FISCHER-TROPSCH LIQUIDS REFINING PLANT Team Foxtrot Presentation #4 – April 9, 2013 Mentor: Dan Rusinak, PE Team: Mudassir Ali Stephen Drake Kevin Meaux Brandon Sieve CHE 397 University of Illinois at Chicago Chemical Engineering Department 1 University of Illinois at Chicago
Fischer-Tropsch Liquids refining Plant . Team Foxtrot Presentation #4 – April 9, 2013 Mentor: Dan Rusinak, PE Team: Mudassir Ali Stephen Drake Kevin Meaux Brandon Sieve. CHE 397 University of Illinois at Chicago Chemical Engineering Department. Today, Team Foxtrot will Address: - PowerPoint PPT Presentation
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FISCHER-TROPSCHLIQUIDS REFINING PLANT
Team FoxtrotPresentation #4 – April 9, 2013
Mentor: Dan Rusinak, PE
Team:Mudassir Ali
Stephen DrakeKevin MeauxBrandon SieveCHE 397
University of Illinois at ChicagoChemical Engineering Department
1University of Illinois at Chicago
Today, Team Foxtrot will Address:
• Questions/Topics from Presentation #3 • Complete PFD • Process Control Scheme• Plant Layout• Refined Economics
Appendices1. Design Basis 2. Block Flow Diagram 3. Process Flow Diagram showing major equipment 4. Material and Energy Balance (w/ Integration Review)5. Calculations 6. Annotated Equipment List 7. Economic Evaluation factored from Equipment Costs 8. Utilities 9. Conceptual Control Scheme 10. General Arrangement – Major Equipment Layout 11. Distribution and End-use Issues Review12. Constraints Review13. Applicable Standards14. Project Communications File15. Information Sources and References
3University of Illinois at Chicago
Topics from Last Presentation
4
Distillate Bottoms Condenser Pressure
Reboiler Temp
Trays Height Diameter
T-101 LPG C5+ 253 psia 793 F 25 6.5’ 42’
T-102 Naphtha C11+ 0.2 psia 312 F 15 5.5’ 62’
T-100 Jet Diesel 0.2 psia 304 F 15 12.5’ 42’
T-103 LPG C5+ 253 psia 879 F 15 4’ 42’
T-104 Naphtha C11+ 1.2 psia 350 F 43 4’ 98’
T-105 Jet/Diesel
Wax/Res 0.2 psia 484 F 29 15.5’ 70’
T-106 Jet Diesel 0.1 290 F 29 7.5’ 70’
- Oligomerization - Hydrocracker
University of Illinois at Chicago
Detailed PFD with Level Controls• The next slides will consist of:
• Require 10 floating roof storage tanks (for naphtha, jet, diesel, VGO, and residuum) and 2 pressurized storage tanks (for LPG and cold condensate)
• 4 storage tanks in process area, 8 in tank farm • Pipeline access every 2 days, will transfer 75% of tank contents• Dike areas must contain the maximum amount of liquid in a tank• $2,600/m3 of storage
Liquid NFPA-30 Designation
LPG Class 1A
Naphtha Class IB Jet Fuel Class IC, Class IIA
Diesel Class IC, Class IIA Gas Oil Class IIIB
University of Illinois at Chicago 19
Tank Farm
S-107
LPG tank, pressurized D=26.2’,H=9.8’
Gasoline tank, floating roof D=26.2’,H=30’
Jet Fuel tank, floating roofD=26.2’,H=30’
Diesel tank, floating roof D=32.8’,H=32.8’
Pip
e R
ack
Bund (Concrete): 6’ High
Bund
Bun
d
Bund
50’
25’ 25’
S-105
S-102
S-100
S-103
S-104
S-106
S-101
50’
University of Illinois at Chicago 20
Economics• 20 year plant life• 30 workers,5 managers
• Total Cost: $7.3 MM/year • Utility, catalyst, and maintenance costs: $28.5 MM/year