CN216281315U - Main steam temperature optimization control device of double-slag-chamber coal-fired unit - Google Patents
Main steam temperature optimization control device of double-slag-chamber coal-fired unit Download PDFInfo
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Abstract
The utility model provides a main steam temperature optimization control device of a double slag chamber coal-fired unit. The utility model comprises a steam-water separator, a superheater, a program control simulator, a desuperheater, a main regulator, an auxiliary regulator, a desuperheating water valve, an actuator, a transmitter and the like. A dynamic correction feedforward is introduced through the relevant logic operation of a program control simulator, various disturbance variable feedforward is controlled, the dynamic correction feedforward is combined with an amplitude limiting module, a smoothing module and the like, parameters such as a boiler main control instruction, a slag chamber operation condition and the like are brought into the dynamic feedforward, an optimal feedforward value is obtained through calculation, and the main controller and the auxiliary controller are controlled and adjusted, so that the optimal control is realized. After the device is adopted, the fluctuation range of the steam temperature can be reduced, the adjusting quality is improved, the working strength of operators is reduced, the economical efficiency of unit operation is improved, and the stable control of the main steam temperature is realized.
Description
Technical Field
The utility model relates to the field of temperature control of coal-fired units, in particular to a main steam temperature optimization control device of a double-slag-chamber coal-fired unit.
Background
With the rapid development of economy, the environmental pollution problem is increasingly serious, and the requirements for energy conservation and consumption reduction are increasingly strong. In the development of the power industry, along with the continuous construction of a large-capacity thermal generator set, the improvement of the operation efficiency and the thermal economy of the generator set is very urgent. Today, computer technology is rapidly developing, and many advanced control technologies and methods are applied to various controls of boilers.
The main steam temperature adjusting process of the boiler in the thermal power plant is a typical large-delay control process, a heated object is a multi-volume and large-inertia system, a controlled system has serious nonlinearity and time-varying characteristics, and disturbance factors influencing the main steam temperature are many, such as unit load, a combustion state and the like, so that the steam temperature adjusting is difficult. The existing boiler steam temperature control device has the advantages that the number of devices is large, temperature control and pressure control are mainly adjusted manually, the operation process is complicated, the energy consumption is large, the labor intensity of operators is high, the fluctuation range of steam pressure borne by a boiler is large, the pressure bearing capacity of the device design is easily exceeded, the phenomenon of gas leakage of the boiler is easily caused, the maintenance difficulty is large, the period is long, and the failure rate of the device is high.
In order to ensure that the automatic control of the main steam temperature can be safely and stably put into operation for a long time under complex working conditions and solve the problems of large lag and nonlinearity of the main steam temperature control, automatic debugging workers at home and abroad introduce various control methods into the main steam temperature control in field practice, and stable and reliable field application or simulation experiments are implemented. In recent years, researchers have proposed a composite control method based on a genetic algorithm and a neural network, such as PID control, fuzzy adaptive prediction function control, state variable prediction control and the like, and the composite control method is used for field control of main steam temperature of a thermal power generating unit and obtains a good control effect. The researches have good promotion effect on exploring the main steam temperature control method under the complex working condition, but the defects of complex structure, various parameter setting rules and the like exist, so that the main steam temperature control method is difficult to be supported on the aspect of effective software and hardware in actual application, and the field actual application is difficult to popularize.
SUMMERY OF THE UTILITY MODEL
According to the technical problem provided by the utility model, the main steam temperature optimization control device of the double slag chamber coal-fired unit is provided. The utility model can reduce the working intensity of field operators, improve the economical efficiency of unit operation and ensure that the system has stronger stability. The technical means adopted by the utility model are as follows:
a main steam temperature optimization control device of a double slag chamber coal-fired unit comprises a steam-water separator, a main superheater, an auxiliary superheater, a program control simulator, a desuperheater, a main regulator, an auxiliary regulator, a desuperheating water valve, an actuator, a main temperature transmitter and an auxiliary temperature transmitter; the steam-water separator is connected with one end of an auxiliary superheater, the other end of the auxiliary superheater is connected with a desuperheater, the other end of the desuperheater is simultaneously connected with a desuperheater water valve, an auxiliary temperature transmitter and a main superheater, wherein the main temperature is the temperature of main steam, the auxiliary temperature is the temperature of the desuperheater water outlet, the auxiliary temperature transmitter, an auxiliary regulator, an actuator, a desuperheater water valve and the desuperheater form an inner loop, the main temperature transmitter, the main regulator, a program simulation controller and the whole inner loop jointly form an outer loop, the input end of the main temperature transmitter is connected with the main superheater, the output end of the main regulator is connected with the auxiliary regulator, the program control simulator is used for adjusting the main regulator and the auxiliary regulator based on collected dynamic feedforward data, and the inner loop is used for adjusting the main regulator and the auxiliary regulator when the temperature of the desuperheater water is disturbed or the temperature of the desuperheater changes to cause the change of the steam guide temperature, and (3) adjusting the system in time, specifically, taking the output of the main regulator as the input of the auxiliary regulator, and directly acting the output of the auxiliary regulator on the temperature-reducing water valve to control the opening degree of the temperature-reducing water valve so as to realize the adjustment of the flow of the temperature-reducing water.
Further, a secondary superheater is arranged between the steam-water separator and the desuperheater.
Further, the program simulation controller comprises a first dynamic feedforward device, a second dynamic feedforward device, a third dynamic feedforward device, a fourth dynamic feedforward device and an adder, the first dynamic feedforward device, the second dynamic feedforward device, the third dynamic feedforward device, the fourth dynamic feedforward device and the adder are connected in series in sequence, and the first dynamic feedforward device is used for adding the following two calculation results: the first part is a deviation value of the actual temperature of the outlet of the superheater and the set temperature and is multiplied by a numerical value of a corresponding coefficient, and the second part is a difference value of the actual temperature of the outlet of the desuperheater and the theoretical temperature of the outlet of the desuperheater and is multiplied by a corresponding coefficient; the second dynamic feedforward device is used for acquiring the numerical value of the outlet temperature of the final desuperheater, and multiplying the numerical value by a corresponding coefficient after differential operation; the third dynamic feedforward device is used for collecting a numerical value obtained by the boiler main control instruction through corresponding function calculation; and the fourth dynamic feedforward device is used for acquiring a temperature setting deviation value when the boiler is switched from single slag chamber operation to double slag chamber operation.
The steam temperature control device is simple in structure and arrangement and reasonable in layout, fluctuation range of steam temperature can be reduced, adjustment quality is improved, working strength of operators is reduced, economy of unit operation is improved, and stable control of main steam temperature is achieved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a main steam temperature optimization control device of a double slag chamber coal-fired unit.
FIG. 2 is a flow chart of the dynamic feedforward calculation of the program control simulator according to the present invention.
In the figure: 1. a steam-water separator; 2. a secondary superheater; 3. a desuperheater; 4. a temperature-reducing water valve; 5. a secondary temperature transmitter; 6. a primary superheater; 7. a primary temperature transmitter; 8. a main regulator; 9. a secondary regulator; 10. an actuator; 11. and controlling the simulator by a program.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
As shown in fig. 1, the embodiment of the utility model discloses a main steam temperature optimization control device of a double slag chamber coal-fired unit, which comprises a steam-water separator, a main superheater, an auxiliary superheater, a program control simulator, a desuperheater, a main regulator, an auxiliary regulator, a desuperheating water valve, an actuator, a main temperature transmitter and an auxiliary temperature transmitter; the steam-water separator 1 contains a large amount of steam in the boiler; the steam-water separator 1 is connected with one end of an auxiliary superheater 2 in an outlet connection mode, the other end of the auxiliary superheater 2 is connected with a desuperheater 3, the other end of the desuperheater 3 is simultaneously connected with a desuperheater water valve 4, an auxiliary temperature transmitter 5 and a main superheater 6, the main temperature is the main steam temperature, the auxiliary temperature is the desuperheater water outlet temperature, the auxiliary temperature transmitter is a desuperheater outlet steam temperature transmitter, the main temperature control transmitter 7 is a superheater outlet temperature transmitter, the auxiliary temperature transmitter 5, an auxiliary regulator 9, an actuator 10, the desuperheater water valve 4 and the desuperheater 3 form an inner loop, the main temperature transmitter 7, a main regulator 8, a program simulation controller 11 and the whole inner loop form an outer loop together, the input end of the main temperature transmitter is connected with the main superheater, the output end of the main regulator is connected with the auxiliary regulator, and a dynamic correction feedforward is introduced by using a program control simulator, the feedforward of various disturbance variables is controlled, and is combined with an amplitude limiting module, a smoothing module and the like, parameters such as a boiler main control instruction, a slag chamber operation condition and the like are brought into dynamic feedforward, an optimal feedforward value is obtained through calculation, and the main controller and the auxiliary controller are controlled and adjusted, so that optimal control is realized. The inner loop is equivalent to a single-loop control system which is formed by taking the output of the main controller as a given value, taking the temperature of the leading steam as an adjusted quantity and taking the desuperheater as a control object. Since the control object lag and inertia of this system are small, its control process is stable. When the temperature of the desuperheating water is disturbed or the temperature after the desuperheater is changed to cause the change of the leading steam temperature, the system can be adjusted in time, and the disturbance, particularly the influence of the disturbance of the desuperheating water on the superheated steam temperature, can be quickly and stably reduced; the outer circuit is a low speed circuit with respect to the inner circuit, the main task of which is to maintain the main steam temperature equal to the setpoint value. Specifically, the output of the main regulator is used as the input of the auxiliary regulator, and the output of the auxiliary regulator is directly applied to the temperature-reducing water valve to control the opening degree of the temperature-reducing water valve, so that the adjustment of the flow of the temperature-reducing water is realized.
In a preferred embodiment, a secondary superheater 2 is arranged between the steam-water separator and the desuperheater.
The program simulation controller comprises a first dynamic feedforward device, a second dynamic feedforward device, a third dynamic feedforward device, a fourth dynamic feedforward device and an adder, wherein the first dynamic feedforward device, the second dynamic feedforward device, the third dynamic feedforward device, the fourth dynamic feedforward device and the adder are sequentially connected in series, and the first dynamic feedforward device is used for adding the following two calculation results: the first part is a deviation value of the actual temperature of the outlet of the superheater and the set temperature and is multiplied by a numerical value of a corresponding coefficient, and the second part is a difference value of the actual temperature of the outlet of the desuperheater and the theoretical temperature of the outlet of the desuperheater and is multiplied by a numerical value of a corresponding coefficient; the second dynamic feedforward device is used for acquiring the numerical value of the outlet temperature of the final desuperheater, and multiplying the numerical value by a corresponding coefficient after differential operation; the third dynamic feedforward device is used for collecting a numerical value obtained by the boiler main control instruction through corresponding function calculation; and the fourth dynamic feedforward device is used for acquiring a temperature setting deviation value when the boiler is switched from single slag chamber operation to double slag chamber operation.
Specifically, as shown in fig. 2, a cascade control strategy with main steam temperature as a main regulation and desuperheating water outlet temperature as a secondary regulation is adopted, and temperature prediction logic, differentiation of outlet temperature of a final desuperheater, a boiler main control instruction and double slag chamber temperature compensation are introduced to serve as dynamic feedforward of a main regulator. The temperature of the main steam has complex dynamic and strong coupling characteristics. Conventional PID control focuses only on the relationship between individual input and output variables in the control loop and cannot compensate for the relationship between strongly or less strongly coupled input and output variables. In actual operation, the temperature of the outlet steam is influenced by the desuperheater in the desuperheater, specific combustion conditions and operation conditions. Therefore, temperature prediction logic, differentiation of the final desuperheater outlet temperature, boiler main control commands and dual slag chamber temperature compensation are introduced as dynamic feed-forward of the main regulator.
The method specifically comprises the following steps:
step 1, introducing a temperature prediction logic, wherein the temperature prediction logic comprises two parts: the first part is a deviation value of the actual temperature of the outlet of the superheater and the set temperature, and is multiplied by a corresponding coefficient; the second part is the difference between the actual temperature at the outlet of the desuperheater and the theoretical temperature at the outlet of the desuperheater, and the difference is multiplied by a corresponding coefficient. (the theoretical temperature of the outlet of the desuperheater is calculated by a corresponding function of the unit load). The calculation results of the two parts are added and pass through a certain hysteresis logic, and are multiplied by corresponding coefficients to form temperature prediction dynamic feedforward, which is the dynamic feedforward of the first part.
And 2, obtaining the dynamic feedforward of the second part after differential operation and limit value of the outlet temperature of the final-stage desuperheater.
And 3, the main control instruction of the boiler is subjected to corresponding functions and multiplied by corresponding coefficients, and finally, the dynamic feedforward of the third part is obtained through calculation after the limit value is carried out, namely different dynamic feedforward is set under different loads.
And 4, experiments prove that when the operation of the boiler is switched from the single slag chamber operation to the double slag chamber operation, the temperature of main steam can generate certain fluctuation and rise, so that the working condition of the double slag chamber operation is introduced into dynamic feedforward, namely when the single slag chamber is switched to the double slag chamber operation, the dynamic feedforward is correspondingly improved, the output of a main loop is increased, and the rear temperature set value of the desuperheater is properly increased to prevent overtemperature. And setting the temperature deviation value of the single/double slag chambers to be 30 ℃, passing through the smoothing module, multiplying the temperature deviation value by a corresponding coefficient, and finally obtaining the dynamic feedforward of the fourth part after the temperature deviation value passes through a limit value.
And 5, summing the dynamic feedforward of the four parts to obtain the dynamic feedforward of the main regulator, wherein the dynamic feedforward range is within (-35, 35).
And 6, taking the output of the main regulator as the input of the auxiliary regulator, directly acting the output of the auxiliary regulator on the actuator, controlling the opening of the temperature-reducing water valve, and realizing the regulation of the temperature-reducing water flow, so that the temperature of the regulated main steam reaches a set value curve along a reference track, thereby realizing the optimal control.
When the program control simulator 11 detects that the temperature of the current steam is lower than the current preset value, internal operation logic is started, a dynamic feedforward process is started, the auxiliary regulator 9, the main regulator 8 and the actuator 10 are started, the current steam is heated by reducing the opening degree of the temperature reduction water valve, and when the temperature of the current steam is higher than the current preset value, the current steam is cooled by increasing the opening degree of the temperature reduction water valve, so that the purpose of controlling the temperature of the expected set boiler main steam is achieved.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the utility model has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (3)
1. A double slag chamber coal-fired unit main steam temperature optimization control device is characterized by comprising a steam-water separator, a main superheater, an auxiliary superheater, a program control simulator, a desuperheater, a main regulator, an auxiliary regulator, a desuperheating water valve, an actuator, a main temperature transmitter and an auxiliary temperature transmitter; the steam-water separator is connected with one end of an auxiliary superheater, the other end of the auxiliary superheater is connected with a desuperheater, the other end of the desuperheater is simultaneously connected with a desuperheater water valve, an auxiliary temperature transmitter and a main superheater, wherein the main temperature is the temperature of main steam, the auxiliary temperature is the temperature of the desuperheater water outlet, the auxiliary temperature transmitter, an auxiliary regulator, an actuator, a desuperheater water valve and the desuperheater form an inner loop, the main temperature transmitter, the main regulator, a program simulation controller and the whole inner loop jointly form an outer loop, the input end of the main temperature transmitter is connected with the main superheater, the output end of the main regulator is connected with the auxiliary regulator, the program control simulator is used for adjusting the main regulator and the auxiliary regulator based on collected dynamic feedforward data, and the inner loop is used for adjusting the main regulator and the auxiliary regulator when the temperature of the desuperheater water is disturbed or the temperature of the desuperheater changes to cause the change of the steam guide temperature, and (3) adjusting the system in time, specifically, taking the output of the main regulator as the input of the auxiliary regulator, and directly acting the output of the auxiliary regulator on the temperature-reducing water valve to control the opening degree of the temperature-reducing water valve so as to realize the adjustment of the flow of the temperature-reducing water.
2. The main steam temperature optimization control device of the double slag chamber coal-fired unit according to claim 1, characterized in that a secondary superheater is arranged between the steam-water separator and the desuperheater.
3. The main steam temperature optimization control device of the double slag chamber coal-fired unit according to claim 1, wherein the program simulation controller comprises a first dynamic feedforward device, a second dynamic feedforward device, a third dynamic feedforward device, a fourth dynamic feedforward device and an adder, the first dynamic feedforward device, the second dynamic feedforward device, the third dynamic feedforward device, the fourth dynamic feedforward device and the adder are connected in series in sequence, and the first dynamic feedforward device is used for adding the following two calculation results: the first part is a deviation value of the actual temperature of the outlet of the superheater and the set temperature and is multiplied by a numerical value of a corresponding coefficient, and the second part is a difference value of the actual temperature of the outlet of the desuperheater and the theoretical temperature of the outlet of the desuperheater and is multiplied by a numerical value of a corresponding coefficient; the second dynamic feedforward device is used for acquiring the numerical value of the outlet temperature of the final desuperheater, and multiplying the numerical value by a corresponding coefficient after differential operation; the third dynamic feedforward device is used for collecting a numerical value obtained by the boiler main control instruction through corresponding function calculation; and the fourth dynamic feedforward device is used for acquiring a temperature setting deviation value when the boiler is switched from single slag chamber operation to double slag chamber operation.
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| CN117212770A (en) * | 2023-08-17 | 2023-12-12 | 华电电力科学研究院有限公司 | Combustion intensity identification method and system based on superheater energy storage condition prediction |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117212770A (en) * | 2023-08-17 | 2023-12-12 | 华电电力科学研究院有限公司 | Combustion intensity identification method and system based on superheater energy storage condition prediction |
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