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

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.)
Pumps
P1: Sodium Hydroxide Feed
P2: Surge Tank
P3: DMS Reactor Feed
P4: Sulfur Feed
P5: DMS Product
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

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 (CE index 478.6, NF refinery inflation index = )
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 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 to determine that the ratio of stainless steel cost to carbon steel (raw material) cost (roughly stainless steel is 4 times more expensive)

11. Evaporator (vertical tube) 17000 13500 640 480 0.6 565376.0903
Amount
Equipment a b
Supper
0.75*Supper n
Ce (Carbon Steel)
Ce (Stainless Steel) 1
Compressor/Expander
4200 27
5000
3750
0.8
Evaporator (vertical tube)
17000
13500
640
480
0.6
Cone Roof Tank
5700
700
4000
3000
0.7
Pumps
3300 48
500
375
1.2
Propellers
4300
1920 75
56.25
Insulated reactors
14000
15400
100
U-Tube, Shell and Tube Heat Exchangers
10000 88
1000
750
76000
304000

12. Equipment type Number We Need Cost
Compressor/Expander 4
$379,598.37
Evaporator (Vertical Tube) 1
$2,261,504.36
Cone Roof Tank
$3,133,506.05
Pumps 5
$1,243,900.90
Propellers 3
$630,469.27
Insulated reactors
$5,284,385.33
U-Tube, shell and tube heat exchanger
$1,520,000
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 v.12, no. 10, p
Goheen, D. W. (1956). Process of Making Methyl Mercaptan. US Patent: US
Halfdan, Smedslund Tor. (1958). Vapor Phase Oxidation. Us Patent: US
“Lignin.” Kirk-Othmer Encyclopedia of Chemical Technology. 5th Edition
Towler, Gavin. Chemical Engineering Design
“Sulfur.” Wikipedia.
“Methyl Mercaptan.” Wikipedia.