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The Potential of Interpolation 73Th
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The Potential of Interpolation 75de
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Techniques for Uniting Lyapunov-Bas
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94 M. Lazar et al.Lipschitz continu
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96 M. Lazar et al.let X T ⊆ X den
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98 M. Lazar et al.S 0 {j ∈S|0
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100 M. Lazar et al.Fig. 1. State-sp
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102 M. Lazar et al.[11] Grimm, G.,
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Model Predictive Control for Nonlin
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ReferencesModel Predictive Control
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116 F.A.C.C. Fontes, L. Magni, and
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On the Computation of Robust Contro
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142 M. Srinivasarao, S.C. Patwardha
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Numerical Methods for Efficient and
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L i (s i ,u i ):=Numerical Methods
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182 A. Grancharova, T.A. Johansen,
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194 V. Sakizlis et al.presented her
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196 V. Sakizlis et al.linear PWA fu
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198 V. Sakizlis et al.non-linear sy
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200 V. Sakizlis et al.Remark 1. For
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202 V. Sakizlis et al.One should no
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204 V. Sakizlis et al.g0.050.10.15x
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Interior-Point Algorithms for Nonli
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n p,2 ≤Interior-Point Algorithms
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Hard Constraints for Prioritized Ob
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A Nonlinear Model Predictive Contro
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Robustness and Robust Design of MPC
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MPC for Stochastic SystemsMark Cann
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y i (k) =∑n um=1MPC for Stochasti
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MPC for Stochastic Systems 259we ha
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MPC for Stochastic Systems 261form
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MPC for Stochastic Systems 263( )κ
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MPC for Stochastic Systems 265Fig.
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MPC for Stochastic Systems 267⎡
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NMPC for Complex Stochastic Systems
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284 H. Chen et al.of the moving hor
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286 H. Chen et al.Hence, at each sa
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288 H. Chen et al.control inputs in
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290 H. Chen et al.Corollary 1. The
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292 H. Chen et al.c A[mol/l]10−10
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294 H. Chen et al.[CSA97] H.Chen,C.
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296 L. Xie, P. Li, and G. Woznyand
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298 L. Xie, P. Li, and G. WoznyDeta
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300 L. Xie, P. Li, and G. Wozny3.2
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302 L. Xie, P. Li, and G. WoznyFig.
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304 L. Xie, P. Li, and G. Wozny[3]
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306 H. Arellano-Garcia et al.applic
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308 H. Arellano-Garcia et al.Fig. 1
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310 H. Arellano-Garcia et al.RECIPE
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312 H. Arellano-Garcia et al.optimi
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314 H. Arellano-Garcia et al.The re
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Interval Arithmetic in Robust Nonli
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Optimal Online Control of Dynamical
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State Estimation Analysed as Invers
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Minimum-Distance Receding-Horizon S
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New Extended Kalman Filter Algorith
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NLMPC: A Platform for Optimal Contr
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384 K. Naidoo et al.polymer control
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386 K. Naidoo et al.are two key qua
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388 K. Naidoo et al.1. It greatly s
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390 K. Naidoo et al.However, with t
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392 K. Naidoo et al.Fig. 4. Bounded
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394 K. Naidoo et al.1. Maintain pro
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396 K. Naidoo et al.7 Commissioning
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Application of the NEPSAC Nonlinear
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Integrating Fault Diagnosis with No
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524 M. Alamirmin V (x u(·,x),T) un
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526 M. AlamirDefinition 4. The syst
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528 M. Alamir♭V is radially unbou
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530 M. AlamirBut according to the s
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532 M. AlamirFig. 2. Stabilization
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534 M. AlamirFig. 3. Closed loop be
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A New Real-Time Method for Nonlinea
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A Two-Time-Scale Control Scheme for
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566 X.-B. Hu and W.-H. Chen2 Online
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568 X.-B. Hu and W.-H. Chentime alo
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570 X.-B. Hu and W.-H. ChenFig. 3.
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572 X.-B. Hu and W.-H. ChenTable 4.
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574 M. Fujita et al. CameraCameraTa
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576 M. Fujita et al.J(u, t) =∫t+T
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578 M. Fujita et al.ξ 2[rad/s]6420
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580 M. Fujita et al.Acknowledgement
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582 A. Casavola, D. Famularo, and G
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4. c(t) ∈Cfor all t ∈ Z + ;5. T
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Distributed Model Predictive Contro
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608 W.B. Dunbar and S. Desaand sequ
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610 W.B. Dunbar and S. Desademand r
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612 W.B. Dunbar and S. Desabacklog
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614 W.B. Dunbar and S. Desacasescas
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Robust Model Predictive Control for
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630 J.J. Arrieta-Camacho, L.T. Bieg
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Author IndexAlamir, Mazen 523Alamo,
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Lecture Notes in Control and Inform
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