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Equipment design Ethylbenzene production by liquid phase

KUWAIT UNIVERSITYCOLLEGE OF ENGINEERING & PETROLEUMCHEMICAL ENGINEERING DEPARTMENT. Equipment design Ethylbenzene production by liquid phase. Done by: Mohammed Almohsen Supervised By: Prof. M. A. Fahim Eng. Yusuf Ismail. Distillation column:. Distillation T-101

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Equipment design Ethylbenzene production by liquid phase

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  1. KUWAIT UNIVERSITYCOLLEGE OF ENGINEERING & PETROLEUMCHEMICAL ENGINEERING DEPARTMENT Equipment designEthylbenzene production by liquid phase • Done by: Mohammed Almohsen • Supervised By: • Prof. M. A. Fahim • Eng. Yusuf Ismail

  2. Distillation column: • Distillation T-101 • Separate and recycle Ethylbenzene

  3. COLUMN DIAMETER: LIQUID VAPOR FLOW FACTOR FOR TOP FOR BOTTOMS TAKE PLATE SPACING AS 0.6 M FROM FIGURE BASE K1 = 0.08TOP K1 = 0.12 CORRECTION FOR SURFACE TENSIONS BASE K1 = 0.066TOP K1 = 0.1078

  4. FLOODING VELOCITY: DESIGN FOR 85% FLOODING AT MAXIMUM FLOW RATE BASE TOP

  5. MAXIMUM VOLUMETRIC FLOW RATE BOTTOM TOP NET AREA REQUIRED: TAKING DOWNCOMER AREA AS 12 per cent OF TOTAL AREA COLUMN CROSS-SECTIONAL AREA COLUMN DIAMETER: USE SAME DIAMETER ABOVE AND BELOW FEED =6.328M=20.76FT

  6. COLUMN HEIGHT: Column height = (Number of stage * Plate spacing) + Column Diameter H = 27.9m =91.6 FT

  7. LIQUID FLOW PATTERN: MAXIMUM VOLUMETRIC LIQUID RATE FROM FIGURE DOUBLE PASS PLATE IS USED

  8. Column diameter = Column area = Downcomer area = Net area = Active area = Hole area = PROVISIONAL PLATE DESIGN:

  9. Take weir height = Hole diameter = Plate thickness = FROM FIGURE WEIR LENGTH ASSUME

  10. CHECK WEEPING: MAXIMUM LIQUID RATE TURNDOWN PERCENTAGE = 0.80 MINIMUM LIQUID RATE MAXIMUM WEIR CREST: MINIMUM WEIR CREST:

  11. AT MINIMUM RATE FROM FIGURE MINIMUM VAPOR VELOCITY THROUGH HOLE: ACTUAL MINIMUM VAPOR VELOCITY SO MINIMUM OPERATING RATE WILL BE ABOVE WEEP POINT.

  12. PLATE PRESSURE DROP: MAXIMUM VAPOR VELOCITY THROUGH HOLES Plate thickness / hole dia. = 1.25 FROM FIGURE DRY PLATE DROP RESIDUAL DROP TOTAL PLATE PRESSURE DROP

  13. DOWN COMER LIQUID BACK-UP: DOWNCOMER PRESSURE LOSS TAKE AREA UNDER APRON HEAD LOSS IN THE DOWNCOMER BACK-UP IN DOWNCOMER CHECK RESIDENCE TIME SATISFACTORY

  14. CHECK ENTRAINMENT FROM FIGURE ψ =0.013 , well below 0.1

  15. Angle subtended by the edge of the plate = 85 Mean length, unperforated edge strips =9.3136 Area of unperforated edge strips=0.4191 m Mean length of calming zone,approx =4.7738 Area of calming zones =0.4296 m Total area for perforations, Ap =23.0532 PERFORATED AREA: FROM FIGURE

  16. FROM FIGURE NUMBER OF HOLES: AREA OF ONE HOLE: NUMBER OF HOLES:

  17. AREA OF CONDENSER AREA OF REBOILER

  18. THICKNESS CALCULATIONS:

  19. SPECIFICATION SHEET OF BENZENE COLUMN T-101

  20. Column cost: Cost of tray =1,100$/trays Cost of trays = 52,800$ Cost of Vessel: Diameter outside=6m Volume outside=895 Volume inside=878 Volume of metal=17 Weight of metal=296,080lb Cost of vessel 2007 =547,200$ Vessel type: Large ,No Internals , Medium Cost of reboiler: Cost 2007 = 39,300$ Cost of condenser: Cost 2007 =19,800$ Total cost of without insulation=659,100$ Insulation cost = 52,728$ Total cost of T-101=711,828$ COST CALCULATIONS: FROM: WWW.MATCHE.COM

  21. Heat exchanger: • 3 heat exchanger has been designE-102 ,E103 and e-105. • The type of the 3 heat exchanger are shell and tube.

  22. TRY AND ERROR ASSUME BECAUSE THERE IS PHASE CHANGE Cooler E-102 detailed calculation: • Heat load: COOLING FLOW:

  23. TEMPERATURE CORRECTION FACTOR: CALCULATION: USING ONE SHELL PASS AND TWO TUBE PASSES FROM FIGURE

  24. ASSUME PROVISIONAL AREA: CHOOSE TUBE MATERIAL TO BE carbon steel WITH THE FOLLOWING PROPERTY OUTER DIAMETER Do = 25 MMINNER DIAMETER Di = 20 MMTUBE LENGTH = 4.88 M

  25. AREA OF ONE TUBE NUMBER OF TUBES Nt = provisinal area / area of one tube = 792.36 = 793 USING 1.25 TRIANGULAR PITCH

  26. TUBE BUNDLE DIAMETER: CONSTANT USING SPLIT RING FLOATING HEAD TYPE FROM FIGURE Bundle diametrical clearance = 71 mm Shell diameter =Bundle diameter+Bundle diametrical clearance =1037.13 mm=1.037

  27. TUBE-SIDE COEFFICIENT: METHOD 1 • Mean water temperature = • Tube cross sectional area = • Total flow area=Tubes per pass x Cross sectional area=

  28. Water mass velocity=mass flow rate/total flow area= • Water linear velocity Ut = mass velocity / density = • Inside coefficient for water hi:

  29. REYNALDO NUMBER • PRANDTL NUMBER TUBE-SIDE COEFFICIENT: METHOD 1I FROM FIGURE HEAT TRANSFER FACTOR

  30. INSIDE COEFFICIENT FOR WATER Hs:

  31. SHELL-SIDE COEFFICIENT: • Choose baffle spacing = • Tube pitch = • Cross flow area= • Mass velocity Gs= mass flow rate/cross flow area =

  32. Equivalent diameter for triangular arrangement • Mean shell side diameter temperature: • Reynaldo number • Prandtl number

  33. CHOOSE 25% BAFFLE CUT HEAT TRANSFER FACTOR FROM FIGURE

  34. OVERALL HEAT TRANSFER COEFFICIENT: • Thermal conductivity of steel = • Outside coefficient (fouling factor) = • Inside coefficient (fouling factor) = CLOSE TO INITIAL VALUE ASSUMED

  35. PRESSURE DROP: TUBE SIDE: FROM FIGURE HEAT TRANSFER FACTOR

  36. SHELL SIDE: Linear velocity = FROM FIGURE

  37. SHELL THICKNESS CALCULATIONS:

  38. Cost Calculations: • From www.matche.com • Heat transfer area = 3,269ft2 • Exchanger Type: Carbon steel • Internal Pressure: 450 psi • Cost with out insulation: 110,900$ • Insulation cost: 8,872$ • Final cost 2007:119,772$

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