1. Name: Marius Støre Govatsmark
Thesis: Integrated optimization and control, 2003.
Classification: Open

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

3. 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

4. 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

5. 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