PRELIMINARY DESIGN OF PROPYLENE GLYCOL PLANT FROM PROPYLENE OXIDE AND WATER USING ACID Preliminary Design of Propylene Glycol Plant from Propylene Oxide and Water Using Acid Catalyst with Capacity of 50,000 Ton/Year.
PRELIMINARY DESIGN OF PROPYLENE GLYCOL PLANT
FROM PROPYLENE OXIDE AND WATER USING ACID
CATALYST WITH CAPACITY OF 50,000 TON/YEAR
By:
Aisyah Hanifah
D500122004
Supervisor:
Eni Budiyati, S.T., M.Eng
Ir. Nur Hidayati, M.T., Ph.D.
CHEMICAL ENGINEERING DEPARTMENT
FACULTY OF ENGINEERING
UNIVERSITAS MUHAMMADIYAH SURAKARTA
2016
268'XIN
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ONTUf,
f,NICNE'TY)D{ItrrI3
MOTTO
Ever Tried
Ever Failed
No Matter
Try Again
Fail Again
Fail Better
Get Successful
iv
DEDICATION
This work is dedicated for:
Umi is the one who give a spirit for me, advise me, and also give me a direction
so that I can finish this final report.
Abi is my role model. Even he is hard but I know that he did for me. Thanks for
your money. I will replace it later and make you feel happy
My brother Muhammad Taufik Al-Haqim and Muhammad Zaki Faizal, you are
good brother in the world. Reach your dream. Do not disappoint us.
My partner Diah Ayu Anggraeni. When I am so lazy, you are the one who always
give me a spirit. Thanks mba di
For my grandmother and grandfather. Thank you for your praying.
Nanik, Anggi, Rendra, Mala, Mba Delta and Salam from international class and
listi you are everything for me. No one can replace you. Thanks for your spirit. I
will keep my finger cross for all of you
For my friends, chemical engineering, 2012. Thanks for togetherness. Thanks for
beautiful memories with you :’)
v
PREFACE
Bissmillahirrahmanirrohim
The author thanks Allah SWT for His blessing and mercy, in completing the
final project en titled “Preliminary Design of Propylene Glycol Plant from
Propylene Oxide and Water using Acid Catalyst with Capacity of 50,000
Ton/Year”.
This report is final task as a requirement to obtain bachelor degree (S.T) in
The Department of Chemical Engineering Faculty of Universitas Muhammadiyah
Surakarta. Upon finishing this task, it is expected to understand the theory that have
been studied and can be used as alternative industry plant in the future.
The author aware that the completing of The Final Project Report is
impossible without the help of adviser and other parties. Therefore, in this
opportunity authors are grateful to all those who helped completing The Final
Project Report, in particular to:
1. Allah SWT who has given me His mercy and His blessing.
2. Rois Fatoni, ST, MSc, Ph.D. as Head of Department of Chemical
Engineering of Universitas Muhammadiyah Surakarta.
3. Ms. Eni Budiyati, S.T., M.Eng as first supervisor
4. Ir. Nur Hidayati, M.T., Ph.D. as second supervisor
5. All the lecturer in Department of Chemical Engineering of Universitas
Muhammadiyah Surakarta.
6. My partner Diah Ayu Anggraeni and All my friends from international
class 2012
7. My Family who always gives a support to the Author.
Author aware that this report is far from perfect because of limited
capabilities and existing deficiencies in making final task Report. Author hope
that the report will be useful for those who may concern
Surakarta, November 2016
The Writer
vi
TABLE OF CONTENTS
TITLE .................................................................................................................. i
APPROVAL ....................................................................................................... ii
AUTHOR’S DECLARATION ........................................................................... iii
MOTTO .............................................................................................................. iv
DEDICATION .................................................................................................... v
PREFACE ........................................................................................................... vi
TABLE OF CONTENTS .................................................................................... vii
LIST OF TABLE ................................................................................................ ix
TABLE OF FIGURE .......................................................................................... xii
ABSTRACT ........................................................................................................ xiii
CHAPTER I INTRODUCTION ......................................................................... 1
1.1 Background ........................................................................................... 1
1.2 Capacity of The Plant............................................................................ 1
1.3 Literature Review.................................................................................. 5
1.4 The Usefulness of Products .................................................................. 6
1.5 Properties of Physical and Chemical Raw Materials and Products ...... 7
CHAPTER II PROCESS DESCRIPTION ......................................................... 11
2.1 The Specification of Raw Materials and Products ................................ 11
2.2 The Process Concept ............................................................................. 12
2.3 The Thermodynamic Review ................................................................ 12
2.4 The Flowchart ....................................................................................... 15
2.5 The Process Stages ................................................................................ 15
2.6 The Flowchart of Material Balance and Heat Balance ......................... 16
2.7 The Plant Layout and Equipment ......................................................... 30
CHAPTER III THE SPESIFICATION of THE EQUIPMENT ......................... 36
3.1 Main Equipment.................................................................................... 36
3.2 Supporting Equipment .......................................................................... 42
CHAPTER IV PROCESS SUPPORT UNIT AND LABORATORY
4.1 Process Support Unit............................................................................. 57
vii
4.2 Liquid Waste Treatment Unit ............................................................... 73
CHAPTER V MANAGEMENT
5.1 Company ............................................................................................... 75
5.2 Organizational Structure ....................................................................... 76
5.3 Employee Status and Salary Status ....................................................... 82
5.4 Health and Safety .................................................................................. 87
5.5 Production Management ....................................................................... 88
5.6 Production Plant .................................................................................... 88
5.7 Production Control ................................................................................ 89
CHAPTER VI ECONOMICAL ANALYSIS ..................................................... 91
6.1 Basic Calculation .................................................................................. 91
6.2 Cost Calculation .................................................................................... 93
6.3 General Expenses .................................................................................. 95
6.4 Feasibility Analysis ............................................................................... 96
6.5 The Result of Calculation ..................................................................... 97
CHAPTER VII CONCLUSION ......................................................................... 104
BIBLIOGRAPHY ............................................................................................... 105
ATTACHMENT ................................................................................................. 106
viii
LIST OF TABLE
Table 1.1 Import of propylene glycol in Indonesia from 2011 to 2015………….2
Table 1.2 Data of propylene glycol production capacity abroad………………....3
Table 2.1 ΔG°f value each components ………………………………….……..12
Table 2.2 Value of ΔH°f each component………………………………….……13
Table 2.3 Component of Mass Flow………………………………….………….17
Table. 2.4 Mass balance of Mixer (M-110) ……………………………………..18
Table. 2.5 Mass balance of Reactor (R-120) ……………………………………18
Table. 2.6 Mass balance of Reactor ( R-130) ……………………………………18
Table 2.7 Mass balance of Distillation Tower (D-140) …………………………19
Table 2.8 Mass balance of Neutralizer (R-150).…………………………………19
Table 2.9 Mass balance of Decanter (H-160).…………………………………...20
Table 2.10 Mass balance of Distillation Tower (D-170) ………………………..20
Table 2.11 Mass balance of Distillation Tower (D-180) ………………………..21
Table. 2.12 The Total of material balance……………………………………….22
Table. 2.13 Heat balance of Mixer (M-110) …………………………………….24
Table. 2.14 Heat balance of Reactor (R-120) …………………………………...23
Table. 2.15 Heat balance of Reactor (R-130) …………………………………...24
Table. 2.16 Heat balance of Heat Exchanger (E-132) …………………………..24
Table. 2.17 Heat balance of Distillation tower (D-140) …………………………24
Table. 2.18 Heat balance of Cooler (E-142) …………………………………….25
ix
Table. 2.19 Heat balance of Cooler (E-143) …………………………………….25
Table. 2.20 Heat balance of Cooler (E-147) …………………………………….26
Table. 2.21 Heat balance of neutralizer (R-150) ………………………………...26
Table. 2.22 Heat balance of Decanter (H-160) ……………………………....….27
Table. 2.22 Heat balance of Distillation tower (D-170) …………………………27
Table. 2.23 Heat balance of Heat Exchanger (E-174) …………………………..28
Table. 2.24 Heat balance of Distillation tower (D-180) …………………………28
Table. 2.25 Heat balance of Cooler (E-185) …………………………………….29
Table. 2.26 Heat balance of Cooler (E-186) …………………………………….29
Table 2.27 Building plant of Propylene glycol with capacity of 50,000 tons /
year………………………………….………………………………….………...31
Table 4.1. Need of cooling water (kg/h) ………………………………………...69
Table 4.2. Need of water for steam (kg/h) ………………………………………69
Table 4.3. Power in process unit………………………………….……………...71
Table 4.4. Power in utility unit………………………………….……………….72
Table 5.1 Schedule for each group………………………………….……………84
Table 5.2 Position and requirements………………………………….………….84
Table 6.1 Cost Index Chemical Plant Year 1990-2010………………………….92
Table 6.2 Physical Plant Cost……………………………………………………97
Table 6.3 Fixed Capital Cost (FCI) ……………………………………………...99
Table 6.4 Working Capital Investment…………………………………………..99
x
Table 6.5 Manufacturing Cost…………………………………………………...99
Table 6.6 General Expense……………………………………………………..100
Table 6.7 Fixed Cost……………………………………………………………101
Table 6.8 Variable Cost………………………………………………………...102
Table 6.9 Regulated Cost………………………………….……………………102
xi
TABLE OF FIGURE
Figure 1.1 Need of Propylene glycol in Indonesia………………………………...2
Figure 2.1 Flowchart of Qualitative………………………………….…………..15
Figure 2.2The flowchart of mass balance………………………………………..17
Figure 2.3 Layout of Precipitated Silica Plant…………………………………...32
Figure 2.4 Layout of equipment of Propylene…………………………………...34
Figure 4.1. Diagram process of water treatment…………………………………62
Figure 5.1 Organizational Structure……………………………………………...81
Figure 6.1 Relationship between Years and Cost Index…………………………93
Figure 6.2 Graphic of Parameters of Economic Analysis………………………103
xii
Abstrak
Di Indonesia, pabrik propilen glikol adalah industry yang menawarkan kesempatan
baik untuk Negara. Propilen glikol dihasilkan dari reaksi propilen oksida dan air
menggunakan katalis asam dengan perbandingan propilen oksida: air: methanol
adalah 43,04: 802,8: 71,87 lbmol. Proses menggunakan reaktor RATB (Reaktor
Alir Tangki Berpengaduk). Reaktor beroperasi pada suhu 30°C dan tekanan 1 atm.
Reaksi pada reaktor berjalan pada kondisi fase cair, irreversible dan eksotermis.
Unit pendungkung dari pabrik terdiri dari unit penyedia air, unit suplai uap air,
listrik dan kebutuhan bahan bakar dan laboratorium untuk menjaga kualitas bahan
baku dan produk dalam keadaan standar. Perusahan ini adalah perusahaan
perseroan terbatas (PT) dengan system organisasi terstruktur dan pegawai.
Perusahan ini terletak di Gresik profinsi Jawa. Terlihat dari analisis ekonomi bahwa
Percent Return on Investment (ROI) sebelum pajak adalah 25.42 % dan ROI setelah
pajak adalah 17.79 %. Pay out Time (POT) sebelum pajak adalah 2.8 tahun. Break
Even Point (BEP) adalah 45.96 %, Shut down Point (SDP) adalah 21.51 %,
menghasilkan Discounted Cash Flow (DCF) 30.28 %, dari data analisi yang
didapatkan, bisa disimpulkan bahwa pabrik menguntungkan dan kemungkinan
untuk dibangun.
Kata Kunci: propilen oksida, katalis asam, air, RATB.
xiii
Abstract
In Indonesia, propylene glycol plant is an industry that can provide a good
opportunity for the country. Propylene glycol is produced by a reacting of propylene
oxide and water using an acid catalyst by a ratio of propylene oxide: water:
methanol is 43.04: 802.8: 71.87 lbmol. The process using CSTR reactor
(Continuous stirred tank reactor). The reactor operates at temperature of 30°C and
a pressure of 1 atm. The reaction in the reactor is carried out at liquid phase,
irreversible, and exothermic condition. Supporting units of the plant consists of the
units of the water provider, the unit of steam supply, electricity and fuel needs, and
laboratories to maintain the quality of materials and products to conform to the
standards. This company is a limited liability company (PT) with a system of
organizational structure and staff. The company is located in Gresik Java Province.
The economic analysis showed that Pretax Percent Return on Investment (ROI) is
25.42 % and ROI after tax is 17.79 %. Pay out Time (POT) before taxed is 2.8 year.
Break Even Point (BEP) of 45.96 %, Shut down Point (SDP) of 21.51 %, and was
obtained Discounted Cash Flow (DCF) of 30.28 %, were obtained the data
feasibility analysis, it can be concluded that the plant is profitable and feasible to
be established.
Keywords: Propylene Oxide, acid catalyst, water, CSTR
xiv
FROM PROPYLENE OXIDE AND WATER USING ACID
CATALYST WITH CAPACITY OF 50,000 TON/YEAR
By:
Aisyah Hanifah
D500122004
Supervisor:
Eni Budiyati, S.T., M.Eng
Ir. Nur Hidayati, M.T., Ph.D.
CHEMICAL ENGINEERING DEPARTMENT
FACULTY OF ENGINEERING
UNIVERSITAS MUHAMMADIYAH SURAKARTA
2016
268'XIN
oqd "cs'hl "J's 'ruoluc slou
lueluuedoc
Surreeur8ug Iuorr.uor{f, Jo pBoH
m
916
)lNl
k+
11
rosr,r.rednS
',(q penorddy
g
l0u Jeqr.uersc 'uyu1e;n5
'C't{d
''I'hl
'1te,(eptg
rnN'rl
'8uA'W ''1'5'11e,(rpng lug
reaA/suoJ 000'0gJo fitcede3
'Z
'l
losrruedng
q11,,'r 1s,{1e1e3
prcy Sursq rale,11 puu oplxo eue1,(dor6 urorg
1ue14 1oc,(19 eue1.(dor4 go u8rseq ,&eutut1e.r4
1ca[or6 IBUU Jo
c
hIIN
qeJlueH qe(sry
oru€N
v00 z(,t 00s
YIUVXYUNS I{VAI(IW,{WYHIII I SVIISUflAINO
CNTUflf,NICNfl .{O AITNJYd
INUITIUVdf, (I
ol]tll
ONTUf,
f,NICNE'TY)D{ItrrI3
MOTTO
Ever Tried
Ever Failed
No Matter
Try Again
Fail Again
Fail Better
Get Successful
iv
DEDICATION
This work is dedicated for:
Umi is the one who give a spirit for me, advise me, and also give me a direction
so that I can finish this final report.
Abi is my role model. Even he is hard but I know that he did for me. Thanks for
your money. I will replace it later and make you feel happy
My brother Muhammad Taufik Al-Haqim and Muhammad Zaki Faizal, you are
good brother in the world. Reach your dream. Do not disappoint us.
My partner Diah Ayu Anggraeni. When I am so lazy, you are the one who always
give me a spirit. Thanks mba di
For my grandmother and grandfather. Thank you for your praying.
Nanik, Anggi, Rendra, Mala, Mba Delta and Salam from international class and
listi you are everything for me. No one can replace you. Thanks for your spirit. I
will keep my finger cross for all of you
For my friends, chemical engineering, 2012. Thanks for togetherness. Thanks for
beautiful memories with you :’)
v
PREFACE
Bissmillahirrahmanirrohim
The author thanks Allah SWT for His blessing and mercy, in completing the
final project en titled “Preliminary Design of Propylene Glycol Plant from
Propylene Oxide and Water using Acid Catalyst with Capacity of 50,000
Ton/Year”.
This report is final task as a requirement to obtain bachelor degree (S.T) in
The Department of Chemical Engineering Faculty of Universitas Muhammadiyah
Surakarta. Upon finishing this task, it is expected to understand the theory that have
been studied and can be used as alternative industry plant in the future.
The author aware that the completing of The Final Project Report is
impossible without the help of adviser and other parties. Therefore, in this
opportunity authors are grateful to all those who helped completing The Final
Project Report, in particular to:
1. Allah SWT who has given me His mercy and His blessing.
2. Rois Fatoni, ST, MSc, Ph.D. as Head of Department of Chemical
Engineering of Universitas Muhammadiyah Surakarta.
3. Ms. Eni Budiyati, S.T., M.Eng as first supervisor
4. Ir. Nur Hidayati, M.T., Ph.D. as second supervisor
5. All the lecturer in Department of Chemical Engineering of Universitas
Muhammadiyah Surakarta.
6. My partner Diah Ayu Anggraeni and All my friends from international
class 2012
7. My Family who always gives a support to the Author.
Author aware that this report is far from perfect because of limited
capabilities and existing deficiencies in making final task Report. Author hope
that the report will be useful for those who may concern
Surakarta, November 2016
The Writer
vi
TABLE OF CONTENTS
TITLE .................................................................................................................. i
APPROVAL ....................................................................................................... ii
AUTHOR’S DECLARATION ........................................................................... iii
MOTTO .............................................................................................................. iv
DEDICATION .................................................................................................... v
PREFACE ........................................................................................................... vi
TABLE OF CONTENTS .................................................................................... vii
LIST OF TABLE ................................................................................................ ix
TABLE OF FIGURE .......................................................................................... xii
ABSTRACT ........................................................................................................ xiii
CHAPTER I INTRODUCTION ......................................................................... 1
1.1 Background ........................................................................................... 1
1.2 Capacity of The Plant............................................................................ 1
1.3 Literature Review.................................................................................. 5
1.4 The Usefulness of Products .................................................................. 6
1.5 Properties of Physical and Chemical Raw Materials and Products ...... 7
CHAPTER II PROCESS DESCRIPTION ......................................................... 11
2.1 The Specification of Raw Materials and Products ................................ 11
2.2 The Process Concept ............................................................................. 12
2.3 The Thermodynamic Review ................................................................ 12
2.4 The Flowchart ....................................................................................... 15
2.5 The Process Stages ................................................................................ 15
2.6 The Flowchart of Material Balance and Heat Balance ......................... 16
2.7 The Plant Layout and Equipment ......................................................... 30
CHAPTER III THE SPESIFICATION of THE EQUIPMENT ......................... 36
3.1 Main Equipment.................................................................................... 36
3.2 Supporting Equipment .......................................................................... 42
CHAPTER IV PROCESS SUPPORT UNIT AND LABORATORY
4.1 Process Support Unit............................................................................. 57
vii
4.2 Liquid Waste Treatment Unit ............................................................... 73
CHAPTER V MANAGEMENT
5.1 Company ............................................................................................... 75
5.2 Organizational Structure ....................................................................... 76
5.3 Employee Status and Salary Status ....................................................... 82
5.4 Health and Safety .................................................................................. 87
5.5 Production Management ....................................................................... 88
5.6 Production Plant .................................................................................... 88
5.7 Production Control ................................................................................ 89
CHAPTER VI ECONOMICAL ANALYSIS ..................................................... 91
6.1 Basic Calculation .................................................................................. 91
6.2 Cost Calculation .................................................................................... 93
6.3 General Expenses .................................................................................. 95
6.4 Feasibility Analysis ............................................................................... 96
6.5 The Result of Calculation ..................................................................... 97
CHAPTER VII CONCLUSION ......................................................................... 104
BIBLIOGRAPHY ............................................................................................... 105
ATTACHMENT ................................................................................................. 106
viii
LIST OF TABLE
Table 1.1 Import of propylene glycol in Indonesia from 2011 to 2015………….2
Table 1.2 Data of propylene glycol production capacity abroad………………....3
Table 2.1 ΔG°f value each components ………………………………….……..12
Table 2.2 Value of ΔH°f each component………………………………….……13
Table 2.3 Component of Mass Flow………………………………….………….17
Table. 2.4 Mass balance of Mixer (M-110) ……………………………………..18
Table. 2.5 Mass balance of Reactor (R-120) ……………………………………18
Table. 2.6 Mass balance of Reactor ( R-130) ……………………………………18
Table 2.7 Mass balance of Distillation Tower (D-140) …………………………19
Table 2.8 Mass balance of Neutralizer (R-150).…………………………………19
Table 2.9 Mass balance of Decanter (H-160).…………………………………...20
Table 2.10 Mass balance of Distillation Tower (D-170) ………………………..20
Table 2.11 Mass balance of Distillation Tower (D-180) ………………………..21
Table. 2.12 The Total of material balance……………………………………….22
Table. 2.13 Heat balance of Mixer (M-110) …………………………………….24
Table. 2.14 Heat balance of Reactor (R-120) …………………………………...23
Table. 2.15 Heat balance of Reactor (R-130) …………………………………...24
Table. 2.16 Heat balance of Heat Exchanger (E-132) …………………………..24
Table. 2.17 Heat balance of Distillation tower (D-140) …………………………24
Table. 2.18 Heat balance of Cooler (E-142) …………………………………….25
ix
Table. 2.19 Heat balance of Cooler (E-143) …………………………………….25
Table. 2.20 Heat balance of Cooler (E-147) …………………………………….26
Table. 2.21 Heat balance of neutralizer (R-150) ………………………………...26
Table. 2.22 Heat balance of Decanter (H-160) ……………………………....….27
Table. 2.22 Heat balance of Distillation tower (D-170) …………………………27
Table. 2.23 Heat balance of Heat Exchanger (E-174) …………………………..28
Table. 2.24 Heat balance of Distillation tower (D-180) …………………………28
Table. 2.25 Heat balance of Cooler (E-185) …………………………………….29
Table. 2.26 Heat balance of Cooler (E-186) …………………………………….29
Table 2.27 Building plant of Propylene glycol with capacity of 50,000 tons /
year………………………………….………………………………….………...31
Table 4.1. Need of cooling water (kg/h) ………………………………………...69
Table 4.2. Need of water for steam (kg/h) ………………………………………69
Table 4.3. Power in process unit………………………………….……………...71
Table 4.4. Power in utility unit………………………………….……………….72
Table 5.1 Schedule for each group………………………………….……………84
Table 5.2 Position and requirements………………………………….………….84
Table 6.1 Cost Index Chemical Plant Year 1990-2010………………………….92
Table 6.2 Physical Plant Cost……………………………………………………97
Table 6.3 Fixed Capital Cost (FCI) ……………………………………………...99
Table 6.4 Working Capital Investment…………………………………………..99
x
Table 6.5 Manufacturing Cost…………………………………………………...99
Table 6.6 General Expense……………………………………………………..100
Table 6.7 Fixed Cost……………………………………………………………101
Table 6.8 Variable Cost………………………………………………………...102
Table 6.9 Regulated Cost………………………………….……………………102
xi
TABLE OF FIGURE
Figure 1.1 Need of Propylene glycol in Indonesia………………………………...2
Figure 2.1 Flowchart of Qualitative………………………………….…………..15
Figure 2.2The flowchart of mass balance………………………………………..17
Figure 2.3 Layout of Precipitated Silica Plant…………………………………...32
Figure 2.4 Layout of equipment of Propylene…………………………………...34
Figure 4.1. Diagram process of water treatment…………………………………62
Figure 5.1 Organizational Structure……………………………………………...81
Figure 6.1 Relationship between Years and Cost Index…………………………93
Figure 6.2 Graphic of Parameters of Economic Analysis………………………103
xii
Abstrak
Di Indonesia, pabrik propilen glikol adalah industry yang menawarkan kesempatan
baik untuk Negara. Propilen glikol dihasilkan dari reaksi propilen oksida dan air
menggunakan katalis asam dengan perbandingan propilen oksida: air: methanol
adalah 43,04: 802,8: 71,87 lbmol. Proses menggunakan reaktor RATB (Reaktor
Alir Tangki Berpengaduk). Reaktor beroperasi pada suhu 30°C dan tekanan 1 atm.
Reaksi pada reaktor berjalan pada kondisi fase cair, irreversible dan eksotermis.
Unit pendungkung dari pabrik terdiri dari unit penyedia air, unit suplai uap air,
listrik dan kebutuhan bahan bakar dan laboratorium untuk menjaga kualitas bahan
baku dan produk dalam keadaan standar. Perusahan ini adalah perusahaan
perseroan terbatas (PT) dengan system organisasi terstruktur dan pegawai.
Perusahan ini terletak di Gresik profinsi Jawa. Terlihat dari analisis ekonomi bahwa
Percent Return on Investment (ROI) sebelum pajak adalah 25.42 % dan ROI setelah
pajak adalah 17.79 %. Pay out Time (POT) sebelum pajak adalah 2.8 tahun. Break
Even Point (BEP) adalah 45.96 %, Shut down Point (SDP) adalah 21.51 %,
menghasilkan Discounted Cash Flow (DCF) 30.28 %, dari data analisi yang
didapatkan, bisa disimpulkan bahwa pabrik menguntungkan dan kemungkinan
untuk dibangun.
Kata Kunci: propilen oksida, katalis asam, air, RATB.
xiii
Abstract
In Indonesia, propylene glycol plant is an industry that can provide a good
opportunity for the country. Propylene glycol is produced by a reacting of propylene
oxide and water using an acid catalyst by a ratio of propylene oxide: water:
methanol is 43.04: 802.8: 71.87 lbmol. The process using CSTR reactor
(Continuous stirred tank reactor). The reactor operates at temperature of 30°C and
a pressure of 1 atm. The reaction in the reactor is carried out at liquid phase,
irreversible, and exothermic condition. Supporting units of the plant consists of the
units of the water provider, the unit of steam supply, electricity and fuel needs, and
laboratories to maintain the quality of materials and products to conform to the
standards. This company is a limited liability company (PT) with a system of
organizational structure and staff. The company is located in Gresik Java Province.
The economic analysis showed that Pretax Percent Return on Investment (ROI) is
25.42 % and ROI after tax is 17.79 %. Pay out Time (POT) before taxed is 2.8 year.
Break Even Point (BEP) of 45.96 %, Shut down Point (SDP) of 21.51 %, and was
obtained Discounted Cash Flow (DCF) of 30.28 %, were obtained the data
feasibility analysis, it can be concluded that the plant is profitable and feasible to
be established.
Keywords: Propylene Oxide, acid catalyst, water, CSTR
xiv