Abstract
This paper proposes a sliding mode controller (SMC) with modified Nelder-Mead tuning, for the control of nonlinear chemical processes, which are represented as first order plus dead time process with negative gain (FOPDT-NG). In the controller design, the SMC controller parameter in continuous part is obtained based on the time constant and dead time of the process, and controller parameters in the discontinuous part is obtained using Nelder-Mead tuning equations. Even though the controller parameters of conventional SMC are tuned using Nelder-Mead tuning, zero dynamics are noticed in the closed loop response of few FOPDT-NG processes and, with few other FOPDT-NG processes tracking of set-point is unachievable. This work proposes modification in the Nelder-Mead tuning equations using Nelder-Mead optimization to overcome the above disadvantages. Four different types of FOPDT-NG processes are considered in this work, and for every type the Nelder-Mead tuning equations are modified, for the design of proposed controllers. The performances of proposed controllers are evaluated for FOPDT-NG processes and also for three different chemical processes taken from literature. A simulation results demonstrate that, the proposed controller prevailed the performance of the conventional SMC in tracking the set-point and the elimination of zero dynamic behavior of FOPDT-NG processes. Hence, the proposed controllers provide improved closed loop performances as compared to the conventional SMC.
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Author contributions: All the authors have accepted responsibility for the entire content of this submitted manuscript and approved submission.
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Research funding: None declared.
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Conflict of interest statement: The authors declare no conflicts of interest regarding this article.
Nelder-Mead Optimization technique contains of B (Best point), G (Good point), W (Worse point), M (Mid-point), E (Expansion point), R (Reflect point), C (Construction point) and S (Shrink point). The discontinuous part of SMC consists of K D and δ, which are tuning parameters.
A.1 Algorithm
Generate an initial configuration K randomly, where K1 = [KD1 δ1], K2 = [KD2 δ2] and K3 = [KD3 δ3].
Calculate f(K1), f(K2), f(K3) for finding B, G, W, where B < G < W.
Compute M, E and f(E).
Compare f(E) and f(G), if f(E) < f(G) replace W with E, go to step 8; else Compute R and f(R) go to step 5.
Compare f(R) and f(W), if f(R) < f(W) replace W with R go to step 6.
Compare f(R) and f(G), if f(R) ≥ f(G) Compute C and f(C) go to step 7; else go to step 8.
Compare f(C) and f(W), if f(C) < f(W) replace W with C go to step 8; else compute S, replace G with M and replace W with S go to step 8.
Rearrange the B, G, W, where B < G < W and repeat step (3) until some predefined stopping criteria.
A.2 Symbols used
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Sliding surface |
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Derivative of sliding surface |
r(t) | Reference value (set-point) |
x(t) | The measured variable (controlled variable) |
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Error signal |
![]() |
Derivative of error signal |
K | System gain |
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System time constant |
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Dead time |
λ | Tuning parameter of continuous part of SMC |
n | Order of the system |
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Control law of sliding mode control |
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Continuous control law of sliding mode control |
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Discontinuous control law of sliding mode control |
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Tuning parameter of reaching mode |
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Tuning parameter discontinuous part of SMC |
G(s) | Process transfer function |
x(s) | Laplace transform of controlled variable |
u(s) | Laplace transform of manipulated variable |
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The natural frequency |
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Damping ratio |
sgn | The signum function |
B | Best point |
G | Good point |
W | Worse point |
M | Mid-point |
E | Expansion point |
R | Reflect point |
C | Construction point |
S | Shrink point |
Abbreviations
- SMC
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Sliding Mode Control
- PID
-
Proportional + Integral + Derivative
- VSC
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Variable Structure Control
- FOPDT
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First Order Plus Dead Time
- FOPDT-NG
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First Order Plus Dead Time with Negative Gain
- P
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Proportional
- PI
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Proportional + Integral
- PD
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Proportional + Derivative
- VS-PI
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Variable Structure based Proportional plus Integral
- VS-PID
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Variable Structure based Proportional plus Integral plus Derivative
- ISE
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Integral of the Squared Error
- MATLAB
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MATrix LABoratory
- IAE
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Integral of the Amplitude Error
- SP
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Set-point
- CO
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Controller Output
- PV
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Process Variable
- ITAE
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Integral of the Time Weighted Amplitude Error
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Articles in the same Issue
- Frontmatter
- Research Articles
- Three-phase modeling and optimization of benzene alkylation in commercial catalytic reactors
- Control of negative gain nonlinear processes using sliding mode controllers with modified Nelder-Mead tuning equations
- Novel control strategy for non-minimum-phase unstable second order systems: generalised predictor based approach
- Modelling adiabatic flame temperature for methane with an overview for advanced combustion process: flameless combustion
- Evaluation the effect of the ambient temperature on the liquid petroleum gas transportation pipeline
- Performance of molecular dynamics simulation for predicting of solvation free energy of neutral solutes in methanol
- Reviews
- Phase equilibria modeling of biorefinery-related systems: a systematic review
- On the drag force closures for multiphase flow modeling
Articles in the same Issue
- Frontmatter
- Research Articles
- Three-phase modeling and optimization of benzene alkylation in commercial catalytic reactors
- Control of negative gain nonlinear processes using sliding mode controllers with modified Nelder-Mead tuning equations
- Novel control strategy for non-minimum-phase unstable second order systems: generalised predictor based approach
- Modelling adiabatic flame temperature for methane with an overview for advanced combustion process: flameless combustion
- Evaluation the effect of the ambient temperature on the liquid petroleum gas transportation pipeline
- Performance of molecular dynamics simulation for predicting of solvation free energy of neutral solutes in methanol
- Reviews
- Phase equilibria modeling of biorefinery-related systems: a systematic review
- On the drag force closures for multiphase flow modeling