fabrication of nanofiltration hollow- fiber membrane for the ...
Energy Analysis of CO Separation Process with Hollow Fiber · PDF filewith Hollow Fiber...
Transcript of Energy Analysis of CO Separation Process with Hollow Fiber · PDF filewith Hollow Fiber...
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Fifth Annual Conference on Carbon Capture & Sequestration
Capture – Membranes (2)
Energy Analysis of CO2 Separation Process with Hollow Fiber Membrane
Using ASPEN Simulation Method
Hyung-Taek Kim and Hyun-Min ShimDept. of Energy Studies
Ajou University, Suwon Korea
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Contents
Background
Purpose of the Study
Simulation & Analysis Method
Schematic of Process
Results of Simulation
Conclusion
Future Work
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Background• Carbon Dioxide (CO2)- Major source of greenhouse gas from Power Plant & Industrial Process- CO2 Emission : Korea ranked 10th in the world- Kyoto Protocol : Expected to add carbon tax, emission trade
• For sustainable development, Korea must prepare for the duty for reduction of CO2 emission.
• Methods of CO2 separation : Absorption, Adsorption, Membrane- Absorption : Low conc. CO2 recovery process & large scale
Commercial plant / Blazing of absorbent, Leakage
- Adsorption : High conc. CO2 recovery process & middle scaleShort lifetime of adsorbent
- Membrane : More environmental-friendly than absorptionHigh conc. CO2 recovery process & small scaleNeed to construct commercial plant in Korea
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Purpose of the study
• Perform simulation of CO2 separation process with hollow fibermembrane by ASPEN plus & Excel.
• It is possible to analyze the actual process including unit equipments, and obtain optimum operation parameters of product or intermediate.ex) pressure, temperature, enthalpy, flow, composition etc
• Evaluating energy analysis of CO2 separation process and calculating cost of operation are required for CO2 separation & recovery.
Scale : 1,000 Nm3/day of LNG Flue GasTarget Recovery rate : 90%
Purity of CO2 : 99%
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Schematic of Hollow Fiber Membrane
H2O > CO2> O2>N2 N2
CO2N2
flue Gasflue Gas
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2.01.7O2
100100Total11.018.2H2O13.98.8CO2
72.271.3N2
Wt %Vol %Composition
0.167Pressure ratio (P2/P1)60 GPUPermeability [CO2]50 cmLength of HF20Selectivity [CO2/N2]
1000 m3/dayFeed rate0.1P2 (atm)16,000Num of HF6P1 (atm)
AmountParameterAmountParameter
2) Parameters of Hollow Fiber Membrane
1) Composition of LNG Flue Gas
Simulation & Analysis Method (1/2)• Operating Conditions
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Simulation & Analysis Method (2/2)
• Final Results
- Volume of Permeate (VP)- Volume of Retentate (VR)- CO2 Purity at Permeate - CO2 Recovery (%)- Required Surface Area of Membrane (A)
- Required amount of MembraneModule (n)
Initial Input Parameters for Membrane Module
- Permeability (Barrer) - Selectivity(CO2/N2) - Thickness of Selective layer (mm)
• Initial Input Parameters for Variables of Process
- Pressure Ratio( R ) : P feed / P perm- Stage-cut : Q feed / Q perm- Operating Temperature- Plasticizing
• Operating Conditions → Simulation for CO2 Separation Process (Supplement ofMembrane Model with Excel in ASPEN code) → Simulating Results → FindingOptimal Conditions → Energy Analysis by Exergy Method → Calculating Capital Cost
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Schematic of Process• Evaluated CO2 Separation Plant (Capacity: real exhaust gas, 1000 Nm3/day)at the Korea Research Institute of Chemical Technology (KRICT)
1. H2O removal process
2. CO2 separation process
3. CO2 liquefaction process (Not yet)
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Simulation of H2O Removal Process
FLUEGAS
COOLIN1
HTFLUG1
COOLOUT1
PHTFLUE
COOLIN2
COOLFLUE
COOLOUT2 DRYFLUE
DRN-H2O
PRECOOL
COMP
CONDENSCO2SEP
• Simulation of H2O Removal Process by ASPEN code
Gas Pre-CoolerT: 150 / 40P: 1 kg/cm2
CompressorTmax : 150OP : 6 kg/cm2
CondenserT: 150 / 25P: 6 kg/cm2
H2O SeparatorTmax : 25OP : 5.6 kg/cm2
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•
••••
•
Simulation of H2O Removal Process
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•
Simulation of H2O Removal Process
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Simulation of 1 Membrane Module
•
2 1 ( 1)( 1) 1 0i ix xy y
R R Rα αα α −⎛ ⎞− + − − − + =⎜ ⎟
⎝ ⎠
1 2
( ) ( )( ) ( )
( ) ( )
out out
A out A i ave
out
i ave
Vy VyAJ Q Px P y
VyPermeate flux x Ry
= =−
=× −
1
2
2 1
: selectivity : Feed composition : Permeate composition: Feed Pressure: Permeate Pressure : Pressure ratio( ) : Permeate rate : membrane area
i
xyPPR P PVA
α
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flux and conc. of
2. Simulation with variation of membrane property1) Fix permeability as 20, then change selectivity 20~1002) Fix selectivity as 20, then change permeability 20~1003) Change permeability as well as selectivity 20~100
Simulation of 1 Membrane Module
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•
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3636.5
3737.5
3838.5
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40
5 6 7 8 9 10 11 12 13 14 15
� � (atm)
� � (%)
9.49.59.69.79.89.91010.110.210.310.4� � (m3/hr)
ya V
� � � � � � � � � � , � � � � � �
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5 6 7 8 9 10 11 12 13 14 15
� � (atm)
� � � (m2)
0102030405060708090100� � � �
Area Module
Simulation of 1 Membrane Module
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� � � � � � � � � � � � � � �
02468
101214
10 20 30 40 50 60 70 80 90 100
� � � � �
� � (m3/hr)
V
� � � � � � � � � ,� � � � � �
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5060
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10 20 30 40 50 60 70 80 90 100
� � � � �
� � (%)
0.00E+001.00E+002.00E+003.00E+004.00E+005.00E+006.00E+007.00E+008.00E+009.00E+00� � (%)
ya XT
Simulation of 1 Membrane Module
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1. Permeability = 20, selectivity = 20~100
� � � � � � � � � � � � � � � � � �
02468
1012
20 30 40 50 60 70 80 90 100
� � �
� � �(m3/hr)
00.10.20.30.40.50.60.7� � � �
permeate rate CO2 conc of permeate
� � � � � � � � � � � � � � � � � �
240
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250
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260
20 30 40 50 60 70 80 90 100
� � ����
(m2)
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membrane area No of modules
Simulation of 1 Membrane Module
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� � � � � � � � � � � � � � � � � � �
050
100150200250300
20 30 40 50 60 70 80 90 100
� � �
� � � (m2)
0
20
40
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100� � � � �
membrane area No of modules
2. Selectivity =20, permeability = 20~100
Simulation of 1 Membrane Module
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� � � ,� � � � � � � � � � � � � � � � � �
02468
1012
20 30 40 50 60 70 80 90 100
� � � � � � �
� � � (m3/hr)
00.10.20.30.40.50.60.7� � � �
permeate rate CO2 conc of permeate
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membrane area No of modules
3. Permeability & selectivity = 20~100
Simulation of 1 Membrane Module
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Simulation of 4 membrane
DRYFLUE PERM1
RET1
4
PRET-11
DRNW-1
PRET-12
PRET-13
DRNW-2
CWIN-1
PRET-14
CWOUT-1
PERM2
RET2
PRET-21
DRNW-3
PRET-22
PRET-23
DRNW-4
CWIN-2
PRET-24
CWOUT-2
PERM3
RET3
PRET-31
DRNW-5
PRET-32
PRET-33
DRNW-6
CWIN-3
CWOUT-3
PRET-34
RET4
PERM4
MEMB-1
PUMP-1
BTK-1 COMP-1
BTK-2
AFCOOL-1
MEMB-2
BTK-3
COMP-2
BTK-4
AFCOOL-2
MEMB-3
BTK-5 COMP-3
BTK-6
AFCOOL-3
MEMB-4
User Model (Excel) for Membrane Modules in ASPEN code
• Simulation of CO2 Separation Process by ASPEN (Excel) code (Peng-Rob equation)
Linkage
→ 4 cascade of hollow fiber membraneCO2 Separation Process
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Simulation of 4 membrane
-98.7498.6171.9554.45Recovery (%)
110.06( 1 )0.27 ( 1)1.17( 2)6.03( 7)Required Module (EA)
-41.641.8105.5145.91Flow rate (m3/day)
Total4321Stage
• 4 cascade membrane modules without recycling retentate
feedfeed
permeatepermeate
COQCOQ
CO][][
)(2
22 ×
×=ψ
• Recovery, ψ (%)
Qfeed
[CO2]feed
Qretemtate
Qpermeate
[CO2]permeate
Pfeed
Ppermeate
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Simulation of 4 membrane• 4 cascade membrane modules without recycling retentate
875154.4516/0.1
Pfeed / Pperm328071.9526/1
119498.6136/1
1(0.5)199.098.7446/1
119798.3446/1218994.4036/1347067.8426/1
20403225.6716/1
Pfeed / Pperm
EXPSIMEXPSIM
Required amount of Module (7m2)Recovery (%)
StageValue (kgf/cm2)Parameter
Comparison of result for Experiment/SimulationOperating Conditions
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Simulation of CO2 Liquefaction Process
LPERCO2
LCOMP
PLPERCO2
LCONDS
CBS
CPLPRCO2
CBR
LQCO2TK
VCO2
LCO2
VCO2MIX
MXCO2
• Simulation of CO2 Liquefaction Process by ASPEN code (Peng-Rob equation)
ChillerT: 25 / -57P: 51.8 kg/cm2
CompressorT: 25P: 52 kg/cm2
CO2 V-L Separator
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Conclusions
1. Simulation method for CO2 membrane separation is developed- Simulation program composed with H2O removal, membrane modules and CO2 liquefaction processes
2. Evaluation of optimal condition of 1 membrane - Obtaining optimum parameters with fixing the concentration of
retreate and pressure as well as the variation of permeability and selectivity
3. Development of membrane model using ASPEN & EXCEL - Performing the simulation between ASPEN and EXCEL (User model)
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Future Work
1. Refine of membrane model using ASPEN & EXCEL - Link between ASPEN and EXCEL (User model)
2. Evaluation of optimum operation parameter - Obtaining the optimum parameters with change of pressure,
selectivity, permeability etc. with 4 membrane module
3. Simulation for detail equipments- Energy requirement calculations for Vacuum pump, Compressor,
Condenser for CO2 liquefaction process
4. Energy requirement & cost calculations through exergy analysis - Using each stream results by simulation for exergy calculation
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Thank you