Mô phỏng công nghệ hóa học và dầu khí - Dynamic modeling

Nhóm Mô phỏng Công nghệ Hoá học và Dầu khí Trường Đại học Bách khoa Hà Nội DYNAMIC MODELING 4 – Column Dynamics Nội dung  Tiếp tục case FHT-Dyn1.hsc  Chuyển sang SSMod  Add DePropanizer Column  Dynamic Simulation Analyses  Develop a Control Strategy  Test Model 2 Add a Distilation Column Connections Name Depropanizer Number of Stagers 24 Inlet Stream ColFeed Inlet Stage 12 Condenser Type Full Reflux Condenser Energy Stream Q-Cond Overhead Vapour Outlet Propane Reboiler Energy Stream Q-Reb Bottoms Liquid Outlet C4+ 3 Add a Distilation Column Pressure Profile Condenser Pressure 1925 kPa (280 psia) Reboiler Pressure 2070 kPa (300 psia) Condenser Pressure Drop 0 kPa (0psia) Specifications Reflux Ratio 2 4 Add a Distillation Column 5 Add a Distillation Column 6 Add a Distillation Column 7 Add a Distilation Column 8 Adding Column Specifications Column Specification Types Column Component Fraction Name Lights Stage Condenser Flow Basis Mole Fraction Phase Vapour Spec Value 0.95 Components Ethane, Propane 9  Run  Save as Column_SS.hsc Adding Column Specification 10 Column_SS.hsc 11 Sizing Vessels 12 Sizing the Column Tray Section 13 Running the Tray Sizing Utility 14 Add Section: thực hiện tính toán Performance tab → Results page View Pressure Drop at each stage Size the Column Tray Section Rating – Tray Sections Section Diameter 4.42 Weir Height 50.08 Weir Length 3.126 Tray Spacing 0.55 Tray Volume (calculated) 8.439 15  Performance tab → Result page  điền các giá trị nhận được vào bảng sau: Size the Column Tray Section 16 Calculated 17 Cond P=1925 kPa & Reb P=1945 kPa save as ClmSize.hsc Add Valves to the Boundary Streams  Delete Old Propane & C4+ Streams  Enter Column Environment  Add two new Boundary Streams  Add a valve downstream  Specify a Pressure Drop: 70 kPa  Size the valves: opening 50%  Cv of Propane Valve = ? Cv of C4+ Valve = ? 18 Delete C3 & C4+ Streams 19 Add Valves to the Boundary Streams 20 Connect Streams to Vessels 21 Add Valves to the Boundary Streams 22 Sizing Valve C3 23 Sizing Valve C4+ 24 Connect Streams  Return to the Main Environment  Design tab  Connection page  Connect SubFlowsheets Streams Propane Out & C4+ Out to the MainFlowsheet Streams Propane & C4+  Dynamic tab of Streams Propane & C4+: active only Pressure Spec  Dynamic tab of Stream ColFeed: deactive Pressure Spec  Dynamic tab of Stream Reflux (SubFlowsheet): active Molar Flow Spec 25 Connections 26 Active Pressure Spec C3 27 Active Pressure Spec C4+ 28 Deactive Pressure Spec ColFeed 29 Active Molar Flow Spec Reflux 30 Clm-Specs.hsc 31 Adding Pressure Controller Connections Controller Name Cond-PC Process Variable Source Condenser, Vessel Pressure Output Tagert Object C3 Valve Parameters Action Direct PV Minimum 1725 kPa PV Maximum 2070 kPa Mode Auto SP 1925 kPa Kc 2.0 TI 2.0 minutes 32 Add Cond-PC 33 Add Cond-PC 34 Adding Condenser Level Control Connections Controller Name Condenser-LC Process Variable Source Condenser, Liquid Percent Level Output Tagert Object Reflux Parameters Action Direct PV Minimum 0% PV Maximum 100% Mode Auto SP 50% Kc 2.0 TI 10 minutes 35 Adding Reboiler Duty Control Connections Controller Name Tray 23-TC Process Variable Source Main TS, Stage Temp., Stage 23 Output Tagert Object Q-Reb Parameters Action Reverse PV Minimum 100oC PV Maximum 200oC Mode Auto SP 140oC Kc 2.0 TI 10 minutes 36 Adding Reboiler Duty Control 37 Adding Reboiler Level Control Connections Controller Name Reboiler-LC Process Variable Source Reboiler, Liquid Percent Level Output Tagert Object C4+ Valves Parameters Action Direct PV Minimum 0% PV Maximum 100% Mode Auto SP 50% Kc 2.0 TI 10 minutes 38 Sub-Flowsheet 39 Main Flowsheet 40 Save as Clm-Control.hsc Exercise  Create Strip Chart:  Cold Feed Mass Flow  Condenser Mass Flow  Butane Mass Flow  Propane Mass Flow  Change Output Variable for the Condenser- LC to Cond-Q, from Reflux  Changer the NGL-Feed Composition 41