Che 451 chemical engineering design PIPELINE DESIGN

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Presentation transcript:

Che 451 chemical engineering design PIPELINE DESIGN Prof. Dr. Bekir Zühtü UYSAL Res. Asist. Melda ESKİTOROS 091140003 EMRE AKASLAN

index 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 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

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 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 12.440-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

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: 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

CALCULATIONS AND CHEMCAD 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