1 / 44

PROPYLEN OXIDE CO-PRODUCTION WITH t-BUTYL ALCOHOL BY THE TEXACO HYDROPEROXIDATION PROCESS

Kuwait University College of Engineering & Petroleum Depatment of Chemical Engineering. PROPYLEN OXIDE CO-PRODUCTION WITH t-BUTYL ALCOHOL BY THE TEXACO HYDROPEROXIDATION PROCESS. Designer: Sultan Alharbi Supervised by: Prof.M.Fahim ENG: Yousif Ismail. Outline :.

kim-hinton
Télécharger la présentation

PROPYLEN OXIDE CO-PRODUCTION WITH t-BUTYL ALCOHOL BY THE TEXACO HYDROPEROXIDATION PROCESS

An Image/Link below is provided (as is) to download presentation Download Policy: Content on the Website is provided to you AS IS for your information and personal use and may not be sold / licensed / shared on other websites without getting consent from its author. Content is provided to you AS IS for your information and personal use only. Download presentation by click this link. While downloading, if for some reason you are not able to download a presentation, the publisher may have deleted the file from their server. During download, if you can't get a presentation, the file might be deleted by the publisher.

E N D

Presentation Transcript

  1. Kuwait University College of Engineering & Petroleum Depatment of Chemical Engineering PROPYLEN OXIDE CO-PRODUCTION WITH t-BUTYL ALCOHOL BY THE TEXACO HYDROPEROXIDATION PROCESS Designer: Sultan Alharbi Supervised by: Prof.M.Fahim ENG: Yousif Ismail

  2. Outline : 1- Heat exchanger ( heater , cooler ) 2- Distillation column 3- Reactor 4- Pump design 5- Compressor

  3. Heat Exchanger Design Objectives: For E-104: - To increase the temperature For E-103: - To decrease the temperature

  4. Assumptions: - Use shell and tube heat exchanger. - Assume the refrigent inter in tube side in cooler and steam in heater The value of the overall heat transfer coefficient was assumed to be: - For (E-103) = 300 w/m^2C. - For (E-104) = 900 w/m^2C. - For E-103 refrigent inlet temperature (t1) = -10 C refrigent outlet temperature (t2) = 35 C -For E-104 Steam inlet temperature (t1) = 200 C Steam outlet temperature (t2) = 70 C

  5. Main design procedures: Main design procedure: Calculate the duty or heat load. Where, m: mass flow rate, kg/hr Cp: specific heat, kJ/kg°C ∆T: temperature difference, °C Collect physical properties.

  6. -Calculate Log mean Temperature Where, DTm = Ft DTlm. ∆Tlm : log mean temperature difference. T1 : inlet shell side fluid temperature. T2 : outlet shell side temperature fluid temperature. t1 : inlet tube side fluid temperature . t2 : outlet tube side fluid temperature. -Assume U : overall heat transfer coefficient, W/m2oC -Calculate heat transfer area required.

  7. - Calculate area of one tube, m2. Where -Outer diameter (do), (mm) -Length of tube (L), (mm) - Calculate number of tubes = provisional area / area of one tube

  8. - Calculate bundle diameter. Where - Outside diameter (mm). - Number of tubes. - K1 & n1 are constant.

  9. - Calculate shell diameter. Ds = Db + Bundle diametrical clearance - Find tube side heat transfer coefficient hi, W/m2°C - Find shell side heat transfer coefficient ho, W/m2°C

  10. Calculate U overall heat transfer coefficient using: Where : - Uo : overall coefficient based on outside area of the tube ,w/m^2.C - ho : outside fluid film coefficient, w/m^2.C, from Table (12.2) - hi : inside fluid film coefficient ,w/m^2, from Table (12.2) - hod : outside dirt coefficient (fouling factor) ,w/m^2.C - hid : inside dirt coefficient (fouling factor),w/m^2.C - kw : thermal conductivity of the wall material w/m.Cs for cupronickel - di : tube inside diameter m - do : tube outside diameter m

  11. -Calculate tube and shell side pressure drop. - Calculate Shell thickness. Where - t: shell thickness (in). - P: internal pressure (psig). - ri: internal radius of shell (in). - EJ: efficiency of joints. - S: working stress (psi). - Cc: allowance for corrosion (in).

  12. Results

  13. Distillation ColumnT-(102) design Objective : To separate TBHP from t-Butanol Assumptions 1. Tray column. 2. Sieve plate. 3. Material of the distillation is carbon steel. 4. Plate spacing= 0.6 m 5. Efficiency = 50% 6. Flooding % = 85% 7. Weir height = 50 mm 8. Hole diameter = 5 mm 9. Plate thickness =5 mm

  14. Main design procedures: 1) Actual number of stages = (hysys number stages/η) 2) FLV= ( Lw / Vw)*( ρv / ρL)^.5 Where:- Lw: liquid flow rate ρL: liquid density Vw: vapor flow rate, ρv :vapor density FLv: liquid-vapor flow factor 3) Find K1 (Top) & K1 (Bottom) from fig. K1correction = (σ/0.02)^.2*K1 Where:- σ: Surface tension

  15. 4)Uf (bottom)= K1 ((ρL- ρv)/ ρv) 0.5 Uf (Top) = K2 ((ρL- ρv)/ ρv) 0.5 Where: Uf : flooding vapor velocity K1: constant obtained from figure 5) uv = uf * x Where:- Uv : maximum velocity X : percentage of flooding at max flow

  16. 6) Max flow-rate = (Lw*Mwt / ρL*3600) Where:- Max.: Maximum Volumetric Flow rate. Lw: liquid flow rate ρL: liquid density M.wt: molecular weight 7) Anet = Mmax/uv Where:- Anet: Net area required 8) Ad = An/(1-y*10^-2) Where: Ad: down comer area

  17. 9) D =(Ad*4/(3.14))^.5 Where:- D: column diameter 10) H= (Tray spacing * actual NO. stage ) + D Where:- H: Column height 11) MVL =(Lbottom*Mwt)/(3600* ρL) Where:- MVL: maximum volumetric liquid rate

  18. 12) Ac = (3.14/4)*D^2 Ad = 0.12Ac An = Ac-Ad Aa = Ac-2Ad Ah take %10 Aa as first trial = %10*Aa Where: - Ac: column area Aa: active area Ah: hole area Ad= Downcomer area

  19. 13)max Lw = Lw*Mwt/3600 min Lw @ % turn down = %*max Lw max how =750 (max Lw/ρL*wierlength)^(2/3) min how =750 (min Lw/ ρL*wierlength)^(2/3) actual minimum vapor = vapor rate min/Ah Where:- max Lw: maximum liquid rate. min Lw : minimum liquid rate.

  20. 14) The actual min vapor velocity = vapor rate min/An 15) uh = Vw max/Ah hr = 12.5E+03/ ρL Where:- uh: maximum vapor velocity through holes max.Vw: maximum volumetric flow rate hd: dry plate drop hr: Residual head

  21. Aap= wier length*hap • hdc= 166*(max liquid flowrate/ ρL*Aap)^2 • hb= Minimum rate (hw + how) + ht + hdc • Where:- • Aap: Area under arpon • hdc: head losses in the down comer • tr= • Where : • tr : residence time , should be > 3 s

  22. 18) Percent flooding = Where :- uv: vapor velocity, uf: flooding vapor velocity 19) Number of holes Area of one hole = (π/4)*(hole diameter^2) Total number of holes = Ah / area of one hole Holes on one plate = total Number of holes/number of stages

  23. 20) Area of condenser& reboiler = Q/(U*∆T) 21) Thickness = [(ri P)/(Ej S-0.6P)]+Cc Where:- ri = Inside radius of the shell P =Maximum allowable internal pressure S = Maximum allowable working stress EJ = Efficiency of joints Cc = Allowance for corrosion

  24. Reactor Design Objectives: - R-101: To produce TBHP from Isobutane and oxygen. (CH3) 3 CH + O2 → (CH3)3COOH

  25. Assumptions: -The limiting reactant is (CH3) 3CH in the R-101 reactor . -The conversion equal to 0.24 in the R-101 reactor

  26. Main design procedures: 1.Find Volume: V=(Fao-Fa)/-ra = (Fao-Fa)/kCao(1-X) Where Fao : inlet mass flow Fa : outlt mass flow K : kinetic rate Cao : density*Fao/total mass flow rate X : conversion

  27. 2. Find diameter of reactor Volume = PI * (D/2)^2 * H = PI * D^3 Where H = 4D D = (V/PI)^1/3 3. Calculate the height of reactor: Height of reactor (H) = 4 * Diameter Total height of reactor = 0.5 + 0.5 + H+ 2 (D/2)

  28. 4. Calculate the thickness Where, t is thickness in inch P is internal pressure in psig, ri is the radius of the reactor, in, S is the stress value of carbon steel (S=13700 psia), Ej is the joint efficiency (Ej=0.85 for spot examined welding), Cc is the corrosion allowance (Cc=1/8 in) 6. Calculate cost from www.matche.com

  29. Compressor Design Objectives: -To increase gases pressure.

  30. Main design procedures: • 1.Calculate the compression factor (n) using the following equation: Where, P1,2 : is the pressure of inlet and outlet respectively (psia) T1,2 : is the temperature of the inlet and outlet respectively (R)

  31. 2. Calculate the work done in Btu/lbmol by: Where, R is the ratio of the specific heat capacities (Cp/Cv) 3. Calculate the horse power, Hp using the following equation: Hp=W*M Where, M is the molar flow rate in lbmol/s 4. Calculate the efficiency of the compressor using the following equation:

  32. Where , Mw :is the molecular weight of the gas in the stream CP :is the specific heat capacity (Btu/lb◦ F ) 5. Calculate the cost of the compressor from www. Matche . com

  33. Pump Design • Assumptions: • Centrifugal pump. • Design procedures: • 1.Calculate the flow rate • m= ρ *Q • 2.Calculate the work shift • Ws = -ha * g • 3.Assume efficiency ζ.

  34. 4.Calculate the Brake horse power • = (-Ws * m) / (ζ * 1000) • 5.Calculate the diameter, d. • Where, • ∆P is the pressure difference between the inlet and outlet streams in kpa • Q: flow rate kg/s • ρ: the density of the fluid kg/m3 • μ: viscosity cp • D: pipe diameter mm 6. Calculate the cost of the compressor from www. Matche . com

  35. Thank you for listening

More Related