CHE 451 CHEMICAL ENGINEERING DESIGN
PIPELINE DESIGN
Prof. Dr. Bekir Zühtü UYSAL
Res. Asist. Melda ESKİTOROS
091140003 EMRE AKASLAN
INDEX
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AIM
PROPERTIES OF MEOH
MATERIAL SELECTION
DETAILED FLOW CHART
ASSUMPTIONS
PIPELINE DESIGN
TANK DESIGN
CHEMCAD CALCULATIONS
ERROR CALCULATION
ECONOMIC RESULTS
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 180 000 tons/year.
PROPERTIES OF MEOH
Property
Value
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
MATERIAL SELECTION
Pipe Material:
Carbon Steel
Tank Material:
Carbon Steel
FLOW CHART
EQUIPMENT LIST
Equipment
#
Cost (TL)
Total Cost (TL)
Intermediate Tank (Carbon Steel) H=8,97m D=5,98m
1
6038
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)
1
6921
6921
Gate Valve GTK-16
8
250
2000
Globe Valve (304 Stainless Steel) GV-16
2
260
520
Control Valve Stevi 12.440-P
1
3040
3040
Check Valve (Stainless Steel) CLV-50
2
220
440
Filter (304 Stainless Steel) PTY-20
3
155
465
Tee
7
13
91
90 Elbow
13
9
117
45 Elbow
2
9
18
PEC FOR PIPELINE
17668
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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
PIPE DESIGN, OPTIMUM DIAMETER
TANK OPTIMIZATION
h/D - Cost
50000
45000
40000
Cost (TL)
35000
30000
25000
20000
15000
10000
0
0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9
1
1.1 1.2 1.3 1.4 1.5 1.6 1.7 1.8 1.9
h/D
2
2.1
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
THICKNESS MINIMIZATION
CHEMCAD CALCULATIONS
ERROR ON CALCULATIONS
WHEN COMPARING EXCEL
CALCULATIONS AND CHEMCAD
CALCULATION
WE HAVE 7,7 % ERROR.
ECONOMICAL CALCULATIONS
•Total Annual Cost for Pipeline: 32051 TL/yr
•Total Annual Cost for Intermediate Tank: 1465 TL/yr
•Total Annual Cost: 33516 TL/yr
THANKS
FOR YOUR
ATTENTION