1. Team: FOXTROT Mentor: Dan Rusinak Crew: Ali, Mudassir Drake, Stephen Meaux, Kevin Sieve, Brandon Foxtrot, University of Illinois at Chicago 1

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3.  Is Cobalt a better choice for a catalyst as compared to Iron? ◦ Catalyst comparison: $8/lb Fe vs. $40/lb Co ◦ Fe gives a better alpha value for wax (0.95) when compared to Co (0.92) ◦ The diesel output of Fe plants (58%) are similar to Co plants (60%) Foxtrot, University of Illinois at Chicago 3 Co prices tend to be volatile compared to iron. Also need to contend with hazardous waste disposal.

4.  How to model the SCBR? ◦ On a preliminary level we will avoid modeling the SCBR by using the syncrude composition predicted by De Klerk ◦ If time is available for further modeling we plan to use an equilibrium reactor simulation in Aspen Foxtrot, University of Illinois at Chicago 4

5. 5  What role does the rwgs reaction play? ◦ The functional form of Keq for the wgs is ◦ Keq(603 K) is 142 ◦ The rwgs reaction is not thermodynamically favored ◦ We will need to look at kinetics to see if wgs significantly effects our feed requirements

6. Energy Density (Btu/gal) $/MM Btu Energy Efficiency $/ MM Btu of Product Natural Gas 140$3.2444%$7.43 Crude Oil 138,000$16.7980%$21.00 6 Foxtrot, University of Illinois at Chicago6

7. 7 Area 1 SBCR Area 2 Alkylation/ Separation Units Area 3 Hydrocracker/ Separation Units Area 4 Transportation fuels

8. Foxtrot, University of Illinois at Chicago 8 FT Reaction Hydrocracking Alkylation

9. Foxtrot, University of Illinois at Chicago 9 FT Reaction Area PFD

10. Foxtrot, University of Illinois at Chicago 10 Arno De Clerk

11. Foxtrot, University of Illinois at Chicago 11 Material Balance for FT Reaction Area Stream No. 123456789101112 Description Syngas Feed H2 Permeate Syngas to Reactor Wax Fischer- Tropsch Products Recycle Hot Condensat e Fischer- Tropsch Products Cold Condens ate Aqueous Products Tail Gas Hot and Cold Condensate Unit lb-mol/hr CO 3809.580.003809.580.001523.830.00 1523.830.00 1523.830.00 H2 9524.171714.537809.640.003123.860.00 3123.860.00 3123.860.00 N2 77.920.0077.920.0077.920.00 77.920.00 77.920.00 H2O 0.00 2285.750.00 2285.750.002285.750.00 CO2 394.170.00394.170.00394.170.00 394.170.00 394.170.00 C1 0.00 98.290.00 98.290.00 98.290.00 C2 alkene 0.00 22.860.00 22.860.00 22.860.00 C2 alkane 0.00 22.860.00 22.860.00 22.860.00 C3-C4 alkene 0.00 137.140.00 137.14 0.00 137.14 C3-C4 alkane 0.00 41.140.00 41.14 0.00 41.14 C5-C10 alkene 0.00 176.000.00 176.00 0.00 176.00 C5-C10 alkane 0.00 75.430.00 75.43 0.00 75.43 C5-C10 oxygenate 0.00 29.710.00 29.71 0.00 29.71 C11-C22 alkene 0.00 130.290.00130.290.00 130.29 C11-C22 alkane 0.00 308.580.00308.580.00 308.58 C11-C22 oxygenate 0.00 6.860.006.860.00 6.86 C22+ alkene 0.00 16.000.00 C22+ alkane 0.00 1124.590.00 aqueous alcohol 0.00 89.140.00 89.140.0089.140.00 aqueous carboxylic acid 0.00 6.860.00 6.860.006.860.00 Total 13805.841714.5312091.311140.598550.690.00445.728104.96459.442381.755263.78905.16

12. Foxtrot, University of Illinois at Chicago 12 h 603k KJ/Kgmole h 603 K Btu/lbmole 3 (lbmol/hr) 4 (lbmol/hr) 5 (lbmol/hr) h in Btu/hr h out Btu/hr CO-101625-43791381001524-166825016-66730007 H2878437857810031242956030711824123 N288453811780 296984 H2O-275552-1187380022860-271404830 CO2-382185-1646873940 -64914586 C1-64012-2758300980-2711068 C2 alkene655552824800230645679 C2 alkane-67688-2916700230-666688 C3-C4 alkene36524157390013702158458 C3-C4 alkane-82339-3548100410-1459791 C5-C10 alkene78513383001760595454 C5-C10 alkane-132063-5690700750-4292494 C5-C10 oxygenate-187950-8098900300-2406577 C11-C22 alkene-79576-34290001300-4467566 C11-C22 alkane-365094-157322003090-48545824 C11-C22 oxygenate151065100704462 C22+ alkene-197500-8510501600-1361693 C22+ alkane-511033-2202090112500-247644300 aqueous alcohol-309600-13340900890-11892675 aqueous carboxylic acid-527235-2271900070-1557900 total 1209111418551-201882312-714530839 Q reactor=-512648527Btu/hour Q reactor= -150.2MW Energy Balance for FT Reaction Area

13. Foxtrot, University of Illinois at Chicago 13 Akylation Area PFD

14. Foxtrot, University of Illinois at Chicago 14 Hydrocracking Area PFD

15. Alkylation vs. Oligomerization o Foxtrot needed a process to convert LPG, Naptha, and Distillate olefins to heavier hydrocarbons o Oligomerization tends to be more expensive; it requires more H2, more expensive catalyst, and produces straight chain alkanes o Alkylation reacts olefins with paraffins which produces twice as much high quality naptha product o Alkylation also has the advantage of producing branched naptha (a very high quality naptha), which can be blended with lower-quality naptha produced by hydrocracker o Diesel with lower Cetane rating can be blended with high-quality diesel to improve cold weather properties 15 Foxtrot, University of Illinois at Chicago 15

16. Foxtrot, University of Illinois at Chicago 16  <5000 BPD plant has TIC of $120,000 to $150,000 per BPD  >20,000 BPD plant has TIC of $75,000 to $100,000 per BPD  These values include an SMR/ATR unit, but no alkylation unit  FT synthesis/refining accounts for 35% of TIC  Therefore, TIC = 210 – 262 MM$  We will produce 80k lb/day of steam *Estimates obtained from private communication with Rentech

17. Foxtrot, University of Illinois at Chicago 17 Per Gallon [2] Per Barrel Barrel/Year (Million) Annual Revenue (Million) Diesel Fuel $3.97$1671.06$177 Naptha$3.63$1520.26$40 Jet Fuel$3.30$1390.26$36 LPG$0.99$420.14$6 Total1.72$259

18.  US Geological Survey, Minerals Commodities Summaries.  Dividing Wall Columns, Michael A. Schultz, Douglas G. Stewart, James M. Harris, Steven P. Rosenblum, Mohammed S. Shakur and Dennis E. O’Brien UOP.  Dividing Wall Columns,2010 AiChE, Jacobs consultancy.  STRATCO, Alkylation unit.  Bechtel Article, 2001  M E DRY, 2008  Fischer Tropsch refining, arno de klerk.  US Energy Information Administration, www.eia.gov Foxtrot, University of Illinois at Chicago 18

19. Foxtrot, University of Illinois at Chicago 19  Questions please.

20.  Sequence Distillation  A (lightest) B ( Middle) C (Heaviest) Foxtrot, University of Illinois at Chicago20

21.  Energy lost  Thermal inefficiency Foxtrot, University of Illinois at Chicago21

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24.  Because the Petlyuk arrangement has fewer pieces of major equipment than does the conventional two-column sequence, total capital costs may be reduced. Foxtrot, University of Illinois at Chicago24

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26.  Reduces the energy cost by 30%  Reduces equipment cost by 50%  Reduction is the capital cost by 40% Foxtrot, University of Illinois at Chicago26

27.  Alkylation is a major way of upgrading petroleum  Formation of heavier highly branched alkanes from the reaction between isobutanes and alkenes. Foxtrot, University of Illinois at Chicago27

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31.  Utilizes a liquid-full reactor system where the heat of reaction is removed with an internal heat exchanger.  Vaporization is prevented by maintaining the reactor system at sufficient pressure.  The obvious advantage of the liquid-full system (STRATCO ) is that the isobutane remains in the liquid state continuously available for reaction in higher concentrations. Foxtrot, University of Illinois at Chicago31

32.  Easy operation  No worries about the acid or hydrocarbon levels in the reactor system  High internal circulation rates for even heat dissipation  Highly dispersed hydrocarbon in acid emulsion Foxtrot, University of Illinois at Chicago32

33.  Increased interfacial catalyst area provided by mixing  Reduced acid consumption  Superior quality alkylate 1.5 octane number advantage  Ease of reactor operation Foxtrot, University of Illinois at Chicago33

34.  Upgrading waxes to alkanes  It is a hydrogen addition technology that removes heteroatoms, increases the H:C ratio of the product  It is nearly isothermal giving a conversion of 70-80% conversion of wax to products  Will use a divided wall column and a low pressure column to separate products Foxtrot, University of Illinois at Chicago34

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