Alstom Technology Limited

General Electric Technology Gmbh

Other

Xinsheng Lou

Abhinaya Joshi

Carl H Neuschaefer

Hao Lei

Armand A Levasseur

Shu Zhang

Jundong Zhang

George D Mylchreest

Bruce Wilhelm

Chuan Wang

Greg N Liljedahl

James A McCombe

Shizhong Yang

John M Peluso

Stanley Kmiotek

Michael Chris Tanca

Armand Alfred Levasseur

Method and system for adjusting a measured reheat outlet steam temperature ('R') to approximate a reheat outlet steam temperature setpoint ('R') in a boiler. An Ris compared to an R. If the Ris less than the Rand a position of a fuel nozzle tilt (&#x201c;TILT&#x201d;) is below a high limit of the fuel nozzle tilt (&#x201c;TILT&#x201d;), the TILTis increased while a flow rate of a secondary flue gas recirculation (&#x201c;SFGR&#x201d;) is kept constant. If the Ris less than the Rand the TILTis at the TILT, the SFGRis increased. If the Ris greater than the Rand the SFGRis greater than a low limit of flow rate of the SFGR (&#x201c;SFGR&#x201d;), the SFGRis decreased, while the TILTis kept constant. If the Ris greater than the Rand the SFGRis at the SFGR, the TILTis decreased.

Method and apparatus for reheat steam temperature control of oxy-fired boilers

An automatic tuning control system and method for controlling air pollution control systems such as a dry flue gas desulfurization system is described. The automatic tuning control system includes one or more PID controls and one or more supervisory MPC controller layers. The supervisory MPC controller layers are operable for control of an air pollution control system and operable for automatic tuning of the air pollution control systems using particle swarm optimization through simulation using one or more dynamic models, and through control system tuning of each of the PID controls, MPC controller layers and an integrated MPC/PID control design.

Automatic tuning control system for air pollution control systems

A method for controlling at least one operational parameter of a plant () having a combustion unit () can include estimating a status of at least one operational variable of the plant to identify an estimated value for the operational variable. For each operational variable, the estimated value for the operational variable can be compared with a measured value of the operational variable to determine an uncertainty value based on a difference in value between the measured value and the estimated value for the operational variable. A control signal can be generated based on a reference signal, the measured value, and the deviation value for sending to at least one element of the plant () for controlling a process of the plant ().

Apparatus and method for controlling at least one operational parameter of a plant

A control system for optimizing a chemical looping ('CL') plant includes a reduced order mathematical model ('ROM') that is designed by eliminating mathematical terms that have minimal effect on the outcome. A non-linear optimizer provides various inputs to the ROM and monitors the outputs to determine the optimum inputs that are then provided to the CL plant. An estimator estimates the values of various internal state variables of the CL plant. The system has one structure adapted to control a CL plant that only provides pressure measurements in the CL loops A and B, a second structure adapted to a CL plant that provides pressure measurements and solid levels in both loops A, and B, and a third structure adapted to control a CL plant that provides full information on internal state variables. A final structure provides a neural network NMPC controller to control operation of loops A and B.

Nonlinear model predictive control for chemical looping process

An oxy-combustion boiler unit is disclosed which includes a furnace for combusting fuel and for emitting flue gas resulting from combustion. The furnace has first, second and third combustion zones, and an air separation unit for separating oxygen gas from air and providing a first portion of the separated oxygen to a first oxidant flow, a second portion to a second oxidant flow, and a third portion of the separated oxygen gas to the first, second, and third zones of the furnace. A controller can cause the separated oxygen gas to be distributed so that the first and second oxygen flows have a desired oxygen content, and so that the first, second, and third zones of the furnace receive a desired amount of oxygen based on a combustion zone stoichiometry control.

Oxy-fired boiler unit and method of operating the same

An electricity production system configured to operate in accordance with a method of operating an electricity production system that at least includes the steps of: determining an oxygen distribution between oxygen gas to be separated by an air separation unit ('ASU') and oxygen gas stored in a storage tank of the ASU to be fed to the boiler unit, determining a carbon capture value for a gas processing unit, determining a power consumption value for the gas processing unit and the ASU, determining a total power demand value based on the power consumption value of the gas processing unit and the ASU, and on a determined electricity demand, and controlling the boiler unit, the turbine, the ASU, and the gas processing unit based on the determined total power demand along with correcting signals generated from a coordinated Model Predictive Control.

Oxy fired power generation system and method of operating the same

A control system () for optimizing a chemical looping process of a power plant includes an optimizer (), an income algorithm () and a cost algorithm () and a chemical looping process models. The process models are used to predict the process outputs from process input variables. Some of the process in puts and output variables are related to the income of the plant; and some others are related to the cost of the plant operations. The income algorithm () provides an income input to the optimizer () based on a plurality of input parameters () of the power plant. The cost algorithm () provides a cost input to the optimizer () based on a plurality of output parameters () of the power plant. The optimizer () determines an optimized operating parameter solution based on at least one of the income input and the cost input, and supplies the optimized operating parameter solution to the power plant.

Integrated controls design optimization

A control system for optimizing a chemical loop system includes one or more sensors for measuring one or more parameters in a chemical loop. The sensors are disposed on or in a conduit positioned in the chemical loop. The sensors generate one or more data signals representative of an amount of solids in the conduit. The control system includes a data acquisition system in communication with the sensors and a controller in communication with the data acquisition system. The data acquisition system receives the data signals and the controller generates the control signals. The controller is in communication with one or more valves positioned in the chemical loop. The valves are configured to regulate a flow of the solids through the chemical loop.

Control and optimization system and method for chemical looping processes

A system for optimizing and controlling a circulating fluidized bed combustion (FBC) system () and an air pollution control (APC) system () includes a controller () and an optimizer (). The controller () is connected to the FBC system () and/or the APC system (). The optimizer () is connected to the controller (). The optimizer () provides an optimized setpoint () to the controller () based on an economic parameter () and system outputs () from the FBC system () and the APC system (). The controller () provides an optimized input () to the FBC system () and/or the APC system () based on the optimized setpoint () from the optimizer () to optimize operation of the FBC system () and/or the APC system ().

Modeling and control optimization system for integrated fluidized bed combustion process and air pollution control system

A control system for optimizing an oxy-fuel power plant comprises an optimizer in communication with the oxy-fuel power plant; the oxy-fuel power plant being operative to recycle carbon dioxide from a flue gas stream to a boiler; a control platform; the control platform being operative to control the oxy-fuel power plant; and a simulator; the simulator being operative to simulate performance of the oxy-fuel power plant.

Optimized integrated controls for oxy-fuel combustion power plant

A system for optimizing a power plant includes a chemical loop having an input for receiving an input parameter () and an output for outputting an output parameter (), a control system operably connected to the chemical loop and having a multiple controller part () comprising a model-free controller. The control system receives the output parameter (), optimizes the input parameter () based on the received output parameter (), and outputs an optimized input parameter () to the input of the chemical loop to control a process of the chemical loop in an optimized manner.

Control and optimization system

A control system () for optimizing a power plant includes a chemical loop having an input for receiving an input signal () and an output for outputting an output signal (), and a hierarchical fuzzy control system () operably connected to the chemical loop. The hierarchical fuzzy control system () includes a plurality of fuzzy controllers (). The hierarchical fuzzy control system () receives the output signal (), optimizes the input signal () based on the received output signal (), and outputs an optimized input signal () to the input of the chemical loop to control a process of the chemical loop in an optimized manner.

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West Hartford, CT, United States of America

Xinsheng Lou