CN113531510B - Power station boiler main steam temperature control method - Google Patents
Power station boiler main steam temperature control method Download PDFInfo
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- CN113531510B CN113531510B CN202110679256.XA CN202110679256A CN113531510B CN 113531510 B CN113531510 B CN 113531510B CN 202110679256 A CN202110679256 A CN 202110679256A CN 113531510 B CN113531510 B CN 113531510B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/28—Methods of steam generation characterised by form of heating method in boilers heated electrically
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Abstract
The invention discloses a method for controlling the temperature of main steam of a power station boiler. According to the invention, two independent temperature control systems of the outlet temperature of the secondary superheater and the outlet temperature of the tertiary superheater are respectively designed based on the obtained model, and the temperature difference of the temperature set values of the two temperature control systems is in direct proportion to the unit operation load. In the design of the temperature controller, the tracking performance and the anti-interference performance of respective systems are considered, and the corresponding tracking controller and the anti-interference controller are respectively designed, so that the tracking performance and the anti-interference performance can be respectively and independently adjusted, and the mutual interference of the two performances is avoided. Compared with the traditional single-loop control and cascade control method, the method has better tracking performance and anti-interference performance, can realize quick response to the temperature requirement of the main steam in the load lifting process, can reduce the fluctuation of the temperature, and improves the operation safety and the power generation efficiency of the steam turbine.
Description
Technical Field
The invention belongs to the field of thermal power engineering and automatic control, and particularly relates to a temperature control method for main steam of a power station boiler.
Background
The main steam temperature of the utility boiler is one of important parameters for safe and economic operation of a unit, and if the steam temperature is too high, a superheater is easily burnt out and a steam inlet part of a steam turbine is easily damaged; too low a steam temperature not only affects the economics but also causes excessive steam humidity in the un-staged steam turbine and damage to the blades. Therefore, in order to ensure the safety and the economical efficiency of the operation of the power station unit, the main steam temperature is required to be strictly controlled within a specified range. However, the main steam temperature is affected by many disturbance factors such as coal supply amount, air guiding amount, temperature reduction water temperature and the like, so that temperature fluctuation in actual operation is large. On the other hand, the inertia and the lag of the temperature-reducing water control loop are large, so that the conventional control methods, such as single-loop PID control, cascade-feedforward and other control strategies, are difficult to obtain good tracking performance and interference resistance, and the control quality is difficult to ensure. In practice, the main steam temperature tends to fluctuate widely during system load adjustment, and for some plants the steam temperature deviates from the setpoint by more than 10 ℃ when the unit load is only changed at a rate of 2% MCR/min. At this time, the steam temperature is often controlled through manual operation, and even experienced operators can only reduce the set value of the steam temperature to operate, so that the economy of the unit is reduced, and the labor intensity of the operators is increased.
Disclosure of Invention
The invention provides a power station boiler main steam temperature control method aiming at the defects of traditional single-loop and cascade control strategies and the like, and the method is used for improving the stability of main steam temperature. Two independent control systems are adopted to respectively and independently control the outlet temperature of the secondary superheater and the outlet temperature of the tertiary superheater, and the temperature difference of temperature set values of the two temperature control systems is in direct proportion to the unit operating load; each temperature control system adopts a double-controller structure, the tracking performance and the anti-interference performance of the system are fully considered, and the corresponding tracking controller and the anti-interference controller are respectively designed, so that the tracking temperature setting performance and the disturbance suppression performance of the main steam temperature control system are enhanced.
The invention specifically comprises the following steps:
step 1: establishing a transfer function model of a water spraying temperature reduction process:
obtaining mathematical models of a three-stage water spraying temperature reduction process and a two-stage water spraying temperature reduction process by a system identification method:
wherein s is a laplace operator; t is a unit of 11 、T 12 、T 21 And T 22 Is the inertia time constant; k 1 And K 2 Respectively, a steady state gain coefficient; y is 2 The temperature of steam at the outlet of the secondary superheater; y is 1 Is the outlet steam temperature u of the three-stage superheater 1 And u 2 The opening degrees of a secondary water spray valve and a primary water spray valve are respectively set; l is 1 And L 2 Respectively the pure lag time of the two controlled processes. The parameters in the two models can be obtained by system identification.
And 2, step: two temperature control systems are respectively designed by adopting a double-control structure:
respectively designing two models based on the model established in the step 1The temperature controllers TC1 and TC2 adopt two controllers to form a temperature control system, and simultaneously realize independent control on tracking performance and interference resistance performance; the temperature controller TC1 includes a first tracking controller C 11 And a first disturbance rejection controller C 12 Respectively responsible for the control of the tracking performance of the system and the adjustment of the anti-interference performance; the temperature controller TC2 and the temperature controller TC1 adopt the same structure and comprise a second tracking controller C 21 And a second disturbance rejection controller C 22 ；C 11 、C 12 、C 21 And C 22 PID controllers with incomplete differential form are adopted:
wherein C is ij (s) is the controller, subscript i =1,2,j =1,2.
In order to obtain good control performance, the parameters of the controller need to be set; in the temperature controller TC1, a first tracking controller C 11 The setting formula of (1) is as follows:
wherein the controller parameter K p1 、T i1 、T d1 And T f1 Proportional, integral, derivative and filter coefficients of the first tracking controller are respectively; parameter λ in the above formula 1 Is selected in the range of 0 < lambda 1 ＜min(T 11 ,T 12 ) The larger the numerical value is, the slower the tracking performance of the system is, and the smaller the numerical value is, the faster the tracking speed is, and the determination is carried out according to the working range of the actual temperature-reducing water valve.
First disturbance rejection controller C 12 The setting formula of (1) is as follows:
wherein the controller parameter K p2 、T i2 、T d2 And T f2 Proportional, integral, differential and of the first immunity controller, respectivelyA filter coefficient; parameter β in the above formula 1 Is selected in the range of 0 < beta 1 ＜min(T 11 ,T 12 ) The larger the numerical value is, the poorer the anti-interference performance of the system is, but the better the stability is; the smaller the value, the better the noise immunity, but the worse the stability; determining according to the working range of a temperature reduction water valve of an actual system;
the temperature controller T adopts the same model and controller type c2 Two controllers C in 21 And C 22 The same setting formula is also adopted for parameter setting;
and 3, step 3: calculating the set temperature r of the secondary superheater outlet temperature control system 2 ：
Setting of outlet temperature of tertiary superheater as r 1 The set temperature of the outlet of the secondary superheater changes along with the change of the load size, and is automatically calculated in proportion according to the current load size; suppose the temperature of the superheated steam is set to r 1 Setting of the outlet temperature of the secondary superheater to r 2 Temperature difference Δ r = r between them 1 -r 2 The specific temperature difference is in direct proportion to the actual load setting; the specific calculation formula is as follows:
wherein M is c For the desired value of the current operating load, M t Is the full load number;
and 4, step 4: calculating the control quantity of each controller:
the method includes the steps of calculating internal model prediction output
Wherein
And &>
Respectively the current value and the previous value of the predicted output value of the internal modelThe value of the time and the value of the last time, parameter alpha 1 、α 2 And alpha 3 The calculation formula of (c) is as follows:
wherein T is s For the control period, k in the subscript stands for the sampling instant, T 11 And T 12 Is a model parameter; in the calculation of
Then, according to the temperature set value r 1 Determining a first tracking controller C 11 Input e of 11 ：/>
A first tracking controller C is calculated 11 Control amount u of 11 ：
u 11,k ＝u 11,k-1 +q 0 e 11,k +q 1 e 11,k-1 +q 2 e 11,k-2 +q 3 Δu d11,k-1 ；
Wherein u is 11,k Denotes the first tracking controller C 11 The numerical expression of the subscript of the control quantity at the time k represents the corresponding controller; e.g. of the type 11,k 、e 11,k-1 And e 11,k-2 Respectively representing the current time error, the last time error and the last time error; u. of d11 For auxiliary differential variables, initial value u d11,0 0 is selected; in the above formula,. DELTA.u d11,k-1 ＝u d11,k-1 -u d11,k-2 Outputting increments for internal differential terms, internal intermediate variables q 0 ～q 3 The calculation method of (c) is as follows:
thirdly, calculating a first anti-interference controller C 12 Control action u of 12 ：
Due to the fact that
To obtain a deviation e 12 The calculation result of (2): />
Due to the controller C 11 And C 12 All adopt the same structure, the calculation mode is consistent, u 12 Reference u to the calculation process of 11 (ii) a The difference between the two is the initial values of the input offset, the controller parameters and the internal variables;
fourth, calculate second tracking controller C 21 And a second disturbance rejection controller C 22 Control amount u of 21 And u 22 ：
Second tracking controller C 21 And a second disturbance rejection controller C 22 The structure and calculation mode of (A) are the same as those of (C) 11 And C 12 The consistency is achieved; in determining four parameters K of each PID controller respectively p 、T i 、T d And T f After that, the corresponding coefficient q 0 ～q 3 Will also be uniquely determined;
fifthly, calculating the control quantities u of the two-stage controllers TC1 and TC2 respectively 1 And u 2 ：
In respectively calculating four controllers C 11 、C 12 、C 21 And C 22 After the control action of (c), the control actions u of the temperature controllers TC1 and TC2 can be calculated as follows 1 And u 2 ：
Wherein u 11,k 、u 12,k 、u 21,k And u 22,k Are respectively a controller C 11 、C 12 、C 21 And C 22 The control function of (1); calculating a control action u 1 And u 2 Then the temperature-reducing valve can directly act on a field temperature-reducing valve to implement control; and repeating the steps 3-4.
The invention has the outstanding advantages that the influence of various disturbances on the main steam temperature on the site can be effectively overcome, the fluctuation of the main steam temperature is reduced, and the safety and the economical efficiency of the system operation are further improved.
Drawings
FIG. 1 is a flow chart of a water spray desuperheating process;
FIG. 2 is a block diagram of a superheated steam temperature control system;
FIG. 3 is a diagram of a control system for a two-stage water spraying desuperheating process;
FIG. 4 is a diagram of a primary spray desuperheating process control system.
Detailed Description
A method for controlling the temperature of main steam of a power station boiler specifically comprises the following steps:
step 1: establishing a transfer function model of a water spraying temperature reduction process:
the technological process of the water spraying and temperature reducing process of the power station boiler is shown in figure 1, and low-temperature steam is changed into high-temperature steam for a steam turbine to apply work through a three-stage overheating link. In order to ensure the safety and the operation efficiency of the steam turbine, the steam entering the steam turbine is required to reach a set temperature. If the steam temperature exceeds the expected temperature, the temperature is reduced by spraying water through a primary water spraying valve and a secondary water spraying valve. Physical characteristics of the water spraying and temperature reducing process: the following second order inertia plus hysteresis transfer function model is used to describe the two water spray attemperation processes:
wherein s is a laplace operator; t is a unit of 11 、T 12 、T 21 And T 22 Is the inertia time constant; k 1 And K 2 Respectively, a steady state gain coefficient; y is 2 The temperature of steam at the outlet of the secondary superheater; y is 1 The temperature of steam at the outlet of the tertiary superheater; u. of 1 And u 2 Respectively spraying water in two stagesThe opening degree of the valve and the primary water spray valve; l is 1 And L 2 Respectively the pure lag time of the two controlled processes. The parameters in the two models can be obtained by a conventional system identification method.
Step 2.1: designing a three-level superheater outlet temperature control system:
after the transfer function models (1) and (2) are obtained, controllers are respectively designed for the two loops, a superheated steam temperature control system with a process point is shown in fig. 2, and the whole control system comprises a TC1 and TC2 two-stage control system and respectively realizes control of outlet temperatures of a secondary superheater and a tertiary superheater.
Design of a control system TC1 of outlet temperature of the tertiary superheater: the temperature control system mainly realizes the control of the outlet temperature of the third-level superheater through a second-level water spray valve. A transfer function model (1) of the secondary water spray valve to the outlet temperature of the tertiary superheater is obtained in step 1, and controller design is carried out based on the model (1). Considering that the stability and rationality of the outlet temperature of the tertiary superheater have important influence on the safety and economy of system operation, the tracking performance and the anti-interference performance of the system are fully considered in the design process, and the main steam temperature can still be relatively stable under the condition that the load, the combustion, the wind and smoke system and the like are changed. Due to the traditional single-loop controller, such as PID control, it is difficult to achieve both tracking performance and noise immunity.
As shown in fig. 3, two controllers are used to form a temperature control system in this example, and independent control of tracking performance and noise immunity is achieved. Wherein the first tracking controller C 11 In charge of the control of the tracking performance of the system, a PID controller with an incomplete differential form is selected in the embodiment:
wherein the controller parameter K p1 、T i1 、T d1 And T f1 Respectively setting the proportional, integral, differential and filter coefficients of the first tracking controller according to the following formulas:
parameter λ in equation (4) 1 Selecting parameters for users, wherein the selection range is 0 < lambda 1 ＜min(T 11 ,T 12 ) The tracking performance of the system is slower when the numerical value is larger, the tracking speed is higher when the numerical value is smaller, and the determination is carried out according to the working range of the actual temperature-reducing water valve.
First disturbance rejection controller C 12 In charge of improving the noise immunity of the system, the PID controller with incomplete differential form is selected in the embodiment:
wherein the controller parameter K p2 、T i2 、T d2 And T f2 Respectively setting the proportional, integral, differential and filter coefficients of the first anti-interference controller according to the following formulas:
parameter β in equation (6) 1 Selecting parameters for users, wherein the selection range is more than 0 and less than beta 1 ＜min(T 11 ,T 12 ) The larger the value, the worse the anti-interference performance of the system, but the better the stability; the smaller the value, the better the noise immunity, but the poorer the stability. And determining according to the working range of the temperature-reducing water valve of the actual system.
Step 2.2: designing a secondary superheater outlet temperature control system:
designing a control system TC2 of the outlet temperature of the secondary superheater: the secondary superheater outlet temperature has a great influence on the main steam temperature as an important intermediate variable, and the stability of the temperature point is directly related to the quality of the main steam temperature. A strategy similar to step 2, i.e. a dual controller strategy, is used in the design of the control system.Wherein the second tracking controller C 21 And the PID controller with an incomplete differential form is selected to be responsible for controlling the tracking performance of the system:
wherein the controller parameter K p3 、T i3 、T d3 And T f3 The proportional, integral, derivative and filter coefficients of the second tracking controller, respectively, may be set according to the following equations:
parameter λ in equation (8) 2 Selecting parameters for users, wherein the selection range is 0 < lambda 2 ＜min(T 21 ,T 22 ) The tracking speed of the system is slower when the numerical value is larger; the smaller the number the faster the tracking speed. The determination can be carried out according to the actual working range of the temperature-reducing water valve.
Second disturbance rejection controller C 22 Responsible for improving the immunity of the system, here again a PID controller with an incomplete differential form is chosen:
wherein the controller parameter K p4 、T i4 、T d4 And T f4 The coefficients are proportional, integral, differential and filter coefficients, and can be set according to the following formula:
parameter β in equation (10) 2 Selecting parameters for users, wherein the selection range is more than 0 and less than beta 2 ＜min(T 21 ,T 22 ) The larger the value, the worse the anti-interference performance of the system, but the better the stability; smaller value of immunityThe better the performance, but the worse the stability. And determining according to the working range of the temperature-reducing water valve of the actual system.
And step 3: calculating the set temperature r of the secondary superheater outlet temperature control system 2 ：
The set temperature of the outlet of the secondary superheater changes along with the change of the load size, and can be generally determined empirically and also can be automatically calculated in proportion to the current load size. Assuming that the temperature of the superheated steam is set to r 1 Setting of the outlet temperature of the secondary superheater to r 2 In the present example, the temperature difference Δ r = r is selected 1 -r 2 The temperature is maintained at 10-20 ℃, and the specific temperature difference is in direct proportion to the actual load setting. The specific calculation formula is as follows:
wherein M is c For the desired value of the current operating load, M t Is the full load number.
And 4, step 4: calculating the control quantity of each controller:
control system T for two-stage water spraying temperature reduction process in embodiment c1 Control quantity u is presented as an example 1 A control system T of a primary water spraying and temperature reducing process c2 Control amount u of 2 Is consistent with the process.
(1) Computing internal model prediction outputs
Calculating the predicted output value of the internal model by discretizing the model (1) and the system structure diagram 3 by a posterior difference method
Wherein:
wherein T is s For the control period, it is generally 0.5s or 1s 11 And T 12 Is as defined for formula (1) and k in the subscript represents. In the calculation based on the equations (12) and (13)
Then according to the temperature set value r 1,k And the model predicted output->
Determining an error e 11,k As a first tracking controller C 11 The input of (2):
(2) Calculating a first tracking controller C 11 Control amount u of 11 ：
First tracking controller C 11 The resulting control action is obtained by discretizing the PID controller of equation (3). Here in the form of an incremental PID, giving a first tracking controller C 11 Control amount u of 11 The calculation formula of (2):
u 11,k ＝u 11,k-1 +Δu 11,k (15)；
u 11,k denotes the first tracking controller C 11 The control quantity at the moment k, the numerical value of the subscript represents the corresponding controller, and the control increment delta u 11,k The calculation was performed as follows:
wherein e 11,k 、e 11,k-1 And e 11,k-2 Respectively the current time error and the last time errorAnd the upper time error; k p1 、T i1 、T d1 And T f1 Is as defined in formula (3); u. of d11 For auxiliary differential variables, initial value u d11,0 And 0 is selected, and the specific calculation formula is as follows:
equation (15) can also be written as follows:
u 11,k ＝u 11,k-1 +q 0 e 11,k +q 1 e 11,k-1 +q 2 e 11,k-2 +q 3 Δu d11,k-1 (18)；
each parameter q in the formula (18) 0 、q 1 、q 2 And q is 3 The intermediate parameter variables are respectively calculated in the following specific manner:
(3) Calculating a first disturbance rejection controller C 12 Control amount u of 12 ：
From the structure shown in fig. 3, it can be derived that:
further obtain the deviation e 12 The calculation result of (2):
due to the controller C 11 And C 12 All adopt the same structure, the calculation mode is consistent, u 12 Can refer to u 11 . The difference between the two is the input offset, the controller parameters and the initial values of the internal variables, which are not described in detail herein.
(4) Calculating a second tracking controller C 21 And a second disturbance rejection controller C 22 Control action u of 21 And u 22 ：
Second tracking controller C 21 And a second disturbance rejection controller C 22 Is the same as that of the first tracking controller C in structure and calculation manner 11 And a first disturbance rejection controller C 12 The same can be achieved by the structure shown in formula (15). After determining the four parameters of each PID controller, the corresponding coefficient q 0 ～q 3 And will be uniquely determined, and will not be described in detail herein.
(5) Calculating the control quantities u of the two-stage controllers TC1 and TC2 respectively 1 And u 2 ：
In respectively calculating four controllers C 11 、C 12 、C 21 And C 22 After the control action of (c) is output, u is calculated as follows 1 And u 2 ：
Wherein u is 11,k 、u 12,k 、u 21,k And u 22,k Are respectively a controller C 11 、C 12 、C 21 And C 22 The control function of (1).
When the control system operates, the control system is generally implemented according to the structure shown in fig. 2, and the specific steps are as follows:
step 1: determining object models (1) and (2) by a system identification method;
step 2: from the object models (1) and (2), respectively, lambda is determined 1 、λ 2 、β 1 And beta 2 ；
Step 3: the controllers C are respectively determined by setting formulas (4), (6), (8) and (10) 11 、C 12 、C 21 And C 22 The parameters of (1);
step 4: determination of the setting r of the superheated steam temperature by the operator 1 And determining the set value r of the outlet steam temperature of the secondary superheater according to the formula (11) 2 ；
Step 5: obtaining outlet temperature y of secondary superheater and tertiary superheater by DCS system 2 And y 1 ；
Step 6: according to secondary and tertiary processesOutlet temperature y of the heater 2 And y 1 Respectively calculating the output u of the two-stage controllers TC1 and TC2 according to the step 4 1 And u 2 ；
Step 7: the outputs u of the two-stage controllers TC1 and TC2 are respectively connected 1 And u 2 Outputting to a field temperature-reducing regulating valve;
step 8: repeat Step 4-7.
Claims (1)
1. A method for controlling the temperature of main steam of a power station boiler is characterized by comprising the following steps: the method specifically comprises the following steps:
step 1: establishing a transfer function model of a water spraying temperature reduction process:
obtaining mathematical models of the processes of three-stage water spraying temperature reduction and two-stage water spraying temperature reduction by a system identification method:
and &>
Wherein s is a laplace operator; t is 11 、T 12 、T 21 And T 22 Is the inertia time constant; k 1 And K 2 Respectively, a steady state gain coefficient; y is 2 The temperature of steam at the outlet of the secondary superheater; y is 1 The temperature of steam at the outlet of the tertiary superheater; u. u 1 And u 2 The opening degrees of a secondary water spray valve and a primary water spray valve are respectively set; l is a radical of an alcohol 1 And L 2 Pure lag times of two controlled processes are respectively obtained; the parameters in the two models can be obtained through system identification;
and 2, step: two temperature control systems are respectively designed by adopting a double-control structure:
respectively designing two temperature controllers T based on the model established in the step 1 c1 And T c2 Two controllers are adopted to form a temperature control system, and the independent control of the tracking performance and the interference resistance performance is realized at the same time; temperature controller T c1 Comprising a first tracking controller C 11 And a first disturbance rejection controller C 12 Are respectively responsible for system trackingControl of performance and adjustment of immunity; temperature controller T c2 Same temperature controller T c1 With the same construction, including a second tracking controller C 21 And a second disturbance rejection controller C 22 ；C 11 、C 12 、C 21 And C 22 PID controllers with incomplete differential form are adopted:
wherein C ij (s) is controller, subscript i =1,2,j =1,2;
in order to obtain good control performance, the parameters of the controller need to be adjusted; at the temperature controller T c1 In, the first tracking controller C 11 The setting formula of (1) is as follows:
wherein the controller parameter K p1 、T i1 、T d1 And T f1 Proportional, integral, derivative and filter coefficients of the first tracking controller are respectively; parameter λ in the above formula 1 Is selected in the range of 0 < lambda 1 ＜min(T 11 ,T 12 ) The larger the numerical value is, the slower the tracking performance of the system is, and the smaller the numerical value is, the higher the tracking speed is, and the determination is carried out according to the working range of the actual temperature-reducing water valve;
first disturbance rejection controller C 12 The setting formula of (1) is as follows:
wherein the controller parameter K p2 、T i2 、T d2 And T f2 Proportional, integral, differential and filter coefficients of the first disturbance rejection controller are respectively; parameter β in the above formula 1 Is selected in the range of 0 < beta 1 ＜min(T 11 ,T 12 ) The larger the numerical value is, the poorer the anti-interference performance of the system is, but the better the stability is; numerical valueThe smaller the interference rejection, the better, but the less stable; determining according to the working range of a temperature reduction water valve of an actual system;
the temperature controller T adopts the model and the controller type with the same structure c2 Two controllers C in 21 And C 22 The same setting formula is also adopted for parameter setting;
and step 3: calculating the set temperature r of the secondary superheater outlet temperature control system 2 ：
Setting of outlet temperature of tertiary superheater as r 1 The set temperature of the outlet of the secondary superheater changes along with the change of the load size, and is automatically calculated in proportion according to the current load size; assuming that the temperature of the superheated steam is set to r 1 Setting of the outlet temperature of the secondary superheater to r 2 Temperature difference Δ r = r between them 1 -r 2 The specific temperature difference is in direct proportion to the actual load setting; the specific calculation formula is as follows:
wherein M is c For the desired value of the current operating load, M t Is the full load number;
and 4, step 4: calculating the control quantity of each controller:
the method includes the steps of calculating internal model prediction output
Wherein
And &>
The current value, the last time value and the last time value of the predicted output value of the internal model, respectively, and a parameter alpha 1 、α 2 And alpha 3 The calculation formula of (a) is as follows:
wherein T is s For the control period, k in the subscript represents the sampling time; in the calculation of
Then, according to the temperature set value r 1 Determining a first tracking controller C 11 Input e of 11 ：/>
Second, calculate the first tracking controller C 11 Control amount u of 11 ：
u 11,k ＝u 11,k-1 +q 0 e 11,k +q 1 e 11,k-1 +q 2 e 11,k-2 +q 3 Δu d11,k-1 ；
Wherein u 11,k Denotes a first tracking controller C 11 The numerical expression of the subscript of the control quantity at the time k represents the corresponding controller; e.g. of a cylinder 11,k 、e 11,k-1 And e 11,k-2 Respectively representing the current time error, the last time error and the last time error; u. u d11 For auxiliary differential variables, initial value u d11,0 Is selected to be 0; the parameters in the above formula are calculated as follows:
thirdly, calculating a first anti-interference controller C 12 Control action u of 12 ：
Due to the fact that
To obtain a deviation e 12 The calculation result of (c): />
Due to the controller C 11 And C 12 All adopt the same structure, the calculation mode is consistent, u 12 Reference u for the calculation process of 11 (ii) a The difference between the two is the initial values of the input offset, the controller parameters and the internal variables;
fourth, calculate second tracking controller C 21 And a second disturbance rejection controller C 22 Control amount u of 21 And u 22 ：
Second tracking controller C 21 And a second disturbance rejection controller C 22 The structure and calculation mode of (A) are the same as those of (C) 11 And C 12 Consistency; in determining four parameters K of each PID controller respectively p 、T i 、T d And T f After that, the corresponding coefficient q 0 ～q 4 Will also be uniquely determined;
fifthly, calculating control quantities u of two-stage controllers TC1 and TC2 respectively 1 And u 2 ：
In respectively calculating four controllers C 11 、C 12 、C 21 And C 22 After the control action is output, the temperature controller T can be calculated as follows c1 And T c2 Control action u of 1 And u 2 ：
Wherein u 11,k 、u 12,k 、u 21,k And u 22,k Are respectively a controller C 11 、C 12 、C 21 And C 22 The control function of (2); calculating a control action u 1 And u 2 Then directly acting on the on-site temperature-reducing valve to implement control; and repeating the step 3-4.
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| JPS6446505A (en) * | 1987-08-12 | 1989-02-21 | Hitachi Ltd | Boiler automatic controller |
| JP3293680B2 (en) * | 1993-03-08 | 2002-06-17 | 中部電力株式会社 | Discrete-time model reference type adaptive steam temperature controller for thermal power boiler |
| US8733104B2 (en) * | 2009-03-23 | 2014-05-27 | General Electric Company | Single loop attemperation control |
| US8499561B2 (en) * | 2009-09-08 | 2013-08-06 | General Electric Company | Method and apparatus for controlling moisture separator reheaters |
| JP5840032B2 (en) * | 2012-02-29 | 2016-01-06 | 三菱日立パワーシステムズ株式会社 | Power generation system and steam temperature control method thereof |
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| CN106765052B (en) * | 2016-11-21 | 2019-01-29 | 华北电力大学（保定） | A kind of intelligence computation forecast Control Algorithm of station boiler vapor (steam) temperature |
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