1. Che 451 chemical engineering design PIPELINE DESIGN
Prof. Dr. Bekir Zühtü UYSAL
Res. Asist. Melda ESKİTOROS
EMRE AKASLAN

2. index AIM PROPERTIES OF MEOH MATERIAL SELECTION DETAILED FLOW CHART
ASSUMPTIONS
PIPELINE DESIGN
TANK DESIGN
CHEMCAD CALCULATIONS
ERROR CALCULATION
ECONOMIC RESULTS

3. AIM:
The aim was transporting the product which is methanol, intermediate tank to main storage tanks. To product methanol we will use main components of synthesis gas which are carbon monoxide and hydrogen. It is planned to build the methanol plant with a capacity of tons/year.

4. PROPERTIES OF MEOH Property Value Molecular Weight, (g/mol) 32.04
Molecular Formula
CH3OH
Molecular Weight, (g/mol)
32.04
Density at 25 oC, (g/mL)
0,7866
Liquid Viscosity at 25 oC, mPa.s (=cP)
0.541
Boiling Point, (oC)
64.70
Melting Point, (oC)
-98
Solubility in Water
Miscible
Color
Colorless

5. MATERIAL SELECTION
Pipe Material:
Carbon Steel
Tank Material:
Carbon Steel

6. FLOW CHART

7. EQUIPMENT LIST Equipment # Cost (TL) Total Cost (TL)
Intermediate Tank (Carbon Steel) H=8,97m D=5,98m 1
6038
Centrifuge Pumps SPS 250/2 T-M 2'' 1,5 kW 2 HP 2
2028
4056
300m 3 1/2" SCH40 Pipeline (Carbon Style)
6921
Gate Valve GTK-16 8
250
2000
Globe Valve (304 Stainless Steel) GV-16
260
520
Control Valve Stevi P
3040
Check Valve (Stainless Steel) CLV-50
220
440
Filter (304 Stainless Steel) PTY-20 3
155
465
Tee 7 13 91
90 Elbow 9
117
45 Elbow 18
PEC FOR PIPELINE
17668

8. ASSUMPTIONS
Residence time was chosen as 8 hours
Safety factor of tank was taken as 0.10
Distance between storage tanks was taken 8m
Service life was taken as 16 years
Pressure drop between two tanks was neglected

9. PIPE DESIGN, OPTIMUM DIAMETER

11. TANK OPTIMIZATION

12. h/D: 1,5
Profile # of Intermediate Tank: 24,3
Volume of Intermediate Tank: 251,7 m3
Heigth of Intermediate Tank: 8,97 m
Diameter of Intermediate Tank: 5,98 m
PEC for Intermediate Tank: 6038 TL

13. THICKNESS MINIMIZATION

14. CHEMCAD CALCULATIONS

15. CALCULATIONS AND CHEMCAD
ERROR ON CALCULATIONS
WHEN COMPARING EXCEL
CALCULATIONS AND CHEMCAD
CALCULATION
WE HAVE 7,7 % ERROR.

16. ECONOMICAL CALCULATIONS
Total Annual Cost for Pipeline: TL/yr
Total Annual Cost for Intermediate Tank: 1465 TL/yr
Total Annual Cost: TL/yr

17. THANKS FOR YOUR ATTENTION