seminar skripsi · (triethylene glycol) gas dehydration systems. energy 34, 1910-1916 chen and...
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ANDREAS ADITYA HENDRO 2310100093
PENGENDALIAN DEHIDRASI NATURAL GAS DENGAN TEG MENGGUNAKAN PID CONTROLLER DAN MODEL PREDICTIVE
CONTROL
PEMBIMBING Prof Ir Renanto Handogo MS PhD
Juwari Purwo Sutikno ST MEng PhD
FERRY KURNIAWAN 2310100097
SEMINAR SKRIPSI
Natural Gas
bull mencegah pembentukan hidrat dan kondensasi bebas uap air di fasilitas pengolahan dan transportasi
bull memenuhi spesifikasi kadar air
bull mencegah korosi
KandunganKadar Air TEG Losses
Bagaimana mengontrol air dan TEG yang terikut gas dalam proses dehidrasi di TEG Dehydration
Unit
Bagaimana menentukan paramater tuning yang sesuai untuk proses TEG Dehydration
Melakukan konvergensi simulasi steady state dan dynamic dengan pendekatan proses absorbsi pada TEG Dehydration Unit
Melakukan penilaian unjuk kerja pengendali PID Controller dan Model Predictive Control (MPC) menggunakan metode Integral of The Absolute Value of Error (IAE)
Menentukan parameter tuning yang tepat untuk sistem pengendalian di TEG Dehydration Unit dengan menggunakan PID Controller dan Model Predictive Control (MPC)
Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg
Polimer yang lebih besar TEG dan TREG memiliki sifat terbaik untuk dehidrasi TREG memiliki sifat sedikit lebih baik daripada
TEG tetapi karena biaya tambahan TREG TEG menawarkan yang terbaik kompromi biaya manfaat dan karena itu glikol tersebut
yang paling umum digunakan
PID merupakan kontrol konvensional yang sudah dipakai untuk berbagai macam variabel proses
industri dengan konsep feedback controller
MPC adalah kontrol tingkat lanjut dengan kemampuan yaitu
MPC dapat digunakan untuk multivariabel process dengan mudah dapat digunakan untuk berbagai
macam constraint
Start
Pengumpulan amp Pengolahan Data
Simulasi Process Steady State dengan ASPEN
HYSYS
Validasi Hasil Simulasi
Sizing dan Perubahan ke Dynamic Mode
Analisa Pengendalian dengan MPC
Yes
No
Analisa Pengendalian dengan PID Control
End
Membandingkan pengendalian dengan IAE
Pemilihan Fluid Package Peng Robinson
Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2
Simulasi Steady State TEG Dehydration Unit
TEG Regeneration Package
PumpTEG Cooler
Dry Gas
TEG Flash Gas
TEG Contactor TEG Flash
Drum
KODrum
Rich TEG
Lean TEG
Hot TEG Exch
Cold TEG Exch
ReboilerTo Regenerator
Lean TEG
Sweet Gas
Hydrocarbon liquid
Dehydrated Gas
Water gas
TEG Make-upSaturated Water
Feed Gas
QReboiler
Tabel Validasi
Kolom Kontaktor
Dry Gas Rich TEG
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 002 002 0 2673 2551 456
TEG 0 0 0 7063 7178 -162
Suhu (OC) 4593 4575 039 4586 4574 026
Flowrate (kmolhr) 6461 6451 015 7049 6936 16
Sweet Gas Lean TEG
Design Simulasi Eror() Design Simulasi Eror()
Komponen (mol)
H2O 022 022 0 844 844 0
TEG 0 0 0 9156 9156 0
Suhu (OC) 4824 4824 0 4824 4824 0
Flowrate (kmolhr) 6476 6476 0 5438 5438 0
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Natural Gas
bull mencegah pembentukan hidrat dan kondensasi bebas uap air di fasilitas pengolahan dan transportasi
bull memenuhi spesifikasi kadar air
bull mencegah korosi
KandunganKadar Air TEG Losses
Bagaimana mengontrol air dan TEG yang terikut gas dalam proses dehidrasi di TEG Dehydration
Unit
Bagaimana menentukan paramater tuning yang sesuai untuk proses TEG Dehydration
Melakukan konvergensi simulasi steady state dan dynamic dengan pendekatan proses absorbsi pada TEG Dehydration Unit
Melakukan penilaian unjuk kerja pengendali PID Controller dan Model Predictive Control (MPC) menggunakan metode Integral of The Absolute Value of Error (IAE)
Menentukan parameter tuning yang tepat untuk sistem pengendalian di TEG Dehydration Unit dengan menggunakan PID Controller dan Model Predictive Control (MPC)
Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg
Polimer yang lebih besar TEG dan TREG memiliki sifat terbaik untuk dehidrasi TREG memiliki sifat sedikit lebih baik daripada
TEG tetapi karena biaya tambahan TREG TEG menawarkan yang terbaik kompromi biaya manfaat dan karena itu glikol tersebut
yang paling umum digunakan
PID merupakan kontrol konvensional yang sudah dipakai untuk berbagai macam variabel proses
industri dengan konsep feedback controller
MPC adalah kontrol tingkat lanjut dengan kemampuan yaitu
MPC dapat digunakan untuk multivariabel process dengan mudah dapat digunakan untuk berbagai
macam constraint
Start
Pengumpulan amp Pengolahan Data
Simulasi Process Steady State dengan ASPEN
HYSYS
Validasi Hasil Simulasi
Sizing dan Perubahan ke Dynamic Mode
Analisa Pengendalian dengan MPC
Yes
No
Analisa Pengendalian dengan PID Control
End
Membandingkan pengendalian dengan IAE
Pemilihan Fluid Package Peng Robinson
Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2
Simulasi Steady State TEG Dehydration Unit
TEG Regeneration Package
PumpTEG Cooler
Dry Gas
TEG Flash Gas
TEG Contactor TEG Flash
Drum
KODrum
Rich TEG
Lean TEG
Hot TEG Exch
Cold TEG Exch
ReboilerTo Regenerator
Lean TEG
Sweet Gas
Hydrocarbon liquid
Dehydrated Gas
Water gas
TEG Make-upSaturated Water
Feed Gas
QReboiler
Tabel Validasi
Kolom Kontaktor
Dry Gas Rich TEG
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 002 002 0 2673 2551 456
TEG 0 0 0 7063 7178 -162
Suhu (OC) 4593 4575 039 4586 4574 026
Flowrate (kmolhr) 6461 6451 015 7049 6936 16
Sweet Gas Lean TEG
Design Simulasi Eror() Design Simulasi Eror()
Komponen (mol)
H2O 022 022 0 844 844 0
TEG 0 0 0 9156 9156 0
Suhu (OC) 4824 4824 0 4824 4824 0
Flowrate (kmolhr) 6476 6476 0 5438 5438 0
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Bagaimana mengontrol air dan TEG yang terikut gas dalam proses dehidrasi di TEG Dehydration
Unit
Bagaimana menentukan paramater tuning yang sesuai untuk proses TEG Dehydration
Melakukan konvergensi simulasi steady state dan dynamic dengan pendekatan proses absorbsi pada TEG Dehydration Unit
Melakukan penilaian unjuk kerja pengendali PID Controller dan Model Predictive Control (MPC) menggunakan metode Integral of The Absolute Value of Error (IAE)
Menentukan parameter tuning yang tepat untuk sistem pengendalian di TEG Dehydration Unit dengan menggunakan PID Controller dan Model Predictive Control (MPC)
Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg
Polimer yang lebih besar TEG dan TREG memiliki sifat terbaik untuk dehidrasi TREG memiliki sifat sedikit lebih baik daripada
TEG tetapi karena biaya tambahan TREG TEG menawarkan yang terbaik kompromi biaya manfaat dan karena itu glikol tersebut
yang paling umum digunakan
PID merupakan kontrol konvensional yang sudah dipakai untuk berbagai macam variabel proses
industri dengan konsep feedback controller
MPC adalah kontrol tingkat lanjut dengan kemampuan yaitu
MPC dapat digunakan untuk multivariabel process dengan mudah dapat digunakan untuk berbagai
macam constraint
Start
Pengumpulan amp Pengolahan Data
Simulasi Process Steady State dengan ASPEN
HYSYS
Validasi Hasil Simulasi
Sizing dan Perubahan ke Dynamic Mode
Analisa Pengendalian dengan MPC
Yes
No
Analisa Pengendalian dengan PID Control
End
Membandingkan pengendalian dengan IAE
Pemilihan Fluid Package Peng Robinson
Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2
Simulasi Steady State TEG Dehydration Unit
TEG Regeneration Package
PumpTEG Cooler
Dry Gas
TEG Flash Gas
TEG Contactor TEG Flash
Drum
KODrum
Rich TEG
Lean TEG
Hot TEG Exch
Cold TEG Exch
ReboilerTo Regenerator
Lean TEG
Sweet Gas
Hydrocarbon liquid
Dehydrated Gas
Water gas
TEG Make-upSaturated Water
Feed Gas
QReboiler
Tabel Validasi
Kolom Kontaktor
Dry Gas Rich TEG
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 002 002 0 2673 2551 456
TEG 0 0 0 7063 7178 -162
Suhu (OC) 4593 4575 039 4586 4574 026
Flowrate (kmolhr) 6461 6451 015 7049 6936 16
Sweet Gas Lean TEG
Design Simulasi Eror() Design Simulasi Eror()
Komponen (mol)
H2O 022 022 0 844 844 0
TEG 0 0 0 9156 9156 0
Suhu (OC) 4824 4824 0 4824 4824 0
Flowrate (kmolhr) 6476 6476 0 5438 5438 0
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Melakukan konvergensi simulasi steady state dan dynamic dengan pendekatan proses absorbsi pada TEG Dehydration Unit
Melakukan penilaian unjuk kerja pengendali PID Controller dan Model Predictive Control (MPC) menggunakan metode Integral of The Absolute Value of Error (IAE)
Menentukan parameter tuning yang tepat untuk sistem pengendalian di TEG Dehydration Unit dengan menggunakan PID Controller dan Model Predictive Control (MPC)
Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg
Polimer yang lebih besar TEG dan TREG memiliki sifat terbaik untuk dehidrasi TREG memiliki sifat sedikit lebih baik daripada
TEG tetapi karena biaya tambahan TREG TEG menawarkan yang terbaik kompromi biaya manfaat dan karena itu glikol tersebut
yang paling umum digunakan
PID merupakan kontrol konvensional yang sudah dipakai untuk berbagai macam variabel proses
industri dengan konsep feedback controller
MPC adalah kontrol tingkat lanjut dengan kemampuan yaitu
MPC dapat digunakan untuk multivariabel process dengan mudah dapat digunakan untuk berbagai
macam constraint
Start
Pengumpulan amp Pengolahan Data
Simulasi Process Steady State dengan ASPEN
HYSYS
Validasi Hasil Simulasi
Sizing dan Perubahan ke Dynamic Mode
Analisa Pengendalian dengan MPC
Yes
No
Analisa Pengendalian dengan PID Control
End
Membandingkan pengendalian dengan IAE
Pemilihan Fluid Package Peng Robinson
Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2
Simulasi Steady State TEG Dehydration Unit
TEG Regeneration Package
PumpTEG Cooler
Dry Gas
TEG Flash Gas
TEG Contactor TEG Flash
Drum
KODrum
Rich TEG
Lean TEG
Hot TEG Exch
Cold TEG Exch
ReboilerTo Regenerator
Lean TEG
Sweet Gas
Hydrocarbon liquid
Dehydrated Gas
Water gas
TEG Make-upSaturated Water
Feed Gas
QReboiler
Tabel Validasi
Kolom Kontaktor
Dry Gas Rich TEG
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 002 002 0 2673 2551 456
TEG 0 0 0 7063 7178 -162
Suhu (OC) 4593 4575 039 4586 4574 026
Flowrate (kmolhr) 6461 6451 015 7049 6936 16
Sweet Gas Lean TEG
Design Simulasi Eror() Design Simulasi Eror()
Komponen (mol)
H2O 022 022 0 844 844 0
TEG 0 0 0 9156 9156 0
Suhu (OC) 4824 4824 0 4824 4824 0
Flowrate (kmolhr) 6476 6476 0 5438 5438 0
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg
Polimer yang lebih besar TEG dan TREG memiliki sifat terbaik untuk dehidrasi TREG memiliki sifat sedikit lebih baik daripada
TEG tetapi karena biaya tambahan TREG TEG menawarkan yang terbaik kompromi biaya manfaat dan karena itu glikol tersebut
yang paling umum digunakan
PID merupakan kontrol konvensional yang sudah dipakai untuk berbagai macam variabel proses
industri dengan konsep feedback controller
MPC adalah kontrol tingkat lanjut dengan kemampuan yaitu
MPC dapat digunakan untuk multivariabel process dengan mudah dapat digunakan untuk berbagai
macam constraint
Start
Pengumpulan amp Pengolahan Data
Simulasi Process Steady State dengan ASPEN
HYSYS
Validasi Hasil Simulasi
Sizing dan Perubahan ke Dynamic Mode
Analisa Pengendalian dengan MPC
Yes
No
Analisa Pengendalian dengan PID Control
End
Membandingkan pengendalian dengan IAE
Pemilihan Fluid Package Peng Robinson
Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2
Simulasi Steady State TEG Dehydration Unit
TEG Regeneration Package
PumpTEG Cooler
Dry Gas
TEG Flash Gas
TEG Contactor TEG Flash
Drum
KODrum
Rich TEG
Lean TEG
Hot TEG Exch
Cold TEG Exch
ReboilerTo Regenerator
Lean TEG
Sweet Gas
Hydrocarbon liquid
Dehydrated Gas
Water gas
TEG Make-upSaturated Water
Feed Gas
QReboiler
Tabel Validasi
Kolom Kontaktor
Dry Gas Rich TEG
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 002 002 0 2673 2551 456
TEG 0 0 0 7063 7178 -162
Suhu (OC) 4593 4575 039 4586 4574 026
Flowrate (kmolhr) 6461 6451 015 7049 6936 16
Sweet Gas Lean TEG
Design Simulasi Eror() Design Simulasi Eror()
Komponen (mol)
H2O 022 022 0 844 844 0
TEG 0 0 0 9156 9156 0
Suhu (OC) 4824 4824 0 4824 4824 0
Flowrate (kmolhr) 6476 6476 0 5438 5438 0
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
PID merupakan kontrol konvensional yang sudah dipakai untuk berbagai macam variabel proses
industri dengan konsep feedback controller
MPC adalah kontrol tingkat lanjut dengan kemampuan yaitu
MPC dapat digunakan untuk multivariabel process dengan mudah dapat digunakan untuk berbagai
macam constraint
Start
Pengumpulan amp Pengolahan Data
Simulasi Process Steady State dengan ASPEN
HYSYS
Validasi Hasil Simulasi
Sizing dan Perubahan ke Dynamic Mode
Analisa Pengendalian dengan MPC
Yes
No
Analisa Pengendalian dengan PID Control
End
Membandingkan pengendalian dengan IAE
Pemilihan Fluid Package Peng Robinson
Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2
Simulasi Steady State TEG Dehydration Unit
TEG Regeneration Package
PumpTEG Cooler
Dry Gas
TEG Flash Gas
TEG Contactor TEG Flash
Drum
KODrum
Rich TEG
Lean TEG
Hot TEG Exch
Cold TEG Exch
ReboilerTo Regenerator
Lean TEG
Sweet Gas
Hydrocarbon liquid
Dehydrated Gas
Water gas
TEG Make-upSaturated Water
Feed Gas
QReboiler
Tabel Validasi
Kolom Kontaktor
Dry Gas Rich TEG
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 002 002 0 2673 2551 456
TEG 0 0 0 7063 7178 -162
Suhu (OC) 4593 4575 039 4586 4574 026
Flowrate (kmolhr) 6461 6451 015 7049 6936 16
Sweet Gas Lean TEG
Design Simulasi Eror() Design Simulasi Eror()
Komponen (mol)
H2O 022 022 0 844 844 0
TEG 0 0 0 9156 9156 0
Suhu (OC) 4824 4824 0 4824 4824 0
Flowrate (kmolhr) 6476 6476 0 5438 5438 0
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
MPC adalah kontrol tingkat lanjut dengan kemampuan yaitu
MPC dapat digunakan untuk multivariabel process dengan mudah dapat digunakan untuk berbagai
macam constraint
Start
Pengumpulan amp Pengolahan Data
Simulasi Process Steady State dengan ASPEN
HYSYS
Validasi Hasil Simulasi
Sizing dan Perubahan ke Dynamic Mode
Analisa Pengendalian dengan MPC
Yes
No
Analisa Pengendalian dengan PID Control
End
Membandingkan pengendalian dengan IAE
Pemilihan Fluid Package Peng Robinson
Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2
Simulasi Steady State TEG Dehydration Unit
TEG Regeneration Package
PumpTEG Cooler
Dry Gas
TEG Flash Gas
TEG Contactor TEG Flash
Drum
KODrum
Rich TEG
Lean TEG
Hot TEG Exch
Cold TEG Exch
ReboilerTo Regenerator
Lean TEG
Sweet Gas
Hydrocarbon liquid
Dehydrated Gas
Water gas
TEG Make-upSaturated Water
Feed Gas
QReboiler
Tabel Validasi
Kolom Kontaktor
Dry Gas Rich TEG
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 002 002 0 2673 2551 456
TEG 0 0 0 7063 7178 -162
Suhu (OC) 4593 4575 039 4586 4574 026
Flowrate (kmolhr) 6461 6451 015 7049 6936 16
Sweet Gas Lean TEG
Design Simulasi Eror() Design Simulasi Eror()
Komponen (mol)
H2O 022 022 0 844 844 0
TEG 0 0 0 9156 9156 0
Suhu (OC) 4824 4824 0 4824 4824 0
Flowrate (kmolhr) 6476 6476 0 5438 5438 0
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Start
Pengumpulan amp Pengolahan Data
Simulasi Process Steady State dengan ASPEN
HYSYS
Validasi Hasil Simulasi
Sizing dan Perubahan ke Dynamic Mode
Analisa Pengendalian dengan MPC
Yes
No
Analisa Pengendalian dengan PID Control
End
Membandingkan pengendalian dengan IAE
Pemilihan Fluid Package Peng Robinson
Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2
Simulasi Steady State TEG Dehydration Unit
TEG Regeneration Package
PumpTEG Cooler
Dry Gas
TEG Flash Gas
TEG Contactor TEG Flash
Drum
KODrum
Rich TEG
Lean TEG
Hot TEG Exch
Cold TEG Exch
ReboilerTo Regenerator
Lean TEG
Sweet Gas
Hydrocarbon liquid
Dehydrated Gas
Water gas
TEG Make-upSaturated Water
Feed Gas
QReboiler
Tabel Validasi
Kolom Kontaktor
Dry Gas Rich TEG
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 002 002 0 2673 2551 456
TEG 0 0 0 7063 7178 -162
Suhu (OC) 4593 4575 039 4586 4574 026
Flowrate (kmolhr) 6461 6451 015 7049 6936 16
Sweet Gas Lean TEG
Design Simulasi Eror() Design Simulasi Eror()
Komponen (mol)
H2O 022 022 0 844 844 0
TEG 0 0 0 9156 9156 0
Suhu (OC) 4824 4824 0 4824 4824 0
Flowrate (kmolhr) 6476 6476 0 5438 5438 0
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Pemilihan Fluid Package Peng Robinson
Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2
Simulasi Steady State TEG Dehydration Unit
TEG Regeneration Package
PumpTEG Cooler
Dry Gas
TEG Flash Gas
TEG Contactor TEG Flash
Drum
KODrum
Rich TEG
Lean TEG
Hot TEG Exch
Cold TEG Exch
ReboilerTo Regenerator
Lean TEG
Sweet Gas
Hydrocarbon liquid
Dehydrated Gas
Water gas
TEG Make-upSaturated Water
Feed Gas
QReboiler
Tabel Validasi
Kolom Kontaktor
Dry Gas Rich TEG
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 002 002 0 2673 2551 456
TEG 0 0 0 7063 7178 -162
Suhu (OC) 4593 4575 039 4586 4574 026
Flowrate (kmolhr) 6461 6451 015 7049 6936 16
Sweet Gas Lean TEG
Design Simulasi Eror() Design Simulasi Eror()
Komponen (mol)
H2O 022 022 0 844 844 0
TEG 0 0 0 9156 9156 0
Suhu (OC) 4824 4824 0 4824 4824 0
Flowrate (kmolhr) 6476 6476 0 5438 5438 0
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Tabel Validasi
Kolom Kontaktor
Dry Gas Rich TEG
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 002 002 0 2673 2551 456
TEG 0 0 0 7063 7178 -162
Suhu (OC) 4593 4575 039 4586 4574 026
Flowrate (kmolhr) 6461 6451 015 7049 6936 16
Sweet Gas Lean TEG
Design Simulasi Eror() Design Simulasi Eror()
Komponen (mol)
H2O 022 022 0 844 844 0
TEG 0 0 0 9156 9156 0
Suhu (OC) 4824 4824 0 4824 4824 0
Flowrate (kmolhr) 6476 6476 0 5438 5438 0
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Tabel Validasi
Kolom Regenerasi
To Regenerator Water Gas
Design Simulasi Eror () Design Simulasi Eror ()
Komponen (mol)
H2O 72 73 139 9619 096 02
TEG 27 26 37 002 002 0
Suhu (OC) 165 165 0 102 102 0
Flowrate (kmolhr) 6915 6801 165 1478 1364 772
Hot Lean TEG
Design Simulasi Eror()
Komponen (mol)
H2O 844 844 0
TEG 9156 9156 0
Suhu (OC) 2045 2045 0
Flowrate (kmolhr) 5438 5438 0
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Simulasi Dynamic
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Simulasi Dynamic
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Pemasangan Controller
Simbol Controlled Variable Manipulated Variable
PIC -100 Tekanan Condenser Laju alir Water Gas
PIC-101 Tekanan Flash Drum Laju alir Flash Gas
LIC-100 Level Flash Drum Laju alir To Hot HE
LIC-101 Level Reboiler Laju alir Hot Lean TEG
TIC-100 Suhu top product kolom Regenerator Condenser Duty
TIC-101 Suhu bottom product kolom Regenerator Reboiler Duty
Disturbance
Komposisi H2O pada Sweet Gas
00022 (mol) 00019 (mol) 00024 (mol) -10 +10
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Tuning Parameter
Controller Kc τi (menit) τd (menit)
PIC -100 432 247E-2 55E-3
PIC-101 253 641E-3 -
LIC-100 264 0528 -
LIC-101 267 15 -
TIC-100 884 869E-2 193E-2
TIC-101 147 0632 014
PID
Control Horizon (M) 25
Prediction Horizon (P) 5
Sample Time (T) 20
Model Horizon (N) 2000
MPC
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
+10 disturbance -10 disturbance
Flash Drum
5249
52495
525
52505
5251
0 10000 20000 30000 40000
Pre
ssu
re (
bar
g)
Time (s)
Flash Drum Pressure
9699
97
9701
9702
9703
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
9698
9699
97
9701
0 10000 20000 30000 40000
Leve
l (
)
Time (s)
Flash Drum Level
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
+10 disturbance -10 disturbance
Kolom Regenerator
4994
4996
4998
50
5002
5004
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
4999
50
5001
5002
0 5000 10000 15000
Leve
l (
)
Time (s)
Reboiler Level
900E-02
900E-02
900E-02
900E-02
900E-02
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time(s)
Condenser Pressure
008998
008999
009
009001
0 5000 10000 15000
Pre
ssu
re (
bar
g)
Time (s)
Condenser Pressure
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
+10 disturbance -10 disturbance
Kolom Regenerator
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
PID
204534
204536
204538
20454
204542
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Hot Lean TEG Temp
1019995
102
1020005
102001
0 5000 10000 15000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temp
203
204
205
206
0 2000 4000 6000 8000 10000
Tem
pe
ratu
re (
oC
)
Time(s)
Hot Lean TEG Temperature
1019
10195
102
10205
1021
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
+10 disturbance
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
PID
-10 disturbance
204534
204536
204538
20454
204542
0 5000 10000 15000
Tem
p (
oC
)
Time (s)
Hot Lean TEG Temp
101994
101996
101998
102
102002
0 5000 10000 15000Tem
pe
ratu
re (
OC
)
Time (s)
Water Gas Temp
203
204
205
206
207
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Waktu (s)
Hot Lean TEG Temp
1018
1019
102
1021
1022
0 2000 4000 6000 8000 10000Tem
pe
ratu
re (
oC
)
Time (s)
Water Gas Temperature
MPC
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Kandungan Air pada Dry Gas
78
8
82
84
86
88
9
92
94
96
98
0 10000 20000 30000 40000
Kan
du
nga
n a
ir (
lbM
MSC
F)
Time (s)
Kandungan Air pada Dry Gas
Sebelum dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sebelum Dikontrol (-10disturbance)
Sesudah Dikontrol (-10disturbance)
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Jumlah TEG Losses
470E-02
520E-02
570E-02
620E-02
670E-02
720E-02
770E-02
820E-02
870E-02
0 5000 10000 15000 20000 25000 30000 35000 40000
TEG
Lo
sse
s (g
alM
MSC
F)
Time (s)
TEG Losses
Sebelum Dikontrol (+10disturbance)
Sesudah dikontrol (+10disturbance)
Sesudah Dikontrol (-10disturbance)
Sebelum dikontrol (-10disturbance)
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
10 -10 Vessel Pressure 989E-05 0000101
Vessel Level 0014327 0006476 Condenser Pressure 275E-05 288E-05
Hot Lean TEG 0127799 0126832 Water Gas Temp 0000313 0000539 Reboiler Level 0041899 0014523
Perbandingan IAE
MPC 10 -10 Hot Lean TEG 1032108963 1618996
Water Gas 1440531279 1576381
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Cara untuk meminimalkan TEG Losses adalah dengan cara mengendalikan suhu pada kolom regenerator di mana dapat dilakukan baik menggunakan Proportional Integral Derivative Control (PID) Control maupun dengan Model Predictive Control (MPC)
Dari perbandingan IAE dapat disimpulkan bahwa MPC menghasilkan nilai yang lebih besar dari 2 controller PID untuk temperatur
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
Bahadori A amp Vuthaluru H B 2009 Simple Methodology for Sizing of Absorbers for TEG (Triethylene Glycol) Gas Dehydration Systems Energy 34 1910-1916 Chen and Mathias 1999 Applied Thermodynamics For Process Modelling AiChe Journal February 2002 Vol 48 No 2 Christensen D L 2009 Gas Dehydration(Themodynamic Simulation of The WaterGlycol Mixture) K10 ndash Aalborg University Esbjerg Gandhidasan P Al-Farayedhi A A Al-Mubarak A A 2001 Dehydration of Natural Gas Using Solid Desiccants Energy 26855-68 Gironi F M Maschietti V Piemonte 2012 Modelling Triethylene Glycol ndash Water system for Natural Gas Dehydration Universitagrave degli Studi di Roma ldquoLa Sapienzardquo Roma Italy GPSA 2004 Gas Processors and Suppliers Engineer Databook USATulsa Hernandez-Valencia Vincente N Hlavinka Michael W amp Bullin Jerry A 2006 Design Glycol Units for Maximum Efficiency Texas Bryan Bryan Research amp Engineering Inc Kvamsdal H M Jakobsen JP amp Hoff KA 2009 Dynamic Modeling and Simulation of a CO2 Absorber Column for Post-Combustion CO2 Capture Chemical Engineering and Processing 48 135-144 Nasution Anggi Arifin dan Anton Santoso 2008 Strategi Tuning Unconstrained Model Predictive Control untuk Multivariabel Proses (2x2 Fopdt) dengan Memperhatikan Interaksi Proses Skripsi S1 ITS Surabaya Nivargi J P Gupta D F Shaikh S J amp Shah K T 2005 TEG Contactor for Gas Dehydration Asubhai Media PVT Ltd Oslashi Lars Erik amp Selstoslash Elisabeth Tyvand 2003 Process Simulation of Gycol Regeneration Telemark University College Oyenekan BA amp Rochelle GT 2007 Alternative Stripper Configurations for CO2 Capture by Aqueous Amine AlCheJournal 53(12) 3144-3154 Prosim 2010 ProSim Plus Application Example Natural Gas Dehydration Unit with Tryethylene Glycol Labegravege France Seborg Dale E Edgar Thomas F amp Mellichamp Duncan A 2004 Process and Dynamic Control 2nd edition John Wiley amp Sons Inc Singapore Tu H amp Rinard IH 2006 ForeSee ldquoA Hierarchial Dynamic Modelling and Simulation System for Complex Processesrdquo Computers amp Chemical Engineering 30(9) 1324-1345
THANK YOU
TERIMA KASIH
谢谢
THANK YOU
TERIMA KASIH
谢谢
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