Plantwide Control of Chemical Looping CombusCon
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1 Plantwide Control of Chemical Looping CombusCon T. McFarland and B. Erik YdsCe Carnegie Mellon University Pi2sburgh, PA 15213
2 ObjecCves Develop theory for plantwide control that guarantees stability Input- Output Stability Lyapunov Stability Develop procedure for determining control variables Guarantee stability Based on minimal process informacon Apply procedure to Chemical Looping CombusCon process
3 Chemical Process Networks Follow a set of principal rules ConservaCon Laws (Mass, Energy, Stoichiometry) Second Law of Thermodynamics (Entropy ProducCon) State of a Chemical Process Network (CPN) Extensive Intensive
4 Topological properces of CPNs State Space System CPNs as directed graphs Extensive Variables,, act as inventories
5 Passive Systems Passivity defined by Storage FuncCon, W Advantageous Stability ProperCes norm input- output stable Lyapunov stability A Network of Passive Nodes is Passive Apply decentralized control to achieve passivity Stability properces apply network wide
6 A Thermodynamic Storage FuncCon Entropy is concave Availability useful work of a system converges, does not converge Must control some extensive variables, Z c Minimal control for passivity : 1 extensive variable per independent phase
7 Control Structure Design General Control Law, Locally Lipschitz concnuous Develop a procedure for the control system based on minimal control Draw digraph of process Determine control degrees of freedom Control Total Mass Inventories Control Phase Inventories AddiConal degrees of freedom Meet physical constraints OpCmizaCon
8 Chemical Looping CombusCon Process Power Generation for Carbon Sequestration OxidaCon- ReducCon > 90 % CO2 effluent Low NOx emissions No oxygen- nitrogen separacon Iron Oxide used for simulacons
9 Determining Control Degrees of Freedom # of streams T able 1: C L C C ontrol D egrees of Freedom Node Unit ¼ s f F con t 1 C ompressor Mixer O xidation R xr H E X (steam) Splitter C ompressor Solids Storage R eduction R xr H E X Steam C ondenser Splitter Mixer C ompressor Solids Storage C ontrol D egrees of Freedom 9 # of non- terminal feeds # of non- controllable phases
10 Assigning Control Variables ) Total Mass Inventory 2) Phase Mass Inventory 3) AddiConal DOF 3a) Physical Constraints CDOF 0 3b) Terminal Flows c) OpCmizaCon
11 ProperCes of Extensive Variable Control Extensive state variables are deg. 1 homogeneous funccons State 1 varies from State 2 only in quancty, intensive variables same value By sedng extensive state, we have a one to one transformacon Control of extensive variables gives a much more constrained system If the plant is highly constrained and a specific objeccve drives the change in plant state Driving Setpoints (Energy, Oxygen Inventory) Tracking Setpoints (Methane Flow, ReducCon Energy )
12 State Control : A Feasible Trajectory State Control : move the plant from one state to another Feasible, Stable trajectory Define an augmented state vector : terminal flows and objeccve funccon Find a relaconship of augmented vectors, diagonal matrix RelaConships ( ) defined by AcCve constraints (T, P) KineCc RelaConships Balance EquaCons Ex : Move along constant temperature trajectory
13 Results of State Control Random demand swings applied Demand change Compare to previous and calculate Based on predetermined relaconships among variables, encre state determined
14 Gas Phase Inventory
15 Total Mass/Solid Phase Inventory
16 Controlling Energy, Not Temperature Achieve temperature control without explicit control law Gas Temp fluctuates slightly Heat capacity varies Solid Temp held constant
17 Summary Developed a plantwide control procedure (stability driven) Establish local passivity first Remaining degrees of freedom reduce operacng space based on economics/ safety independent of choice of controller Inventory controllers stabilize CLC process State Control DeterminisCc model for setpoints Feasible trajectories Plants with Constrained Extensive State
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