Evaluation Of Co Capture With Membranes From -Books Pdf

Evaluation of CO capture with membranes from

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blended with selected PEO and PEO-PDMS copolymer additives with improved separation performance and long term performance sustainability; (2) the 2nd generation membrane: composite hollow fibre membranes developed in this study with multi-layer coating using selected CO2-philic PEO-PA block copolymers (PEBAX ) as selective layer.




CO2CRC PARTICIPANTS
Core Research Industry Government Supporting
Participants Participants Participants
CSIRO ANLEC R D CanSyd Australia
Curtin University BG Group Charles Darwin University
Geoscience Australia BHP Billiton Government of South Australia
GNS Science BP Developments Australia Lawrence Berkeley National Laboratory
Monash University Brown Coal Innovation Australia Process Group
Simon Fraser University Chevron The Global CCS Institute
University of Adelaide State Government Victoria Dept of State University of Queensland
University of Melbourne Development Business Innovation
University of New South Wales INPEX
University of Western Australia KIGAM
NSW Government Dept Trade Investment
Western Australia Dept of Mines and Petroleum
Evaluation of CO2 capture with high
performance hollow fibre membranes from
Final Report
ANLEC Project 3 1110 0087
Dr Hongyu Li Professor Vicki Chen Jingwei Hou
and Dr Guangxi Dong
February 2015
CO2CRC Report No RPT14 5254
Acknowledgements
The authors wish to acknowledge financial assistance provided to the CO2CRC by the Australian
Government through its CRC program and through Australian National Low Emissions Coal Research
and Development ANLEC R D ANLEC R D is supported by Australian Coal Association Low
Emissions Technology Limited and the Australian Government through the Clean Energy Initiative
CO2CRC Limited
School of Earth Sciences University of Melbourne
Level 3 253 283 Elgin Street VIC 3010
PO Box 1182 Carlton VIC 3053
p 61 3 9035 9729
www co2crc com au
Reference Li H Chen V Dong G and Hou J 2015 Evaluation of CO2 Capture with High
Performance Hollow Fibre Membranes from Flue Gas Final Report ANLEC report Cooperative
Research Centre for Greenhouse Gas Technologies Canberra Australia CO2CRC Publication
Number RPT14 5254 pp 109
CO2CRC 2015
Unless otherwise specified the Cooperative Research Centre for Greenhouse Gas Technologies
CO2CRC retains copyright over this publication through its incorporated entity CO2CRC Ltd You
must not reproduce distribute publish copy transfer or commercially exploit any information
contained in this publication that would be an infringement of any copyright patent trademark design
or other intellectual property right
Requests and inquiries concerning copyright should be addressed to the Commercial Manager
CO2CRC PO Box 1130 Bentley WA 6102 AUSTRALIA Telephone 61 8 6436 865
Executive Summary
This final technical report is prepared for ANLEC R D Project 3 1110 0087 This project
aimed to fabricate high performance hollow fibre membranes for CO2 capture from flue gases
and to assess their performance with both a laboratory synthesised gas mixture and real flue
gases from a power plant In concluding this project we were expected to
1 Select one or two polymers and additives commercial polymers as materials for
production of hollow fibre membranes with potential for superior performance based on
the CO2 permeability and CO2 N2 selectivity
2 Develop 2 hollow fibre membranes with improved CO2 permeability of at least 50
higher and comparable CO2 N2 selectivity compared to benchmark hollow fibre
3 Evaluate the tolerance of the hollow fibre membranes to impurities in flue gas with the
objective of achieving stabilised selectivity and permeance over one month operation
4 Test the performance of membranes developed in this project with real flue gas on site
a power plant
The project started with an extensive State of the Art assessment of material selection and
baseline performance criteria that considered the major techno economic issues for large
scale deployment Fundamental technology background for membrane gas separation and
its application in CO2 capture particularly in post combustion flue gas CO2 capture were
reviewed This was followed by identification of benchmark membrane performances based
on materials that are currently being synthesised and fabricated at scale in hollow fibre
configurations Those materials were poly p phenylene oxide polyimide Matrimid and
polyethersulfone PES They exhibit a permeance in the range of 50 GPU and CO2 N2
selectivity of 25 In conjunction with the good mechanical properties and manufacturing
maturity of these materials and in line with the use of MEA as the solvent benchmark for CO2
capture these polymers were considered to be the benchmark materials in this study As
such the CO2 N2 separation target for this project was set as the CO2 permeance surpassing
50 GPU and CO2 N2 selectivity over 25
Based on the extensive review screening and selecting benchmark polymer materials we
selected two materials for hollow fiber membrane development for laboratory and on site
tests with flue gas
1 the 1st generation membrane hollow fiber membranes fabricated using Matrimid
blended with selected PEO and PEO PDMS copolymer additives with improved
separation performance and long term performance sustainability
2 the 2nd generation membrane composite hollow fibre membranes developed in this
study with multi layer coating using selected CO2 philic PEO PA block copolymers
PEBAX as selective layer
Membranes of both generations were fabricated in house with their separation performance
tested with clean CO2 and N2 pure gases no impurities and CO2 N2 gas mixture in the
laboratory For the 1st generation membranes improved CO2 permeance between 24 34
GPU and CO2 N2 selectivity between 30 40 than commercially available products were
For the 2nd generation membranes a new protocol for dissolving Pebax 1074 grade polymer
using simple and environmentally friendly mixed solvent solution was developed followed by
systematic studies on the phase structure of Pebax dense membranes including blended
membranes and their related gas separation performances Based on this fundamental
knowledge composite hollow fiber membrane development was conducted through selection
of suitable microporous substrates selection of materials for protective gutter layer and
design and construction of a unique dip coating facility funded by CO2CRC suitable for
hollow fiber composite membranes At the best combination of the conditions screened in
this study CO2 permeance up to 560 GPU and CO2 N2 selectivity above 46 was achieved at
room temperature whereas 950 GPU and CO2 N2 selectivity of 30 was achieved at the
commonly reported temperature of 35 C This performance was better than the best
reported results for composite hollow fibers for CO2 capture
In the Phase 2 membrane development the separation performance of the candidate
Matrimid hollow fibre membrane was evaluated in the laboratory for tolerance to NO
impurity the primary impurity present in the flue gas after the pre treatment column and
water by testing with a synthesised CO2 N2 NO gas mixture with addition of water vapour
The test results indicated that the trace amounts of NO only had minor impact on the CO2 N2
separation performance for the Matrimid hollow fibre membrane with 4 Silwet L 7607
Both CO2 permeance and CO2 N2 selectivity dropped less than 10 compared with the
mixed gas permeation results without NO However the performance tested with humidified
gas gas feed passing through a water humidifier to add water vapour to the feed to the
membrane indicated severe reduction in CO2 N2 selectivity 70 and limited CO2
permeance up to 16 at water vapour activity between 0 6 and 0 86 stressing the
importance of water removal pre treatment process in membrane applications for flue gas
In evaluation of the composite hollow fiber membranes we observed that similar to that of
Matrimid based hollow fiber membranes the presence of NO did not affect the membrane
separation performance significantly The presence of a small amount of water at low activity
of 0 08 and 0 16 had an insignificant influence on the separation performance while the
evaluation at higher water activity level was not conducted due to the restricted resource in
the lab environment
With the purpose designed and constructed mobile membrane test unit the on site test with
the 1st generation Matrimid hollow fibre membrane was conducted at Delta Electricity at
Vales Point with untreated flue gas as the expected pre treatment facility linked to the other
capture plant on the same site was unavailable Seven membrane modules were prepared
with 5 modules tested on site A decrease in both CO2 permeance 15 GPU at the highest
and CO2 N2 selectivity up to 15 in comparison with the results obtained with pure gases in
the laboratory was observed However 2 of them both with 4 Silwet additive fabricated
with 15 cm air gap exhibited minimal loss of separation performance after 3 days operation
with untreated real flue gas indicating good integrity against real industrial conditions
Despite the good chemical and mechanical stability of the 1st generation membrane
prolonged tests with flue gas on site was discontinued due to the interrupted supply of flue
gas caused by power plant maintenance
When the flue gas supply was resumed the subsequent on site tests were conducted with
the 2nd generation composite hollow fiber membranes because much better performance had
been observed for the second generation membranes in lab tests The on site test of the 2nd
generation membrane composite hollow fiber membranes made with polyvinylidene fluoride
PVDF microporous fiber as substrate coated with multiple Polymer poly 1 trimethylsilyl
1 propyne PTMSP as gutter layer and PEBAX as selective layer were conducted with
three membrane modules that had been evaluated in lab tests In the first 14 days of tests
minimal pre treatment of the flue gas feed was facilitated through regular change of the
desiccant column and draining of the water trap bottle used for collection of condensed
water in the piping line Relatively stable permeance and selectivity were observed with all
three modules with CO2 permeance of 90 120 GPU and CO2 N2 selectivity of 3 5 While the
CO2 permeance and the CO2 N2 selectivity was lower than what was achieved in the lab with
synthetic gas mixture the mechanical integrity of the membrane was maintained through the
flue gas exposure in that when the membrane module was brought back to the UNSW and
dried followed by testing with pure gas only 12 reduction of CO2 permeance from 500 to
441 GPU and 5 reduction in CO2 N2 selectivity 31 2 to 29 6 was experienced
When the membrane was subjected to the flue gas without pre treatment severe loss of
permeance and selectivity of all three modules were observed and permanent damage to
the membrane mechanical integrity was suspected as evidenced by the irreversible reduction
of membrane selectivity after drying tested in the lab The damage to the membrane was
most likely due to flooding of the membrane module by condensed water in the feed line
In conclusion 2 generations of membrane were developed and tested with both lab and on
site conditions Improved CO2 separation performance was achieved with the first generation
membrane compared with existing membranes while the 2nd generation composite
membrane achieved excellent separation performance with potential to make a membrane
process competitive for CO2 capture On site test results for both generation membranes
demonstrated that the stable membrane separation performance could be achieved but
performance was severely impacted when subjected to flue gas without pre treatment
Flooding of the membrane module by condensed water in the pipeline could cause
irreversible damage to the membrane fibers
These observations suggest that pre treatment of flue gas particularly removal of water is
essential prior to feeding to the membrane system Systematic evaluation of the influence of
membrane performance by water vapour should be conducted through well controlled
experiments In addition the stable performance of the hollow fibre membranes in the field
indicate that further development of membranes with improved characteristics is highly likely
to lead to a membrane process with suitable separation performance for flue gas treatment
Executive Summary i
List of Tables iii
List of Figures iv
1 Introduction 1
1 1 Description of the project 1
1 2 Milestones and deliverables 3
1 3 Layout of this report 4
2 Membrane Gas Separation for CO2 Capture A state of the art review 6
2 1 Membrane separation mechanisms 8
2 2 Membrane structures 9
2 3 Selection of membrane materials 10
2 4 Membrane fabrication process 16
2 4 1 Phase inversion 17
2 5 Hollow fiber membrane fabrication 18
2 6 Fabrication of composite membranes 19
2 6 1 Fabrication of thin film composite TFC membrane 19
2 7 Evaluation of membrane performance 21
2 8 Constraints of large scale implementation 22
2 8 1 Physical ageing 22
2 8 2 Membrane plasticization 24
2 9 Effect of minor components 25
Water vapor 25
2 10 Economic considerations 26
2 11 Membrane process design 27
2 12 Research benchmarks 30
3 Development Hollow fiber membranes using Matrid blended with selected additives
1st generation membrane 32
3 1 Hollow fiber membrane fabrication 32
3 2 Gas permeation tests 35
3 2 1 Evaluation of PEG additive on gas separation performance 35
3 2 2 Evaluation of PEG PDMS additive on gas separation performance 37
3 3 Effect of additive on membrane CO2 plasticization 38
4 Development of composite membrane for CO2 capture from flue gas 2nd generation
membrane 41
4 1 Fabrication and evaluation of PEBAX dense film 41
4 2 The effect of blending on PEBAX dense membrane structure and separation
performance 45
4 2 1 The effect of pressure and the performance with mixed gas 51
4 3 Development of thin film composite TFC membranes 53
4 3 1 Flat sheet TFC membrane 53
4 3 2 Composite hollow fiber membranes 54
4 3 3 Screening the substrate 55
4 3 4 Stability of PTMSP gutter layer 60
4 3 5 Comparison with TFC membranes in literature 61
5 Membrane performance in the presence of NO and water vapour 63
5 1 Matrimid blended hollow fiber membranes 63
5 1 1 Effect of NO in the feed mixture 63
5 1 2 The effect of water vapour and temperature 67
5 2 Pebax composite hollow fiber membranes 70
6 Pilot Plant Design 74
6 1 Feed composition property 74
6 2 Selection of equipment 75
6 3 Nomenclature 83
7 On site tests in Vales Point Power Plant Milestone 4 84
7 1 On site installation 84
7 2 Floor Plan for the CO2CRC Membrane CO2 Capture Facility 86
7 3 On Site Test of the 1st Generation Membrane Milestone 5 87
7 3 1 Raw Flue Gas Composition 87
7 3 2 On Site Tests of blended Matrimid hollow fiber membranes 89
7 3 3 Results from On site Test 1st generation membrane 90
7 3 4 Modifications on the Flue Gas Feed Inlet Connection 93
7 4 On Site Test of the composite hollow fiber Membranes Milestone 6 94
7 4 1 Modifications on the membrane unit for the 2nd generation membrane test 94
7 4 2 Results from on site test 2nd generation membrane 95
8 Conclusions and recommendations 101
8 1 Conclusions 101
8 2 Recommendations 104
9 References 105
List of Tables
Table 1 1 Key milestones and specific tasks 3
Table 2 1 Membrane materials used in industrial scale gas separation applications 6
Table 2 2 CO2 N2 gas separation properties for variety of membrane materials 13
Table 2 3 Maturity of membrane development in gas separation applications 15
Table 2 4 Packing density of typical membrane module configuration 17
Table 2 5 Summary of the polymeric membrane materials for CO2 capture from flue gas 31
Table 3 1 Gas permeation test results for Matrimid hollow fibers with 0 4 8 and 12 wt PEO PDMS
Copolymer conducted using pure gases 37
Table 4 1 CO2 permeability and CO2 N2 selectivity of Pebax 1657 and 1074 membranes cast with
different polymer concentration solutions Gas permeation tests conducted at 200 psi and 35 C 43
Table 4 2 CO2 permeability and CO2 N2 selectivity of Pebax 1657 and 1074 dense membranes cast
with different solvent evaporation rate 200 psi and 35 C 44
Table 4 3 Thermal properties of Pebax 1657 blend membranes with IM22 and Silwet 49
Table 4 4 Thermal properties of Pebax 1074 blend membranes with IM22 and Silwet 50
Table 4 5 CO2 separation performance of PES PEBAX composite membrane 54
Table 4 6 Water flux of hollow fibre substrate pump rate 20mL min 55
Table 4 7 CO2 permeability and CO2 N2 selectivity of PES and PVDF substrates coated with gutter
layers only tested at room temperature 56
Table 4 8 Gas permeation test results of composite hollow fibers with PES and PVDF substrates 57
Table 4 9 CO2 permeability and CO2 N2 selectivity of composite hollow fiber membranes using
PTMSP as gutter layer 60
Table 5 1 Percentage change in CO2 and CO2 N2 selectivity for humidified pure gas 69
Table 6 1 Flue gas composition at the Vales Point Power Station 74
Table 6 2 Specifications of the major equipment 76
Table 6 3 Potential hazards causes consequences and controls 77
Table 6 4 Operating conditions of the membrane capture pilot plant 78
Table 6 5 Process conditions and gas composition for each line 79
Table 7 1 Flue gas composition at Vales Point Power Station 88
Table 7 2 CO2 N2 separation performance of the selected membrane modules 90
Table 7 3 Composite hollow fiber membranes developed in this study Selected modules for
tests on site with flue gas were highlighted 96
Table 7 4 Comparison of the membrane pure gas test results in lab before and after the on site test 99
List of Figures
Figure 2 1 Mass transport mechanisms in pressure driven membrane systems 8
Figure 2 2 Physical structure and morphologies of common membranes 10
Figure 2 3 Robeson upper bound correlation for CO2 N2 8 12
Figure 2 4 Methods of membrane fabrication process 16
Figure 2 5 SEM image of in house fabricated Matrimid asymmetric hollow fibre membrane 17
Figure 2 6 Schematic of a typical hollow fiber spinning process 18
Figure 2 7 Structure of multilayer TFC membrane and scheme of dip coating facility for hollow fibre
production developed during this project 20
Figure 2 8 SEM image of a hollow fibre membrane with a coated dense layer formed using a dip
coating technique 21
Figure 2 9 O2 flux profile of PES hollow fibre membrane as a function of time 57 23
Figure 2 10 CO2 permeation isotherm as a function of feed pressure pure CO2 feed stream 66 24
Figure 2 11 Effect of Membrane selectivity on capture cost of CO2 4 27
Figure 2 12 Effect of CO2 permeability on the cost of CO2 capture for different vacuum membrane
systems single stage membrane system two stage cascade membrane system and two
stage cascade membrane system RR 86 28
Figure 2 13 Stage gates to large scale implementation 29
Figure 3 1 Chemical structures of Matrimid Silwet L 7607 and PEG 400 33
Figure 3 2 Laboratory scale hollow fibre spinning equipment located at UNSW 34
Figure 3 3 In house fabricated Matrimid hollow fibre membrane and membrane module with 4 to 5
strains of fibers potted inside the stainless steel tube 34
Figure 3 4 Schematic representation of gas permeation test rig 35
Figure 3 5 Gas separation performance for Matrimid hollow fibers with 0 4 8 and 12 wt PEG The
gas permeation tests for CO2 and N2 were conducted at 6 bars at room temperature 36
Figure 3 6 CO2 N2 mixed gas 22 78 vol separation performance closed symbols are pure gas
results and open symbols indicate the mixed gas results 36
Figure 3 7 CO2 N2 mixed gas 22 78 vol separation performance closed symbols are pure gas
results and open symbols indicate the mixed gas results 38
Figure 3 8 CO2 permeance as a function of feed pressure for Matrimid hollow fibers with different
PEG contents The arrows indicate the estimated plasticization pressure 39
Figure 3 9 CO2 permeance as a function of feed pressure for Matrimid hollow fibers with different
PEO PDMS copolymer contents the arrows indicate the estimated plasticization pressure 39
Figure 3 10 CO2 permeance over time under a constant pressure 20 bar for pure Matrimid
Matrimid with 8 wt PEG and Matrimid with 8 wt PEO PDMS copolymer membranes 40
Figure 4 1 Chemical structure of general PEBAX PA and PE changes with the grades of particular
products 41
Figure 4 2 Phase images of Pebax 1657 a and 1074 b dense membranes obtained from SPM
scanning 43
Figure 4 3 CO2 and N2 permeability of Pebax 1074 membrane in gas mixture solid line compared
with pure gas dash line the initial value the value at 24hours 44
Figure 4 4 CO2 N2 selectivity of Pebax 1657 and 1074 membrane in gas mixture Pebax 1657
Pebax 1074 45
Figure 4 5 Chemical structure of PEO PDMS additives a IM22 m n 15 b Silwet 46
Figure 4 6 Phase images of Pebax 1657 blend membranes obtained from SPM 48
Figure 4 7 SPM phase images of Pebax 1074 blend membranes 48
Figure 4 8 CO2 permeability a and selectivity b of Pebax 1657 blend membranes with 10 50 wt
IM22 and Silwet conducted 35 C and 4 bars The dash line indicated the theoretical prediction of CO2
permeability contributed by the miscible PEO in IM22 and Silwet co polymer 51
Figure 4 9 CO2 solid line and N2 dash line permeability of Pebax 1074 blend membranes with
10 40wt IM22 and Silwet 35 C and 200psi 51
Figure 4 10 CO2 permeability a and CO2 N2 selectivity b of Pebax 1657 blend membranes with
20 IM22 30 and 50 Silwet at different measurement pressure operated at 35 C 52
Figure 4 11 CO2 permeability a and CO2 N2 selectivity b of Pebax 1657 blend membranes with 20
IM22 and 30 Silwet in pure gas dash line and CO2 N2 mixture solid line as a function of pressure
tested at 35 C 53
Figure 4 12 SEM image of the PES composite membrane with PEBAX as the coating layer 54
Figure 4 13 Schematic representation of the dip coating facility and the sandwich like coating layer
structure of a composite membrane 55
Figure 4 14 Relative silicon concentration profile within 10 m depth obtained from EDX analysis for
TFC membranes coated with two gutter layers 57
Figure 4 15 Chemical structure formular of PTMSP 123 58
Figure 4 16 SEM outer cross section images of TFC membranes with PVDF substrate 59
Figure 4 17 SEM images of out surface of PVDF hollow fiber substrates coated with PDMS and
PTMSP with 2 and 4 layers of coating 59
Figure 4 18 CO2 permeance and CO2 N2 permselectivity of TFC membrane measured during the
extensive period room temperature 61
Figure 4 19 High performance TFC membranes reported in literatures hollow fibre 31 52 125
126 flat sheet 4 34 48 50 108 127 this study at room temperature the grey frame indicates
the target region defined by MTR for high performance TFC membrane 62
Figure 5 1 Schematic representation of the membrane permeation set up for the pure and mixed gas
as well as for water vapour tests 63
Figure 5 2 Comparison of the CO2 N2 gas separation performance with without NO from Matrimid
hollow fibre membranes with 4 Silwet L 7607 The numbers show on the top of each column are
the actual permeance and selectivity with without NO A CO2 permeance and B CO2 N2 selectivity
Figure 5 3 Simulation results of the CO2 concentration in permeate as function of CO2 N2 selectivity
CO2 permeance is assumed at 20 GPU 67
Figure 5 4 Schematic representation of competitive sorption caused by water vapour 68
Figure 5 5 The effect of temperature and water vapour activity on separation of humidified CO2 69
Figure 5 6 The effect of water vapour in the feed evaluated with gas mixture The legends in both
figures are the same 70
Figure 5 7 Comparison of the CO2 N2 gas separation performance with pure gas and mixed gas
CO2 N2 20 80 vol under 35 C dash line pure gas solid line mixed gas 71
Figure 5 8 Comparison of the CO2 N2 gas separation performance with NO and water under 35 C
dotted line without NO solid line with NO dashed line with water vapour water activity between 0 1
to 0 17 73
Figure 6 1 Legend for the P ID and PFD 80
Figure 6 2 P ID of the membrane capture pilot plant at he Vales Point Power Station 81
Figure 6 3 PFD and stream tables for the membrane capture pilot plant at the Vales Point Power
Station 82
Figure 7 1 Overall dimensions of the mobile membrane unit 84
Figure 7 2 Sampling side of the mobile membrane unit 85
Figure 7 3 The system control side of the mobile membrane unit 85
Figure 7 4 Floor plan for the CO2CRC mobile membrane unit at Vales Point 87
Figure 7 5 CO2 permeance profiles over 3 days on site operation 91
Figure 7 6 CO2 N2 selectivity profiles over 3 days on site operation 91
Figure 7 7 Permeation flux profile of Module 2 over 3 days operation 93
Figure 7 8 Modification of flue gas in let pipe connection 94
Figure 7 9 Modifications of the on site membrane unit for the 2nd generation membrane testing
upper gas flow rate monitor and lower 2 L water trap 95
Figure 7 10 The membrane performance profiles for the composite hollow fiber or 2nd generation
membrane over 17 days on site operation module 1 upper permeance and permeation flux lower
CO2 N2 selectivity 97
Figure 7 11 The 2nd generation membrane performance profiles over 17 days on site operation
module 1 3 upper CO2 permeance lower CO2 N2 selectivity 98
Figure 7 12 Corrosion of the copper membrane module fitting after membrane flooding 100
1 Introduction
Description of the project
This research aimed to fabricate high performance hollow fiber membranes for CO2 capture
from flue gas and to compare their laboratory performance using synthesised gas mixtures
with real flue gas streams in power plants and to demonstrate the feasibility of membrane
application for CO2 capture in black coal fired post combustion flue gas Through this study
issues related to translating lab performance to industrial applications such as the influence
of pre treatment processes the minor components in the flue and effects of long term
exposure are highlighted The outcomes of this project contribute to advancing technology
development for successful demonstration of low emission coal technology in Australia by
identifying and developing appropriate membrane materials and optimising future process
configurations
The challenges for post combustion capture include maintaining acceptable CO2 N2
separation while achieving ultra high permeabilities for low feed pressures and relatively low
CO2 concentration in the feed Recent research and development around the world have
reported the potential of new polymeric materials and modules in gas separation membrane
systems to achieve significantly higher CO2 permeance by two to three orders of magnitude
compared to conventional gas separation membranes In conjunction with smart design of
multi cascade systems it is anticipated that the costs of CO2 capture from flue gas using
membranes could be significantly reduced to provide a significant cost advantage with much
fewer environmental issues compared to MEA solvent adsorption processes
This research study utilised our capacity in fabricating polymeric hollow fibres membranes
with high selectivity and our extensive experience in evaluation and understanding the
performance of membrane systems in gas separation applications We have also embarked
on development of new generation composite hollow fiber membranes with high permeation
rate to handle post combustion flue gas CO2 capture in this project Hollow fibres provide
high surface area and flexible module configurations adaptable to a number of flue gas
separation processes and rapid scale up
The project was defined into three phases


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