Name: Marius Støre Govatsmark

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Presentation transcript:

Name: Marius Støre Govatsmark Thesis: Integrated optimization and control, 2003. Classification: Open 2015-08-21

APID DSPICE SEPTIC/MPC Farming: Oats Work: Statoil Kårstø gassprocessing plant Optimization network: APID DSPICE SEPTIC/MPC Hobby: Cross-country skiing Classification: Open 2015-08-21

Sleipner stabilization and fractionation (1993) -Goal: 1. Processing available feed. 2. High energy efficiency in separation -Challenge: Big variation in feed rates and feed compositions Classification: Open 2015-08-21

Basic control: LT-control MPC controlling the product quality Depropaniser Train 100 – 24-VE-107 24 HC 1015 24 PC 1020 24 PDC 1021 24 PI 1014 Fakkel 24 TI 1020 24 AR 1008 B = C2 C = C3 D = iC4 24-HA-103 A/B 24 TI 1021 24-VA-102 24 LC 1010 21 1 5 6 17 20 33 34 39 48 35 40 18 24 TI 1011 Kjølevann 24 TI 1017 24 FC 1008 24 24 TI FC 1005 1031 24 TI 1038 25 FI 1003 24-PA-102A/B 24 FC 1009 24 TI 1013 Propan Bunn ut deetaniser 24 PD 1009 24 TI 1012 Normalt 0 flow, brukes ved oppstart for å kvitte seg med inertgassar 24 TC 1022 Controlled variables (CV) = Product quality Manipulated variables (MV) = setpoint to PID-controllers 24 AR 1005 C = C3 E = nC4 F = C5+ Disturbance variables (MV) = Measured disturbance (feedforward control) 24 PC 1010 24-VE-107 24 LC 1009 LP Damp 24 LC 1026 Debutaniser 24-VE-108 LP Kondensat Basic control: LT-control MPC controlling the product quality 24 TI 1018

Selection of active temperature controller? Dolgov (2011) Column temperature profile: - Strongly dependent of feed composition Temperature step response: -Signifcant differences in processdynamic: Time delay: 1 min (blue) or 20 min (black) Identify regions: when to use which temperature controller Classification: Open 2015-08-21