Complexity

Complexity / 2019 / Article
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Advanced Control and Optimization for Complex Energy Systems

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Research Article | Open Access

Volume 2019 |Article ID 9361723 | 12 pages | https://doi.org/10.1155/2019/9361723

Performance Analysis of Reheat Steam Temperature Control System of Thermal Power Unit Based on Constrained Predictive Control

Academic Editor: Xiaoqing Bai
Received17 Apr 2019
Revised28 Jun 2019
Accepted08 Jul 2019
Published05 Aug 2019

Abstract

The reheat steam temperature control system of thermal power unit is a complex control object with time-varying parameters and large delay. In order to achieve precise control of reheat steam temperature, the performance of the reheat temperature control system is analyzed according to the data that are obtained based on the constrained predictive control algorithm. Firstly, the process and mathematical model of reheat steam temperature control system are introduced. Then the principle of constrained predictive control algorithm is analyzed. Finally, the steady-state values of control quantities of reheat steam temperature control system under different conditions are given by MATLAB simulation, and, by analyzing the steady-state values and steady-state time of the input and output of the system, the reference values and the regulating law of the control quantities and the specific constraint range of the control quantities of the system are given, which can provide reference data and theoretical basis for the field adjustment of the reheat steam temperature control system in power plant and improve the safety and effectiveness of the system.

1. Introduction

In recent years, China’s electric power industry has developed rapidly. Ultra-supercritical thermal power unit, which has the characteristics of nonlinear, uncertain parameters and time-variation, has become the main unit in coal-fired power generation industry. Thus higher requirements for automatic control of coal-fired power plants are put forward. At the same time, China’s clean energy industry has made great progress, and a variety of clean energy sources have entered the electricity market, which has a certain impact on the traditional coal-fired plants. In order to improve the market competitiveness of coal-fired plants, it is necessary to improve the efficiency of unit continuously. Increasing the pressure and temperature of steam is an effective means to improve competitiveness, but, due to the design requirement of the unit’s infrastructure design and the limitation of metal material of boiler, the upgrading and transformation of operating parameters of unit require a large amount of investment of funds. Therefore, it is very important to improve the control effect of steam temperature on the existing basis.

In thermal power unit, reheat steam temperature is an important parameter that affects the economic value of unit. The reheat steam temperature control system is a complex object with the characteristics of large inertia and hysteresis, and the dynamic characteristics of the system are different during the load variation of generator unit, which make the control of reheat steam temperature extremely difficult. If the reheat steam temperature is too high, it may increase the corrosion of the metal material of pipeline and the heating surface of the boiler through which the steam flows, so that the service life of unit may be reduced. If the steam temperature is too low, the humidity of steam will be very high, which not only makes the last turbine blades more vulnerable to damage, but also reduces the thermal efficiency of unit. The large variation of reheat steam temperature will also cause unit fatigue and reduce the service life of unit. Therefore, understanding the regulating law of the control quantities and the constraint range of the control quantities of the reheat steam temperature control system can not only ensure the safety of thermal equipment, but also have important significance to the stability of reheat steam temperature.

In order to improve the control effect of steam temperature, a large number of scholars have adopted a variety of advanced control strategies to study it. A new cascade feedback control system with load feed-forward of reheat steam temperature is proposed in [1]. Single-Neuron Self-adaptive PSD algorithm controller applied to outer loop and double-degree PID controller is applied to inner loop, which achieves good control effect. In [2], based on the characteristics of superheated steam temperature of a boiler, a new cascade control system is designed. The main regulator adopts multimodel observer control, and the secondary controller adopts weighted synthesizing proportional control. The system integrates the characteristics of the multimodel control with those of the state variable control with observer. The results show that the control system has strong robustness. In [3], an adaptive predictive control algorithm is designed for the reference model, and two compensators are introduced; one is two-order compensator for process; the other one is time delay compensator for the reference model. The algorithm has been applied in a 200MW peak regulating drum boiler for reheating temperature process, and high control accuracy is obtained. As the superheated steam temperature has large inertia, time-delay, and nonlinearity and its dynamic characteristics change with the operating conditions, a self-tuning PID controller based on fuzzy-RBF neural networks is presented for its control in [4], which has the advantages of traditional PID control, neutral networks control, and fuzzy control and optimizes online PID parameters. In [5], a new intelligent control algorithm of cloud models is proposed. The variant dimension cloud model intelligent controller, which contains a one-dimension cloud model controller to eliminate steady-state error, is designed, and it is used for superheated steam temperature control of a supercritical once-through 600MW boiler. In [6], a multimodel internal mode control strategy is proposed, and it has been successfully applied to a 1024 t/h supercritical pressure boiler. Performance studies show that the control strategy ensures that the superheated steam temperature stays within the desired range for both steady and varying loads. In [7], dynamic matrix control (DMC) is applied in controlling steam temperatures of a large-scale once-through boiler-turbine system. Online optimization is performed for the DMC using the step response model. The simulation results show satisfactory performance of the proposed DMC technique. Aiming at the characteristics of large inertia, large time delay, and nonlinearity of Reheater Temperature Control System, a hybrid optimization algorithm (MPSO-RBF) for radial basis function (RBF) neural network based on modified particle swarm optimization (MPSO) is presented in [8]. The results have proved that MPSO-RBF method has good performance index. In [9], a scheme combining neural network identification technology and adaptive inverse control technology is proposed for the control of boiler superheated steam temperature in fossil-fired power plant. The identified inverse model is preset as the controller and connected in series with the controlled object to form an adaptive inverse control system. In [10, 11], active disturbance rejection control (ADRC) is applied in the control of superheated steam temperature. Comparing with PID algorithm, the method achieved an excellent performance. In [12], a nonlinear control strategy for steam power plants is proposed. The strategy decomposes the overall plant into three separate subsystems and applies decoupling with dead time compensation for each one of them. The simulation results show that the method has good performance and robustness. When the superheated steam temperature is controlled by adjusting the cooling water, the nonlinear characteristics of the valve are caused by the flow rate. In [13], by collecting the valve input and output data and fitting the valve flow characteristic curve, a valve opening degree compensator based on the polynomial fitting method was designed. The simulation results show that the method can overcome the nonlinear problem caused by valve flow characteristics. In [14], a system of automatic control over the temperature of superheated steam for the boiler with three-tier steam cooling system is considered. A regulating algorithm rests on a cascade control method with the temperature error correction based on a force signal. The force signal is a speed of steam temperature change after the condensate injection. The simulation results show the effectiveness of the method. Besides, based on robust H∞ control method, the reheat steam temperature control system of boiler is studied in [15]. In [16], according to the characteristics of reheat steam temperature, a hybrid optimization method based on Biogeography-Based Optimization (BBO) algorithm is proposed to optimize the traditional PID controller. It turns out that the optimized PID controller has better tracking ability and better anti-internal and external interference performance in reheat steam control system.

Aiming at the difficulty of reheat steam temperature control, model predictive control is a useful control method. It can deal with multivariable, constrained, and time-delay problems effectively and has good dynamic control performance. Model predictive control (MPC) [1720] was proposed in the 1980s. It has been improved and developed continuously in recent years and has been widely used in many industrial fields such as robots [2124]. The control mechanism of MPC is that, at each sampling time, according to the current measurement information, an open-loop optimization problem in finite time domain is solved online, and the first element of the control sequence is acted on the controlled object. At the next sampling time, the above process is repeated; that is, the optimization problem is refreshed and resolved with new measurements. In addition, in the actual industrial control process, the physical quantity of the system can only be taken in a certain range, such that the opening range of the valve dampers in the unit of thermal power plant can only be taken from 0% to 100%. Executing agencies are not allowed to change too much to prevent damage to them. Therefore, in actual control process, the control input and output must be constrained according to the actual requirement, so that their values can be kept within a certain range. Considering the above factors, the reheat steam temperature control system of 660 MW Ultra-supercritical Once-through Boiler in a power plant is taken as the research object in this paper. And the control process of reheat steam temperature in coal-fired power plant is studied and analyzed by using constrained predictive control algorithm. Through the simulation results, the regulation law and the restriction range of system inputs during the reheat steam temperature system regulation are obtained, which provides theoretical and data support for field regulation. In this way, we can improve the safety and efficiency of reheat steam temperature control and the quality of reheat steam temperature control of ultra-supercritical coal-fired units.

The paper is organized as follows. In Section 2, the technological principle and mathematical model of reheat steam temperature control system are formulated. Then the principle of constrained predictive control algorithm is analyzed in Section 3. In Section 4, we apply constrained predictive control to reheat steam temperature control system and carry out MATLAB simulation. And, by analyzing the simulation results, the input regulation law and appropriate constraint range of system inputs are given. Finally, conclusions are given in Section 5.

2. The Technological Principle and Mathematical Model of Reheat Steam Temperature Control System

2.1. The Technological Principle of Reheat Steam Temperature Control System

At present, in order to improve the operation efficiency of large-scale thermal power unit, the steam which has finished the work in the high-pressure cylinder is reheated generally. The process of steam reheating involves three steps. At first, the steam discharged from high pressure cylinder is resent back to the boiler for heating. Then the reheat steam is heated to a certain temperature. Finally, the reheat steam is sent to the middle- and low-pressure cylinders for work.

There are many ways to regulate reheat steam temperature. The commonly used methods include adjusting flue gas damper opening, swinging burner swing angle, and spraying water to reduce temperature. The process diagram of reheat steam temperature control system is shown in Figure 1. In the control process of steam temperature, reheat steam pipe is generally divided into side A and side B. The burner and the flue gas baffle act on the reheat steam temperature of both sides at the same time. The sprinkler that is installed on the A side and the B side of the reheater can only control the reheat steam temperature of the A side and the B side, respectively. When reheat steam temperature is controlled by flue gas damper, the tail flue of the boiler is divided into two parallel flues. Low temperature reheater is arranged in the main flue, low temperature superheater is arranged in the bypass flue, and economizer is arranged behind them. Temperature regulating damper is installed under economizer. By changing the opening of two flue dampers, the ratio of flue gas that flows through cryogenic reheater and cryogenic superheater is changed, so as to control the temperature of reheat steam. Specifically, when the opening of the flue gas damper increases, the reheat steam temperature increases; otherwise the reheat steam temperature decreases. The way of adjusting the swing angle of the burner is to change the up and down inclination angle of the swing burner nozzle, which will adjust the position of the high temperature flame center in the furnace, so as to change the flue gas temperature at the outlet of the furnace and control the reheat steam temperature. Similar to the flue gas damper, the reheat steam temperature increases with the increase of burner swing angle; otherwise the reheat steam temperature decreases. In case of emergency, sprinklers on both sides of reheater can spray water to cool down.

In general, adjusting flue gas damper opening and burner swing angle is the main control means in the control process of reheat steam temperature system. The performance of burner swing angle regulation and flue gas damper regulation is stable, and heat shock is small, so the two control methods have higher thermal economy. Although spray desuperheating has a rapid effect on reheat steam temperature control, it will reduce the thermal efficiency of the unit, so it is not the main method of regulation. Usually only in the process of unit start-up and shutdown, or in the case of accident, spray desuperheating is used as an auxiliary emergency means. Besides, in the normal operation of the unit, small amount of cooling water can be used intermittently, or it can be combined with other temperature regulation methods as a fine-tuning method of reheat steam.

2.2. The Mathematical Model of Reheat Steam Temperature Control System

From the above analysis, we can learn that the ideal control method for the reheat steam temperature should be to use the burner swing angle and the flue gas damper to adjust the reheat steam temperature roughly and use the method of water spraying to reduce the temperature to achieve fine adjustment. As an emergency safety measure, the sprinkler valve should be kept as small as possible. At the same time, the variance of burner swing angle and flue gas damper opening must be limited to a certain range.

According to the requirements of reheat temperature control process, the mathematical model [25] of reheat steam temperature control system for 660 MW ultra-supercritical once-through boiler in a power plant is established:where are the control quantities of the system and are the output of the system. It should be noted that the model is established based on the input variance and output variance of reheat steam temperature control system. For example, in model (1), is the variance of the reheat steam temperature on the A side of reheater, rather than the actual reheat steam temperature. If the initial temperature of reheat steam is 580°C and the expected temperature is 590°C, then is the change of the initial temperature, that is, 10°C. Similarly, is the variance of reheat steam temperature on the B side of reheater, is the variance of the flue gas damper opening, is the variance of the burner swing angle, is the variance of the sprinkler valve opening on the A side of reheater, and is the variance of the sprinkler valve opening on the B side of reheater.

The transfer functions of burner swing angle-reheat steam temperature, flue gas damper-reheat steam temperature, and spray desuperheating-reheat steam temperature can be described by the mode of first-order inertia plus pure delay. The expression of the transfer functions is as follows:where is the gain, is the first-order inertia time, and is the delay time. The transfer function form of in model (1) is determined by (2).

3. Theoretical Analysis of Constrained Predictive Control [26]

The theoretical analysis of predictive control algorithm is usually based on the state space equation of the system model. Therefore, the transfer function model of the research object in this paper needs to be transformed into the state space model. The transformation method can be easily found in many data [27], so it is no longer detailed.

The state space incremental model of the linear discrete time system is considered as follows:where

In the model ((3a), (3b), and (3c)), is the state increment; is the increment of control input; is the increment of measurable external interference; is the controlled output; is the constrained output; is the system matrix of the corresponding dimension.

The control objective is to make the controlled output track the given reference input . At the same time, the control quantity, control increment, and output of the system satisfy the following control constraints and output constraints:

At time, the measured value of state is . According to the basic principle of predictive control, the optimization problem of constrained MPC is described as follows.

Question 1satisfies system dynamics and the following time-domain constraints ((8a), (8b), and (8c)): whereIn the above optimization problems, and are weighted matrices, and they are given as follows: is a reference sequence of control output, and it is given as is a sequence of control quantity. As an independent variable for constrained optimization problems, it is defined as is the p step control output based on model ((3a), (3b), and (3c)) prediction at time, and it is defined as

Specifically, the controlled output and constrained output of predictive control are calculated by equation ((7a), (7b), (7c), (7d), (7e), and (7f)), where (7b), (7d), and (7f) indicate that the measured states are the initial condition for predicting the future dynamics of the system. If the states are not all measurable, the estimated states are used as the initial conditions for predicting the future dynamics of the system.

can be calculated by the equation where

The constrained optimization problem is a quadratic programming (QP) problem, so we transform it into a QP description. The specific transformation process is detailed in [15].

The constraint MPC optimization Question 1 is converted into the following QP problem description:

The QP problem ((16a) and (16b)) has a solution to any weighting matrix , which is denoted as . Obviously, is a function that is related to the measured value , the control horizon , and the prediction horizon . According to the basic principle of predictive control, the first step of the obtained open-loop control sequence will be applied to the controlled system. At the next sampling time, the constrained optimization question 1, that is, QP problem ((16a) and (16b)), will be refreshed with the new measured value and solved again. Therefore, the closed-loop control law of constrained MPC is defined as

4. Performance Analysis of Reheat Steam Temperature Control System with Variable Load

4.1. Simulation Results

The transfer functions [25] of spray desuperheating (valve opening), reheat steam temperature, burner swing angle, reheat steam temperature and flue gas damper, and reheat steam temperature of a 660MW ultra-supercritical once-through boiler under 400MW, 500MW, and 600MW load are shown in Tables 1, 2, and 3.


Load

400MW
500MW
600MW


Load

400MW
500MW
600MW


Load

400MW
500MW
600MW

According to the mathematical model in Tables 1, 2 and 3, we simulate the control effect of reheat steam temperature system of boiler based on constraint predictive control algorithm when the loads of generator unit are 400MW, 500MW, and 600MW, respectively. The initial temperature of reheat steam is set to 580°C and the expected output temperature of reheat steam is set to 590°C; that is, the reference input is . The sampling period is 10 seconds. The prediction horizon is p=100, and the control horizon is m=3. The output error weighting matrix of quadratic performance index is ywt = , and control quantity weighting matrix of quadratic performance index is uwt = .

In order to make comparison and analysis, the constraints of are set to 0~8, 0~10, 0~12, and 0~15, respectively, where . Note that if we want to rise the reheat steam temperature, should be greater than or equal to 0 and should be close to or equal to 0. Therefore, the constraints of should start from 0. The unit of is %. The unit of is degree.

When the load of generator unit is 400MW, , the simulation results of reheat steam temperature control system are shown in Figures 2 and 3.

From Figures 2 and 3, we can see that the steady state values of are 13.94, 5.62, 0.26, and 0, respectively, and the time that is required for the input and output to reach the steady state is about 120 sampling periods, that is, 1200s. Similarly, we can obtain the steady state time of the and and the steady state values of under different loads and different input constraints, and they are shown in Tables 4, 5, 6, and 7. According to the data that is obtained from the simulation, we can analyze the control performance of the reheat steam temperature control system.


400MW500MW600MW

0.511.520.511.520.511.52
Steady-state time of 12010090859587858060555045
Steady-state time of 12010090859587858060555045
Steady-state value of 13.9413.212.6312.1212.6212.7812.6112.4410.6310.8910.5610.20
Steady-state value of 5.625.846.026.181.211.131.221.340.960.821.001.20
Steady-state value of 0.260.240.230.220.120.130.120.110.420.450.420.38
Steady-state value of 000000000000


400MW500MW600MW

0.511.520.511.520.511.52
Steady-state time of 1101009590105100989560555555
Steady-state time of 1101009590105100989560555555
Steady-state value of 11.1610.519.989.5511.1210.9410.7910.6810.109.819.409.05
Steady-state value of 6.486.676.846.972.002.092.172.231.261.421.651.85
Steady-state value of 0.190.180.170.160.030.020.0100.370.330.290.25
Steady-state value of 000000000000


400MW500MW600MW

0.511.520.511.520.511.52
Steady-state time of 115105100951101009590105959080
Steady-state time of 115105100951101009590105959080
Steady-state value of 9.258.658.188.059.739.599.469.359.098.718.338.03
Steady-state value of 7.067.257.397.432.782.872.923.011.822.042.252.42
Steady-state value of 0.150.130.120.1100000.260.220.180.14
Steady-state value of 00000.070.080.010.010000


400MW500MW600MW

0.511.520.511.520.511.52
Steady-state time of 1301301301301201051031001081009895
Steady-state time of 1301301301301201051031001081009895
Steady-state value of 7.577.577.577.577.917.817.747.677.677.467.347.23
Steady-state value of 7.587.587.587.583.853.903.953.992.622.742.812.87
Steady-state value of 0.110.110.110.1100000.100.080.070.06
Steady-state value of 00000.200.210.220.220000

Since the dynamic characteristics of reheat steam temperature control system are different during the change of generators load, that is, the model parameters of reheat steam temperature control system are changing with the change of generator load, so the models of reheat steam temperature control system under one or several loads can only provide the system input under the one or several loads at the site, and they cannot provide the basis for the field adjustment of the control system under other loads. Therefore, we need to analyze the input and output of the system based on the existing models under the three loads and get the regulation law of the control quantities, which can provide a theoretical basis for the actual field adjustment.

4.2. Analysis of Control Quantities of Reheat Steam Temperature Control System

From the steady-state values of Tables 4, 5, 6, and 7, we can see that and are relatively large, and they play major roles during the regulation of reheat steam temperature. and are close to 0, which means that the opening of the two sprinkler valves remains almost unchanged. It is consistent with the control requirement that spray desuperheating is not as the main regulating method during the regulation of reheat steam temperature.

Control quantities and do not play a major role during the control process of reheat steam temperature, so we mainly analyze and . Firstly, the change of is analyzed. From the Tables 47, it can be seen that when is equal and the constraint of control quantities is invariable, the three steady-state values of do not change much under the three loads. That is to say, when the reheat steam temperature rises from 580°C to 590°C and the load of generator unit is 400MW, the variance of flue gas damper opening is basically the same as that under 500MW and 600MW load. Besides, the smaller the constraint range of is, the closer the three steady-state values of are under the three loads. Thus, although the model parameters of reheat steam temperature control system change with the change of generator load, the adjustment of flue gas damper opening just has little change under different loads. Taking Table 7 as an example, when and , the three steady-state values of , which are 7.57, 7.91, and 7.67, respectively, are the closest under the three loads. The variation range of is between 7.57 and 7.91, and the change is not obvious. Therefore, under any other load, the control quantity can take the value from 7.57 to 7.91.

Next, we analyze the change of according to the Tables 47. It can be seen that when the is equal and the constraint of control quantities is invariable, changes greatly under the three loads. And the higher the generators’ load is, the smaller the is. Taking Table 5 as an example, when , under 400MW, 500MW, and 600MW load, the steady-state values of are 6.48, 2.00, and 1.26, respectively, which means if the reheat steam temperature rises from 580°C to 590°C, the swing angle of the burner needs to be increased by 6.48 under 400 MW load, while the opening of burner swing angle needs to be increased by 2.00 and 1.26, respectively, under 500MW and 600MW loads. It shows that, in the process of regulating the reheat steam temperature control system, with the increase of the load of the generator unit, the adjusting range of burner swing angles should be gradually reduced. Therefore, in the actual field adjustment, the higher the generator load is, the smaller the adjustment range of the burner swing angles should be, so as to avoid damaging thermal equipment caused by excessive reheat steam temperature.

The correctness of the above analysis can also be verified by Simulink simulation. Taking Table 6 as an example, under different loads, we take the steady-state value of , respectively, at , as the system input and set the increment of to 4 in the Simulink simulation. In this way, we can learn the effect of reheat steam temperature when the adjusting range of burner swing angles is too large. The simulation results are shown in Figures 4, 5, and 6.

From Figure 4, we can see that when the load of the generator unit is 400MW and the increment of is 4, that is, , the reheat steam temperature rises by about 14°C. It is 4°C higher than the desired output, but it still meets the maximum deviation of system output, which is 5°C. When the load of the generator unit is 500MW, we can see that the reheat steam temperature rises by about 14.8°C from Figure 5, and it is approaching the maximum deviation of output. From Figure 6, we can see that the reheat steam temperature rises by about 15.4°C under 600MW load, and it has exceeded the maximum deviation of system output. Thus, in order to ensure the safety of the thermal equipment, the higher the load of the generator unit is, the smaller the adjustment range of the burner swing angles should be.

4.3. Analysis of the Constraint Range of Control Quantities

In this paper, the control quantities are the variance of system input. Taking the as an example, it is not the actual opening of the flue gas damper, but it is the opening variance of the flue gas damper. If the original opening of the flue gas damper is 50 and , then the actual opening of the flue gas damper is 60. In the actual process, the opening of the control quantities has a maximum value, so it is necessary to restrict the range of control quantities of the system to ensure that the control quantities do not exceed their maximum value. Next, we analyze the constraints of the control quantities and give an appropriate constraint range for reference during field adjustment of reheat temperature control system.

Firstly, the constraint range of the control quantities should not be too small; otherwise the reheat steam temperature cannot reach the desired temperature. Figures 7 and 8 are the simulation results of input and output of the reheat steam temperature system when the generator load is 400MW, . The initial temperature of reheat steam is 580°C and the desired temperature is 590°C.

It can be easily seen from Figure 7 that when is limited to 0~, the steady state values of the reheat steam temperature are about 588.0 and 587.9, which do not reach the desired temperature. From Figure 8, we can be seen that the steady-state values of have reached the maximum value of input constraint range, which is 6, and the steady-state values of have almost reached the minimum value of input constraint range, which is 0. This shows that in the reheat steam temperature control system, if the constraint range of the control quantities is too small, even if reach the upper bound of the constraint range and the is close to lower bound, the final reheat steam temperature cannot reach the desired temperature. Therefore, there must be a minimum upper bound for the constraint range of the control quantities. Next, we try to find out the minimum upper bound of the constraint range of the control quantities under 400MW, 500MW, and 600MW loads, respectively, by simulation.

When the load of the generator unit is 400MW and , the input and output of the system are shown in Figures 9 and 10. From Figure 10, we can see that the steady-state values of have reached the upper bound of input constraint range, which is 7.5, and the steady-state values of are 0.03 and 0, respectively, which have almost reached the lower bound of input constraint range. As can be seen from Figure 9, the steady-state values of are 590 and 589.9, respectively, which reach the desired temperature basically. It can be considered that the minimum upper bound of input constraint is about 7.5 under 400MW load. Similarly, we can get the minimum upper bound of input constraint under 500MW and 600MW loads, which are about 5.3 and 4.5, respectively. From the minimum upper bound of the input constraint range under the three loads, we can see that the higher the generator load is, the smaller the minimum upper bound of the input constraint range is. This also shows that, in the actual operation process, with the increase of the generator load, the adjusting range of system inputs should be gradually reduced.

Next, we also make a simple analysis of the maximum upper limit of input constraint range. We can observe the change of system input by simulation when the constraint range of system inputs is too large. When the load of generator unit is 400MW, , the variation curve of input and output of the system is shown in Figures 11 and 12. From the two figures, we can see that although the system output can reach the desired value, the steady-state value of has reached 29.0, which means that if the initial opening of is greater than 71, the final value of has exceeded the maximum opening it can reach. This is obviously unreasonable. Therefore, the upper limit value of the control quantities constraint range should not be too large; otherwise it may exceed the maximum range of the control quantities opening. What is the maximum upper bound of the control quantities constraint range? If we want to get an exact value, we need a huge amount of data. Since our existing data is limited, we can only analyze it based on the existing data and get a rough analysis result. Compared with the steady-state value of in other constraint ranges, when the constraint range of system inputs is 0~, the steady-state value of has the largest fluctuation. Therefore, in the existing data, we can roughly consider that the maximum upper bound value of the constraint range of the control quantities is 15.

From the analysis of Section 4.3 of the control quantities of reheat steam temperature control system, we can learn that, with the increase of the load of the generator unit, the adjusting range of burner swing angles should be gradually reduced, and large adjustment of the control quantities may cause reheat steam temperature being too high and the equipment is damaged, which means that, under different loads, the smaller the fluctuation of is, the better the stability and robustness of the system are. By observing and analyzing the data in Tables 47, we can see that when the constraint range of is 0~ and , the fluctuation of steady-state values of is the smallest under different loads compared with that in other constraint ranges. In order to provide reference values of and input constraint for adjustment of reheat steam temperature system in power plant, the most appropriate input values and input constraint in the existing data are given in Table 8.


, =2400MW500MW600MW

7.577.677.23
7.583.992.87
0.1100.06
00.220

5. Conclusions

Aiming at the problem of reheat steam temperature control, the reheat steam temperature control system of 660MW thermal power generator unit is studied based on the constrained predictive control algorithm in this paper. Under the condition of input constraint, steady state value of control quantities and the time that system reaches steady state in different constraint ranges are listed in tabular form. By analyzing the data in the tables, the reference values of system input and input constraint are given. These data and analysis provide reference for field adjustment of reheat steam temperature system in power plant.

Data Availability

The experimental data used to support the findings of this study are included within the article.

Conflicts of Interest

The authors declare that there are no conflicts of interest regarding the publication of this paper.

Acknowledgments

This work is supported in part by the National Natural Science Foundation of China under Grants 61873006, 61473034, and 61673053 and in part by the National Key Research and Development Projects 2018YFC1602704 and 2018YFB1702704 and Beijing Major Science and Technology Special Projects under Grant No. Z181100003118012.

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Copyright © 2019 Xiaoli Li et al. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.


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