Technological Institute of the Philippines

PRODUCTION OF BENZYL
ALCOHOL VIA
HYDROGENATION OF
BENZALDEHYDE

OVERALL ENERGY
BALANCE

Members (Group 5)

Ayuson, Jeremy Franceska D.

Pasag, Shaira Marie E.

Relacion, Zhydrell D.

Salvador, Nehemiah Gabriel B.

 Technological Institute of the Philippines

PRODUCTION OF BENZYL ALCOHOL VIA HYDROGENATION OF

BENZALDEHYDE

LIST OF NOMENCLATURE

ENERGY BALANCE

Table. 1.1 List of Nomenclature for Material Balance

Symbol Description Conventional

Unit

m Mass Flow Rate kg/day

n Molar Flow Rate kmol/day

o
T Temperature C

P Pressure kPa

Cp Heat Capacity at k𝐽 𝑘𝑚𝑜𝑙- oC -1

Constant Pressure

QT Total Entalphy kJ d-

QFeed Enthalpy of Feed kJ d-

Stream

QProduct Enthalpy of Product kJ d-

Stream

∆𝐻f Heat of Formation 𝑘𝐽 𝑘𝑚𝑜𝑙-1

∆𝐻𝑟𝑥𝑛◦ Standard Enthalpy of 𝑘𝐽 𝑘𝑚𝑜𝑙-1

Reaction
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∆𝐻𝑠𝑜l Heat of Solution 𝑘𝐽 𝑘𝑚𝑜𝑙-1

∆𝐻𝑣𝑎𝑝, λ Enthalpy of 𝑘𝐽 𝑘𝑚𝑜𝑙-1

Vaporization

∆𝐻R Residual Enthalpy 𝑘𝐽 𝑘𝑚𝑜𝑙-1

Table. 1.2 Physical Properties of the Components

Component Formula Molar Mass

kg/kmol

Benzyl Alcohol C7H8O 108.14

Hydrochloric Acid HCl 36.458

Water H2O 18.01528

Benzene C6H6 78.11

Carbon Dioxide CO 28.01

Benzaldehyde C7H6O 106.12

Aluminum Chloride AlCl3 133.34

Sodium Hydroxide NaOH 39.997

Activated Carbon C 12.08

Hydrogen Gas H2 2.014

Rhodium Rh 102.9055
 Technological Institute of the Philippines

EQUIPMENT Benzaldehyde OPERATING 50oC

NAME Fluidized Reactor TEMPERATURE
EQUIPMENT R-101 OPERATING 1 bar
CODE PRESSURE
PROCESS Benzaldehyde is produced through the reaction of benzene, and
DESCRIPTION carbon dioxide
 Technological Institute of the Philippines

Stream Conditions
Stream T, oC P, bar
Stream 2-6 45 1
Stream 7,8 50 1

Enthalpy Balance:

QT = QFeed + n∆H rxnO + Qproduct

Heat Capacity Constants of Components in R-101

*Reference: Yaws, C.L. Chemical Properties Handbook

QFeed:

Hydrogen Chloride:

QHCl = nHCl CpHCl ∆T

QHCl = (29.18994496 J mol-1 oC -1 ) x ( 14.87473716 kmol d-1) x (50-45) oC

QC6H6 = 2170.963795 kJ d-1

Benzene:

QC6H6 = nC6H6 CpC6H6 ∆T

QC6H6 = (193.6165724 kmol d-1) x (20.07419434 J mol-1 oC -1) x (50-45)oC

QC6H6 = 19433.48351 kJ d-1

Carbon Monoxide:

QCO = nCO CpCO ∆T

QCO = (193.6264875 kmol d-1) x (29.29952684 J mol-1 oC -1) x (50-45)oC

QCO = 28365.82234 kJ d-1

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Aluminum Chloride:

QAlCl3 = n AlCl3 Cp AlCl3 ∆T

Q AlCl3 = (6.805533947 kmol d-1) x (91.12 J mol-1 oC -1) x (50-45)oC

Q AlCl3 = 3100.601266 kJ d-1

QProduct:

Hydrogen Chloride:

QHCl = nHCl CpHCl ∆T

QHCl = (29.18433285J mol-1 oC -1 ) x ( 14.87473716 kmol d-1) x (50-45) oC

QHCl = 2170.546402 kJ d-1

Benzene:

QC6H6 = nC6H6 CpC6H6 ∆T

QC6H6 = (63.50623577 kmol d-1) x (25.0115375 J mol-1 oC -1) x (50-45)oC

QC6H6 = 7941.942987 kJ d-1

Carbon Monoxide:

QCO = nCO CpCO ∆T

QCO = (63.5094879 kmol d-1) x (29.27577576 J mol-1 oC -1) x (50-45)oC

QCO = 9296.447632 kJ d-1

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (130.1120953kmol d-1) x (104.032525J mol-1 oC -1) x (50-45)oC

QC7H6O = 67679.44903 kJ d-1

Aluminum Chloride:

QAlCl3 = n AlCl3 Cp AlCl3 ∆T

Q AlCl3 = (6.805533947 kmol d-1) x (91.12 J mol-1 oC -1) x (50-45)oC

 Technological Institute of the Philippines

Q AlCl3 = 3100.601266 kJ d-1

n ∆Hrxno:

Composition Heat of Formation

CO -110.54
C6H6 82.93
C7H6O -36.8

CO + C6H6 → C7H6O

∆H (kj mol-1) = product - reactant

∆H = -36.8 kj mol-1 – (-110.54 kj mol-1+ 82.93 kj mol-1) (1000)

∆H = -9190 kj kmol-1

Qreaction = ∆H x limiting reactant

Qreaction = (-9190 kj kmol-1 ) x (193.6165724 kmol d-1)

Qreaction = -1779336.301 kJ d-1

Qtotal:

Qtotal = Qproduct + QFeed + Qrxn

Qtotal = ( 53070.87091 kj kmol-1 ) + ( 90188.98731 kj kmol-1 ) + (-1779336.301 kj

kmol-1)

Qtotal = -1636076.443 kj kmol-1

Cooling Duty:

Assuming 5% loss

Qreq’d = Qtotal x 1.05

Qreq’d = -1636076.443 kj kmol-1 x 1.05

Qreq’d = -1717880.265

Cooling Water Requirement

 Technological Institute of the Philippines

Operating Conditions of Cooling Water

Inlet Temperature 30oC 303.15 K

Outlet Temperature 50 oC 323.15 K
Pressure 1 bar 1 bar
Qreq’d = QCw = mCp∆T

1717880.265 = mw (4.184 kJ kg-1 -K-1) x (323.15 K - 303.15 K)

mw = 20529.16186 kg d-1
 Technological Institute of the Philippines

EQUIPMENT HCl PRE- OPERATING 100oC

NAME HEATER TEMPERATURE
EQUIPMENT HX-101 OPERATING 3 bar
CODE PRESSURE
PROCESS To pre-heat the hydrochloric acid solution.
DESCRIPTION

Stream Conditions
Stream T, oC P, bar
Stream 1 30 1
Stream 2 90 1

Enthalpy Balance:

QT = QFeed + Qproduct

Heat Capacity Constants of Components in HX-101

*Reference: Yaws, C.L. Chemical Properties Handbook

QFeed:

Hydrogen Chloride:

QHCl = nHCl CpHCl ∆T

QHCl = (29.207296 J mol-1 oC -1 ) x ( 14.87473716 kmol d-1) x (90-30) oC

QHCl = 950430.7492 kJ d-1

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QProduct:

Hydrogen Chloride:

QHCl = nHCl CpHCl ∆T

QHCl = (29.1430027 J mol-1 oC -1 ) x ( 14.87473716 kmol d-1) x (90-30) oC

QHCl = 948338.5892 kJ d-1

Q T:

QT = (950430.7492 kJ d-1 + 948338.5892 kJ d-1)

QTotal = 1898769.338 kJ d-1

Heating Duty:

Assuming 5% loss

Qreq’d = Qtotal x 1.05

Qreq’d = 1898769.338 kJ d-1 x 1.05

Qreq’d = -1993707.805 kJ d-1

Heating Water Requirement

Operating Conditions of Heating Water

Inlet Temperature 70oC 343.15 K

Outlet Temperature 90 oC 363.15 K
Pressure 1 bar 1 bar
Qreq’d = QCw = mCp∆T

-1993707.805 kJ d-1 = mw (4.184 kJ kg-1 -K-1) x (363.15 K - 343.15 K)

mw = 23825.38008 kg d-1
 Technological Institute of the Philippines

EQUIPMENT PRE-HEATER OPERATING 179oC

NAME TEMPERATURE
EQUIPMENT HX-102 OPERATING 1 bar
CODE PRESSURE
PROCESS To heat the solution in preparation for the evaporator.
DESCRIPTION

Stream Conditions
Stream T, oC P, bar
Stream 8 50 1
Stream 9 179 1

Enthalpy Balance:

QT = QFeed + Qproduct

Heat Capacity Constants of Components in HX-102

*Reference: Yaws, C.L. Chemical Properties Handbook

 Technological Institute of the Philippines

QFeed:

Benzene:

QC6H6 = nC6H6 CpC6H6 ∆T

QC6H6 = (63.50623577 kmol d-1) x (25.0115375 J mol-1 oC -1) x (179-50)oC

QC6H6 = 204902.1291 kJ d-1

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (130.1120953kmol d-1) x (104.032525 mol-1 oC -1) x (179-50)oC

QC7H6O = 1746129.785 kJ d-1

Aluminum Chloride:

QAlCl3 = n AlCl3 Cp AlCl3 ∆T

Q AlCl3 = (6.805533947 kmol d-1) x (91.12 J mol-1 oC -1) x (179-50)oC

Q AlCl3 = 79995.51267 kJ d-1

QProduct:

Benzene:

QC6H6 = nC6H6 CpC6H6 ∆T

QC6H6 = (63.50623577 kmol d-1) x (108.1438371 J mol-1 oC -1) x (179-50)oC

QC6H6 = 885947.2344 kJ d-1

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

 Technological Institute of the Philippines

QC7H6O = (130.1120953kmol d-1) x (154.3581779 mol-1 oC -1) x (179-50)oC

QC7H6O = 2590818.707 kJ d-1

Aluminum Chloride:

QAlCl3 = n AlCl3 Cp AlCl3 ∆T

Q AlCl3 = (6.805533947 kmol d-1) x (91.12 J mol-1 oC -1) x (179-50)oC

Q AlCl3 = 79995.51267 kJ d-1

∆Hvap:

Benzaldehyde:

QC7H6O = nC7H6O ∆H

QC7H6O = 51114.31849x 130.1120953 kmol d-1

QC7H6O = 6650591.078 kJ d-1

Benzene:

QC6H6 = nC6H6 ∆H

Q C6H6 = 41360.66217x 63.50623577 kmol d-1

Q C6H6 = 2626659.964 kJ d-1

Qtotal:

Qtotal = Qproduct + QFeed + Qvap

Qtotal = ( 1951031.914 kj kmol-1 ) + ( 3556761.454 kj kmol-1 ) + (9264117.741 kj

kmol-1)

Qtotal = 14785044.41 kj kmol-1

Heating Duty:
 Technological Institute of the Philippines

Assuming 5% loss

Qreq’d = Qtotal x 1.05

Qreq’d = 14785044.41 kJ d-1 x 1.05

Qreq’d = 15524296.63 kJ d-1

Heating Steam Requirement

Operating Conditions of Heating Steam

Inlet Temperature 170 443.15 K

Outlet Temperature 185 458.15 K
Pressure 2.02 bar 2.02 bar
Qreq’d = QCw = mCp∆T

15524296.63 kJ d-1 = mw (4.184 kJ kg-1 -K-1) x (458.15 K - 443.15 K)

mw = 21825.85849 kg d-1
 Technological Institute of the Philippines

EQUIPMENT CATALYST OPERATING 179oC

NAME EVAPORATO TEMPERATURE
R
EQUIPMENT E-101 OPERATING 1 bar
CODE PRESSURE
PROCESS To filter AlCl from the reaction.
DESCRIPTION

Stream Conditions
Stream T, oC P, bar
Stream 9 179 1
Stream 10 179 1
Stream 11 179 1

Enthalpy Balance:

QT = QFeed + Qproduct + Qresidue

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Heat Capacity Constants of Components in E-101

QFeed:

Benzene:

QC6H6 = nC6H6 CpC6H6 ∆T

QC6H6 = (63.50623577 kmol d-1) x (25.0115375 J mol-1 oC -1) x (0)oC

QC6H6 = 0 kJ d-1

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (130.1120953kmol d-1) x (104.032525 mol-1 oC -1) x (0)oC

QC7H6O = 0 kJ d-1

Aluminum Chloride:

QAlCl3 = n AlCl3 Cp AlCl3 ∆T

Q AlCl3 = (6.805533947 kmol d-1) x (91.12 J mol-1 oC -1) x (0)oC

Q AlCl3 = 0 kJ d-1

QProduct:

Benzene:

QC6H6 = nC6H6 CpC6H6 ∆T

QC6H6 = (63.50623577 kmol d-1) x (108.1438371 J mol-1 oC -1) x (0)oC

QC6H6 = 0 kJ d-1
 Technological Institute of the Philippines

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (130.1120953kmol d-1) x (154.3581779 mol-1 oC -1) x (0)oC

QC7H6O = 0 kJ d-1

Aluminum Chloride:

QAlCl3 = n AlCl3 Cp AlCl3 ∆T

Q AlCl3 = (6.805533947 kmol d-1) x (91.12 J mol-1 oC -1) x (0)oC

Q AlCl3 = 0 kJ d-1

∆Hvap:

Benzaldehyde:

QC7H6O = nC7H6O ∆H

QC7H6O = 51114.31849x 130.1120953 kmol d-1

QC7H6O = 6650591.078 kJ d-1

Benzene:

QC6H6 = nC6H6 ∆H

Q C6H6 = 41360.66217x 63.50623577 kmol d-1

Q C6H6 = 2626659.964 kJ d-1

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Qtotal:

Qtotal = Qproduct + QFeed + Qvap

Qtotal = (0 kj kmol-1 ) + (0 kj kmol-1 ) + (9264117.741 kj kmol-1)

Qtotal = 9277251.041 kj kmol-1

Heating Duty:

Assuming 5% loss

Qreq’d = Qtotal x 1.05

Qreq’d = 9264117.741 kJ d-1 x 1.05

Qreq’d = 9727323.628 kJ d-1

Heating Steam Requirement

Operating Conditions of Heating Steam

Inlet Temperature 170 443.15 K

Outlet Temperature 185 458.15 K
Pressure 2.02 bar 2.02 bar
Qreq’d = QCw = mCp∆T

9727323.628 kJ d-1 = mw (4.184 kJ kg-1 -K-1) x (458.15 K - 443.15 K)

mw = 12988.19075 kg d-1
 Technological Institute of the Philippines

EQUIPMENT CONDENSER OPERATING 110oC

NAME TEMPERATURE
EQUIPMENT HX-104 OPERATING 1 bar
CODE PRESSURE
PROCESS To flash the HCl from benzene, benzaldehyde, and water.
DESCRIPTION

Stream Conditions
Stream T, oC P, bar
Stream 10 179 1
Stream 13 110 1

Enthalpy Balance:

QT = QFeed + Qproduct

Heat Capacity Constants of Components in HX-104

*Reference: Yaws, C.L. Chemical Properties Handbook

QFeed:

Benzene:

QC6H6 = nC6H6 CpC6H6 ∆T

QC6H6 = (63.18870459 kmol d-1) x (44.09247 J mol-1 oC -1) x (110-179)oC

QC6H6 = -192244.0782 kJ d-1

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Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (128.8109743 kmol d-1) x (73.10237832 mol-1 oC -1) x (110-179)oC

QC7H6O = -649730.8118 kJ d-1

QProduct:

Benzene:

QC6H6 = nC6H6 CpC6H6 ∆T

QC6H6 = (63.50623577 kmol d-1) x (17.18313373 J mol-1 oC -1) x (110-179)oC

QC6H6 = -74918.8173 kJ d-1

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (130.1120953kmol d-1) x (132.0315382 mol-1 oC -1) x (110-179)oC

QC7H6O = -1173490.664 kJ d-1

Qtotal:

Qtotal = Qproduct + QFeed

Qtotal = (-841974.89 kj kmol-1 ) + (-1248409.482 kj kmol-1 )

Qtotal = -2090384.372 kj kmol-1

Cooling Duty:

Assuming 5% loss

Qreq’d = Qtotal x 1.05

 Technological Institute of the Philippines

Qreq’d = -2090384.372 kJ d-1 x 1.05

Qreq’d = -2194903.59 kJ d-1

Cooling Steam Requirement

Operating Conditions of Cooling Steam

Inlet Temperature 100 373.15 K

Outlet Temperature 110 383.15 K
Pressure 1 bar 1 bar
Qreq’d = QCw = mCp∆T

-2194903.59 kJ d-1 = mw (4.184 kJ kg-1 -K-1) x (458.15 K - 443.15 K)

mw = 12988.19075 kg d-1
 Technological Institute of the Philippines

EQUIPMENT FLASH DRUM OPERATING 110oC

NAME TEMPERATURE
EQUIPMENT FD-101 OPERATING 1 bar
CODE PRESSURE
PROCESS To flash the benzene from the condensed benzaldehyde.
DESCRIPTION

Stream Conditions
Stream T, oC P, bar
Stream 13 110 5
Stream 14 110 1
Stream 15 110 1

Enthalpy Balance:

QT = QFeed + Qproduct

Heat Capacity Constants of Components in FD-101

 Technological Institute of the Philippines

*Reference: Yaws, C.L. Chemical Properties Handbook

QFeed:

Benzene:

QC6H6 = nC6H6 CpC6H6 ∆T

QC6H6 = (63.18870459 kmol d-1) x (44.09247 J mol-1 oC -1) x (0)oC

QC6H6 = 0 kJ d-1

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (128.8109743 kmol d-1) x (73.10237832 mol-1 oC -1) x (0)oC

QC7H6O = 0 kJ d-1

QProduct:

Benzene:

QC6H6 = nC6H6 CpC6H6 ∆T

QC6H6 = (63.50623577 kmol d-1) x (17.18313373 J mol-1 oC -1) x (0)oC

QC6H6 = 0 kJ d-1

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (130.1120953kmol d-1) x (132.0315382 mol-1 oC -1) x (0)oC

QC7H6O = 0 kJ d-1
 Technological Institute of the Philippines

Qtotal:

Qtotal = Qproduct + QFeed

Qtotal = (0 kJ kmol-1 ) + (0 kJ kmol-1 )

Qtotal = 0 kJ kmol-1

Heating Duty:

Assuming 5% loss

Qreq’d = Qtotal x 1.05

Qreq’d = 0 kJ d-1 x 1.05

Qreq’d = 0 kJ d-1

Heating Steam Requirement

Operating Conditions of Heating Steam

Inlet Temperature 100 373.15 K

Outlet Temperature 110 383.15 K
Pressure 1 bar 1 bar
Qreq’d = QCw = mCp∆T

0 kJ d-1 = mw (4.184 kJ kg-1 -K-1) x (458.15 K - 443.15 K)

mw = 0 kg d-1
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EQUIPMENT BENZYL OPERATING 22.6OC

NAME ALCOHOL TEMPERATURE
REACTOR
EQUIPMENT R-102 OPERATING 1 bar
CODE PRESSURE
PROCESS To make a reaction in Rh/C, benzaldehyde solution, and
DESCRIPTION hydrogen gas.

Stream Conditions
Stream T, oC P, bar
Stream 16-18 30 1
Stream 19-20 22.6 1
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Enthalpy Balance:

QT = QFeed + n∆H rxnO + Qproduct

Heat Capacity Constants of Components in R-101

*Reference: Yaws, C.L. Chemical Properties Handbook

QFeed:

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (128.8109743 kmol d-1) x (92.5048294 mol-1 oC -1) x (22.6-30)oC

QC7H6O = -88175.71532 kJ d-1

Hydrogen Gas:

QH2 = n H2 Cp H2 ∆T

Q H2 = (129.1954847kmol d-1) x (25.97 J mol-1 oC -1) x (22.6-30)oC

Q H2 = -24,829.01 kJ d-1

Rhodium on Carbon:

QRh/C = n Rh/C Cp Rh/C ∆T

Q Rh/C = (22.13898203 kmol d-1) x (244.09044 J mol-1 oC -1) x (22.6-30)oC

Q Rh/C = -39988.96261 kJ d-1

QProduct:

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

 Technological Institute of the Philippines

QC7H6O = (40.96189363 kmol d-1) x (87.93023144 J mol-1 oC -1) x (22.6-30)oC

QC7H6O = -26653.23703 kJ d-1

Hydrogen Gas:

QH2 = n H2 Cp H2 ∆T

Q H2 = (41.08457711 kmol d-1) x (25.84 J mol-1 oC -1) x (22.6-30)oC

Q H2 = -7,854.72 kJ d-1

Rhodium on Carbon:

QRh/C = n Rh/C Cp Rh/C ∆T

Q Rh/C = (22.13898203 kmol d-1) x (244.09044 J mol-1 oC -1) x (22.6-30)oC

Q Rh/C = -39988.96261 kJ d-1

Benzyl Alcohol:

QC7H8O = n C7H8OCp C7H8O∆T

Q C7H8O= (87.84908452 kmol d-1) x (116.0816932 J mol-1 oC -1) x (22.6-30)oC

Q C7H8O= -75462.76153 kJ d-1

n ∆Hrxno:

Composition Heat of Formation

H2 0
C7H6O -36.8
C7H8O -100.4

C7H6O + H2 → C7H8O

∆H (kj mol-1) = product - reactant

∆H = -100.4kj mol-1 – -36.8 kj mol-1+ 0 kj mol-1) (1000)

∆H = -63600 kj kmol-1

Qreaction = ∆H x limiting reactant

Qreaction = (-63600 kj kmol-1 ) x (128.8109743 kmol d-1)

 Technological Institute of the Philippines

Qreaction = -8192377.968 kJ d-1

Qtotal:

Qtotal = Qproduct + QFeed + Qrxn

Qtotal = ( 152993.6854 kJ kmol-1 ) + ( -149,959.68 kJ kmol-1 ) + (-8192377.968 kJ

kmol-1)

Qtotal = -8,495,331.34kJkmol-1

Cooling Duty:

Assuming 5% loss

Qreq’d = Qtotal x 1.05

Qreq’d = -8,495,331.34 kJ d-1 x 1.05

Qreq’d = -8920097.902 kJ d-1

Cooling Water Requirement

Operating Conditions of Cooling Water

Inlet Temperature 25oC 288.15 K

Outlet Temperature 15 oC 298.15 K
Pressure 1 bar 1 bar
Qreq’d = QCw = mCp∆T

8920097.902 = mw (4.184 kJ kg-1 -K-1) x (323.15 K - 303.15 K)

mw = 213195.4565 kg d-1
 Technological Institute of the Philippines

EQUIPMENT COOLER OPERATING 30oC

NAME TEMPERATURE

EQUIPMENT HX-105 OPERATING 1 bar

CODE PRESSURE

PROCESS To increase the temperature of benzaldehyde

DESCRIPTION

Stream Conditions
Stream T, oC P, bar
Stream 15 110 1
Stream 16 30 1

Enthalpy Balance:

QT = QFeed + n∆H rxnO + Qproduct

Heat Capacity Constants of Components in R-101

*Reference: Yaws, C.L. Chemical Properties Handbook

QFeed:

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

 Technological Institute of the Philippines

QC7H6O = (128.8109743 kmol d-1) x 132.0315382 J mol-1 oC -1) x (110-30)oC

QC7H6O = - 1360568.886 kJ d-1

QProduct:
Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (128.8109743 kmol d-1) x (92.5048294 J mol-1 oC -1) x (110-30)oC

QC7H6O = - 953250.9764 kJ d-1

Qtotal:

Qtotal = Qproduct + QFeed

Qtotal = (- 953250.9764 kj kmol-1 ) + (- 1360568.886 kj kmol-1 )

Qtotal = -2313819.863 kJ kmol-1

Cooling Duty:

Assuming 5% loss

Qreq’d = Qtotal x 1.05

Qreq’d = -2313819.863 kJ d-1 x 1.05

Qreq’d = -2194903.59 kJ d-1

Cooling Steam Requirement

Operating Conditions of Cooling Steam

Inlet Temperature 100 373.15 K

Outlet Temperature 110 383.15 K
Pressure 1 bar 1 bar
Qreq’d = QCw = mCp∆T

-2313819.863 kJ d-1 = mw (4.184 kJ kg-1 -K-1) x (458.15 K - 443.15 K)

mw = 116133.4061 kg d-1
 Technological Institute of the Philippines

EQUIPMENT HEATER OPERATING 30OC

NAME TEMPERATURE

EQUIPMENT HX-106 OPERATING 1 bar

CODE PRESSURE

PROCESS To preheat benzyl alcohol solution and Rh/C.

DESCRIPTION

Stream Conditions
Stream T, oC P, bar
Stream 19 22.6 1
Stream 21 30 1

Enthalpy Balance:

QT = QFeed + Qproduct

Heat Capacity Constants of Components in R-101

 Technological Institute of the Philippines

*Reference: Yaws, C.L. Chemical Properties Handbook

QFeed:

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (40.96189363 kmol d-1) x (9.130070494 J mol-1 oC -1) x (30-22.6)oC

QC7H6O = 2767.488826 kJ d-1

Rhodium on Carbon:

QRh/C = n Rh/C Cp Rh/C ∆T

Q Rh/C = (22.13898203 kmol d-1) x (244.09044 J mol-1 oC -1) x (30-22.6)oC

Q Rh/C = 39988.96261 kJ d-1

Benzyl Alcohol:

QC7H8O = n C7H8OCp C7H8O∆T

Q C7H8O= (87.84908452 kmol d-1) x (116.0816932 J mol-1 oC -1) x (30-22.6)oC

Q C7H8O= 75462.76153 kJ d-1

QProduct:

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (40.96189363 kmol d-1) x (92.5048294 J mol-1 oC -1) x (30-22.6)oC

QC7H6O = 28039.88007 kJ d-1

Rhodium on Carbon:

QRh/C = n Rh/C Cp Rh/C ∆T

Q Rh/C = (22.13898203 kmol d-1) x (244.09044 J mol-1 oC -1) x (30-22.6)oC

 Technological Institute of the Philippines

Q Rh/C = 39988.96261 kJ d-1

Benzyl Alcohol:

QC7H8O = n C7H8OCp C7H8O∆T

Q C7H8O= (87.84908452 kmol d-1) x (121.69357 J mol-1 oC -1) x (30-22.6)oC

Q C7H8O= 109520.1625 kJ d-1

Qtotal:

Qtotal = Qproduct + QFeed

Qtotal = ( 78230.25036 kJ kmol-1 ) + ( 177549.0051 kJ kmol-1 )

Qtotal = 255779.2555 kJkmol-1

Heating Duty:

Assuming 5% loss

Qreq’d = Qtotal x 1.05

Qreq’d = 255779.2555 kJ d-1 x 1.05

Qreq’d = 268568.2183 kJ d-1

Heating Water Requirement

Operating Conditions of Heating Water

Inlet Temperature 30oC 303.15 K

Outlet Temperature 25 oC 298.15 K
Pressure 1 bar 1 bar
Qreq’d = QCw = mCp∆T

268568.2183 = mw (4.184 kJ kg-1 -K-1) x (323.15 K - 303.15 K)

mw = 12837.86894 kg d-1
 Technological Institute of the Philippines

EQUIPMENT PRE-HEATER OPERATING 179oC

NAME TEMPERATURE

EQUIPMENT HX-107 OPERATING 1 bar

CODE PRESSURE

PROCESS To pre-heat the solution in preparation for distillation.

DESCRIPTION

Stream Conditions
Stream T, oC P, bar
Stream 22 30 1
Stream 24 202 1

Enthalpy Balance:

QT = QFeed + Qproduct + Qvap

Heat Capacity Constants of Components in R-101

*Reference: Yaws, C.L. Chemical Properties Handbook

QFeed:
 Technological Institute of the Philippines

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (40.96189363 kmol d-1) x (92.5048294 J mol-1 oC -1) x (202-30)oC

QC7H6O = 651737.753 kJ d-1

Benzyl Alcohol:

QC7H8O = n C7H8OCp C7H8O∆T

Q C7H8O= (87.84908452 kmol d-1) x (121.69357 J mol-1 oC -1) x (202-30)oC

Q C7H8O= 1838795.019 kJ d-1

QProduct:

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (40.96189363 kmol d-1) x (160.0202854 J mol-1 oC -1) x (202-30)oC

QC7H6O = 1127414.232 kJ d-1

Benzyl Alcohol:

QC7H8O = n C7H8OCp C7H8O∆T

Q C7H8O= (87.84908452 kmol d-1) x (203.1830902 J mol-1 oC -1) x (202-30)oC

Q C7H8O= 3070105.135 kJ d-1

∆Hvap:

Benzaldehyde:

QC7H6O = nC7H6O ∆H

QC7H6O = 50518.82718 x 40.96189363kmol d-1

QC7H6O = 2069346.825 kJ d-1

 Technological Institute of the Philippines

Benzyl Alcohol:

QC6H8O = nC6H8O ∆H

Q C6H8O = 71382.01497 x 87.84908452 kmol d-1

Q C6H8O = 6270844.666 kJ d-1

Qtotal:

Qtotal = Qproduct + QFeed + Qvap

Qtotal = ( 2490532.772 kJ d-1 ) + ( 4197519.368 kJ d-1 ) + (2069346.825 kJ d-1

Qtotal = 8757398.965 kJ d-1

Heating Duty:

Assuming 5% loss

Qreq’d = Qtotal x 1.05

Qreq’d = 8757398.965 kJ d-1 x 1.05

Qreq’d = - 9195268.913 kJ d-1

Cooling Water Requirement

Operating Conditions of Cooling Water

Inlet Temperature 203oC 476.15 K

Outlet Temperature 180 oC 453.15 K
Pressure 1 bar 1 bar
Qreq’d = QCw = mCp∆T

9195268.913 = mw (4.184 kJ kg-1 -K-1) x (323.15 K - 303.15 K)

mw = 95553.13111 kg d-1
 Technological Institute of the Philippines

EQUIPMENT DISTILLATION OPERATING 202.5oC

NAME COLUMN TEMPERATURE

EQUIPMENT C-101 OPERATING 1 bar

CODE PRESSURE

PROCESS To separate benzaldehyde from benzyl alcohol.

DESCRIPTION

QFeed:

Benzaldehyde:

QC7H6O = nC7H6O CpC7H6O ∆T

QC7H6O = (40.96189363 kmol d-1) x (160.0202854 J mol-1 oC -1) x (202-30)oC

QC7H6O = 1127414.232 kJ d-1

Benzyl Alcohol:

QC7H8O = n C7H8OCp C7H8O∆T

Q C7H8O= (87.84908452 kmol d-1) x (203.1830902 J mol-1 oC -1) x (202-30)oC

Q C7H8O= 3070105.135 kJ d-1

 Technological Institute of the Philippines

EQUIPMENT GAS ABSORBER OPERATING 20oC

NAME TEMPERATURE

EQUIPMENT G-101 OPERATING 101.3 kPa

CODE PRESSURE

PROCESS To produce HCl solution.

DESCRIPTION
 Technological Institute of the Philippines

QFeed:

Water:

QH2O = nH2O CpH2O∆T

QH2O = (128.8109743 kmol d-1) x (92.5048294 mol-1 oC -1) x (22.6-30)oC

QH2O = -88175.71532 kJ d-1

Hydrogen Chloride:

QHCL = n HCL Cp HCL ∆T

Q HCL = (129.1954847kmol d-1) x (25.97 J mol-1 oC -1) x (22.6-30)oC

Q H2 = -24,829.01 kJ d-1

Carbon Monoxide:

QCO = n COCp CO∆T

Q CO= (22.13898203 kmol d-1) x (244.09044 J mol-1 oC -1) x (22.6-30)oC

Q Rh/C = -39988.96261 kJ d-1

 Technological Institute of the Philippines

EQUIPMENT NEUTRALIZATIO OPERATING 30oC

NAME N REACTOR TEMPERATURE

EQUIPMENT R-103 OPERATING 101.3 kPa

CODE PRESSURE

PROCESS To make a reaction in HCl solution and NaOH.

DESCRIPTION

Stream Conditions
Stream T, oC P, bar
Stream 27,28 20 1
Stream 29 30 1

Enthalpy Balance:

QT = QFeed + n∆H rxnO + Qproduct

Heat Capacity Constants of Components in R-101

 Technological Institute of the Philippines

*Reference: Yaws, C.L. Chemical Properties Handbook

QFeed:

Water:

QH2O = nH2O CpH2O∆T

QH2O = (128.8109743 kmol d-1) x (92.5048294 mol-1 oC -1) x (22.6-30)oC

QH2O = -88175.71532 kJ d-1

Hydrogen Chloride:

QHCL = n HCL Cp HCL ∆T

Q HCL = (129.1954847kmol d-1) x (25.97 J mol-1 oC -1) x (22.6-30)oC

Q H2 = -24,829.01 kJ d-1

Carbon Monoxide:

QCO = n COCp CO∆T

Q CO= (22.13898203 kmol d-1) x (244.09044 J mol-1 oC -1) x (22.6-30)oC

Q Rh/C = -39988.96261 kJ d-1

Sodium Hydroxide:

QNaOH = n NaOHCp NaOH∆T

Q NaOH= (22.13898203 kmol d-1) x (244.09044 J mol-1 oC -1) x (22.6-30)oC

Q NaOH= -39988.96261 kJ d-1

QProduct:

Water:

QH2O = nH2O CpH2O∆T

 Technological Institute of the Philippines

QH2O = (128.8109743 kmol d-1) x (92.5048294 mol-1 oC -1) x (22.6-30)oC

QH2O = -88175.71532 kJ d-1

Hydrogen Chloride:

QHCL = n HCL Cp HCL ∆T

Q HCL = (129.1954847kmol d-1) x (25.97 J mol-1 oC -1) x (22.6-30)oC

Q H2 = -24,829.01 kJ d-1

Carbon Monoxide:

QCO = n COCp CO∆T

Q CO= (22.13898203 kmol d-1) x (244.09044 J mol-1 oC -1) x (22.6-30)oC

Q Rh/C = -39988.96261 kJ d-1

Sodium Hydroxide:

QNaOH = n NaOHCp NaOH∆T

Q NaOH= (22.13898203 kmol d-1) x (244.09044 J mol-1 oC -1) x (22.6-30)oC

Q NaOH= -39988.96261 kJ d-1

n ∆Hrxno:

Composition Heat of Formation

H2 0
C7H6O -36.8
C7H8O -100.4

C7H6O + H2 → C7H8O

∆H (kj mol-1) = product - reactant

∆H = -100.4kj mol-1 – -36.8 kj mol-1+ 0 kj mol-1) (1000)

∆H = -63600 kj kmol-1

Qreaction = ∆H x limiting reactant

Qreaction = (-63600 kj kmol-1 ) x (128.8109743 kmol d-1)

 Technological Institute of the Philippines

Qreaction = -8192377.968 kJ d-1

Qtotal:

Qtotal = Qproduct + QFeed + Qrxn

Qtotal = ( 152993.6854 kJ kmol-1 ) + ( -149,959.68 kJ kmol-1 ) + (-8192377.968 kJ

kmol-1)

Qtotal = -8,495,331.34kJkmol-1

Cooling Duty:

Assuming 5% loss

Qreq’d = Qtotal x 1.05

Qreq’d = -8,495,331.34 kJ d-1 x 1.05

Qreq’d = -8920097.902 kJ d-1

Cooling Water Requirement

Operating Conditions of Cooling Water

Inlet Temperature 25oC 288.15 K

Outlet Temperature 15 oC 298.15 K
Pressure 1 bar 1 bar
Qreq’d = QCw = mCp∆T

8920097.902 = mw (4.184 kJ kg-1 -K-1) x (323.15 K - 303.15 K)

mw = 213195.4565 kg d-1