Designer: Mohammed Albannay Supervised by: Prof.M.Fahim ENG: Yousif Ismail

Table of content Distillation column design. Reactor design. Pump design. Compressor design. Heat exchanger design.

Distillation Column design Objective : T-100 :Separates Propylene from PO, EB, MBA, & ACP. T :Separates styrene from water

Assumptions 1-Tray spacing= 0.6 m 2-Percent of flooding at maximum flow rate=85% 3- Percent of down comer area of total area=12% 4- The hole area =10% the active area. 5-weir height=50 mm 6-Hole diameter=5 mm 7-Plate thickness=5 mm 8-Turndown percentage=70%

For column diameter 1-calculate the liquid –vapors flow factor for top and bottom FLV= Lw / Vw * (ρv / ρl) ½ Where:- LW = liquid mole flow rate in kmol /h Vw = vapors mole flow rate in kmol / h ρv = density of the vapors in kg / m³ ρl = density of the liquid in kg / m³ Main design procedures:

2-from fig get constant for the top and the bottom  top k1 and bottom k1 (FLV, tray spacing ) 3-calculate the correction factor for top and the bottom K = (σ / 0.02) ^0.2 * K1 Where:- σ = liquid surface tension in N/m 4-calculate the flooding velocity for top and bottom Uf = K *( (ρl –ρV) / ρV)½ Where:- Uf = flooding vapour velocity in m/s K= constant obtain from fig ρl = density of liquid in kg / m³ ρv = density of vapour in kg / m³

5-Assume the flooding percentage is 85% at max flow rate for the top and the bottom UV = 0.85 * Uf 6-calculate the net area for the top and the bottom An = V / UV Where: An = net area in m² V = Volumetric flow rate in m³ / s UV = vapour velocity in m/s Volumetric flow rate for top and bottom : V=(Vw*Mwt )/ ρv

7-Assume as first - trail take down comer as 12% of total cross sectional area for the top and the bottom Ad = An / 0.88 Where: Ad = area of the down comer in m² An = net area in m² 8-calculate the diameter for the top and the bottom D = ((4 /3.14) * Ad) ½ Where: D = Diameter in m Ad = area of the down comer in m² 9- We take the maximum column diameter (top or bottom)

11-calculate the liquid flow pattern Max liquid volumetric flow rate = (Lm *MW) / (ρL * 3600) 12-calculate the areas Ac = (3.14 / 4)*D² Where: Ac = total cross sectional area in m² Ad = 0.12 * Ac Where: Ad = area of the down comer in m² 10- we calculate Total height : Total height = (actual no. of stage * tray spacing )+2 Note : From fig we have double pass plate

An =Ac –Ad Where: An = net area in m² Aa = Ac – 2Ad Where: Aa = active area in m² Ah = 0.1 * Aa Where: Ah = hole area in m²

13- Use fig to get L W / D  from 14-Assume weir length Lw = 50 mm Hole diameter dh = 5 mm Plate thickness = 5 mm 14-Check weeping h ow max = 750 * (L wd / (L W *ρl)) ^2/3 h ow min = 750 * (L wd / (L W *ρl)) ^2/3 At min rate = Lw + h ow min Where:- h ow =Weir liquid crest 15-calculate the weep point Where: U h = min vapor velocity through the hole in m/s dh = hole diameter in m K2 = constant from fig (At min rate) U h = k *(25.4-dh)/ρv½ (A d /A c )*100

16-calculate the actual vapour velocity Calculate the actual vapour velocity = min vapour rate / Ah 17-Calculate plate pressure drop U H = Vv / Ah Where: UH = max. vapor velocity through holes m/s Vv = volumetric flow rate in m³ / s (bottom) Ah = hole area in m² Actual vapor velocity should be >U h

HD = 51 * (Uh/ C 0 )² * ρ V / ρ L Where: HD = dry plate drop Uh = min vapour velocity in m/s Hr = 12.5E3 / ρL Where: Hr = residual head Ht = HD + L w + h OW max + Hr Where: Ht = total pressure drop in mm For C o :from fig )Plate thickness /dh 2)Ah/Ap=Ah/Aa

18-down comer liquid backup Hap = L W – 10 Aap = L W * Hap *0.001 Where: Aap = area of apron Lw = weir length Hdc = 166 * (L Wd max / (ρl * Aap))^2 Backup down comer Hb = Hdc + Ht + h ow max + L w Head losses in down comer

19-Calculate the residence time tr = (Ad * Hb * ρl) / Lwd max 19-Calculate the flooding percentage Flooding percentage = U V / uf (bottom) * Calculate the area of the hole A = (3.14 / 4 ) * (dh * )² 21-Calculate number of hole Number of hole = Ah / A U V =vol. flow rate bottom/ An tr should be > 3 s

22-Calculate the thickness, Where: t: thickness of the separator in (in) P: operating pressure in Pisa ri: radius of the separator in (in) S: is the stress value of carbon steel = Pisa Ej: joint efficiency (Ej=0.85 for spot examined welding) C0: corrosion allowance = calculate the cost

Distillation column design Cost estimation: where, H: column height V: volume of the column M: mass of the column

Distillation Column Equipment Name Separates Propylene from PO, EB, MBA, & ACP.Objective T-101Equipment Number Mohammed albannayDesigner Tray columnType Epoxidation of Ethyl benzene Hydroperoxide sectionLocation Carbon steelMaterial of Construction miniral woolInsulation Cost ($) Column Flow Rates Recycle (kgmole/hr)1129.1Feed (kgmole/hr) 284.1Bottoms (kgmole/hr)844.96Distillate (kgmole/hr) Key Components Propylene oxideHeavy Propylene Light

Dimensions 22Height (m)4.18Diameter (m) 4Reflux Ratio33Number of Trays sieveType of tray0.6Tray Spacing -Number of Caps/Holes53017Number of Holes Cost Trays400000Vessel 30000Reboiler40000Condenser Unit

Distillation ColumnEquipment Name Separates styrene from waterObjective T-103-2Equipment Number Mohammed albannayDesigner tray columnType Styrene production sectionLocation Carbon steelMaterial of Construction miniral woolInsulation Cost ($) Column Flow Rates Recycle (kgmole/hr) 697.4Feed (kgmole/hr) Bottoms (kgmole/hr) 191.3Distillate (kgmole/hr) Key Components M-PH-ketonHeavystyreneLight

Dimensions 6Height (m)2.48Diameter (m) 0.624Reflux Ratio7Number of Trays sieveType of tray0.6Tray Spacing -Number of Caps/Holes70248Number of Holes Cost Trays50000Vessel 32000Reboiler27900Condenser Unit

Reactor Design Objectives: Epoxidation of ethyl benzene hydroperoxide to Propylene oxide and MBA SymbolSpecies EBHPC 6 H 5 CH(CH 3 )OOH PropyleneCH 3 CHCH 2 POCH 3 CHOCH 2 MBAC 6 H 5 CH(CH 3 )OH

-The limiting reactant is ethyl benzene hydroperoxide For CRV-101 CSTR Reactor. Assumptions:

1.Design equation for CSTR : Where : FAo : entering molar flow rate mol/h X : conversion of EBHP ( ethyl benzene hydroproxide ) V : volume of CSTR m3 rA : rate of reaction Main design procedures:

2.Define rate law : Where: rA = rate of reaction. CA = outlet concentration mol/m3 K = Arrhenius constant h-1

3. Taking Pseudo first order equation: (internet) Where : X : conversion of EBHP ( ethyl benzene hydroproxide ) K : Arrhenius constant. t : time in h

4. Use stoichiometric relationships and feed specifications to express the rate law as a function of conversion Where CA : outlet concentration mol/m3 CAo : entering concentration mol/m3 X : conversion of EBHP ( ethyl benzene hydroproxide ) FAo : entering molar flow rate mol/h Qo : entering volumetric flow rate m3/h

3. Calculate the Volume of reactor after combining : 4.For thickness calculation : For radius ri = D/2 L=4D 5.Height of reactor :

5. Calculate the thickness Where, t is thickness in inch P is internal pressure in psig, r i is the radius of the reactor, in, S is the stress value of stain steel (S= 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

ReactorEquipment Name Epoxidation of ethyl benzene hydroperoxideObjective CRV-101Equipment Number Mohammed AlbannayDesigner CSTRType Propylene Epoxidation sectionLocation Stain steelMaterial of Construction miniral woolInsulation

Operating Condition Volume of Reactor (m 3 )115Operating Temperature ( o C) -Catalyst Type320Operating Pressure (psia) -Catalyst Density (Kg/m 3 )184.87Feed Flow Rate (mole/s) -Catalyst Diameter (m)99.9Conversion (%) 25.9Reactor Height (m)-Weight of Catalyst (Kg) 6.48Reactor Diameter (m)-Number of Beds 0.028Reactor Thickness (m)-Height of Bed/s (m) Cost ($)25.9Height of Reactor (m)

Pump Design Objective :  Increase liquid pressure of ACP & MBA fed to CRV Assumptions:-  Centrifugal pump

Pump Design Design procedures:- 1.Calculate the actual head (ft) P1:inlet pressure( lb/ft2 ) P2:outlet pressure( lb/ft2 ) : specific weight (Ib/ft) =mass density(Ib/ft3)*gravity(ft2/sec) 2- calculate Water hourse power: 3- Overall Efficiency:

pumpEquipment Name Increase liquid pressure of ACP & MBA fed to CRV Objective P-101-2Equipment Number Mohammed AlbannayDesigner Centrifugal PumpType Styrene production section Location Carbon steelMaterial of Construction miniral woolInsulation 5832Cost Operating Condition 176.9Outlet Temperature ( o C)176.9Inlet Temperature ( o C) 3.867Outlet Pressure (psia)2.5Inlet Pressure (psia) Power (Hp)0.75Efficiency (%)

PumpEquipment Name Increase liquid pressure of ACP & MBA fed to CRV-101-2Objective P-102-2Equipment Number Mohammed AlbannayDesigner Centrifugal Pump Type Styrene production sectionLocation Carbon steelMaterial of Construction miniral woolInsulation 25164Cost Operating Condition 82.51Outlet Temperature ( o C)82Inlet Temperature ( o C) 400Outlet Pressure (psia)1.547Inlet Pressure (psia) 25.9Power (Hp)0.75Efficiency (%)

Compressor : Objective:  K-103 Increase Pressure of propylene fed to CRV  K-104 :Increase Pressure of stream fed to T-103 Assumptions: type of compressor : Reciprocating

Main procedure: 1- ratio of spesific heat of gas at constant pressure to spesific heat of gas at constant volume(K). P1=inlet pressure,Ibf/ft^2 P2=inlet pressure,Ibf/ft^2 T1=inlet temperature, R T2=inlet temperature, R

2- calculate power(ft.Ibf/Ibm) V1:spesific volume of gas at intake condision,ft^3/Ibm

3- calculate horse power(hp) qfm1:cubic feet of gas per minute at intake condition,ft^3/min 4-Ep=effeciency of the compressor. Hp/760

CompressorEquipment Name Increase Pressure of propylene fed to CRV-101Objective K-103Equipment Number Mohammed AlbannayDesigner CentrifugalType Epoxidation of Ethyl benzene Hydroperoxide sectionLocation Carbon steelMaterial of Construction miniral woolInsulation Cost Operating Condition 233.7Outlet Temperature ( o C)68.98Inlet Temperature ( o C) 320Outlet Pressure (psia)14.7Inlet Pressure (psia) Power (Hp)0.8Efficiency (%)

CompressorEquipment Name Increase Pressure of stream fed to T-103Objective K-104Equipment Number Mohammed AlbannayDesigner centrifugalType Epoxidation of Ethyl benzene Hydroperoxide sectionLocation Carbon steelMaterial of Construction miniral woolInsulation Cost Operating Condition 171Outlet Temperature ( o C)100Inlet Temperature ( o C) 440Outlet Pressure (psia)133Inlet Pressure (psia) Power (Hp)0.8Efficiency (%)

Heat Exchanger Design (cooler) Objective E-109 :Increase Temperature of stream fed to T-103 E-117 :Decrease Temperature of stream fed to V-100 E-111 :Increase Temperature of stream fed to T-105 E-112 :Increase Temperature of stream fed to T-105

Assumptions 1-Assume a counter current flow heat exchanger because it provides more effective heat transfer. 2-The value of the overall heat transfer coefficient was assumed in the shell and tube heat exchanger design. 3-Assume the outer, the inner diameter and the length of the tube on both the Shell and tube heat exchanger design.

Design Procedures (A) Shell & Tube heat exchanger 1)Calculate Heat Load Q=Heat Load= m*cp*(T2-T1) Where: m= mass flow rate ( Kg/h) cp= Heat capacity ( KJ/kg°C) T2= inlet temperature of shell side°C T1= outlet temperature of shell side°C

2) Calculate Log mean Temperature difference ∆Tlm= ((T1-t2) – (T2-t1))/ln((T1-t2)/ (T2-t1)) where: ∆Tlm: Log mean temperature difference°C. T1 : Inlet shell side fluid temperature°C T2 : Outlet shell side fluid temperature °C t1 : Inlet tube side temperature°C t2: Outlet tube side temperature°C

3) Calculate the two dimensionless temperature ratios: R= (T1-T2)/(t2-t1) S = (t2-t1)/(T1-t1) Where: T1 : Inlet shell side fluid temperature T2 : Outlet shell side fluid temperature t1 : Inlet tube side temperature t2: Outlet tube side temperature

4) From Figure determine Ft by using R and S ratios Where : Ft : temperature correction factor. 5) Calculate True temperature difference ∆Tm= Ft *∆Tlm 6) Choose U from table depending on the type of flows in shell and tube sides. Where: U: Over all heat transfer coefficient.

7) Calculate provisional area 8) Assume inlet tube diameter, outlet tube diameter, and tube length.

9) Calculate area of one tube A = 3.14*L*do*10-3 Where: L: Tube length ( m) do: outlet diameter (mm) 10) Define number of tubes Nt=( Provisional Area / Area of one tube ) 11) Calculate bundle diameter Db=Do(Nt/K1)(1/n1) Where: Db: bundle diameter (mm). Do: tube outer diameter (mm). Nt: number of tubes. K1 and n1 are constants using triangle pitch of 1.25.

12) From Figure determine bundle diametrical clearance.

13) Calculate shell diameter Ds = Db+Dc Where: Db : bundle diameter( mm). Dc : clearance diameter( mm). 14) For Tube side coefficient calculate: - Mean temperature =((t1+t2)/2) - Tube cross sectional area A= (3.14/4)*di^2

- Tubes per pass = (Nt/assumed pass) - Total Flow area = (Tubes per pass * A) Where: A : Tube cross sectional area, m2 - mass velocity = (m/ Total Flow area) Where: m : mass Flow rate Tube side, kg/s - Linear velocity ut= (mass velocity/ ρ) Where: ρ : Tube Flow density, kg/m3

Tube side Heat Transfer Cofficient: Where: hi : Tube inside coefficient, W/m2°C. t : Mean temperature ( °C). ut : Linear velocity ( m/s). di : Tube inside diameter ( mm).

15) For Shell side coefficient calculate: - baffle spacing = (Ds/5) - Tube pitch = 1.25 * do - As = ((pt – do)*DslB/pt) Where: As : Cross Flow area, m2 pt : tube pitch lB : baffle spacing, m

. 16) Calculate over all coefficient 1/Uo= (1/ho)+(doln(do/di)/(2kw))+(do/di)(1/hi) where Uo: overall heat transfer coefficient hi: the tube side heat transfer coefficient ho: the shell side heat transfer coefficient do: outer diameter di: inner diameter Kw: wall thermal conductivity

Pressure drop for shell and tube side: Where; Np is the number of passes of tubes. jf is friction factor. ΔP is the pressure drop (Pa).

18) Thickness: (t) = ((Pri)/(SEj-0.6P)) + Cc Where : P: maximum internal pressure, kPa ri: inside radius of shell, m(ri=D/2) Ej: efficiency of joints as a fraction S: maximum allowable stress(for carbon steel), kPa Cc: allowance for corrosion, m

CoolerEquipment Name Decrease Temperature of stream fed to V-100 Objective E-117Equipment Number Mohammed AlbannayDesigner Shell and tube heat exchanger Type Ethyl benzene oxidation sectionLocation WaterUtility Carbon steelMaterial of Construction miniral woolInsulation 32400Cost ($) Operating Condition Shell Side 25Outlet temperature ( o C)141.1Inlet temperature ( o C) Tube Side 30Outlet temperature ( o C)10Inlet temperature ( o C) 16911Number of Tubes8Number of Tube Rows 1.057Shell Diameter (m)1.049Tube bundle Diameter (m) 47.99LMTD ( o C)7.827e7Q total (Btu/hr) Heat Exchanger Area (m 2 )17.6U (Btu/hr. o F. ft 2 )

HeaterEquipment Name Increase Temperature of stream fed to T-103Objective E-109Equipment Number Mohammed AlbannayDesigner Shell and tube heat exchanger Type Epoxidation of Ethyl benzene Hydroperoxide sectinoLocation SteamUtility Carbon steelMaterial of Construction miniral woolInsulation 27000Cost ($) Operating Condition Shell Side 100Outlet temperature ( o C)17.142Inlet temperature ( o C) Tube Side 80Outlet temperature ( o C)150Inlet temperature ( o C) 226Number of Tubes1Number of Tube Rows 2.9Shell Diameter (m)2.8Tube bundle Diameter (m) 49.3LMTD ( o C)1.025e7Q t ota l (Btu/hr) 299.5Heat Exchanger Area (m 2 )105.6U (Btu/hr. o F. ft 2 )

HeaterEquipment Name Increase Temperature of stream fed to T-105Objective E-111Equipment Number Mohammed AlbannayDesigner Shell and tube heat exchanger Type Epoxidation of Ethyl benzene Hydroperoxide sectionLocation SteamUtility Carbon steelMaterial of Construction miniral woolInsulation 21600Cost ($) Operating Condition Shell Side 147.3Outlet temperature ( o C)87.37Inlet temperature ( o C) Tube Side 170Outlet temperature ( o C)250Inlet temperature ( o C) 288Number of Tubes2Number of Tube Rows 2.5Shell Diameter (m)2.4Tube bundle Diameter (m) 78.3LMTD ( o C)1.463e7Q t ota l (Btu/hr) 226.3Heat Exchanger Area (m 2 )88U (Btu/hr. o F. ft 2 )

HeaterEquipment Name Increase Temperature of stream fed to T-105Objective E-112Equipment Number Mohammed AlbannayDesigner Shell and tube heat exchanger Type Epoxidation of Ethyl benzene Hydroperoxide sectionLocation SteamUtility Carbon steelMaterial of Construction miniral woolInsulation 20520Cost ($) Operating Condition Shell Side 164.7Outlet temperature ( o C)147.3Inlet temperature ( o C) Tube Side 90Outlet temperature ( o C)120Inlet temperature ( o C) Number of Tubes3Number of Tube Rows 1.9Shell Diameter (m)1.8Tube bundle Diameter (m) 91.79LMTD ( o C)7.341e6Q t ota l (Btu/hr) Heat Exchanger Area (m 2 )88U (Btu/hr. o F. ft 2 )