Production of Dimethyl Sulfoxide from Lignin

1. Production of Dimethyl Sulfoxide from Lignin Team Bravo is: Jake Biberstein, Stan Das, Jeff Umbach, Russ Boyer, Krista Sutton, Mike Czepizak Project Lead: Jake Biberstein

2. Conceptual Control Scheme General Arrangement Distribution and End Use Constraints Review Applicable Standards Project Communications File Information Sources and References Project Outline • Design Basis • Block Flow Diagram • Process Flow Diagram • Material and Energy Balances • Calculations • Annotated Equipment List • Economic Evaluation • Utilities

3. Presentation Outline • Preliminary Process Flow Sheet • M & E Balances • Stream Data • Sample Calculations • Cost Data

4. Preliminary PFD

5. Process Flow Diagram Legend • Tanks • T1: Black Liquor/NaOH Mixing Tank • T2: NaOH Storage Tank • T3: Surge Tank • T4: Molten Sulfur Storage Tank • T5: Spent Black Liquor Storage Tank • T6: DMSO Product Storage Tank • Reaction Units • A: Black Liquor/Molten Sulfur Cooker • D: DMS Oxidation Column • Separation Units • B: Desiccator • C: DMS/N2 Evaporator • E: DMS/DMSO Evaporator

6. Process Flow Diagram Legend (Cont.) • Heat Exchangers • H1: BL Preheater • H2: Sulfur Preheater • H3: Separation Cooler • H4: Expander Cooler • H5: DMS Preheater • Compressors/Expanders • C1: DMS Recycle Compressor • C2: N2 Recycle Compressor • E1: DMS Reactor Turboexpander • Pumps • P1: Sodium Hydroxide Feed • P2: Surge Tank • P3: DMS Reactor Feed • P4: Sulfur Feed • P5: DMS Product

7. Closeup of 1st Reaction Step

8. Closeup of 2nd Reaction Step

9. Necessary Equipment • 4 Storage Tanks • 2 Mixing Tanks with Propellers • 5 Pumps • 1 Jacketed CSTR • 1 Reactor • 1 Evaporators • 5 Shell and Tube Heat Exchangers • 3 Compressors • 1 Turboexpander • 1 Desiccator

10. Preliminary Costing Ce = a + bSn • Ce = purchased equipment cost on a U.S. Gulf Coast Basis, January 2006 (CE index 478.6, NF refinery inflation index = 1961.6) • a, b = cost constants (Table 6.6 Chemical Engineering Design, Towler) • S = size parameter (Units given in Table 6.6 Chemical Engineering Design, Towler) • n = exponent for that type of equipment • Since we don't know the exact size of our equipment yet I'm using 0.75 of Supper • All prices from ChE design Towler are for carbon steel unless specified • Since most of our equipment has to be stainless steel we used www.worldsteelprices.com to determine that the ratio of stainless steel cost to carbon steel (raw material) cost (roughly stainless steel is 4 times more expensive)

12. Total Cost of Equipment $ 14,453,364.28 Total Cost of Installation $ 57,813,457.13 [ Assuming installation = 5(Cost of Equipment)] Total Cost of Engineering $ 4,336,009.29 [Assuming Engineering Costs = 0.30(Cost of Equipment)] Total Cost of Equipment + Installation + Engineering Costs $ 76,602,830.70

13. Estimated Cost per kg • Price of DMSO = $50/kg (from Fischer Chemical) • Price of Black Liquor = $0.27 /kg (calculation shown below) • Calculated value using energy density and cost of energy Energy Density of Black Liquor Estimated Cost of Energy

14. References • Goheen, D. W. “Chemicals from Lignin by Nucleophilic Demethylation.” Forest Products Journal. 1962. v.12, no. 10, p. 471-473. • Goheen, D. W. (1956). Process of Making Methyl Mercaptan. US Patent: US2840614. • Halfdan, Smedslund Tor. (1958). Vapor Phase Oxidation. Us Patent: US2825744. • “Lignin.” Kirk-Othmer Encyclopedia of Chemical Technology. 5th Edition. 2004. • Towler, Gavin. Chemical Engineering Design. 2007. • “Sulfur.” Wikipedia. • “Methyl Mercaptan.” Wikipedia.