Operator & Fractional Order Based Nonlinear Robust Control for a Spiral Counter-Flow Heat Exchanger with Uncertainties and Disturbances ^†

Abstract

This paper studies operator and fractional order nonlinear robust control for a spiral counter-flow heat exchanger with uncertainties and disturbances. First, preliminary concepts are presented concerning fractional order derivative and calculus, fractional order operator theory. Then, the problem statement about nonlinear fractional order derivative equation with uncertainties is described. Third, the design of an operator fractional order controller and fractional order PID controller and determination of several related parameters is described. Simulations were performed to verify tracking and anti-disturbance performance by comparison to different control cases; verification is described and concluding remarks provided.

1. Introduction

Heat exchangers which transfer heat energy from one fluid to another have been used widely in industrial applications such as refineries, chemical and petrochemical plants, and sewage treatment [1]. Heat exchangers help to minimize energy consumption and reduce waste heat emission. In industry, there are many different application types for heat exchangers. A spiral heat exchanger, for instance, is suitable for dirty fluids and viscous fluids and has the additional advantages of small size, high heat transfer efficiency, and ease of maintenance, among others. In industrial processes, the output temperature of the heated or cooled fluid often has certain requirements due to industry safety or product quality [2,3,4,5]. Thus, it is important to control output temperature on the heated or cooled fluid side in real-world applications. However, because the flow rate and fluid temperature often change, it is very difficult to control the output temperature.

Fractional order derivatives as an extension of integer order derivatives have been widely used to describe practical application objects following their first being proposed by Leibniz in 1695 [6]. Although the use of integer order derivatives to describe dynamic systems applications using traditional methods has a clear physical geometric interpretation, in certain real-world applications dynamic systems described by fractional order derivatives can be more accurate than those described by integer order derivatives; examples include viscoelastic systems, liquids, heat diffusion and dielectric polarization, electrode-electrolyte polarization, nonlinear thermoelastic system etc. [7,8,9,10,11]. Thus, a heat exchanger is suitable for description by fractional order derivative [12,13]. In a feedback control system, a proportion integral derivative (PID) control with only three parameters to tune is widely used thanks to its simple structure and high robustness. For nonlinear control systems with large delay times and disturbances, it is difficult to achieve good control performance. Fractional order PID (FOPID) control extends the conventional PID controller, having five parameters to tune and being more flexible than the traditional PID controller. FOPID control has better control performance in applications, as proven by many studies in recent years [14,15,16,17].

Nonlinear robust control is a problem that has been considered by many researchers in many different fields. In [18,19], the authors consider the right coprime factorization needed to compensate for the nonlinearity of the system and provide robust control performance in an improved system. The right coprime factorization suit is required for both linear feedback control and nonlinear feedback control. This provides a convenient approach to study the input–output stability of nonlinear feedback control systems. In [20,21,22,23], the authors studied robustness using right coprime factorization of a nonlinear system with perturbations. Operator-based nonlinear robust control is a simple method to improve stability and anti-disturbance using only the output signal of the plant.

A spiral heat exchanger (See Appendix A) is a nonlinear system with several uncertainties and many disturbances in the changes in the flow rate, fluid temperature, fluid density, fluid pressure on the two fluids side, etc., as well as a large delay time. It is very difficult to control under complex operating conditions. In application, the spiral heat exchanger mathematical model described via fractional order differential equation is more accurate than other methods [24,25,26,27]. Therefore, motivated by the above references, this paper presents a mathematical model of a spiral heat exchanger using a fractional order derivative system. Operator-based fractional order control is employed to improve robustness in a nonlinear system with uncertainties, disturbances, and a high delay time. A fractional order operator controller and fractional order PID controller are designed to account for uncertainties and disturbance, and the different control cases in tracking performance and stability are analyzed. Finally, the proposed control schemes are simulated and analyzed. This paper focuses on verifying operator and fractional order nonlinear robust control for a spiral counter-flow heat exchanger with uncertainties and disturbances by simulation (See Appendix A). In the future, we intend to study operator and fractional order nonlinear robust control for a spiral counter-flow heat exchanger with uncertainties and disturbances using experimental equipment (See Appendix A), to determine the optimal parameters for fractional order PID control, and to study MIMO control problems using fractional order derivatives [28,29].

The rest of this paper is constructed as follows. In Section 2, preliminaries regarding fractional order calculus and derivative and fractional order operator theory are described, and a problem statement concerning fractional order equations for a spiral-plate heat exchanger is presented. In Section 3, a fractional order operator controller is designed and the different control cases are analyzed in terms of tracking performance and stability. Simulations verifying operator and fractional order-based robust nonlinear control for a spiral counter-flow heat exchanger with uncertainties and disturbances are reviewed in Section 4. Finally, conclusions are provided in the final section.

2. Preliminaries and Problem Statement

A basic overview of fractional order integral and operator theory are presented in this section.

Definition 1

(The definition of Caputo’s fractional order calculus [6]).

$$\begin{array}{c}\hfill D^{-\beta }f\left(t\right)=\frac{1}{\mathsf{\Gamma }\left(\beta \right)}{\int }_a^t{(t-\tau )}^{\beta -1}f\left(\tau \right)d\left(\tau \right),\beta >0\end{array}$$

(1)

where $\mathsf{\Gamma }(\dot{)}$ is Gamma function, $\mathsf{\Gamma }\left(ϵ\right)={\int }_0^{\infty }{e}^{-t}{t}^{ϵ-1}$.

Definition 2

(The definition of Caputo’s fractional order derivative [6]).

$$\begin{array}{c}\hfill {}_a^C{D}_t^{q}f\left(t\right)=\frac{1}{\mathsf{\Gamma }(n-q)}{\int }_a^t{\displaystyle \frac{f^{\left(n\right)}\left(t\right)}{{(t-\tau )}^{n-q-1}}}d\tau ,n-1<q<n\end{array}$$

(2)

where n is a integer that is equal to or greater than q. If n = 1, then $0<q<1$.

$$\begin{array}{c}\hfill {}_a^C{D}_t^{q}f\left(t\right)=\frac{1}{\mathsf{\Gamma }(1-q)}{\int }_a^t{\displaystyle \frac{f^{\prime }\left(t\right)}{{(t-\tau )}^{-q}}}d\tau \end{array}$$

(3)

2.1. Lipschitz Operators Theory

Definition 3

([30]). Let $X^e$ and $Y^e$ be two extended linear spaces which are associated, respectively, with two Banch spaces, X and Y, of measurable functions defined on the time domain $[0,\infty )$, and let D be a subset of $X^e$. A nonlinear operator $A:D\to Y^e$ is called a generalized Lipschitz operator on D if there exists a constant L such that

$${\parallel \left[A\left(x\right)\right]}_T-{\left[A\left(\tilde{x}\right)\right]}_T{\parallel }_Y\le L{\parallel x_T-{\tilde{x}}_T\parallel }_X$$

for all $x,\tilde{x}\in D$ and for all $T\in [0,\infty )$.

Note that the least such constant L is provided by

$$\parallel A\parallel :=\underset{T\in [0,\infty )}{sup}\underset{x_T\ne {\tilde{x}}_T}{\underset{x,\tilde{x}\in D}{sup}}{\displaystyle \frac{{\parallel \left[A\left(x\right)\right]}_T-{\left[A\left(\tilde{x}\right)\right]}_T{\parallel }_Y}{\parallel x_T-{\tilde{x}}_T{\parallel }_X}}$$

(4)

which is a semi-norm for general nonlinear operators and is the actual norm for linear operator A. The actual norm for a nonlinear operator A is provided by

$$\begin{array}{c}\hfill \begin{array}{cc}\hfill {\parallel A\parallel }_{Lip}& =\parallel A\left(x_0\right){\parallel }_Y+\parallel A\parallel \hfill \\ \hfill & =\parallel A\left(x_0\right){\parallel }_Y+\underset{T\in [0,\infty )}{sup}\underset{x_T\ne {\tilde{x}}_T}{\underset{x,\tilde{x}\in D}{sup}}{\displaystyle \frac{{\parallel \left[A\left(x\right)\right]}_T-{\left[A\left(\tilde{x}\right)\right]}_T{\parallel }_Y}{\parallel x_T-{\tilde{x}}_T{\parallel }_X}}\hfill \end{array}\end{array}$$

(5)

for any fixed $x_0\in D$.

Theorem 1.

Let $X^e$ and $Y^e$ be two extended linear spaces which are associated, respectively, with two Banch spaces, X and Y, of measurable functions defined on the time domain $[0,\infty )$, and let D be a subset of $X^e$. A nonlinear operator $A_d$ fractional order operation, defined in [30], is a generalized Lipschitz operator on D.

Proof. 

Let $A_d\left(x\right)$, meaning mapping from $x\to A_d$, where $A_d$ is a fractional order operation. For any $x_1,x_2\in X^e$; however, $x_1\ne x_2$ extended linear space.

$$\begin{array}{cc}\hfill \parallel A_d\left(x_1\right)-A_d\left(x_2\right)\parallel & =\parallel D_x^q\left(x_1\right)-D_x^q\left(x_2\right)\parallel \hfill \\ \hfill & =\parallel {\displaystyle \frac{1}{\mathsf{\Gamma }(n-q)}}{\int }_a^t\frac{x_1^{\left(n\right)}\left(\tau \right)}{{(t-\tau )}^{n-q-1}}d\tau -{\displaystyle \frac{1}{\mathsf{\Gamma }(n-q)}}{\int }_a^t\frac{x_2^{\left(n\right)}\left(\tau \right)}{{(t-\tau )}^{n-q-1}}d\tau \parallel \hfill \end{array}$$

(6)

Because $n\ge q$, $x_1,x_2>\tau$, then $\mathsf{\Gamma }(n-q){\int }_a^t\frac{1}{{(t-\tau )}^{n-q-1}}>0$

Therefore,

$$\begin{array}{cc}\hfill \parallel A_d\left(x_1\right)-A_d\left(x_2\right)\parallel & ={\displaystyle \frac{1}{\Gamma (n-q)}}\parallel {\int }_a^t\frac{x_1^{\left(n\right)}\left(\tau \right)}{{(t-\tau )}^{n-q-1}}d\tau -{\int }_a^t\frac{x_2^{\left(n\right)}\left(\tau \right)}{{(t-\tau )}^{n-q-1}}d\tau \parallel \hfill \\ \hfill & \le {\displaystyle \frac{1}{\Gamma (n-q)}}{\int }_a^t\frac{1}{t-{\tau }^{n-q-1}}d\tau \parallel {\int }_a^t{x}_1^{\left(n\right)}\left(t\right)d\tau -{\int }_a^t{x}_2^{\left(n\right)}\left(t\right)d\tau \parallel \hfill \\ \hfill & \le {\displaystyle \frac{1}{\Gamma (n-q)}}L\parallel x_1-x_2\parallel \hfill \\ \hfill & =H\parallel x_1-x_2\parallel \hfill \end{array}$$

(7)

Obviously there exists $A_d$ which is the least constant of H.

Proof completed. □

Right Coprime Factorization

Operator P + $\mathsf{\Delta }$ P:V → Y denotes a nonlinear system with uncertainties. Where P is the nominal object, $\mathsf{\Delta }$P means the uncertainties of object V and Y stands for the input and output space of the object.

Right factorization:

By appling an intermediate variable w ∈ W, W is called a quasi-state space of P and the input and output of the operator P are described as y = N(w) and v = D(w), respectively. If D is invertible, w(t) = D${}^{-1}$(v)(t), then P(v(t)) = N(w(t)) = ND${}^{-1}$(v)(t); if, furthermore, N and D are two stable operators, the operator P is said to have a right factorization, as shown in Figure 1.

Right coprime factorization:

After right factorization of a object P into (N, D), if two operators R and S satisfy the following Bezout identity, the factorization is said to be right coprime factorization:

$$\begin{array}{c}\hfill RN+SD=M\end{array}$$

(8)

where R is invertible and M is a unimodular operator. The block diagram of the right coprime factorization of a nonlinear system P is shown in Figure 2. Figure 2 shows an operator-based feedback controller for a nonlinear plant P, with the operators R and S serving as the controller.

For a nonlinear real object $\tilde{P}$, it can be represented as a nominal object P with bounded uncertainty $\mathsf{\Delta }P$ and $\tilde{P}=P+\mathsf{\Delta }$. The right factorization of the nominal object P and the overall object $\tilde{P}$ are

$$\begin{array}{c}\hfill P=N{D}^{-1}\end{array}$$

(9)

and

$$\begin{array}{c}\hfill P+\mathsf{\Delta }P=(N+\mathsf{\Delta }N)D^{-1}\end{array}$$

(10)

where N, $\mathsf{\Delta }N$, and D are stable operators, D is invertible, and $\mathsf{\Delta }N$ is unknown while the upper and lower bounds are known. If the following Bezout identity is satisfied and if $\tilde{M}$ is a unimodular operator, then the nonlinear feedback control system is said to be BIBO stable.

$$\begin{array}{c}\hfill R(N+\mathsf{\Delta }N)+SD=\tilde{M}\end{array}$$

(11)

With the operators S and R determined, if they further satisfy the following condition then the robustness of the uncertain system is guaranteed:

$$\begin{array}{c}\hfill \parallel R((N+\mathsf{\Delta }N)-RN)M^{-1}{\parallel }_{Lip}<1\end{array}$$

(12)

where ${\parallel •\parallel }_{Lip}$ is a Lipschitz operator norm. The robust operator-based feedback control system with uncertainty is shown in Figure 3.

Theorem 2

([30]). Let $D^e$ be a linear subspace of the extended linear space $U^e$ associated with a given Banach space $U_B$, and let $(R(N+\mathsf{\Delta }N)+RN)M^{-1}\in Lip\left(D^e\right)$. Let the Bezout identity of the nominal plant and the exact plant be $RN+SD=M\in \mathcal{U}(W,U)$, $R(N+\mathsf{\Delta }N)+SD=\tilde{M}$, respectively. If

$$\begin{array}{c}\hfill \parallel (R(N+\mathsf{\Delta }N)-RN)M^{-1}\parallel <1\end{array}$$

(13)

then the system shown in Figure 3 is robust stable for $\mathsf{\Delta }N$.

Theorem 3

([30]). Let $D^e$ be a linear subspace of the extended linear space $U^e$ associated with a given Banach space $U_B$, and let $(R(N+\mathsf{\Delta }N)-RN+S(D+\mathsf{\Delta }D)-SD)M^{-1}\in Lip\left(D^e\right)$. Let the Bezout identity of the nominal plant and the exact plant be $RN+SD=M\in \mathcal{U}(W,U)$, $R(N+\mathsf{\Delta }N)+S(D+\mathsf{\Delta }D)=\tilde{M}$, respectively. If

$$\begin{array}{c}\hfill \parallel (R(N+\mathsf{\Delta }N)-RN+S(D+\mathsf{\Delta }D)-SD)M^{-1}\parallel <1\end{array}$$

(14)

then the system shown in Figure 4 is robust stable for $\mathsf{\Delta }N,\mathsf{\Delta }D$.

Theorem 4.

Let $D^e$ be a linear subspace of the extended linear space $U^e$ associated with a given Banach space $U_B$, and let $(R(N+\mathsf{\Delta }N)-RN+SD)M^{-1}\in Lip\left(D^e\right)$. Let the Bezout identity of the nominal plant and the exact plant be $RN+SD=M\in \mathcal{U}(W,U)$, $R(N+\mathsf{\Delta }N)+SD=\tilde{M}$, respectively. If

$$\begin{array}{c}\hfill \parallel R(N+\mathsf{\Delta }N)-RN\parallel <\frac{1}{\parallel M^{-1}\parallel }\end{array}$$

(15)

then the system shown in Figure 3 is robust stable for $\mathsf{\Delta }N$.

Proof. 

$$\begin{array}{c}\hfill \parallel (R(N+\mathsf{\Delta }N)-RN)M^{-1}\parallel <\parallel R(N+\mathsf{\Delta }N)-RN\parallel \parallel M^{-1}\parallel \end{array}$$

(16)

If

$$\begin{array}{c}\hfill \parallel R(N+\mathsf{\Delta }N)-RN\parallel <\frac{1}{\parallel M^{-1}\parallel }\end{array}$$

(17)

then

$$\begin{array}{c}\hfill \parallel (R(N+\mathsf{\Delta }N)-RN)M^{-1}\parallel <1\end{array}$$

(18)

According to Theorem 2, the system shown in Figure 3 is robust stable for $\mathsf{\Delta }N$.

Proof completed. □

Theorem 5.

Let $D^e$ be a linear subspace of the extended linear space $U^e$ associated with a given Banach space $U_B$, and let $(R(N+\mathsf{\Delta }N)-RN+S(D+\mathsf{\Delta }D)-SD)M^{-1}\in Lip\left(D^e\right)$. Let the Bezout identity of the nominal plant and the exact plant be $RN+SD=M\in \mathcal{U}(W,U)$, $R(N+\mathsf{\Delta }N)+S(D+\mathsf{\Delta }D)=\tilde{M}$, respectively. If the condition

$$\begin{array}{c}\hfill \parallel R(N+\mathsf{\Delta }N)-RN+S(D+\mathsf{\Delta }D)-SD\parallel <\frac{1}{\parallel M^{-1}\parallel }\end{array}$$

(19)

is satisfied, then the system shown in Figure 4 is robustly stable for $\mathsf{\Delta }N$, $\mathsf{\Delta }D$.

Proof. 

In the same method with Theorem 4, this theorem was proved. □

2.2. Problem Statement

According to the law of heat-energy balance of two fluids, the fractional order derivative model for a spiral-plate parallel flow heat exchanger is derived as follows [13]:

$$\begin{array}{c}\hfill \left\{\begin{array}{cc}\hfill & D_{\theta }^{q_1}{T}_h(\theta ,t)={\displaystyle \frac{(k+\mathsf{\Delta }k)FAZ}{Q{L}_1{c}_h{\rho }_h}}(T_c(\theta ,t)-T_h(\theta ,t))\hfill \\ \hfill & D_{\theta }^{q_2}{T}_c(\theta ,t)={\displaystyle \frac{(k+\mathsf{\Delta }k)FAZ}{Q{L}_2{c}_c{\rho }_c}}(T_h(\theta ,t)-T_c(\theta ,t))\hfill \\ \hfill & \theta \in [0,11\pi ]\hfill \end{array}\right.\end{array}$$

(20)

Let $q_1=q$, $q_2=q+\mathsf{\Delta }q$, then,

$$\begin{array}{c}\hfill \begin{array}{cc}\hfill D_{\theta }^{q_2}{T}_c(\theta ,t)& =D_{\theta }^q{T}_c(\theta ,t)-\mathsf{\Delta }{D}_q\hfill \\ \hfill & ={\displaystyle \frac{kFAZ}{Q{L}_2{c}_c{\rho }_c}}(T_h(\theta ,t)-T_c(\theta ,t))\hfill \end{array}\end{array}$$

(21)

Thus,

$$\begin{array}{c}\hfill D_{\theta }^q{T}_h(\theta ,t)={\displaystyle \frac{(k+\mathsf{\Delta }k)FAZ}{Q{L}_1{k}_h}}(T_c(\theta ,t)-T_h(\theta ,t))\end{array}$$

(22)

$$\begin{array}{c}\hfill D_{\theta }^q{T}_c(\theta ,t)+\mathsf{\Delta }{D}_q={\displaystyle \frac{(k+\mathsf{\Delta }k)FAZ}{Q{L}_2{k}_c}}(T_h(\theta ,t)-T_c(\theta ,t))\\ \hfill \theta \in [0,11\pi ]\end{array}$$

(23)

$$\begin{array}{c}\hfill D_{\theta }^q\left(\mathsf{\Delta }T(\theta ,t)\right)+\mathsf{\Delta }{D}_q=FAZ({\displaystyle \frac{1}{k_{c}Q{L}_2}}+{\displaystyle \frac{1}{k_{h}Q{L}_1}})\mathsf{\Delta }T(\theta ,t)\end{array}$$

(24)

where $k=\frac{{\delta }_s}{\lambda }$, $k+\mathsf{\Delta }k=\frac{1}{h_h}+\frac{{\delta }_s}{\lambda }+\frac{1}{h_c}$, $k_c$ = $c_c{\rho }_c$, $k_h$ = $c_h{\rho }_h$, and $\mathsf{\Delta }T(\theta ,t)$ = $T_c(\theta ,t)-T_h(\theta ,t)$. $A=\sqrt{a^2+b^2}$ and $A+\mathsf{\Delta }A$= $\sqrt{a^2+{(b+a\ast 11\pi )}^2}$ $F\in [1,2]$, which is related to the plant of the spiral-plate heat exchanger; ${\rho }_c$ and ${\rho }_h$ are the densities of the cold fluid and the heat fluid, respectively; $c_c$ and $c_h$ are the specific heat capacities of the cold fluid and the heat fluid, respectively; $T_{c,in}$ and $T_{h,in}$ are the input temperatures of the cold fluid and the heat fluid, respectively; $T_{c,out}$ and $T_{h,out}$ are the output temperatures of the cold fluid and the heat fluid, respectively; $q_1$ and $q_2$ are fractional orders of the hot fluid and the cold fluid, respectively; and $Q_{L1}$ and $Q_{L2}$ are the volume flow rate of the hot fluid and the cold fluid, respectively.

$$\begin{array}{c}\hfill T_{c,out}\left(t\right)=T_{h,in}\left(t\right)+FZA{D}_{11\pi }^{-q}[{\displaystyle \frac{1}{k_{c}Q{L}_2}}+{\displaystyle \frac{1}{k_{h}Q{L}_1}}\mathsf{\Delta }T(\theta ,t)]+\mathsf{\Delta }{D}_q\end{array}$$

(25)

where $T_{c,out}\left(t\right)$ = $T(11\pi ,t)$, $T_{c,in}\left(t\right)$ = $T_h(0,t)$, $T_{h,in}\left(t\right)$ = $T_h(11\pi ,t)$, $T_{h,out}\left(t\right)$ = $T_h(0,t)$. $T_{c,in}-T_{h,out}$ is the initial condition of the fractional order integral.

3. Fractional Order Operator Controller Design and Tracking Controller Design

3.1. Operator-Based Fractional Order Controller Design

As shown in Figure 4, provided a nonlinear operator control system, operators V and Y are the input and output space of this plant. Let (N, D) be the right factorization of P. The feedback nonlinear control system shown in Figure 4 is BIBO stable if there exist two stable operators R: Y → V, S: V → V (S being invertible as well) that satisfy the Bezout identity equation:

$$\begin{array}{c}\hfill RN+SD=M\end{array}$$

(26)

where M is a unimodular operator to consider the uncertain term in the nonlinear system. With the designed operators S and R in Figure 4, the following equation can be satisfied:

$$\begin{array}{c}\hfill \parallel R(N+\mathsf{\Delta }N)-RN+S(D+\mathsf{\Delta }D)-SD\parallel <{\displaystyle \frac{1}{\parallel M^{-1}\parallel }}\end{array}$$

(27)

where $\parallel •\parallel$ is a Lipschitz norm. Then, the nonlinear feedback control system is robustly stable where M is an unimodular operator. The mathematical modeling of P considering the uncertain term $\mathsf{\Delta }P$ can be provided for the the spiral heat exchanger system as follows:

$$\begin{array}{ccc}& P+\mathsf{\Delta }P:\hfill & \hfill \\ & T_{c,out}\left(t\right)=T_{h,in}\left(t\right)+FZ(k+\mathsf{\Delta }k)D_{11\pi }^{-q}({\displaystyle \frac{1}{Q{L}_2{k}_c}}+{\displaystyle \frac{1}{Q{L}_1{k}_h}})\mathsf{\Delta }T(\theta ,t))+\mathsf{\Delta }{D}_q\hfill \end{array}$$

(28)

where $T_{c,out}\left(t\right)$ = $T(11\pi ,t)$, $T_{c,in}\left(t\right)$ = $T_h(0,t)$, $T_{h,in}\left(t\right)$ = $T_h(11\pi ,t)$, $T_{h,out}\left(t\right)$ = $T_h(0,t)$. The plant can be right coprime factorized as follows:

$$\begin{array}{ccc}& {(D+\mathsf{\Delta }D)}^{-1}:V\to W\hfill & \hfill \\ & w=(A+\mathsf{\Delta }A){\displaystyle \frac{1}{Q{L}_2{k}_c}}+{\displaystyle \frac{1}{Q{L}_1{k}_h}}\hfill \end{array}$$

(29)

$$\begin{array}{ccc}& (D+\mathsf{\Delta }D):W\to V\hfill & \hfill \\ & Q{L}_1={\displaystyle \frac{(A+\mathsf{\Delta }A)Q{L}_2{k}_c}{[Q{L}_2{k}_{c}w-(A+\mathsf{\Delta }A)]k_h}}\hfill \end{array}$$

(30)

$$\begin{array}{ccc}& D:W\to V\hfill & \hfill \\ & Q{L}_1={\displaystyle \frac{AQ{L}_2{k}_c}{(Q{L}_2{k}_{c}w-A)k_h}}\hfill \end{array}$$

(31)

$$\begin{array}{ccc}& N+\mathsf{\Delta }N:W\to Y\hfill & \hfill \\ & T_{c,out}\left(t\right)=T_{h,in}\left(t\right)+FZ(k+\mathsf{\Delta }k)D_{11\pi }^{-q}\left(w\mathsf{\Delta }T(\theta ,t)\right)+\mathsf{\Delta }{D}_q\hfill \end{array}$$

(32)

$$\begin{array}{ccc}& N:W\to Y\hfill & \hfill \\ & T_{c,out}\left(t\right)=T_{h,in}\left(t\right)+FZk{D}_{11\pi }^{-q}\left(w\mathsf{\Delta }T(\theta ,t)\right)\hfill \end{array}$$

(33)

The operator-based feedback control system is shown in Figure 2. The operators R and S are designed as follows:

$$\begin{array}{ccc}& R:Y\to V\hfill & \hfill \\ & b=k_p{\displaystyle \frac{1}{FZk}}{D}_{11\pi }^q\left(\mathsf{\Delta }T(\theta ,t)\right)\hfill \end{array}$$

(34)

where $\mathsf{\Delta }T(\theta ,t)$ = $T_{c,out}\left(t\right)-T_{h,in}\left(t\right)$.

$$\begin{array}{ccc}& S^{-1}:V\to V\hfill & \hfill \\ & Q_{L1}=(K_M-K_p){\displaystyle \frac{AQ{L}_2{k}_c}{(Q_{L2}{k}_{c}e-A)K_h}}\hfill \end{array}$$

(35)

$$\begin{array}{ccc}& S:V\to V\hfill & \hfill \\ & e=A({\displaystyle \frac{1}{Q_{L2}{k}_c}}+{\displaystyle \frac{1}{Q_{L1}{k}_h}})\hfill \end{array}$$

(36)

Operators R and $S^{-1}$ are designed to satisfy the Bezout identity:

$$\begin{array}{c}\hfill RN+SD=M\end{array}$$

(37)

thus, if

$$\begin{array}{c}\hfill \parallel (R(N+\mathsf{\Delta }N)-RN+S(D+\mathsf{\Delta }D)-SD))\parallel <1/\parallel M^{-1}\parallel \end{array}$$

(38)

is satisfied according to Therom 5, then the system is BIBO stable.

3.2. Fractional Order Operator-Based Control Stability Analysis

In this section, the stability of the fractional order operator-based control system for a spiral-plate exchanger with uncertainties is presented.

$$\begin{array}{c}\hfill \begin{array}{cc}\hfill R(N+\mathsf{\Delta }N)-RN& ={\displaystyle \frac{1}{FZk}}{D}_{11\pi }^q\left(\mathsf{\Delta }T\right)FZ(k+\mathsf{\Delta }k)D_{11\pi }^{-q}\left(w\mathsf{\Delta }T\right)-{\displaystyle \frac{1}{FZk}}{D}_{11\pi }^q\left(\mathsf{\Delta }T\right)FZk{D}_{11\pi }^{-q}\left(w\mathsf{\Delta }T\right)\hfill \\ \hfill & ={\displaystyle \frac{k+\mathsf{\Delta }k}{k}}-1\hfill \\ \hfill & ={\displaystyle \frac{\mathsf{\Delta }k}{k}}\hfill \end{array}\end{array}$$

(39)

$$\begin{array}{c}\hfill \begin{array}{cc}\hfill S(D+\mathsf{\Delta }D)-SD& =A\{{\displaystyle \frac{[Q{L}_2{k}_c-(A+\mathsf{\Delta }A)]k_h}{k_h(A+\mathsf{\Delta }A)Q{L}_2{k}_c}}+{\displaystyle \frac{1}{Q{L}_2{k}_c}}\}-A\{{\displaystyle \frac{[Q{L}_2{k}_c-A]k_h}{k_{h}AQ{L}_2{k}_c}}+{\displaystyle \frac{1}{Q{L}_2{k}_c}}\}\hfill \\ \hfill & =A\{{\displaystyle \frac{Q{L}_2{k}_c-(A+\mathsf{\Delta }A)}{(A+\mathsf{\Delta }A)Q{L}_2{k}_c}}+{\displaystyle \frac{1}{Q{L}_2{k}_c}}\}-A\{{\displaystyle \frac{Q{L}_2{k}_c-A}{AQ{L}_2{k}_c}}+{\displaystyle \frac{1}{Q{L}_2{k}_c}}\}\hfill \\ \hfill & =A\{{\displaystyle \frac{1}{A+\mathsf{\Delta }A}}-{\displaystyle \frac{1}{Q{L}_2{k}_c}}+{\displaystyle \frac{1}{Q{L}_2{k}_c}}\}-A\{{\displaystyle \frac{1}{A}}-{\displaystyle \frac{1}{Q{L}_2{k}_c}}+{\displaystyle \frac{1}{Q{L}_2{k}_c}}\}\hfill \\ \hfill & ={\displaystyle \frac{A}{A+\mathsf{\Delta }A}}-1\hfill \\ \hfill & =-{\displaystyle \frac{\mathsf{\Delta }A}{A+\mathsf{\Delta }A}}\hfill \end{array}\end{array}$$

(40)

thus,

$$\begin{array}{c}\hfill \begin{array}{cc}\hfill \parallel R(N+\mathsf{\Delta }N)-RN+S(D+\mathsf{\Delta }D)-SD\parallel & =\parallel {\displaystyle \frac{\mathsf{\Delta }k}{k}}-{\displaystyle \frac{\mathsf{\Delta }A}{A+\mathsf{\Delta }A}}\parallel \hfill \\ \hfill & <\parallel {\displaystyle \frac{\mathsf{\Delta }k}{k}}\parallel +\parallel {\displaystyle \frac{\mathsf{\Delta }A}{A+\mathsf{\Delta }A}}\parallel \hfill \end{array}\end{array}$$

(41)

According to the stability conditions of the fractional order operator-based control system, if

$$\begin{array}{c}\hfill \begin{array}{c}\hfill \parallel {\displaystyle \frac{\mathsf{\Delta }k}{k}}\parallel +\parallel {\displaystyle \frac{\mathsf{\Delta }A}{A+\mathsf{\Delta }A}}\parallel <1/\parallel M^{-1}\parallel \end{array}\end{array}$$

(42)

that is,

$$\begin{array}{c}\hfill \begin{array}{c}\hfill \parallel M^{-1}\parallel <{\displaystyle \frac{1}{\parallel {\displaystyle \frac{\mathsf{\Delta }k}{k}}\parallel +\parallel {\displaystyle \frac{\mathsf{\Delta }A}{A+\mathsf{\Delta }A}}\parallel }}\end{array}\end{array}$$

(43)

Here, $k_M={\displaystyle \frac{1}{\parallel M^{-1}\parallel }}$

thus,

$$\begin{array}{c}\hfill k_M>\parallel {\displaystyle \frac{\mathsf{\Delta }k}{k}}\parallel +\parallel {\displaystyle \frac{\mathsf{\Delta }A}{A+\mathsf{\Delta }A}}\parallel \end{array}$$

(44)

is a BIBO stable condition.

From

Table A1. Parameters of the spiral-plate heat exchanger.

Meaning	Symbol	Value
Geometric parameter of a spiral function	a	$\frac{0.005}{\pi }$ m/rad
Initial radius of hot fluid side	b	0.08 m
Spiral function angle of the spiral-plate heat exchanger	$\theta$	$[0,11\pi ]$
The width of hot flow channel	${\delta }_h$	0.005 m
The width of cold flow channel	${\delta }_c$	0.005 m
The width of solid wall	${\delta }_s$	0.0018 m
The height of the spiral-plate heat exchanger	Z	0.011 m

, ${\displaystyle \frac{\mathsf{\Delta }k}{k}}={\displaystyle \frac{732}{9278}}=0.07$. ${\displaystyle \frac{\mathsf{\Delta }A}{A+\mathsf{\Delta }A}}={\displaystyle \frac{0.135}{0.215}}=0.627$. Let, $k_M>0.627$, then, the nonlinear control system is BIBO stable.

The fractional order operator-based control system is stable under condition (44), however, the track precision is bad because of model error and disturbances. Therefore, it is rarely used alone. In order to improve the robustness, anti-interference, and tracking performance of the control system, we designed a feedback control system for the tracking controller.

3.3. Tracking Controller Design

The differential equation of fractional order controller $P{I}^{\lambda }{D}^{\delta }$ is described by

$$\begin{array}{c}\hfill u\left(t\right)=K_{p1}e\left(t\right)+K_i{D}_t^{-\lambda }e\left(t\right)+K_d{D}_t^{\delta }e\left(t\right)\end{array}$$

(45)

If $\lambda ,\delta =1$, it is a conventional PID control. It is obvious that the fractional order controller needs to design the three parameters $K_{p1}$, $K_i$, and $K_d$ as well as the orders $\lambda$, $\delta$ of the integral and derivative controllers. The orders $\lambda$, $\delta$ need not necessarily be integers, and can be any real numbers. As shown in Figure 5, the FOPID (fractional order PID) controller generalizes the conventional integer order PID controller and expands it from point to plane. This expansion can provide a great deal more flexibility in PID control design.

3.4. Operator-Based Fractional Order Robust Control for Spiral-Plate Heat Exchanger with Uncertainties and Disturbances

As a spiral heat exchanger is a nonlinear system with uncertainties, disturbances, and a long delay time, it is difficult to improve the tracking performance of the output temperature. While operator-based control is a nonlinear control method to improve stability, tracking performance remains poor. PID feedback control is widely used in application due to its simple form and because it only required three parameters to be adjusted. FOPID, with its five parameters, is an extension of conventional PID. Thus, FOPID is more flexible than the conventional PID. The five cases for output temperature control of the presented spiral heat exchanger were designed to compare tracking performance and stablity for uncertanities and disturbance, as shown Figure 6, Figure 7, Figure 8, Figure 9 and Figure 10.

4. Simulation and Analysis

In this section, the five different cases are simulated and analysed in Matlab with the same uncertainties and disturbances.

4.1. Simulation Conditions

Here,

Table 1. Simulation parameters of the spiral-plate heat exchanger.

Meaning (Symbol)	Value
The densities of the two fluids (${\rho }_c$, ${\rho }_h$)	1000 Kg/m${}^3$
The specific heat capacities of two fluids ($c_c$, $c_h$)	4.2 KJ/(Kg·${}^{\circ }$C)
The input temperature of cold fluid ($T_{c,in}$)	20 ${}^{\circ }$C
The input temperature of hot fluid ($T_{h,in}$)	50 ${}^{\circ }$C
Thermal conductivity of SUS304 ($\lambda$)	16.7 W/(m ${}^{\circ }$C)
Heat transfer coefficients of two fluids ($h_h$, $h_c$)	366 W/m${}^2$· K
Uncertainty of the spiral heat exchanger’s shape ($\mathsf{\Delta }A$)	0.135
Uncertainty of the heat transfer coefficient ($\mathsf{\Delta }k$)	732

shows the simulation parameters for the spiral-plate heat exchanger.

Table 2. Simulation condition of the spiral-plate heat exchanger.

Meaning (Symbol)	Value
Simulation time (t)	[0, 15] s
Reference output temperature ($T_{c,r}$)	40 ${}^{\circ }$C
The orders for fractional order derivative (q)	0.97
The input temperature of cold fluid ($T_{c,in}$)	20 ${}^{\circ }$C
The input temperature of hot fluid ($T_{h,in}$)	50 ${}^{\circ }$C
Uncertainty of the spiral heat exchanger’s shape (${\displaystyle \frac{\mathsf{\Delta }A}{A}}$)	0.627
Uncertainty of the heat transfer coefficient (${\displaystyle \frac{\mathsf{\Delta }k}{k}}$)	0.07

denotes the simulation condition for the spiral-plate heat exchanger. The reference output temperature is the output temperature of the cold fluid. The volume flow rate $Q{L}_2$ on the cold fluid side is the disturbance signal; $Q{L}_2$ is changed from 1 L/Min to 7 L/Min in time 8 s, ${\displaystyle \frac{\mathsf{\Delta }A}{A}}$ and ${\displaystyle \frac{\mathsf{\Delta }k}{k}}$ are the uncertainties of the spiral heat exchanger’s shape and the heat transfer coefficient, respectively. The volume flow rate $Q{L}_1$ on the hot fluid side is the control signal. Considering the actual condition, the maximum input volume flow rate is 10 L/Min.

4.2. Simulation and Analysis

The spiral counter-flow heat exchanger with uncertainties and disturbances described by the special fractional order equation is both a first order or norm fractional order system and a nonlinear system. Thus, the parameters of fractional order PID control cannot be tuned using the conventional tuning method. The parameters of both the conventional and fractional order PID control are tuned using a trial-and-error method. The first proportion is adjusted, then derivative integrals are adjusted in turn until the best parameters are derived. In the future, the parameters of fractional order PID is optimized by particle swarm optimum algorithm.

Table 3. Tuning parameters for operator controller.

Meaning	Symbol	Value
Reference input temperature	$T_{c,r}$	40 ${}^{\circ }$C
The orders for fractional order derivative	q	0.97
Gain of operator	$K_{p1}$	10
Gain	$K_M$	4.0

,

Table 4. Tuning parameters for FOPID Controller with operator controller.

Meaning	Symbol	Value
Reference input temperature	$T_{c,r}$	40 ${}^{\circ }$C
The orders for fractional order derivative	q	0.97
Gain of operator	$K_{p1}$	10
Gain	$K_M$	4.0
Proportional gain	$K_{p1}$	50
Integeral order	$\lambda$	0.9
Integeral gain	$K_i$	1.0
Differential order	$\delta$	0.95
Differential gain	$K_d$	3.0

,

Table 5. Tuning parameters for FOPID Controller without operator controller.

Meaning	Symbol	Value
Reference input temperature	$T_{c,r}$	40 ${}^{\circ }$C
Proportional gain	$K_{p1}$	50
Integeral order	$\lambda$	0.9
Integeral gain	$K_i$	1.0
Differential order	$\delta$	0.95
Differential gain	$K_d$	3.0

,

Table 6. Tuning parameters for PID Controller with operator controller.

Meaning	Symbol	Value
Reference input temperature	$T_{c,r}$	40 ${}^{\circ }$C
The orders for fractional order derivative	q	0.97
Gain of operator	$K_{p1}$	10
Gain	$K_M$	4.0
Proportional gain	$K_{p1}$	10
Integeral gain	$K_i$	0.6
Differential gain	$K_d$	0.05

and

Table 7. Tuning parameters for PID Controller without operator controller.

Meaning	Symbol	Value
Reference input temperature	$T_{c,r}$	40 ${}^{\circ }$C
The orders for fractional order derivative	q	0.97
Proportional gain	$K_{p1}$	10
Integeral gain	$K_i$	0.6
Differential gain	$K_d$	0.05

are the best controller parameters to tune and the parameters of the operator controller.

It is obvious that the fractional order PID control with operator controller has the best tracking performance compared to the others, as shown in Figure 11. The overshoot and settle times for the fractional order PID control with operator controller are shorter than for the fractional order PID control without operator controller. The overshoot and settle times for the conventional PID control with operator controller are smaller than for the conventional PID control without operator controller.

Figure 12 shows that fractional order operator control can improve the stability when uncertainties and disturbances are present, although the tracking performance and anti-disturbance are bad.Figure 13, Figure 14, Figure 15 and Figure 16 show the control performance, control signals, and tracking performance in the control process for the five different control schemes with uncertainties and disturbance; $T_{c,r}$, d, u, and $T_{c,out}$ are the reference output temperature of the cold fluid side, disturbance signal of the volume flow rate in the cold fluid side, control signal of the volume flow rate on the hot fluid side, and output temperature on the cold fluid side, respectively. The performance with operator-based fractional order PID control is the best in terms of anti-disturbance and stability compared to the other control schemes.

5. Conclusions

In this paper, we have proposed operator-based fractional order PID nonlinear robust control with uncertainties and disturbance. First, we introduced the concepts of fractional order and the preliminaries of operator theory as extended to fractional order and nonlinear fractional order equations. Then, operator-based nonlinear fractional order controller design and fractional order PID tracking controller design were covered and the parameters of the operator controller and fractional order PID controller were determined. Finally, the robust stability and tracking performance of the operator-based nonlinear robust control system with uncertainties and disturbance were analyzed via simulation in Matlab. However, the tuning parameters of the fractional order controller continue to require adjustment offline or by hand, and robust control performance requires continued research as well.