WO2011069700A2 - Verfahren und vorrichtung zum regeln einer dampferzeugung in einer dampfkraftanlage - Google Patents
Verfahren und vorrichtung zum regeln einer dampferzeugung in einer dampfkraftanlage Download PDFInfo
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- WO2011069700A2 WO2011069700A2 PCT/EP2010/064376 EP2010064376W WO2011069700A2 WO 2011069700 A2 WO2011069700 A2 WO 2011069700A2 EP 2010064376 W EP2010064376 W EP 2010064376W WO 2011069700 A2 WO2011069700 A2 WO 2011069700A2
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- WIPO (PCT)
- Prior art keywords
- state
- evaporator
- steam
- observer
- feedwater
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D5/00—Controlling water feed or water level; Automatic water feeding or water-level regulators
- F22D5/26—Automatic feed-control systems
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K13/00—General layout or general methods of operation of complete plants
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K13/00—General layout or general methods of operation of complete plants
- F01K13/02—Controlling, e.g. stopping or starting
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B35/00—Control systems for steam boilers
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
- Y10T137/00—Fluid handling
- Y10T137/0318—Processes
- Y10T137/0324—With control of flow by a condition or characteristic of a fluid
- Y10T137/0374—For regulating boiler feed water level
Definitions
- the invention relates to a method for regulating the production of steam from feed water in an evaporator of a steam power plant, wherein in a first control system a state controller calculates several medium states in the evaporator with the help of an observer and determines therefrom a Suitebergmas- senstrom as a control variable of the first control system ,
- the efficiency of a steam power plant increases with the temperature of the steam generated in the power boiler and with the constancy of the quality of the steam provided downstream of the evaporator unit.
- the steam generation in a steam power plant is usually from feed water, which is called in ei ⁇ nem high pressure preheater, also called economizer, preheated and then evaporated in an evaporator.
- the feed water is in this case brought to a high pressure before the high pressure preheater by means of a feed ⁇ water pump and driven by the high pressure preheater and evaporator.
- the control of the steam temperature after the evaporator is done by adjusting a mass flow of the feedwater as a control variable, which is introduced into the evaporator.
- the rule ⁇ behavior of the steam temperature with this manipulated variable is very sluggish, so that an adjustment of the feedwater mass flow only after several minutes on the temperature to be controlled affects.
- the temperature to be controlled is heavily influenced by numerous disturbances, such as load changes, soot bubbles in the boiler, change of fuel, etc. Precise temperature control is difficult to achieve for these reasons.
- the state controller according to the invention is a linear-quadratic controller.
- a linear quadratic regulator may contain a linear quadratic optimal ⁇ state feedback.
- its parameters can be determined such that a quality criterion for the control quality can be optimized.
- both an accurate and stable control can be achieved.
- the invention is based on the consideration that in a state control several - sometimes not measurable - states for determining the manipulated variable, or the controller control signal, are returned.
- states such as temperature, pressure, enthalpy, or other state variable can be used at multiple locations along the evaporator in the algorithm.
- states are not measurable, a so-called observer circuit is needed, with the aid of which the required states, which can be characterized by state variables, can be estimated or calculated.
- observer circuit is needed, with the aid of which the required states, which can be characterized by state variables, can be estimated or calculated.
- estimate is used as synonyms in the following: The advantage of this concept is that it can respond very quickly and accurately to disturbances that act on the evaporator.
- the steam turbine is a steam powered Anla ⁇ ge. It may be or include a steam turbine, a steam process plant, or any other facility powered by steam energy.
- the evaporator may be understood below to mean any system in which water is evaporated, wherein a preheater, in particular a high-pressure preheater, may be enclosed.
- the medium may be feedwater, steam or a mixture of feedwater and steam.
- a medium state - also referred to below as a simplified state - can be an energy, a temperature, a pressure, an enthalpy or another state of the medium.
- a closed-loop control can be understood to mean a control loop which regulates the controlled variable on the basis of an estimated state, for example in the form of a state space representation.
- one or more supply items within the controlled system by an observer estimates ge ⁇ and the control system - or the regulator - again ⁇ out, so returned be.
- the repatriation, which forms about ⁇ together with the controlled system the control loop can be done by the observer, who can thus ER- put a measuring device.
- the observer computes or estimates the states of the system, in this case the medium in the evaporator, and may include a state differential equation, an output equation, and an observer vector.
- the output of the observer can be compared with the output of the controlled system. The difference can affect the state-differential equation via the observer vector.
- the observer works independently of the state controller.
- the state controller uses a state of steam leaving the evaporator as a controlled variable, such as the steam temperature, or the enthalpy of the steam.
- Actuating variable is advantageously used the feedwater mass flow.
- a desired value for the feedwater mass flow to a controller of a second control system for controlling the feedwater mass flow is passed.
- This can use the setpoint as a controlled variable.
- a manipulated variable of the second control system can directly or indirectly the speed of a feedwater pump, the position of a valve, e.g. in the feed water line, or another parameter suitable for adjusting the feedwater mass flow.
- an enthalpy of the medium is used to calculate the medium states as the state variable.
- multiple states and in sequence whose multiple enthalpies are used.
- the steam parameters, such as enthalpy and / or pressure and temperature should, depending on the load, be kept at desired values and controlled accordingly when load changes occur.
- the advantages of an enthalpy state control ie the use of an enthalpy or a product of enthalpy and a further variable, such as a water mass flow, as state, are that state control systems achieve a higher control quality and the control becomes faster.
- the process is expediently designed so that slightly superheated steam exits at the end of the evaporator, which is close to the saturated steam limit.
- pressure eg in sliding pressure mode
- the evaporation end point or the saturated steam point changes, which can lead to wet steam when considered in temperature.
- the pressure does not need to be explicitly considered as well as the enthalpy combines both Tempe ⁇ temperature and pressure in one size.
- deviations of the absolute enthalpies of enthalpy setpoint values are used as state variables.
- the LQR method relates to linear control problems.
- the mathematical controller problem can be linearized when using enthalpy states and thus made accessible for easier calculation, because there is a linear relationship between inlet and outlet enthalpy.
- the conversion is conveniently carried out by means of appropriate water / steam-table relationships using e.g. the measured vapor pressure.
- the feedwater flow acts in a non-linear manner on the control variable enthalpy at the evaporator inlet and outlet, so that the controller problem - despite the use of enthalpies - is non-linear.
- linearization is expediently used in the calculation of the states.
- ⁇ taken that move the states only a rich Abweichungsbe- about an operating point.
- the Sys tem ⁇ can be assumed to be linear.
- Measured values is updated.
- the measured values are expediently current measured values which were recorded by measuring a currently present medium parameter, such as pressure, temperature and the like.
- the operating point on which the state calculation is based can be adapted to a current medium state.
- a further advantageous embodiment of the invention provides that the control system of the state controller has a matrix equation, for example in the form of a feedback matrix, for the calculation of which medium values measured during the steam generation are used.
- the state feedback can take place via a matrix equation whose parameters are at least partially determined using current measured values.
- the controller can constantly adapt to the actual operating conditions.
- a load-dependent change in the dynamic evaporator behavior can be automatically taken into account.
- an increase of the robustness of the control algorithm can be achieved. Due to the fact that the controller algorithm is very robust, only very few parameters have to be set during commissioning. Commissioning time and effort is therefore significantly reduced compared to all previously known methods.
- the matrix equation is calculated by a control technology of the steam power plant.
- the control system can be a control system that controls the steam power plant in its regular operation.
- the matrix equation is converted into a set of scalar differential equations.
- a relatively simple integration of the matrix equation can be achieved by integration backwards over time. Since no real-time information is available in the real world, backward integration-equivalent integration can be achieved by integrating the set of scalar differential equations of opposite sign, which stably leads to the same stationary solution.
- the observer is a Kalman filter designed for linear-quadratic state feedback.
- the interaction of the linear-quadratic controller with the Kalman filter is called LQG (Linear Quadratic Gaussian) controller or LQG algorithm called.
- the observer calculates the heat introduced into the medium in the evaporator.
- This can be defined as a disturbance and used in the control algorithm.
- the disturbance variable can be defined as a state and, in particular, estimated or determined with the aid of the observer. Disturbances that act directly on the evaporator are expressed by the fact that the warm-up period in the evaporator changes.
- the invention also relates to an apparatus for controlling the production of steam from feed water in an evaporator of a steam power plant, with a control system, the observer a loading and includes a state regulator, which is prepared to be several medium conditions in the evaporator with the help of egg ⁇ nes observer to to calculate and from this a feedwater mass flow as a control variable of the first control system.
- the state controller is a linear-quadratic controller.
- An accurate and stable control can be achieved.
- the apparatus is adapted to perform one, several or all of the method steps proposed above.
- FIG. 6 shows an overview of a controller construction.
- FIG. 1 shows a schematic representation of a detail of a steam power plant with a steam power plant comprising a steam turbine 2, a boiler 4, an evaporator 6 and a superheater 8.
- the boiler 4 gives off heat to the evaporator 6, flows into the feed water 10, which is pumped by a feedwater pump 12 to the evaporator 6 and receives the heat.
- a valve 14 With the help of a valve 14, the Spei ⁇ sewasserstrom can be regulated.
- the feedwater flow is controlled by means of the valve 14 and / or the feedwater pump 12, wherein a desired flow of the feedwater 10 upstream of the evaporator 6 is the controlled variable and a valve position and / or a pump power is the manipulated variable.
- a temperature sensor 18 and a pressure sensor 19 measure the temperature T w and the pressure p w of the feedwater 10 and a sensor 20, the actual feed water flow mi in front of the evaporator. 6
- a temperature sensor 22 and a pressure sensor 24 measure the steam temperature T D and the vapor pressure p D of the steam 16 after the evaporator 6.
- the evaporator 6 may include a preheater, not shown.
- evaporator is also understood to mean a system comprising an evaporator with a preheater
- the evaporator 6 is a forced-circulation steam generator in which the passage of the water or steam flow from the feed pump
- the feed water 10 can successively flow through a feedwater preheater and the evaporation part, in particular also the superheater 8, so that the heating of the feedwater 10 to the saturated steam temperature, evaporation and superheating takes place continuously in one pass
- the evaporator 6 is part of a Benesson boiler.This can be driven in the supercritical range, the feedwater 10 from the feedwater pump
- the feedwater mass flow can be regulated depending on the load.
- a control cascade with a first or outer control system 26 and a second or inner control system 28 is shown schematically.
- the outer control system 26 comprises a linear-quadratic regulator 30, in particular an LQG regulator.
- the measured actual feed-water flow mi, the measured temperature T w of the feed water 10, the measured temperature T D and the measured temperature are measured as input variables
- Pressure p D of the steam 16 and the setpoint temperature T 3 of the steam 16 is supplied to the evaporator 6.
- the setpoint temperature T s of the steam 16 is the controlled variable of the controller 30.
- the setpoint mass flow m s of the feedwater 10 is output as a manipulated variable from the controller 30.
- This setpoint mass flow m E is supplied to a control loop 32 of the inner control system 28 as the setpoint for the controlled variable. ben.
- the measured feedwater flow mi is the control variable of the control loop 32.
- the control loop 32 has a position of the control valve 14 and / or a power of the feedwater pump 12 as a control variable.
- the regulator 30 does not act on the process directly via an actuator, but transfers the desired value m s for feedwater mass flow to the subordinate control circuit 32, with which it thus forms a cascade of the outer control system 26 and the inner control system 28.
- Pressure p w of the feedwater 10 before the evaporator 6 are required by the controller 30 as additional information to determine the specific enthalpy hi of the feedwater 10 upstream of the evaporator 6.
- the enthalpy hi can be determined via the water-steam panel. From the vapor pressure p D and the steam temperature T D , the specific enthalpy h 2 of the steam 16 after the evaporator 6 is calculated.
- FIG. 3 shows a model of the evaporation section in the evaporator 6, which is divided into three first-order delay elements 34, such that a third-order delaying behavior results in their series connection.
- the three delay elements can each be PT elements that are realized by a negative-feedback integrator 36.
- the time constants of these delay elements are load-dependent and increase with decreasing load and vice versa.
- An input state is characterized by the input enthalpy hi of the evaporation path.
- the two central states x 2, 3 are calculated and not measurable competent ⁇ en, which are estimated by the observer.
- the actual mass flow mi of the feedwater 10 is aufmultipli approach to the enthalpy hi, so that the product results in a performance.
- This is easily adjustable by means of the feedwater pump 12 and / or the valve 14 and can thus be used as a control variable. Since the enthalpy hi is substantially constant, the actual mass flow m ⁇ of the feedwater 10 alone can
- Manipulated variable can be used.
- mi is multiplied in each delay element 34 in each case to the given enthalpy, as represented by multipliers 38, so that a power is formed as a variable.
- a power is formed as a variable.
- 1/3 of an assumed firing rate Q F is added to these outputs, so that the entire firing rate Q F is introduced into the dynamic model of the entire evaporation length.
- the state xi is the initial enthalpy h 2 . It can be seen that a state x is constant, its derivative is therefore zero, if the enthalpy difference over a delay element 34 multiplied by the feedwater flow ⁇ in addition to the third of the combustion output Q F is zero, enthalpy difference times feedwater flow mi and QF / 3 hold the balance. In this case, the system is in a retracted state and therefore in equilibrium with feedwater supply and heating.
- this nonlinear system of equations must be converted into a linear system by means of linearization.
- the states and the input are first expressed as a sum of stationary values and the deviations around these stationary values.
- the stationary states result from the nonlinear system equations by setting the time derivatives of the states equal to zero. This is indicates that there is no change over time in the system and that these are in a stationary rest position.
- the steady state is defined as the target state.
- y (t) C (t) ⁇ x (t) + D (t) ⁇ u (t), where the input u (t) in many cases does not directly affect the output y (t) and thus D (t ) Is zero.
- the matrices A and B change with the load or with the current desired value of the enthalpy h 2s downstream of the evaporator 6. This means that the dynamics are adapted to the current load case and the process is thus over the entire load. rich is tracked.
- a condition control is a linear control in which the actual states ⁇ stands of a process 40 with the corresponding Sollzu- are compared and the resulting difference multiplied by a factor on the process will be activated.
- the calculated actual states x (t) are compared with predetermined target states x so ii (t).
- a vector or matrix in the following contains the three states xi, x 2, X 3 and Q F in the present case as a fourth size, and the corresponding desired values.
- a feedback vector K (t) with the sizes Ki, K 2 , K 3 can be used.
- u (t) is the manipulated variable and y (t) is the output variable of the process.
- the current values of the actual states x (t) must be known and available.
- the states X2, 3 and QF can not be measured.
- the reason for this is that the exact measuring point of the two states within the evaporator can not be determined.
- the first two delay elements of the model only represent the temporal dynamics of the process. However, this does not say anything about the local dynamics, which is why a measuring point for the temperature can not be determined.
- wet steam is present, which additionally makes it difficult to determine their enthalpy. Therefore, another way must be found to determine the states.
- This state determination, or state estimation, can be achieved by state feedback.
- the control by state feedback is a pure proportional control. This means that the states are only negatively attributed multiplied by a factor. This type of feedback can lead to a system deviation, which means that specified setpoints are not reached. In order to ensure that these setpoints are achieved, the implementation of an integral part makes sense.
- the implementation of an integral component on a circuit is achieved, in which the control ⁇ difference between the output and reference value in a ⁇ integrator is fed back and to the manipulated variable with houseschal- tet.
- An immeasurable disturbance variable is the fluctuation in the firing heat output Q F , which has a great influence on the present process.
- the fluctuation is caused by varying calorific values of the burned primary energy sources (coal, oil or gas).
- FIG. 5 shows the structure of the disturbance variable observer.
- the model of the evaporation path in the evaporator 6 analogous to FIG. 3, but with small changes.
- H 2 indicates a specific enthalpy.
- This estimated enthalpy H 2 is compared with the enthalpy h 2 measured via pressure and temperature, and the difference, that is, the observer error e, is compared to the observed enthalpy h 2 . th, so calculated process switched, but not directly, but as a product with an observer correction L, the so-called observer vector.
- This is a four-dimensional vector, ie it contains four components, Li, L 2 , L 3 and L 4 , each of which is multiplied by the observer error - a scalar.
- the reconstruction of the distance states is performed by the bill loading ⁇ a dynamic system model in parallel with the ECH-th process.
- the deviation between measured variables from the process and the corresponding values which are determined with the system model is the observer error e.
- the individual states of the distance model are each corrected by the Li-weighted observer error, which stabilizes it.
- the corresponding correction component is switched with the observer error, with the aim of achieving the steady state, ie the equilibrium state.
- the estimated Feue ⁇ security benefit Q - in contrast to the real firing Q F - is used here as a fourth component X 4 of the Computing device tors X, and accordingly, the Korrekturkompo ⁇ component L 4 is switched to the observer error e to the estimated combustion capacity Q ,
- the observer correction L also called the feedback vector, is to be calculated so that the observer error is corrected, ie disappears.
- the observer can be realized as a nonlinear observer, since the input variable mi is measurable.
- the nonlinear system can thus be rewritten directly into a state space representation. This is known under the name of extended Luenberger observer or extended caiman filter (extended caiman filter - EKF). It is parallel to the process equitable net ⁇ a nonlinear model.
- the feedback vector L (t) which stabilizes the observer error is obtained from a linear model. The Linearization takes place by inserting the respective measured feedwater mass flow ⁇ ⁇ .
- the control in the first control system 26 comprises a linear-quadratic controller, in particular an LQG controller 30.
- An LQG controller is a common implementation of a linear-quadratic (LQ) controller and a Kalman filter.
- An LQ controller can be a so-called optimal controller, which is based on a quadratic quality criterion. With this quality criterion and an algorithm, a feedback vector K (t) of the state control is calculated.
- a Kalman filter is a special observer or state estimator, in which additionally measurement inaccuracies at the output (measurement noise) and model inaccuracies (process noise) can be considered or co-modeled. By means of an algorithm, the further feedback vector L (t) for the observer can be determined.
- Such an LQG controller is shown in FIG.
- the measured enthalpy h.2 after the evaporator 6, the current feedwater mass flow mi, the enthalpy hi before the evaporator 6 and the desired enthalpy h2 s after the evaporator 6 are transferred to the LQG controller module as inputs, which are derived from the desired temperature of the steam 16 and calculate its pressure.
- calculation matrices A, B, A otlS C 0bs / RRegier, QRegier, Robs and Q obs are transferred.
- A, B, A 0bs , Co bs result from the linearized system representation, RRegier / QRegier / Robs and Q 0 bs contain weighting factors for setting the desired controller behavior (sensitivity, aggressiveness).
- the output is the required feedwater mass flow m s , which is calculated from the difference of the disturbance variables on the circuit m Gs and the state control Am. It should be noted here that the disturbance variable on the circuit m Gs is calculated with the estimated combustion heat output Q. This disturbance variable circuit m Gs is used in other concepts over the coalmask. pilot operated, but here it is calculated directly via the estimated rated thermal input Q.
- the state control Am is the result of the state control.
- the LQG controller 30 comprises the observer 42 shown in FIG. 5, to which the measured input enthalpy hi, the measured output enthalpy h.sub.2 and the measured feedwater flow mi are supplied as input variables.
- the eighth Obs ⁇ the return vector L (t) is supplied to compensate for the observer error e.
- the return vector L (t) is calculated by means of a solver L KR of the Kalman-Riccati differential equation to which the calculation matrices A 0b s, C obs , R 0b s and Q 0 bs are transferred.
- the LQG controller 30 comprises a module 44 for calculating the desired states X s , which are required for the state feedback.
- the inputs to the construction ⁇ stone 44 are the tasks senthalpie hi and the target Ricoenthalpie .2 S.
- the LQG controller 30 comprises a solver L RR for the controller Riccati differential equation which calculates the feedback vector K (t).
- the calculation matrices A, B, ⁇ Regier and QRegier are transferred to this.
- the use of the feedback vector K (t) is analogous to that of the feedback vector L (t). While that
- L (t) compensate for the observer error e by Aufmultipli ⁇ cation and recirculation, is the return vector K (t) multiplied up a state error, and is used to supply Level control, that is to a fluctuation compensation or to compensate for the control error of the LQG controller 30: From the difference of the state vector X (t) with the components Xi, X 2 and Xs and the also three-dimensional state vector for the target states Xs (t) is the dynamic portion of the LQG controller 30 generates, with which the state control is performed:
- K x ⁇ x, -X ls ) + K 2 (X 2 -X 2s ) + K 3 (X 3 -X is ) Am.
- the dynamic component or state control Am is on
- the disturbance variable on the circuit m Gs is a calculated target mass flow, also called the basic setpoint, which results from the quotient of the estimated firing output Q and the resulting enthalpy difference Ah over the evaporation section.
- This desired mass flow or basic setpoint m Gs of dynamic control component is most negatively added up so that the target Suitebergmassentrom m s results, the manipulated variable of the first control system 26.
- This Sollmassentrom m s is passed to the second control system 28 as a control variable, which this Setpoint mass m s sets using one or more suitable components, for example, the feedwater pump 12 and / or the valve 14th
- K (t) R Kgler -B T (t) -S (t).
- ⁇ - A (t) ⁇ P (t) + P (t) ⁇ A T (t) -P (t) ⁇ C T ( ⁇ R 0 l ⁇ C (t) ⁇ P (t) + Q 0bs . dt
- the observer feedback matrix L (t) can be calculated using the solution matrix P (t):
- P and S are the matrices according to which the matrix Riccati equations are solved, and here only represent intermediate quantities in order to determine L and K, respectively.
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- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
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- Control Of Steam Boilers And Waste-Gas Boilers (AREA)
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Abstract
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CN201080063341.3A CN102753789B (zh) | 2009-12-08 | 2010-09-28 | 调节蒸汽动力设备中的蒸汽产生的方法和设备 |
EP10760329.2A EP2510198B1 (de) | 2009-12-08 | 2010-09-28 | Verfahren und vorrichtung zum regeln einer dampferzeugung in einer dampfkraftanlage |
US13/514,313 US20130133751A1 (en) | 2009-12-08 | 2010-09-28 | Method and device for regulating the production of steam in a steam plant |
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DE102009047652 | 2009-12-08 |
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WO2013072464A3 (de) * | 2011-11-17 | 2014-05-30 | Siemens Aktiengesellschaft | Verfahren und vorrichtung zum regeln einer temperatur von dampf für eine dampfkraftanlage |
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EP2244011A1 (de) * | 2009-03-24 | 2010-10-27 | Siemens AG | Verfahren und Vorrichtung zum Regeln der Temperatur von Dampf für eine Dampfkraftanlage |
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- 2010-09-28 WO PCT/EP2010/064376 patent/WO2011069700A2/de active Application Filing
- 2010-09-28 US US13/514,313 patent/US20130133751A1/en not_active Abandoned
- 2010-09-28 EP EP10760329.2A patent/EP2510198B1/de not_active Not-in-force
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Cited By (6)
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WO2013072464A3 (de) * | 2011-11-17 | 2014-05-30 | Siemens Aktiengesellschaft | Verfahren und vorrichtung zum regeln einer temperatur von dampf für eine dampfkraftanlage |
CN104053866A (zh) * | 2011-11-17 | 2014-09-17 | 西门子公司 | 调节用于蒸汽发电设备的蒸汽温度的方法和装置 |
US10012114B2 (en) | 2011-11-17 | 2018-07-03 | Siemens Aktiengesellschaft | Method and device for controlling a temperature of steam for a steam power plant |
CN103199545A (zh) * | 2013-03-29 | 2013-07-10 | 中冶南方工程技术有限公司 | 动态无功补偿装置最优二次高斯控制器及其设计方法 |
CN117588736A (zh) * | 2024-01-18 | 2024-02-23 | 常州高凯电子有限公司 | 一种压电式高温水蒸气发生器控制系统及方法 |
CN117588736B (zh) * | 2024-01-18 | 2024-05-10 | 常州高凯电子有限公司 | 一种压电式高温水蒸气发生器控制系统及方法 |
Also Published As
Publication number | Publication date |
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CN102753789B (zh) | 2016-03-02 |
US20130133751A1 (en) | 2013-05-30 |
WO2011069700A3 (de) | 2012-07-26 |
EP2510198B1 (de) | 2016-07-27 |
EP2510198A2 (de) | 2012-10-17 |
CN102753789A (zh) | 2012-10-24 |
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