carbon dioxide separation from flue gases: a · pdf filecarbon dioxide separation from flue...

Review ArticleCarbon Dioxide Separation from Flue Gases A TechnologicalReview Emphasizing Reduction in Greenhouse Gas Emissions

Mohammad Songolzadeh1 Mansooreh Soleimani1

Maryam Takht Ravanchi2 and Reza Songolzadeh3

1 Department of Chemical Engineering Amirkabir University of Technology PO Box 15875-4413 Tehran Iran2 Catalyst Research Group Petrochemical Research and Technology Company National Petrochemical CompanyPO Box 1435884711 Tehran Iran

3Department of Petroleum Engineering Petroleum University of Technology PO Box 6198144471 Ahwaz Iran

Correspondence should be addressed to Mansooreh Soleimani soleimanimautacir

Received 17 August 2013 Accepted 31 October 2013 Published 17 February 2014

Academic Editors D-W Han and V A Rogov

Copyright copy 2014 Mohammad Songolzadeh et al This is an open access article distributed under the Creative CommonsAttribution License which permits unrestricted use distribution and reproduction in any medium provided the original work isproperly cited

Increasing concentrations of greenhouse gases (GHGs) such as CO2in the atmosphere is a global warming Human activities are

a major cause of increased CO2concentration in atmosphere as in recent decade two-third of greenhouse effect was caused by

human activities Carbon capture and storage (CCS) is a major strategy that can be used to reduce GHGs emissionThere are threemethods for CCS pre-combustion capture oxy-fuel process and post-combustion capture Among them post-combustion captureis the most important one because it offers flexibility and it can be easily added to the operational units Various technologies areused for CO

2capture some of them include absorption adsorption cryogenic distillation andmembrane separation In this paper

various technologies for post-combustion are compared and the best condition for using each technology is identified

1 Introduction

There are ten primary GHGs including water vapor (H2O)

carbon dioxide (CO2) methane (CH

4) and nitrous oxide

(N2O) that are naturally occurring Perfluorocarbons

(CF4 C2F6) hydrofluorocarbons (CHF

3 CF3CH2F and

CH3CHF2) and sulfur hexafluoride (SF

6) are only present

in the atmosphere due to industrial processes Water vaporis the most important abundant and dominant greenhousegas and CO

2is the second-most important one (Table 1)

Concentration of water vapor depends on temperature andother meteorological conditions and not directly uponhuman activities So it was not indicated in Table 1 [1ndash3]

CO2

is the primary anthropogenic greenhouse gasaccounting for 77 of the human contribution to the green-house effect in recent decade (26 to 30 percent of all CO

2

emissions) Main anthropogenic emissions of CO2come

from the combustion of fossil fuels CO2concentration in

flue gases depends on the fuel such as coal (12ndash15mol- CO

2) and natural gas (3-4mol- CO

2) In petroleum

and other industrial plants CO2concentration in exhaust

stream depends on the process such as oil refining (8-9molCO2) and production of cement (14ndash33mol-CO

2) and iron

and steel (20ndash44mol-) From 2004 to 2011 global CO2

emissions from energy uses were increased 26 (Figure 1)[4ndash10] Figure 2 indicates that power plant (55 of globalCO2emissions) transportation (23) and industry (19)

have highest share in the CO2emission in USA Cement

and petrochemical plants are two major industries for CO2

emission such that cement industry contributes about 5to global anthropogenic CO

2emissions Also petrochemical

industries are a large share of CO2emission for example only

in Iran petrochemical industries emissionwas about 15MtonCO2year [11ndash16]The Kyoto Protocol is the first international agreement

on emissions of GHGs In this protocol industrializedcountries agreed to stabilize or reduce the GHGs emissionsin the commitment period 2008ndash2012 by 52 on average(compared to their 1990 emissions level) Overall the resultof global CO

2emissions (Figure 1) shows the failure of

Hindawi Publishing Corporatione Scientific World JournalVolume 2014 Article ID 828131 34 pageshttpdxdoiorg1011552014828131

2 The Scientific World Journal

Table 1 The main greenhouse gases and their concentration [2 3]

Compound Preindustrialconcentration (ppmv)

Concentrationin 2011 (ppmv)

Atmosphericlifetime (years) Main human activity source GWPlowastlowast

Carbon dioxide (CO2) 280 3885 sim100 Fossil fuels cement production land use 1

Methane (CH4) 0715 1871748 12 Fossil fuels rice paddies waste dumpslivestock 25

Nitrous oxide (N2O) 027 0323 114 Fertilizers combustion industrial processes 298CFC-12 (CCL2F2) 0 0000533 100 Liquid coolants foams 10900CF-113 (CCl2CClF2) 0 000000075 85 na 6130HFC 23 (CHF3) 0 0000018 270 Electronics refrigerants 11700HCFC-22 (CCl2F2) 0 0000218 12 Refrigerants 1810HFC 134 (CF3CH2F) 0 0000035 14 Refrigerants 1300HCFC-141b (CH3CCl2F) 0 000000022 93 na 725HCFC-142b (CH3CClF2) 0 000000020 179 na 2310HFC 152 (CH3CHF2) 0 00000039 14 Industrial processes 140Perfluoromethane (CF4) 000004 000008lowast 50000 Aluminum production 6500Perfluoroethane (C2F6) 0 0000003lowast 10000 Aluminum production 9200Sulfur hexafluoride (SF6) 0 000000712lowast 3200 Dielectric fluid 22800lowastConcentration in 2011lowastlowastGlobal warming potentials (GWPs) measure the relative effectiveness of GHGs in trapping the Earthrsquos heat

05

10152025303540

Year1990 1993 1996 1999 2002 2005 2008 2011

1000

mill

ion

tonn

es C

O2

Figure 1 Global CO2emissions from fossil fuel combustion and

cement production [23]

Kyoto protocol therefore in 2011 Durban COP meetingthis protocol was extended until 2017 Several countries withhigh GHGs emission like China India Brazil and evenIran have added to this Protocol Intergovernmental Panelon Climate Change (IPCC) predicted the atmosphere maycontain up to 570 ppmv CO

2by the year 2100 causing a rise

of mean global temperature and sea level around 19∘C and38m respectively [15 17ndash20] Given that the earthrsquos averagetemperature continues to rise Intergovernmental Panel onClimate Change (IPCC) stated global GHG emissions mustbe reduced by 50 to 80 percent by 2050 to avoid dramaticconsequences of global warming [21ndash23]

Carbon capture and storage (CCS) is the most indi-cated technology to decrease CO

2emission from fossil fuels

sources to atmosphere Also CO2separated from flue gases

can be used in enhanced oil recovery (EOR) operationswhereCO2is injected into oil reservoirs to increase mobility of

oil and reservoir recovery [24 25] Pure CO2has many

applications in foodbeverage and different chemical indus-tries such as urea and fertilizer production foam blowing

0

500

1000

1500

2000

2500

3000

1990

1992

1994

1996

1998

2000

2002

2004

2006

2008

Year

Tone

gas

CO2

equi

vale

nt Electric powerindustry

Transportation

Industry

AgricultureCommercialResidential

Figure 2 US GHG Emissions Allocated to Economic Sectors [2]

carbonation of beverages and dry ice production or even inthe supercritical state as supercritical solvent [26ndash28]

From this definition CCS consists of three basic stages(a) separation of CO

2 (b) transportation and (c) storage

Operating costs of these stages have been estimated in 2008

(i) CO2separation from exhausting gases 24 to 52 C

ton-CO2

(ii) transportation to storage location 1 to 6 Cton-CO2

per 100 km

(iii) storage minus28 to 42 Cton-CO2

Therefore CO2separation is a major stage in CCS The

CCS total costs can vary from minus3 to 106 Cton-CO2(negative

values are expected for the injection of CO2in EOR) There

are threemajor approaches for CCS pre-combustion captureoxy-fuel process and post-combustion capture (Figure 3)[25 30 31]

The Scientific World Journal 3

FuelCombustionAir

flue gas

Post-combustion capture

FuelCombustion

Oxy fuel combustion

FuelCombustion

COPre-combustion capture

CO2 for storage

CO2 for storage

CO2 for storage

CO2 containing

CO2 capture

CO2 capture

O2

H2O2air

Figure 3 Three basic approaches of CO2capture [29]

Pre-combustion capture involves reaction of a fuel withoxygen or air and in some cases steam to produce a gasmainly composed of carbon monoxide and hydrogen whichis known as synthesis gas (syngas) or fuel gas The producedcarbon monoxide is reacted with steam in a catalytic reactorcalled shift converter to give CO

2andmore hydrogen CO

2is

then separated usually by cryogenic distillation or chemicalabsorption process resulting in a hydrogen-rich fuel that canbe used in many applications such as furnaces gas turbinesengines and fuel cells [32 33]

A main advantage of post-combustion is the higher CO2

concentration and pressure achieved in the output streamThe main disadvantage of pre-combustion capture is systemneeds long-term development in a number of enabling tech-nical areas to achieve targeted efficiency towards a hydrogeneconomy This disadvantage has limited application of thisapproach and increased investments costs of pre-combustioncapture [34 35]

In oxy-fuel combustion nearly pure oxygen is used forcombustion instead of ambient air and this results in a fluegas that is mainly CO

2and H

2O which are separated by

condensing waterThreemajor advantages of this method arehigh CO

2concentration in output stream (above 80 vv)

high flame temperature and easy separation of exhaust gasesThe major disadvantages of oxy-fuel combustion are highcapital cost and large electric power requirement to separateoxygen from air [36ndash38]

The principle of post-combustion capture is CO2sepa-

ration from flue gas after combustion Generally the CO2

in flue gas is diluted (8ndash15 CO2) with inert gases such as

nitrogen argon and water in addition to oxygen Flue gasesare normally at atmospheric pressure and high temperatures(between 320K and 400K) [39ndash41] Post-combustion capturedoes not require expensive technologies such as syngas sep-aration hydrogen turbine fuel cell Post-combustion captureis the most important to prevent CO

2emissions because it

offers flexibility and does not need to change combustioncycle If the capture plant shuts down the power plant canstill operate [42 43] Major disadvantage of this method isunfavorable condition of flue gases

Because of the importance in selecting suitable processfor CO

2separation in this research various technologies for

this purpose have been focused

2 CO2 Separation Technologies

Based on economical and environmental considerations it isnecessary to apply efficient and suitable technology for CO

2

separation with low operating cost and energy consumptionUp to now there are several gas separation technologiesbeing investigated for post-combustion capture namely (a)absorption (b) adsorption (c) cryogenic distillation and (d)membrane separation (Figure 4) [39 44] Although variousnew methods were suggested for CO

2separation Granite

and Brien [45] reviewed some of the most novel methodsfor carbon dioxide separation from flue and fuel gas streamssuch as use of electrochemical pumps and chemical loopingfor CO

2separation

21 Absorption Absorption stripping is an important tech-nology for CO

2capture from fuel gas in this technology

desired component in mixed gases are dissolved in a solvent(bulk phase) [46] The general scheme of this process isdepicted in Figure 5

The flue gas (containing CO2) is cooled (between 318 and

323K) and fed to the absorption column (scrubber) wherethe solvent absorbs CO

2 The CO

2-rich solution is fed into

a heater to increase the temperature of solution then to astripper column to release the CO

2 The released CO

2is

compressed and the regenerated absorbent solution is cooledand recycled to the absorber column [47 48]

Energy required for post-combustion CO2capture is an

important issueThus recent studies suggest that reduction ofthe cost of this capture could be achieved by finding suitablesolvents that could process larger amounts of CO

2for a given

mass and require less energy for stripping stage [49 50]

211 Solvents In absorption process flue gas is contactedwith a liquid ldquoabsorbentrdquo (or ldquosolventrdquo) and CO

2is absorbed

by this solvent [21] However the absorbent should havea suitable capacity for CO

2absorption high kinetic rate

for CO2absorption negligible vapor pressure and high

chemical and thermal stability and should be harmless forlabor persons [51ndash53]

The solvents used for CO2absorption can be divided

into two categories physical and chemical solvents Physicalsolvent processes use organic solvents to physically absorbacid gas components rather than reacting chemically butchemical absorption depends on acid-base neutralizationreactions using alkaline solvents [54 55] In the recent yearsmany studies have compared the performance of differentsolvents as listed in Table 2

(1) Alkanolamines Between various solvent groups alka-nolamines group is the most important and more used forCO2separation A major problem in the usage of amines for

CO2absorption is equipment corrosion so Albritton et al

[56] examined corrosion rate of various amine solvents andsuggested corrosion rate could reduce in the following ordermonoethanolamine (MEA) gt 2-amino-2-methyl-1-propanol(AMP) gt diethanolamine (DEA) gt methyl diethanolamine(MDEA)


capture

Absorption

Chemical

Physical

MEA caustic ammonia solution

Selexol Rectisol fluorinated solvents

Adsorption

Physical Alumina zeolite activated carbon

Cryogenic

Membrane

Gas separation

Ceramic membrane

Polyphenyleneoxide polydimethylsiloxane

Gas absorption

Polypropylene

CO2 separation and Chemical CaO MgO Li2ZrO3 Li4SiO4

Figure 4 Different technologies for CO2separation [29]

Condenser

Feed gas cooler

Feed gas

Exhaust gas

Absorber Heater

Liquidstorage tank

Cooler Reboiler

Stripper

gas CO2 product

Figure 5 Schematic diagram of CO2absorption pilot plant

On the other way MEA can react more quickly withCO2than MDEA but MDEA has higher CO

2absorption

capacity and requires lower energy to regenerate CO2[39 57

58] Thus it can be concluded that MEA is one of the bestamine solvents for CO

2separation Idem et al [59] reported

substantial reduction in energy requirements and modestreduction in circulation rates for amine blends relative tothe corresponding single amine system of similar total amineconcentration Wang et al [57] found that when MEAand MDEA are mixed at the appropriate ratio the energyconsumption for CO

2regeneration is reduced significantly

Dave et al [28] compared the performance of several aminesolvents and ammonia solutions at various concentrationsThey showed that 30wt AMP based process has the lowestoverall energy requirement among the solvents considered intheir study (30MEA 30MDEA 25NH

3 and 5NH

3)

[28 60]Knudsen et al [61] studies showed that it is possible to

run the post-combustion capture plant continuously whileachieving roughly 90CO

2separation levels andCASTOR-2

(blended amine solvents) operated in pilot scale with lower

steam requirement and liquid-to-gas ratio (LG) than theconventional MEA solvent

Besides alkanolamines carbonate-bicarbonate buffersand hindered amines are used in the bulk removal of CO

2

owing to the low steam requirement for its regenerationMit-subishi Heavy Industries and Kansai Electric have employedother patented chemical solventsmdashstrictly hindered aminescalled KS-1 KS-2 or KS-3 The regeneration heat of KSsolvents is said to be sim3GJt CO

2 that is 20 lower than

that of MEA with sim37GJt CO2[60 64 77] Generally the

overall cost of amine absorptionstripping technology forCO2capture process is 52ndash77US$ton CO

2[71]

(2) AminoAcidAmino acids have the same functional groupsas alkanolamines and can be expected to behave similarlytowardsCO

2but do not deteriorate in the presence of oxygen

Based on the results of tests the aqueous potassium salts(composed of sarcosine and proline) are considered to bethe most promising solventsThemost common amino acidsused in the gas treating solvents are glycine alanine dimethyl


Table 2 Various solvents suggested for CO2 separation

Group of solvents Advantage Disadvantage Application Reference

Physical

Dimethyl ether ofpolyethylene glycol(Selexol)

(i) Require low energy forregeneration (less than 20 ofthe value for chemicalabsorbent)(ii) Low vapor pressure lowtoxicity and less corrosivesolvent

(i) Dependent on temperatureand pressure therefore theyare not suitable forpost-combustion process(ii) Low capacity for CO2absorption

Natural gas sweetening

[29 39 5762 63]Glycol Capturing CO2 and H2S at

higher concentration

Glycol carbonate Separating CO2 from othergases

Methanol (Rectisol) CO2 removal from variousstreams

Fluorinated solvent

(i) CO2 removal from variousstreams(ii) Separating CO2 fromother gases

Chemical

Alkanolaminesmonoethanolamine(MEA) diethanolamine(DEA) and methyldiethanolamine (MDEA)

(i) React rapidly(ii) High selectively (betweenacid and other gases)(iii) Reversible absorptionprocess(iv) Inexpensive solvent

(i) Low CO2 loading capacity(ii) Solvent degradation inexistence of SO2 and O2 in fluegas (concentrations must beless than 10 ppm and 1 ppm)(iii) High equipmentcorrosion rate(iv) High energy consumption

Important for removing acidiccomponents from gas streams

[58 60 6164ndash66]

Amino acid and aqueousamino acid salt

(i) The possibility of adding asalt functional group(ii) The nonvolatility ofsolvents(iii) Having high surfacetension(iv) Having better resistanceto degradation than otherchemical solvents(v) Better performance thanMEA of the sameconcentration for CO2absorption

Decreased performance in thepresence of oxygen

Suggested for CO2 separationfrom flue gases

[65 67ndash69]

Ammonia

(i) No degradation in thepresence of SO2 and O2 in theflue gases(ii) No corrosion effect(iii) Require low energy toregeneration (13 that requiredwith MEA)(iv) Low costs with aqueousammonia respectively 15and 20 less than with MEA

(i) Reversible at lowertemperatures (not suitable forpost-combustion)(ii) Production of solidproducts and their operatingproblems(iii) Explosion of dryCO2-NH3 reaction in the highconcentration of CO2 in theflue gas (explosive limit forNH3 gas is 15ndash28)

Suggested for CO2 separationfrom flue gases [39 70]

Ionic liquid (IL)

(i) Very low vapor pressure(ii) Good thermal stability(iii) High polarity(iv) Nontoxicity

Increased viscosity with CO2absorption

Suggested for CO2 separationfrom flue gases [71ndash74]


Table 2 Continued


Aqueous piperazine (PZ)

(i) Fast absorption kinetics(CO2 absorption rate withaqueous PZ is more thandouble that of MEA)(ii) Low degradation rates forCO2 separation(iii) Negligible thermaldegradation in concentratedPZ solutions(iv) Favorable equilibriumcharacteristics(v) Very low heat ofabsorption (10ndash15 kCalmolCO2) 80ndash90 energyrequired for aqueous aminesystem

Lower oxidative degradationof concentrated PZ (ie 4times slower than MEA in thepresence of the combination ofFe2+Cr3+Ni2+ and Fe2+V5+)

(i) Effective for treating syngasat high temperatures(ii) Application of additionalamine promoters for naturalgas treating and CO2separation from flue gases

[29 66 7576]

glycine diethyl glycine and a number of sterically hinderedamino acids [65 67 68]

Results of many research groups showed that these sol-vents are suitable for application inmembrane gas absorptionunits because these solvents have better performance anddegradation resistance than other chemical solvents [78]Amino acid salts formed by neutralization of amino acidswith an organic base such as amine showed better CO

2

absorption potential than amino acid salts from neutral-ization of amino acid salts from an inorganic base suchas potassium hydroxide [79 80] Aronu et al [69] stud-ied the performance of amino acids neutralized with 3-(methylamino)propylamine (MAPA) glycine120573-alanine andsarcosine Their results indicated that sarcosine neutralizedwith MAPA has the best CO

2absorption performance Its

performance is also enhanced by promoting with excessMAPA [69]

(3) Ammonia Since ammonia is a toxic gas prevention ofammonia ldquosliprdquo to the atmosphere is a necessity Despite thisdisadvantage chilled ammonia process (CAP) was used forCO2separation (Figure 6) In the CAP CO

2is absorbed in

an ammoniated solution at a lower absorption temperature(275ndash283K) that reduced ammonia emissions from the CAPabsorber Ammonium carbonate solution resulted in approx-imately 38 carbon regeneration compared to MEA solution[70 81 82]

(4) Aqueous Piperazine (PZ) Piperazine (PZ) is as an additiveused for amine systems to improve kinetics of CO

2absorp-

tion such as MDEAPZ or MEAPZ blends Because PZ sol-ubility in water is low concentration of PZ is between 05 and25M As indicated in Table 2 increasing the concentrationof PZ in solution allows for increased solvent capacity andfaster kineticThe presence of potassium in solution increasesthe concentration of CO

3

2minusHCO3

minus in solution thereforesolution has buffering propertyThese competing effects yielda maximum fraction of reactive species at potassium topiperazine ratio of 2 1 [75 83 84]

22 Adsorption Adsorption operation can reduce energyand cost of the capture or separation of CO

2in post-

combustion capture To achieve this goal it is necessary tofind adsorbents with suitable properties In general CO

2

adsorbent must have high selectivity and adsorption capacityand adequate adsorptiondesorption kinetics remain stableafter several adsorptiondesorption cycles and possess goodthermal and mechanical stability [51 85ndash88] The adsorbentsused for CO

2separation placed into two main categories

physical and chemical adsorbents

221 Chemical Adsorption Chemisorption is a subclass ofadsorption driven by a chemical reaction occurring at theexposed surface Adsorption capacities of different chemicaladsorbents are summarized in Table 3

A wide range of metals have been studied including [89]

(i) metal oxides CaO MgO(ii) metal salts from alkali metal compounds lithium

silicate lithium zirconate to alkaline earthmetal com-pounds (ie magnesium oxide and calcium oxide)

(iii) hydrotalcites and double salts

In general one mole of metal compound can react withone mole of CO

2with a reversible reaction The process

consists of a series of cycles wheremetal oxides (such as CaO)at 923K are transformed into metal carbonates form (such asCaCO

3) at 1123 K in a carbonation reactor to regenerate the

sorbent and produce a concentrated stream of CO2suitable

for storage [90 91]Considerable attention was paid to calcium oxide (CaO)

as it has a high CO2adsorption capacity and high raw

material availability (eg limestone) at a low cost Lithiumsalts was recorded a good performance in CO

2adsorption

but it gained less focus due to its high production costAlthough double salts can be easily regenerated due to lowenergy requirement their stability has not been investigated[93 96]


FGD

HX1

AC1

A PM1

CC1

HX2 HX3

A PM2

CC2

FN1

A PM3

CC3HC

PM5PM4

HX4HX6

HX5

PM6

PR1

HX7

FN2PR2

A

Chilmine Y

WT3 WT1WT2

AC2

PM7

RBRGAB

Steam

Condensate

CM1

AC3

CM2

AC4

PR3

CM3

AC4 PM8PIPE

Exhausts chilling

Ammonia removal

Absorptionregeneration

gas wash

CO2 compression

CH1 CH2CH3

CH4

CH5

H2ONH3

HCl

Figure 6 Schematic layout of CO2separation block based on the chilled ammonia process [92]

Table 3 Adsorption capacity of chemical adsorbents for post-combustion CO2

SorbentOperatingtemperature

(K)

Operatingpressure(kPa)

CO2 capturecapacity (mol

CO2kg sorbent)

Regenerationcycles 119899

CO2 capturecapacity remainedafter 119899 cycles ()

Reference

Mesoporous (MgO) 298 101 18 3 100 [93]CaO nanopods 873 101 175 50 611 [94]CaO derived from nanosized CaCO3 923 101 167 100 222 [93]CaO-MgAl2O4 (spinel nanoparticles) 923 101 91 65 846 [93]Nano CaOAl2O3 923 101 60 15 617 [93]Lithium silicate nanoparticles 883 101 577 na na [93]Nanocrystalline Li2ZrO3 particles 843 101 61 8 100 [93]CaOAl2O3 923 101 602 na na [93]Lithium silicate 993 na 818 na na [17]Lithium zirconate 673 100 50 na na [93]Lithium orthosilicate 873 100 613 na na [93]Calcium oxide 873 100 173 na na [93]Magnesium hydroxide 473 1034 30 na na [93]Mesoporous magnesium oxide 373 100 227 na na [93]Lithium Silicate nano particles 873 101 5 na na [95]HTI-HNa 573 134 1109 50 933 [93]

The reaction of CO2adsorptionwith Li

2ZrO3is reversible

in the temperature range of 723ndash863K The capacity oflithium silicate (82moL CO

2kg sorbent at 993K) is larger

than that of lithium zirconate (485moLkg sorbent) [17]Hydrotalcite (HT) contains layered structure with posi-

tively charged cations balanced by negatively charged anions[97 98] Adsorption and final capacity of different adsorp-tiondesorption cycles are listed in Table 3

One way for improving CO2adsorption efficiency is

application of nanomaterials Different nano-materials can beused for CO

2separation (Table 3) However nanomaterials

always have high production cost with complicated synthesisprocess such as carbon nanotubes and graphite nanoplatelets[99 100]

Themain disadvantage of chemical adsorbents is difficultregeneration process and application of these adsorbentsneeds more studies for finding new adsorbents [88 95]

222 Physical Adsorption Physisorption also called physicaladsorption is a process in which the electronic structure of

the atom or molecule is barely perturbed upon adsorptionIf the CO

2adsorption capacity of solid adsorbents reaches

3mmoLg the required energy for adsorption will be lessthan 30ndash50 energy for absorption with optimum aqueousMEA [101]Themajor physical adsorbents suggested for CO

2

adsorption include activated carbons and inorganic porousmaterials such as zeolites [102 103]The adsorption capacitiesof various physical adsorbents are summarized in Table 4

Coal is one of the adsorbents being suggested for CO2

separation The total amount of CO2that can be adsorbed

in coal depends on its porosity ash and affinity for thismolecule [111 112] Sakurovs et al [113] showed that theratio of maximum sorption capacity between CO

2and

methane decreases with increasing carbon content Theaverage CO

2CH4sorption ratio is higher for moisture-

equilibrated coal and decreases with increasing coal rank (14for high rank coals to 22 for low rank coals) [114ndash116]

Activated carbon (AC) has a number of attractive charac-teristics such as its high adsorption capacity high hydropho-bicity low cost and low energy requirement for regeneration


Table 4 Adsorption capacity of physical adsorbents for post-combustion CO2


(K)



CO2kg sorbent)


CO2 capture capacityremained after 119899

cycles ()Reference

Activated carbon 303 110 158 na na [93]AC (4 KOH) 303 30 055 na na [93]AC (EDA + EtOH) 303 30 053 na na [93]AC (4 KOH + EDA + EtOH) 303 30 064 na na [45 70 79]NiO-ACs 298 101 2227 na na [104]13X 393 15198 07 na na [105]5A 393 15198 038 na na [105 106]4A 393 15198 05 na na [105]WEG-592 393 15198 06 na na [105]APG-II 393 15198 038 na na [105]Na-Y 273 10132 49 na na [105]Na-X 373 10132 124 2 na [105]NaKA 373 10132 388 mdash na [105]NaX-h 323 10132 252 2 na [105]NaX-h 373 10132 137 2 na [105]Na-X-c 323 10132 214 2 na [105]Na-X-c 373 10132 141 2 na [105]Cs-X-h 323 10132 242 2 na [105]Cs-X-h 373 10132 148 2 na [105]Cs-X-c 323 10132 176 2 na [105]Cs-X-c 373 10132 115 na na [105]MCM-41 298 100 062 na na [93]MCM-41 (DEA) 348 100 126 na na [93]MCM-41 (50 PEI) 348 100 252 na na [93]Activated carbon 303 30 035 na na [93]MCM-41 (50 PEI) ldquomolecularbasketrdquo 348 100 295 na na [93]

PE-MCM-41 298 100 050 na na [93]PE-MCM-41 (TRI) 298 100 285 na na [93]PE-MCM-41 (DEA) 348 100 236 na na [93]MCM-48 298 100 0033 na na [93]MCM-48 (APTS) 298 100 0639 na na [93]MCM-41 298 100 062 na na [93]Molecular basketrsquoMCM-41 (50 PEI) 348 100 25 8 960 [93]

PE-MCM-41 (TRI) 298 100 18 10 944 [93]PE-MCM-41 (DEA) 298 100 29 7 966 [93]MWNT 303 101 17 20 na [4 93]Unmodified [(Cu3(btc)2]

lowast 298 1818 67 na na [101]CNT (Cu3(btc)2) 298 1818 1352 na na [101]MIL-101lowastlowast 298 1010 084 na na [101]MWCNTMIL-101 298 1010 135 na na [101]MOF-2 298 4545 320 na na [107]MOF-177 298 4545 335 na na [107]Zr-MOFs 273 988 81 na na [107]Ca-Al LDH with ClO

4

minus 406 1 355 na na [108]


Table 4 Continued


(K)



CO2kg sorbent)



cycles ()Reference

Pd-GNP nanocomposite 298 1111 51 na na [109]f-GNP 298 1111 43 na na [109]Pd-GNP nanocomposite 298 1111 45 na na [109]f-GNP 298 1111 38 na na [109]Pd-GNP nanocomposite 298 1111 41 na na [109]f-GNP 298 1111 33 na na [109]Ceria-based oxides doped with 5gallium (III) 298 101 0282 na na [110]

Amine modified layered doublehydroxides (LDHs) 298ndash353 101 074ndash175 na na [108]

lowastCu3(btc)2 btc 135-benzene-tricarboxylatelowastlowastMIL-101 or Cr3(FOH)(H2O)2O[(O2C)C6H4(CO2)]3 sdot 119899H2O (119899 asymp 25) is one of the metal organic frameworks with Lewis acid sites that can be activated byremoval of guest water molecules

[117ndash119] Activated carbons are inexpensive insensitive tomoisture and easy for regeneration These adsorbents havewell developed micro- and mesopore structures that aresuitable for highCO

2adsorption capacity at ambient pressure

[120ndash122]However activated carbon CO

2N2selectivities (ca 10)

are relatively low zeolitic materials offer CO2N2selectivities

5ndash10 times greater than those of carbonaceous materialsThe adsorption capacity and selectivity of zeolites are largelyaffected by their size porous diameter charge density andchemical composition of cations in their porous structuresThe average value of heat adsorption on zeolites (36 kJmoL)is larger than for activated carbon (30 kJmoL) confirmingthe mentioned affirmation Moreover activated carbon canbe regenerated easily and completely Also its capacity did notdecay after 10 consecutive processes cycles [122ndash124]

Due to the increase in cost of raw materials growingresearch interest has been focused on producing AC fromagricultural wastes Some of the agricultural wastes includethe shells and stones of fruits wastes resulting from theproduction of cereals bagasse and coir pith [100] Rosas et al[125] prepared hemp-derived AC monolith by phosphoricacid activation The activated carbons from hemp stemare microporous materials and therefore suitable ones forhydrogen storage and CO

2capture [126]

Siriwardane et al [127] studied CO2adsorption on the

molecular sieve 13X 4A and activated carbonThemolecularsieve 13X showed better CO

2separation thanmolecular sieve

4A At lower pressures (lt50 psi) activated carbon had a lowerCO2separation than themolecular sieves but adsorptionwas

higher for activated carbon than molecular sieves at higherpressures [127 128]

Liu et al [129] indicated that zeolite 5A has highervolumetric capacities and less severe heat effect of the zeolite13X Chabazite zeolites were prepared and exchanged withalkali cations Li Na K and alkaline-earth cations Mg CaBa Zhang et al [130] studied the potential of these zeolites forCO2separation from flue gas by vacuum swing adsorption

It was found that NaCHA and CaCHA hold comparative

advantages for high temperature CO2separation whilst NaX

showed superior performance at relatively low temperatures[130] In physical adsorption the size and volume of the poresare important Micropores are defined as pores 2 nm in sizemesopores between 2 and 50 nm and macropores 50 nm insizeThemicropores make better selective adsorption of CO

2

over CH4[131 132]

Carbon nanotubes (CNTs) are the most famous amongnano-hollow structuredmaterials and their dimension rangesfrom 1 to 10 nm in diameter and from 200 to 500 nm in length[133] Cinke et al [134] indicated that purified single-walledcarbon nanotubes (SWNTs) adsorbed CO

2better than unpu-

rified SWNT In addition multiwalled carbon nanotubes(MWNTs) showed stability for 20 cycles of adsorption andregeneration [135]

More recently nanosystems researchers have synthesizedand screened a large number of zeolitic-typematerials knownas zeolitic imidazolate frameworks (ZIFs) CO

2capacities of

the ZIFs are high and selectivity against CO and N2is good

[136 137] The results of researchers (Burchell and Judkins[138] Dave et al [28] and Yong et al [139]) indicated thatthe CO

2adsorption efficiency of the honeycomb monolith is

twice than activated carbon and 15 times greater than ZIFmaterial [29] Results of Kimber et al [140] showed that CO

2

selectivity of honeycomb monolithic composite decreasedwith increasing in burn-off

Graphite nanoplatelets (GNP) were prepared by acidintercalation followed by thermal exfoliation of naturalgraphite Functionalized graphite nanoplatelets (f-GNP)wereprepared by further treatment of GNP in acidic mediumPalladium (Pd) nanoparticles were decorated over f-GNPsurface by chemical method [109 141 142] Adsorptioncapacity of this adsorbent is presented in Table 4

The presence of several impurity gases (SO119909NO119909H2O)

greatly complicates the CO2separation processes Therefore

conventional adsorption-based CO2separation processes

rely on using a pretreatment stage to remove water SO119909 and

NO119909 which adds considerably to the overall cost Also this

prelayer can be used before the amine absorption column


[143 144] Deng et al [145] showed that the adsorptioncapacities follows the order SO

2gt CO

2gt NO gt N

2on both

zeolites (5A and 13X) Comparing two different adsorbentsthe better separation efficiency can be achieved by 5A zeolite[145]

Zhang et al [130] focused on the effect of water vapour onthe pressurevacuum swing adsorption process The selectedadsorbents in this study were CDX (an aluminazeoliteblend) alumina and 13X zeolite as these adsorbents are eitherthe prelayer for water adsorption or themain CO

2adsorption

layer in the packed bed [130]Metal-organic framework (MOF) materials are crys-

talline with two- or three-dimensional porous structures thatcan be synthesised withmany of the functional capabilities ofzeolites Several MOFs have been proposed as adsorbents forCO2separation processes and among these Cu-BTC [poly-

meric copper (II) benzene-135-tricarboxylate] has provedto be dedicated with CO

2adsorption performances that are

higher than those of typical adsorbents such as 13X zeolite[105 107 146 147]

TheMCM-41 material is one of the mesoporous productswhich was prepared by the hydrothermalmethod frommobilcomposition of matter (MCM) powders Lu et al [148]showed that mesoporous silica spherical particles (MSPs)can be synthesized using low-cost Na

2SiO3thus they can be

cost-effective adsorbents for CO2separation from flue gas

[149 150]Layered double hydroxides (LDHs) have general formula[MII1minus119909

MIII119909(OH)2][X119892minus119909C sdot 119899H2O] with 119909 typically in the range

between 010 and 033 These materials can be readily andinexpensively synthesized with the desired characteristics fora particular application such as CO

2adsorption [108 151]

223 Adsorbent Modification The role of CO2as a weak

Lewis acid is well established Because of the nature ofCO2 the surface of the physical adsorbents can be modified

by adding basic groups such as amine groups and metaloxides to improve CO

2adsorption capacity or selectivity

[152ndash154] Three different methods for the production ofthese adsorbents were investigated activation with CO

2 heat

treatmentwith ammonia gas (amination and ammoxidation)and heat treatment with polyethylenimine (PEI) Howeverit has been suggested that amine modification can producebetter and cheaper CO

2adsorbents [24 104 155 156]

Xu et al [157 158] designed selective ldquomolecular basketrdquoby grafting polyethylenimine (PEI) uniformly on MCM-41CO2adsorption capacity of the adsorbentwas 24 times higher

thanMCM-41 and 2 times higher than PEI [93]The additionof ammoniumhydroxide resulted in the Zr-MOFwith a slightlower adsorption of CO

2and CH

4 however the selectivity

of CO2CH4is significantly enhanced [159 160] Results of

Abid et al [107] showed that the selectivity of CO2CH4

on Zr-MOF is between 22 and 38 while for Zr-MOF-NH4

selectivity is between 26 and 43A nitrogen-rich carbon with a hierarchical micro-mes-

opore structure exhibited a high CO2adsorption capacity

(141mgg at 298K 1 atm) excellent separation efficiency(CO2N2selectivity is ca 32) and excellent stability [161]

Plaza et al [162] results showed that CO2adsorption capacity

of the DETA-impregnated alumina (ge23mmoLg) exhibitedis the highest

Amine modified layered double hydroxides (LDHs) havebeen prepared by several different methods Park et al [163]used dodecyl sulfate (DS) intercalated LDH as precursor andadded (3-aminopropyl) triethoxysilane (APTS) together withN-cetyl-NNN-trimethylammoniumbromide (CTAB) [164]The highest adsorption capacity of amine modified LDHs forCO2was achieved at 175mmoLg by MgAl N3 at 353K and

1 bar According to data in Table 4 this adsorbent has highCO2capacity at high temperature therefore this adsorbent

is suitable for post-combustion CO2capture [108]

Wang et al [114] reported that porous carbons with well-developed pore structureswere directly prepared fromaweakacid cation exchange resin (CER) by the carbonization of amixture with Mg acetate in different ratios [108] The mainparameters of this adsorbent (such as CO

2capacity) are

indicated in Table 4Shafeeyan et al [165] prepared different adsorbents based

on the central composite design (CCD) with three indepen-dent variables (ie amination temperature amination timeand the use of preheat treated (HTA) or preoxidized (OXA)sorbent as the starting material) They demonstrated that theoptimum condition for obtaining an efficient CO

2adsorbent

is using a preoxidized sorbent and amination at 698K for 21 h[165]

Table 4 compares CO2adsorption capacities and stabil-

ity of different absorbents which were studied for post-combustion CO

2capture

224 Different Cycles for CO2Adsorption Five different

regeneration strategies were demonstrated in a single-bedCO2adsorption unit pressure swing adsorption (PSA) tem-

perature swing adsorption (TSA) vacuum swing adsorption(VSA) electric swing adsorption (ESA) and a combinationof vacuum and temperature swing adsorption (VTSA) Thedifference between these technologies is based on the strat-egy for regeneration of adsorbent after the adsorption step(Figure 7) In PSA applications the pressure of the bed isreduced VSA is preferred to the special PSA applicationwhere the desorption pressure is below atmospheric whereasinTSA the temperature is raisedwhile pressure ismaintainedapproximately constant and in ESA the solid is heated by theJoule effect [166ndash169]

For the single-bed cycle configurations the productivityand CO

2recovery followed the sequence

ESA lt TSA lt PSA lt VSA lt VTSA (1)

The performances of PSA TSA VSA VTSA and ESAprocesses for CO

2separation are reported in Table 5 Since

application of adsorption process for CO2capture in indus-

trial scale is very important in recent years some researcheshave been focused on this area for example Lucas et al [170]studied the scale-up CO

2adsorption with activated carbon

23 Cryogenic Distillation Cryogenic method utilized lowtemperatures for condensation separation and purification


Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)

Figure 7 Schematic diagrams of various adsorption cycles (a) TSA (b) PSA (c) VSA and (d) ESA thin lines indicated operation streamsin regenerated step

Table 5 Comparison between several adsorption cycles forCO2 separation process [166]

Process CO2 feed molar fraction() (other gases present)

CO2purity ()

CO2recovery ()

PSA 13 (O2) 995 69TSA 10 95 81TSA 17 na 40ESA 10 2333 9257VSA 15 90 90VSA 17 na 873-bed VSA 12 90ndash95 60ndash70PSAVSA 20 58ndash63 70ndash75PSAVSA 15 (H2O) 59 87VPSA 17 995ndash998 34ndash69VPSA 16 (O2) 99 53ndash70PTSA 10 99 902-bed-2-stepPSA na 18 90

VTSA 17 na 97

of CO2from flue gases (freezing point of pure CO

2is 1955 K

at atmospheric pressure) Therefore under the cryogenicseparation process the components can be separated by

a series of compression cooling and expansion steps Itenables direct production of liquid CO

2that can be stored

or sequestered at high pressure via liquid pumping [171ndash173]The advantages of this technology can be summarized as

follows [6 8 174]

(1) Liquid CO2is directly produced thus making it

relatively easy to store or send for enhanced oilrecovery

(2) This technology is relatively straightforward involv-ing no solvents or other components

(3) The cryogenic separation can be easy scaled-up toindustrial-scale utilization

The major disadvantages of this process are the largeamount of energy required to provide the refrigerationand the CO

2solidification under a low temperature which

causes several operational problems [176ndash178] Thereforemore studies are required for reducing the cost of cryogenicseparation

Clodic et al [179] indicated that the energy requirementfor cryogenic process was in the range of 541ndash1119 kJkg CO

2

Zanganeh et al [6] have constructed a pilot-scaleCO2capture

and compression unit (CO2CCU) that can separate CO

2as

liquid phase from the flue gas of oxy-fuel combustion Theirresults showed that cryogenic is the most cost effective when


S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5

S13 (purge gas) T S14 (purge gas)

C1 (intercooled

S2

P2

External cold energy


P1

Mixture

Step 1 Step 2

S6 (liquid CO2)

S5 (liquid CO2) S9 (liquid CO2)

S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)

Figure 8 Novel CO2cryogenic liquefaction and separation system [175]

the feed gas is available at high pressureTherefore cryogenicis not suitable for post-combustion and it is well effective forseparation stream with high CO

2concentration such as oxy-

fuel combustion Amann et al [180] reported that conversionof O2CO2cycle was more efficient than amine scrubbing

but more difficult to implement because of the specific gasturbine

Xu et al [175] studied a novel CO2cryogenic liquefaction

and separation system (Figure 8) In this system two-stagecompression two-stage refrigeration two-stage separationand sufficient recovery of cryogenic energywere adoptedTheenergy consumption for CO

2recovery is only 0395MJkg

CO2 Furthermore this CO

2cryogenic separation system is

more suitable for gas mixtures with high initial pressure andhigh CO

2concentration [175]

Song et al [181] developed a novel cryogenic CO2capture

system based on Stirling coolers (SC) The operation ofStirling cooler contains four processes isothermal expansionrefrigeration under a constant volume isothermal compres-sion and heating under a constant volume condition Thisnovel cryogenic system can condense and separate H

2O

and CO2from flue gas Their results showed that under

the optimal temperature and flow rate CO2recovery of the

cryogenic process can reach 96 with 15MJkg CO2energy

consumptionTuinier et al [182] exploited a novel cryogenic CO

2

capture process using dynamically operated packed beds(Figure 9) By the developed process above 99ofCO

2could

be recovered from a flue gas containing 10 vol CO2and

1 vol H2O with 18MJkg CO

2energy consumption [181]

Chiesa et al [183] proposed an advanced cycle that amolten carbonate fuel cell (MCFC) was used to separatethe CO

2from the gas turbine exhaust of a natural gas fired

combined cycle power plant In this cycle gas turbine fluegases actually are used as cathode feeding for MCFC WhileCO2is moved from the cathode to anode side concentrate

CO2in the anode exhaust Then the CO

2is concentrated

on the anode side of MCFC allowing to easily treat this

spent fuel stream in a cryogenic process to split combustiblespecies (routed back to gas turbine combustor) from the CO

2

addressed to storage (Figure 10) [183]

24 Membrane Separation Themembrane separation meth-od is a continuous steady-state clean and simple processand ideal as an energy-saving method for CO

2recovery Gas

separation using membranes is a pressure-driven processDue to the low pressure of flue gases driving force is too lowfor membrane processes in post-combustion (low pressureand low CO

2concentration) Membrane processes offer

increased separation performances when CO2concentration

in the feed mixture increases [184ndash186]Membrane separation processes have several advantages

over other CO2separation technologiesThe required process

equipment is very simple compact relatively easy to operateand control clear process and easy to scale up [187 188]

The energy required for the recovery of CO2by mem-

brane processes depends on the target purity flue gascomposition and membrane selectivity for CO

2 Howevre

membrane processes require too much energy for post-combustion CO

2capture therefore low partial pressure of

CO2in the flue gas is a possible disadvantage for the appli-

cation of membranes Another disadvantage of membraneprocess is that the membrane selectivity for the separation ofCO2from SO

119909andNO

119909is very lowMembrane process is not

useful for high flow rate applications [189ndash191]Therefore the useful membrane for post-combustion

CO2capture should have some specification such as [192 193]

(i) high CO2permeability

(ii) high selectivity for CO2separatation from flue gases

(iii) high thermal and chemical stability(iv) resistant to plasticisation(v) resistant to aging(vi) cost effective(vii) low production cost for differentmembranemodules


Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)

Figure 9 Schematic axial temperature and correspondingmass deposition profiles for the cryogenic (a) capture (b) recovery and (c) coolingcycles [182]

Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2

Figure 10 Plant layout showing the integration of the MCFC in a combined cycle with cryogenic CO2separation after oxygen combustion

of the cell an anode exhaust [183]

Many efforts have been made to find new material withsuitable properties (Table 6)

Various groups of materials have been already proposedand experimentally investigated for post-combustion CO

2

capture with membrane process By modifying membranetheir properties can be improved For example when aminefunctional groups are randomly dispersed in the silicamatrix

thismembrane can separate CO2with high selectivity On the

other hand membrane structure can be modified by addingarginine salts [194ndash196]

241 Inorganic Membranes Based on structure inorganicmembranes can be classified into two categories porous and


Table 6 Carbon dioxide and nitrogen gas permeability data for different membranes

Name Feed pressure(atm)

Temperature(K)

119875

lowast (CO2)(barrer)

119875

lowast (N2)(barrer)

120572

(CO2N2)Reference

Ion-exchanged zeolites membraneY (FAU) with 120572-A12O3 support na 308 na na 139 [197]ZSM-5 (MFI) with120572-A12O3 support

na na na na 3 [197]

ZSM-5polymeric silica na 373 1140 na [198]Stainless steel support infiltratedwith a eutectic molten carbonatemixture (LiNaK)

na 923 7780 na 16 [199]

Y-type na 303ndash403 35900ndash89800 na 5 [200]NaY na 313 359000 na 5 [200]Li(20)Y na 308 210000 na 3 [200]K(30)Y na 308 269000 na 9 [200]K(62)Y na 313 150000 na 6 [200]Rb(38)Y na 313 150000 na 3 [200]Cs(32)Y na 313 59900 na 2 [200]20 K2CO3 80 Li2CO3 na 798 2990 na 4 [199]MCM-48 na na 10200 na 08 [189]PEI-modified MCM-48 na 363 14100 na 80 [201]Chitosan 175 295 100 na 100 [192]Swollen chitosan 15 383 482 na 250 [192]Arginine salt-chitosan 15 383 1500 na 852 [194]

PolyacetylenePolytrimethyl-prop-1-ynyl-silane na 298 19000 1800 106 [193]Poly-33-dimethyl-but-1-yne na 298 560 43 130 [193]Poly-1-(dimethyl-trimethylsilanylmethyl-silanyl)-propyne

na 298 310 21 148 [193]

Poly-1-[dimethyl-(2-trimethylsilanyl-ethyl)-silanyl]-propyne

na 298 150 14 107 [193]

Polytrimethyl-(2-prop-1-ynyl-phenyl)-silane na 298 290 24 121 [193]

Poly-1-prop-1-ynyl-2-trifluoromethyl-benzene na 298 130 73 178 [193]

Poly-dec-2-yne na 298 130 14 93 [193]Poly-1-chloro-dec-1-yne na 298 170 16 106 [193]Poly-1-chloro-oct-1-yne na 298 130 11 118 [193]Poly-1-chloro-hex-1-yne na 298 180 10 18 [193]Polyhexyl-dimethyl-prop-1-ynyl-silane na 298 71 43 165 [193]

Polytrimethyl-(1-pentyl-prop-2-ynyl)-silane na 298 120 87 138 [193]

Polyhexyl-dimethyl-(1-propyl-prop-2-ynyl)-silane na 298 70 63 111 [193]

Polyprop-1-ynyl-benzene na 298 25 22 114 [193]Polybut-1-ynyl-benzene na 298 40 45 89 [193]Polyoct-1-ynyl-benzene na 298 48 55 87 [193]Polychloroethynyl-benzene na 298 23 10 230 [193]


Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference

Poly-1-ethynyl-2-methyl-benzene na 298 15 30 50 [193]Polydimethyl-phenyl-(1-propyl-prop-2-ynyl)-silane na 298 54 25 216 [193]

Polyarylene ether6FPT-6FBPA 10 308 2529 218 116 [193]6FPT-BPA 10 35 10 308 1853 137 135 [193]6FPPy-6FBPA 10 308 2946 239 1232 [193]6FPPy-BPA 10 308 2144 170 126 [193]

Fixed site carrier membrane (FSCM)Polarix 20 303 107 na 50 [202]PAAM-PVAPS 10 298 24 times 105 na 80 [203]PVAmPVA blend 145 298 212 times 106 na 145 [204]PEIPVA na 298 104 na 230 [184]PDMAPS 2 296 3 times 105 na 53 [143]

PolyaminePA12 10 308 120 na 51 [152]PA6 10 308 66 na 56 [152]Polyethyleneiminepolyvinylbutyral 0132 318 380 na 32 [193]

Poly[(2-NN-dimethyl)aminoethyl methacrylate] 0237 298 370 na 111 [193]

Poly(vinylbenzyltrimethylammonium fluoride) 0224 296 113 na 983 [193]

Polyethyleneiminepoly(vinylalcohol) 0355 298 650 na 235 [193]

PEIPDMSPEBA1657PDMS 5 298 157 times 106 na 64 [205]Polyarylate

BPAIA 10 308 54 024 225 [193]BPAtBIA 10 308 242 120 202 [193]HFBPAIA 10 308 191 111 172 [193]HFBPAtBIA 10 308 569 388 147 [193]PhThIA 10 308 674 028 241 [193]PhThtBIA 10 308 238 109 218 [193]FBPIA 10 308 124 057 124 [193]FBPtBIA 10 308 368 193 191 [193]TBBPAIA 10 308 493 018 274 [193]TBBPAtBIA 10 308 215 090 239 [193]TBHFBPAIA 10 308 256 107 239 [193]TBHFBPAtBIA 10 308 851 447 190 [193]TBPhThIA 10 308 834 029 288 [193]TBPhThtBIA 10 308 306 128 239 [193]TBFBPIA 10 308 204 070 291 [193]TBFBPtBIA 10 308 695 294 236 [193]DMBPAIA 10 308 124 0063 197 [193]DMBPATbia 10 308 80 039 205 [193]TMBPAIA 10 308 120 058 207 [193]TMBPAtBIA 10 308 446 252 177 [193]DiisoBPAIA 10 308 516 027 191 [193]


Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference

DiisoBPAtBIA 10 308 161 108 149 [193]DBDMBPAIA 10 308 545 022 248 [193]PhAnthIA 10 308 90 036 25 [193]PhAnthtBIA 10 308 259 135 192 [193]FBPIA 10 308 124 057 218 [193]FBPtBIA 10 308 368 193 191 [193]

PolycarbonatesPC 1ndash10 308 60ndash68 0289ndash032 21 [193]TMPC 1ndash10 308 1758ndash186 10 186 [193]TCPC 1 308 666 036 185 [193]TBPC 1 308 423 0182 232 [193]HFPC 10 308 24 16 150 [193]TMHFPC 10 308 111 74 150 [193]NBPC 10 308 91 047 194 [193]PCZ 10 308 22 0105 210 [193]PC-AP 2 308 948 0361 263 [193]FBPC 2 308 151 0592 255 [193]

Polyethylene oxidePEO 78 298 81 007 140 [193]PEO 44ndash146 308ndash318 13ndash52 024ndash1 55 [193]PEO-PBT na 308 120 2 60 [193]EOEMAGE (80202) na 308 773 168 46 [193]EOEMAGE (772323) na 308 680 155 44 [193]EOEMAGE (96425) na 308 580 121 48 [193]

PolyimidesAmine modified polyimide 0368 308 186 na 38 [193]PMDA-BAPHF 68 308 118 066 178 [193]PMDA-3BAPHF 68 308 612 029 211 [193]PMDA-441015840-ODA 68ndash10 308 114ndash27 0049ndash01 233 [193]

PMDA-331015840-ODA 68ndash10 308 050ndash355 0018ndash0145 245ndash278 [193]

PMDA-MDA 10 308 403 020 202 [193]PMDA-IPDA 10 308 297 150 198 [193]PMDA-BAPHF 10 308 176 0943 187 [193]PMDA-BATPHF 10 308 246 150 164 [193]BPDA-BAHF 1ndash10 298ndash308 23ndash277 06ndash139 199ndash377 [193]BPDA-mTrMPD 10 308 137 842 163 [193]BTDA-44-ODA 10 308 0625 00236 265 [193]BTDA-BAPHF 10 308 437 0195 224 [193]BTDA-BAHF 10 308 101 045 224 [193]BTDA-mTrMPD 10 308 309 155 199 [193]BTDA-BAFL 1 298 15 039 385 [193]PI 10 308 200 0063 317 [193]oMeCat-durene 1 303 27 083 33 [193]mMeCat-durene 1 303 20 059 34 [193]DMeCat-durene 1 303 63 205 31 [193]


Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference

mtBuCat-durene 1 303 71 255 28 [193]oMeptBuCat-durene 1 303 67 25 27 [193]TMeCat-durene 1 303 200 81 25 [193]mMetCat-MDA 1 303 22 065 34 [193]mtBuCat-MDA 1 303 63 22 29 [193]TMeCat-MDA 1 303 110 38 30 [193]TMeCat-TMB 1 303 39 12 33 [193]DBuCat-TMB 1 303 95 49 19 [193]mtBuCat-DMOB 1 303 67 021 32 [193]TMeCat-6FiPDA 1 303 54 19 28 [193]6F 3 na 114 58 196 [193]TMMPD 3 na 600 351 171 [193]IMDDM 3 na 196 108 181 [193]ODA 3 na 25 097 258 [193]Matrimid 5218 10 308 65 025 256 [193]

6FDA-based polyimides6FDA-pPDA 10 308 153 080 1912 [193]6FDA-pDiMPDA 10 303 427 267 160 [193]6FDA-durene 10 308 440 3560 124 [193]6FDA-durene 10 303 456 3550 1285 [193]6FDA-mPDA 68ndash10 308 823ndash920 036ndash0447 206ndash227 [193]6FDA-mMPDA 68ndash10 303 401ndash425 212ndash224 179ndash201 [193]6FDA-mTrMPDA 10 308 431 316 136 [193]6FDA-DATr 68 303 2863 131 219 [193]6FDA-DBTF 68 308 2164 117 185 [193]6FDA-PHDoeP 68 303 859 450 191 [193]6FDA-PEPE 68 308 688 0255 270 [193]6FDA-PBEPE 68 303 250 0099 253 [193]6FDA-PMeaP 68 308 241 0086 280 [193]6FDA-341015840ODA 10 303 611 0259 236 [193]6FDA-APAP 10 308 107 0473 226 [193]6FDA-pp1015840ODA 10 303 167 0733 228 [193]6FDA-BAPHF 10 308 191 0981 195 [193]6FDA-BATPHF 10 303 228 130 175 [193]6FDA-BAHF 10 308 512 311 165 [193]6FDA-15-NDA 10 308 23 11 21 [193]6FDA-durene 24 h amidation 10 na 116 133 875 [193]6FDA-durenemPDA (5050) 10 na 846 518 164 [193]6FDA-durenemPDA (5050) 4 hamidation 10 na 549 338 162 [193]

6FDA-durenemPDA (5050) 6 hamidation 10 na 491 327 150 [193]

6FDA-durenemPDA (5050)12 h amidation 10 na 460 294 156 [193]


Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



6FDA-FDAHFBAPP (11) 11 kgcm2 303 4650 199 234 [193]6FDA-ODA 10 308 23 083 277 [193]6FDA-44-ODA 68 303 220 094 234 [193]6FDA-MDA 10 308 19 081 235 [193]6FDA-4BDAF 68 303 19 098 194 [193]6FDA-331015840-ODA 68 308 21 010 21 [193]6FDA-3BDAF 68 303 63 024 263 [193]6FDA-IPDA 10 308ndash328 243ndash274 087ndash139 197ndash279 [193]6FDA-DAF 10 308ndash328 195ndash213 081ndash115 185ndash241 [193]PI-1 1 303 32 14 229 [193]PI-3 1 303 360 165 218 [193]PI-4 1 303 62 24 258 [193]PI-5 1 303 190 73 260 [193]6FDA-BAFL 1 298 98 33 297 [193]

Poly(phenylene oxide)PPO (hollow fiber) 4 308 106 21 [205]PPS 15 308 160 0046 348 [193]PDMPO 15 308 655 35 187 [193]PDPPO 15 308 399 15 266 [193]PDMPO 6891 295 900 37 243 [193]PDMPO (200 brominated) 6891 295 936 38 246 [193]PDMPO (374 brominated) 6891 295 971 37 262 [193]PDMPO (600 brominated) 6891 295 1599 80 200 [193]

Polypyrrole6FDA-TAB 10 308 540 26 208 [193]6FDA-TADPO 10 308 276 12 230 [193]BBL 10 308 012 0003 463 [193]

PolysulfonesPSF 10 308 56 025 224 [193]TMPSF 10 308 21 106 198 [193]HFPSF 10 308 12 067 179 [193]TMHFPSF 10 308 72 40 18 [193]PSF-F 10 308 45 020 225 [193]PSF-O 10 308 43 020 215 [193]PSF-P 10 308 68 032 213 [193]TMPSF-F 10 308 55 061 90 [193]TMPSF-P 10 308 132 057 232 [193]BIPSF 10 308 56 024 233 [193]TMBIPSF 10 308 318 121 263 [193]15-NPSF 10 308 16 0057 281 [193]26-NPSF 10 308 15 0051 294 [193]27-NPSF 10 308 18 0074 243 [193]


Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference

DMPSF 10 308 21 0091 231 [193]HMBIPSF 10 308 255 12 233 [193]DMPSF-Z 10 308 14 0057 246 [193]PSF-AP 2 308 812 0278 292 [193]FBPSF 2 308 138 0484 285 [193]PSF-M 1 308 28 011 255 [193]TMPSF-M 10 308 70 028 250 [193]PSF-BPFL 1 308 10 025 40 [193]341015840-PSF 1 308 15 0066 227 [193]13-ADM PSF 35 308 72 033 218 [193]22-ADM PSF 35 308 95 046 206 [193]PSF (6 Br 92 CequivCSiMe3) 1 308 365 21 174 [193]PSF (3 Br 47 CequivCSiMe3) 1 308 185 124 149 [193]PSF (21 Br 77 CequivCSiMe3) 1 308 282 17 166 [193]PSF (5 Br 45 CequivCSiMe3) 1 308 164 09 182 [193]PSF 1 308 56 025 224 [193]PSF-s-HBTMS 1 308 21 096 222 [193]PSF-o-HBTMS 1 308 70 329 213 [193]PSF-CH2-TMS 1 308 18 095 189 [193]EM3 1 308 29 13 22 [193]EM2 1 308 62 024 26 [193]EM1 1 308 48 016 30 [193]SM3 (degree of substitution =20) 1 308 18 077 23 [193]

SM3 (degree of substitution = 10) 1 308 10 038 26 [193]SM1 1 308 51 017 30 [193]PPSF 1 308 32 010 32 [193]RM3 1 308 27 19 14 [193]RM2 1 308 67 060 11 [193]RM1 1 308 69 061 11 [193]HFPSF 1 308 120 067 179 [193]HFPSF-o-HBTMS 1 308 105 563 186 [193]HFPSF-s-TMS 1 308 41 20 20 [193]HFPSF-o-TMS 1 308 84 47 18 [193]HFPSF-TMS 1 308 110 63 18 [193]TM6FPSF 1 308 72 40 18 [193]TM6FPSF-s-TMS 1 308 96 52 19 [193]TMPSF-TMS 1 308 32 151 213 [193]TMPSF-s-TMS 1 308 663 307 216 [193]TMPSF-HBTMS 1 308 72 336 214 [193]

Other membranesHQDPA-PDA 7 303 0598 0016 374 [193]HQDPA-PDA 7 373 170 0111 153 [193]HQDPA-DBA 7 303 0683 0015 455 [193]HQDPA-DBA 7 373 210 0125 168 [193]HQDPA-MDBA 7 303 118 0034 347 [193]


Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference

HQDPA-MDBA 7 373 237 0160 148 [193]HQDPA-EDBA 7 303 226 0077 294 [193]HQDPA-EDBA 7 373 418 0292 143 [193]12H 5 308 46 021 219 [193]6H6F 5 308 86 044 195 [193]6F6H 5 308 89 042 212 [193]12F 5 308 129 076 170 [193]PBK 10 308 33 013 254 [193]PBK-S 10 308 327 011 297 [193]PBSF 10 308 108 047 230 [193]PESPI 4 308 115 times 105 na 30 [193]PPES na 273 092 0027 34 [193]PPESK na 273 075 0042 18 [193]20 percent DEA immobilized in254 120583mmicroporouspolypropylene supports

016ndash167 298 974ndash4825 na 56ndash276 [200]

Copolymers and polymer blendPEBA 2533 (hollow fiber) 68 273 260 na 32 [206]PEBAPSF composite 34 273 61 times 105 na 30 [206]COPNA na 373 2990 na 14 [200]Pebax na 303 73 na 156 [207]PebaxPEG10 na 303 75 na 158 [207]PebaxPEG20 na 303 80 na 159 [207]PebaxPEG30 na 303 105 na 151 [207]PebaxPEG40 na 303 132 na 151 [207]PebaxPEG50 na 303 151 na 155 [207]PebaxPEG-DME10 na 303 123 na 44 [208]PebaxPEG-DME20 na 303 206 na 45 [208]PebaxPEG-DME30 na 303 300 na 46 [208]PebaxPEG-DME40 na 303 440 na 42 [208]PebaxPEG-DME50 na 303 606 na 43 [208]6FDA-TAB 10 308 540 28 193 [193]6FDAPMDA-TAB (50 50) 10 308 158 070 226 [193]6FDAPMDA-TAB (25 75) 10 308 313 0098 319 [193]6FDAPMDA-TAB (1090) 10 308 111 0036 308 [193]6FDA-TABDAM (7525) 3 308 737 31 238 [193]6FDA-TABDAM (5050) 3 308 155 66 235 [193]6FDA-DAM 3 308 370 295 125 [193]6FDATMPDA na 308 400 235 1702 [193]6FDAPMDA (1 6)-TMMDA(CH2Cl2 cast)

10 308 187 117 160 [193]

6FDAPMDA (1 6)-TMMDA(NMP cast) 10 308 144 876 164 [193]

6FDAPMDA (1 6)-TMMDA(DMF cast) 10 308 886 516 172 [193]

MDI-BPAPEG (75) 2 308 31 070 44 [193]MDI-BPAPEG (80) 2 308 48 10 47 [193]MDI-BPAPEG (85) 2 308 59 120 49 [193]LTDI (20)-BPAPEG (90) 2 308 47 092 51 [193]


Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference

LTDI (40)-BPAPEG (85) 2 308 35 072 48 [193]IPA-ODAPEO3 (80) 2 308 58 11 53 [193]BPDA-pp1015840ODA na 303 18000 na 31 [155]BPDA-ODADAT (oxidized) na 308 599 na 40 [155]BPDA-ODADABAPEO1 (75) 2 308 27 0048 56 [193]BPDA-mDDSPEO1 (80) 2 308 38 0066 58 [193]BPDA-ODADABAPEO2 (70) 2 308 14 025 57 [193]BPDA-ODADABAPEO2 (80) 2 308 36 064 56 [193]BPDA-ODAPEO3 (75) 2 308 75 14 52 [193]BPDA-mDDSPEO3 (75) 2 308 72 14 53 [193]BPDA-mPDPEO4 (80) 2 308 81 15 54 [193]BPDA-ODAPEO4 (80) 2 308 117 23 51 [193]PMDA-ODADABAPEO1 (80) 2 308 14 027 52 [193]PMDA-ODAPEO2 (75) 2 308 40 074 54 [193]PMDA-mPDPEO3 (80) 2 308 99 20 50 [193]PMDA-APPSPEO3 (80) 2 308 159 31 51 [193]PMDA-APPSPEO4 (70) 2 308 136 26 53 [193]PMDA-mPDPEO4 (80) 2 308 151 29 52 [193]PMDA-ODAPEO4 (80) 2 308 167 32 52 [152]PMDA-pDDSPEO4 (80) 2 308 238 49 49 [152]PMDABTDA-BAFL (50 50) 1 298 43 13 33 [193]PMDABTDAndashBAFL (90 10) 1 298 130 38 34 [193]BPDA-BAFLHMDA (50 50) 1 298 054 0014 39 [193]PPES na 298 092 0027 34 [193]PPESPPEK (3 1) na 298 294 0074 40 [193]PPESPPEK (1 1) na 298 412 0089 46 [193]PPESPPEK (1 3) na 298 206 0026 39 [193]PPESPPEK (1 4) na 298 177 0052 34 [193]PPEK 18 na 298 075 0042 18 [193]HQDPA-DPAMDPA 7 303 0957 0023 412 [193]HQDPA-DPAMDPA 7 373 234 0147 159 [193]HQDPA-DPAEDPA 7 303 1334 0036 376 [193]HQDPA-DPAEDPA 7 373 325 0207 157 [193]PI 10 308 200 0063 317 [193]PI10PS 10 308 233 0085 274 [193]PI15PS 10 308 232 009 258 [193]PI20PS 10 308 290 091 319 [193]PI25PS 10 308 429 091 471 [193]PI10PSVP 10 308 358 013 284 [193]PI15PSVP 10 308 371 014 265 [193]PI20PSVP 10 308 565 015 384 [193]PI25PSVP 10 308 655 155 431 [193]NTDA-BDSA(30)CARDOODA 3 303 70 17 41 [193]


Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference

NTDA-BDSA (30)CARDO] 3 303 164 45 36 [193]NTDA-BDSA (30)BAPHF 3 303 23 064 36 [193]NTDA-BDSA (30)ODA 3 303 52 01 52 [193]6FDA-FDAHFBAPP (11) 11 kgcm2 303 465 199 234 [193]6FDA-durenepPDA (8020) 10 308 230 1688 1362 [193]6FDA-durenepPDA (5050) 10 308 126 774 1628 [193]6FDA-durenepPDA (2080) 10 308 5926 281 2109 [193]6FDA-durene331015840-DDS (7525) 10 308 847 591 143 [193]6FDA-durene331015840-DDS (5050) 10 308 198 109 182 [193]6FDA-durene331015840-DDS (2575) 10 308 512 026 197 [193]6FDA-331015840-DDS 10 308 184 008 227 [193]6FDA-6FpDA-DABA-125 4 308 340 201 169 [193]6FDA-6FpDAndashDABA-125annealed 4 308 708 450 157 [193]

6FDA-6FpDA-DABA-125(225 TMOS) 4 308 309 170 182 [193]

6FDA-6FpDA-DABA-125(225 TMOS) annealed 4 308 476 316 151 [193]

6FDA-6FpDA-DABA-125 (150MTMOS) 4 308 440 253 174 [193]

6FDA-6FpDA-DABA-125 (150MTMOS) annealed 4 308 110 707 156 [193]

6FDA-6FpDA-DABA-125 (150PTMOS) 4 35 4 308 323 180 179 [193]

6FDA-6FpDA-DABA-125 (150PTMOS) annealed 4 308 918 559 164 [193]

6FDA-6FpDA-DABA-125(225 PTMOS) 4 308 307 188 163 [193]

6FDA-6FpDA-DABA-125(225 PTMOS) annealed 4 308 909 587 155 [193]

6FDA-6FpDA-DABA-25 4 308 203 120 169 [193]6FDA-6FpDA-DABA-25annealed 4 308 773 485 159 [193]

6FDA-6FpDA-DABA-25 (225TMOS) 4 308 157 106 148 [193]

6FDA-6FpDA-DABA-25 (225TMOS) annealed 4 308 798 487 164 [193]



6FDAndash6FpDA-DABA-25 (225MTMOS) 4 308 166 107 155 [193]


6FDA-6FpDA-DABA-25 (150PTMOS) 4 308 184 094 196 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Poly(5 5 BPABN) 5 308 571 019 301 [193]Poly(7 3 BPABN) 5 308 462 016 289 [193]

Cross-linking polymersPoly(ethyleneoxide-co-epichlorohydrin) (1 1)11

300 298 150 23 652 [193]

Poly(ethyleneoxide-co-epichlorohydrin) (1 1)2

300 298 149 10 149 [193]


300 298 161 05 322 [193]

DM14MM9 (1000) 0967 298 45 066 68 [193]DM14MM9 (1000) 0967 323 107 28 38 [193]DM14MM9 (9010) 0967 298 62 090 69 [193]DM14MM9 (9010) 0967 323 133 34 39 [193]DM14MM9 (7030) 0967 298 96 15 66 [193]DM14MM9 (7030) 0967 323 195 54 36 [193]DM14MM9 (5050) 0967 298 144 225 64 [193]DM14MM9 (5050) 0967 323 260 72 36 [193]DM14MM9 (3070) 0967 298 210 33 63 [193]DM14MM9 (3070) 0967 323 350 106 33 [193]DB30MM9 (1000) 0967 298 93 15 63 [193]DB30MM9 (1000) 0967 323 200 57 35 [193]DB30MM9 (9010) 0967 298 105 16 64 [193]DB30MM9 (9010) 0967 323 210 58 36 [193]DB30MM9 (7030) 0967 298 141 21 67 [193]DB30MM9 (7030) 0967 323 270 77 35 [193]DB30MM9 (5050) 0967 298 179 29 62 [193]DB30MM9 (5050) 0967 323 330 97 34 [193]DB30MM9 (3070) 0967 298 250 42 60 [193]DB30MM9 (3070) 0967 323 410 124 33 [193]DM9MM9 (9010) 0967 298 183 03 68 [193]DM9MM9 (9010) 0967 323 51 13 38 [193]DM23MM9 (9010) 0967 298 145 22 66 [193]DM23MM9 (9010) 0967 323 290 76 38 [193]DB10MM9 (9010) 0967 298 67 011 61 [193]DB10MM9 (9010) 0967 323 27 079 34 [193]DB69MM9 (9010) (cooling) 0967 298 240 43 56 [193]DB69MM9 (9010) (cooling) 0967 323 510 142 36 [193]DB69MM9 (9010) (heating) 0967 298 98 16 62 [193]DB69MM9 (9010) (heating) 0967 323 400 114 35 [193]DM14MM23 (3070) (cooling) 0967 298 240 39 62 [193]DM14MM23 (3070) (cooling) 0967 323 420 12 35 [193]


Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference

DM14MM23 (3070) (heating) 0967 298 250 40 62 [193]Matrimid 5218 10 308 65 025 256 [193]Matrimid 5218 1-daycross-linking 10 308 74 029 256 [193]

Matrimid 5218 3-daycross-linking 10 308 60 024 252 [193]





6FDA-durene 5min cross-linked 10 308 136 111 123 [193]6FDA-durene 10mincross-linked 10 308 918 653 141 [193]

6FDA-durene 15mincross-linked 10 308 700 605 116 [193]


6FDA-durene 60mincross-linked 10 308 214 040 535 [193]lowastPermeability

dense In porous inorganic membranes a porous thin toplayer is supported on a porous metal or ceramic supportZeolite silicon carbide carbon glass zirconia titania andalumina membranes are mainly used as porous inorganicmembranes supported on different substrates such as 120572-alumina 120574-alumina zirconia zeolite or porous stainless steel[17 199 209 210]

Zeolite membrane is the most important group of inor-ganic membranes Zeolite membranes are considered moreexpensive than polymeric membranes and therefore theirunique properties of size selectivity and thermal and chemicalstability should be exploited for successful application [211ndash213]

The dense inorganic membranes (nonporous material)consist of a thin layer of metal such as palladium and itsalloys (metallic membrane) or solid electrolytes such aszirconia Another form of inorganic membrane is the liquid-immobilized membrane where the pores of a membraneare completely filled with a liquid which is permselectivefor certain compounds Recently attempts have been madeto develop dense molten carbonate selective membranes forCO2separation at high temperatures (gt723K)The inorganic

membranes have high thermal stability for CO2separation

but their selectivity and permeability are very low [200 214215]

242 Polymeric Membranes In polymeric membranes theselective layer is generally a nonporous film that trans-ports gases across by the solution-diffusion mechanism

Polyacetylenes polyaniline polyarylene ethers polyarylatespolycarbonates polyetherimides polyethylene oxide poly-imides polyphenylene oxides polypyrroles polysulfonesand amino groups such as polyethyleneimine blends poly-methacrylates are examples of polymericmembranes used forCO2separation [17 216ndash218]

Selective polymeric membranes can be divided into twobasic categories glassy and rubbery Almost glassy poly-meric membranes are more suitable than rubbery polymericmembranes for CO

2separation because of their high gas

selectivity and good mechanical properties On the otherhand rubbery membranes are flexible and soft and theyhave a high permeability but a low selectivity whereas glassypolymers exhibit a low permeability but a high selectivity[206 219ndash221]

Several advantages of polymeric membranes are (i) lowcost of production (ii) high performance separation (iii)ease of synthesis and (iv) mechanical stability Although thepolymeric membranes have high selectivity and permeabilityfor CO

2separation but their thermal stability is very low and

these membrane may be plasticized with influence of CO2

in membrane Therefore application of these membranes forpost-combustion capture is limited and flue gas must first becooled down to 313ndash333K for membrane process [184 222223]

Ren et al [205] prepared polymeric membranes withblock copolymers the balance of the hard and soft blocks canprovide a good CO

2separation performance without loss of

its permeability


Table 7 Comparison between various technologies used for CO2 capture

Technology Advantages Disadvantages Scale

Absorption(i) React rapidly(ii) High absorption capacities(iii) Very flexible

(i) Equipment corrosion(ii) High energy required for regeneratingsolvent

Industrial

Adsorption(i) Low energy consumption and cost ofCO2 capture(ii) Suitable for separating CO2 from dilutestream

Low adsorption capacities (in flue gasesconditions) Pilot

Cryogenic distillation

(i) Liquid CO2 production(ii) Not requiring solvents or othercomponents(iii) Easy scaled-up to industrial-scaleapplication

Require large amount of energy Pilot

Membrane separation (i) Clean and simple process(ii) Continuous steady-state technology

Require high energy for post-combustionCO2 capture

Experimental

Improved polymeric membrane materials with superiorseparation performance can be obtained by synthesizing newpolymers or modification or blending existing commercialpolymers with organic or inorganic compounds [208 224]

Due to high operating cost of membrane processes itis necessary to perform more researches and studies aboutpreparation of suitable membranes

243 Mixed Matrix Membranes Zeolites carbon molecularsieves (CMS) and many polymeric materials offer attractivetransport properties for CO

2separation By mixing mem-

brane material excellent membrane with high performancefor CO

2separation (selectivities of CO

2N2= 178ndash396) can

be prepared [200] A group of scientists proposed the useof membrane based on polymerimmobilized liquid systemespecially polymerized ionic liquid membrane (PILM) orgelled ionic liquid membrane ILMs consisting of aqueoussolutions of 20 DEA immobilized in 254120583m microporouspolypropylene supports have low permeability and suitableselectivity (974 barrer 276 resp) in 2 atm at 298K [225ndash228]

244 Hollow Fiber Membrane Most industrially importantmembranes for gas separations are hollow fiber ones Asym-metric hollowfibermembranes (such as polyvinylidene diflu-oride (PVDF)) with inner skinless structures are favourablefor CO

2separation and absorption in gas-liquid membrane

by low mass-transfer resistance and high permeability Inaddition this process can achieve significantly high adsorp-tion efficiencies due to the much larger surface area for gas-liquid interface than conventional gas absorption processes[206 229ndash232]

According to data in Table 6 inorganic membranes havehigh permeability (about 150000 barrer) and low selectivity(about 15) Of course some of inorganic membranes suchas Y (FAU) with 120572-A1

2O3support and chitosan group are

highly selective for CO2N2separation (selectivity (120572) asymp 100ndash

800) Among polymeric membranes polyamines have highpermeability and selectivity (106 (barrer) and 980 resp) andthe second FSCM membranes have high permeability andfine selectivity (105 (barrer) 230 resp) Other polymeric

membrane groups are not selective for CO2N2separation

and maximum selectivity of these membranes is about 30

25 Novel CO2Capture Technologies These methods include

electrochemical pumps and chemical looping approachesto CO

2separation The molten carbonate and aqueous

alkaline fuel cells have been studied for use in separatingCO2from both air and flue gases Electrochemical pumps

discussed include carbonate and proton conductors Moltencarbonate is nearly 100 selective for CO

2separation but

major disadvantage in the application of molten carbonateelectrochemical cells for CO

2separation is that this process

is not repeatedly Other disadvantages of these technologiesare corrosion difficult operating condition (119879 = 873K) andsensitivity to the presence of SO

119909[45 233]

In chemical looping combustion the oxygen for com-bustion of the fuel is provided by a regenerable metal oxidecatalystThe chemical looping scheme can be presented in thegeneral form [45]

HC +metal oxide

997888rarr CO2+H2O + lower oxide (andor metal)

(2)

lower oxide (andor metal) +O2997888rarr metal oxide (3)

Nickel oxide is one main candidate for the chemicallooping combustion of methane as low as 673K because it isextensive and effective for the chemical looping combustion[45]

26 Discussion Various technologies such as absorptionadsorption cryogenic distillation and membrane have beensuggested for CO

2separation from flue gases (Table 7) In

this paper various technologies for different feed conditionswere investigated Absorption is an important technologyfor CO

2separation Although physical solvents required low

energy for regeneration they have low absorption capacityand selectivity for CO

2separation Selexol is the best physical

solvent and suitable for sweetening natural gas Howeverphysical absorption is not economical for flue gas streams


with CO2concentration lower than 15 vol (95US$ton CO

2

[234])Chemical solvents are classified in main groups such

as alkanolamines ammonia aqueous piperazine (PZ) andamino acids Chemical absorbents such as monoethanol-amine (MEA) have high absorption capacities and are veryflexible for CO

2separation therefore these solvents are

usually preferred to physical solvents Chemical absorptionwith alkanolamines is the only technology that is used in anindustrial scale for post-combustion capture Amines reactrapidly selectively and reversibly with CO

2and are relatively

nonvolatile and inexpensive solvents In this process thecorrosion is the main problem therefore in recent studiesnew amines and various mixtures of them were proposedand compared with previous ones to find suitable solventsSuitable solvents for CO

2separation must have high CO

2

absorption capacity less corrosion less viscosity and lessregeneration energy These studies showed that CASTOR 1and 2 which are blended amine solvents (MEAMDEA)are the best chemical adsorbents so far proposed for post-combustion CO

2capture Experimental results indicated that

amine amino acid salts (AAAS) have better performancethan MEA of the same concentration for CO

2absorption

but do not deteriorate in the presence of oxygen Howeverabsorption has several disadvantages such as it requires highenergy to regenerate solvents (30GJton CO

2for absorption

with 40wt MEA in 210 kPa [235]) therefore need moreefforts in the future to reduce energy consumption in post-combustion CO

2capture with chemical absorption

Adsorption is the one effective technology that canreduce energy and cost of the capture or separation ofCO2in post-combustion capture Adsorption is suitable for

separating CO2from dilute and low flow rate stream but

flue gases conditions are the main problem against industri-alization adsorption process The CaO-MgAl

2O4and nano

CaOAl2O3are the best chemical adsorbents Although the

chemical adsorbents have high capacity and selectivity buttheir regeneration is difficult Physical adsorption is themost suitable for CO

2capture at high pressures and low

temperatures At higher pressure (above 4 bar) activatedcarbons are more efficient than zeolites The energy and costof adsorption for activated carbons are nearly half of that ofzeolites On the other hand zeolites (particularly 13X and 5A)have high selectivity for CO

2separation Generally zeolite

5A may have better adsorption efficiency at co-adsorption ofSO2 NO and CO

2than zeolite 13X

In order to achieve more selective CO2separation from

flue gases the modified adsorbent surface was consideredNew adsorbents such as honeyncomb monolith MOFsCHAs (NaCHA and CaCHA) PMO (MCM and SBA) andMSPs (Na

2SiO4) are suitable adsorbents for selective CO

2

separation but they require more researches and studiesHowever the development of suitable adsorbents with highCO2adsorption capacity which can be replaced absorption

with chemical adsorbent is still demandedCryogenic distillation separation can be used for CO

2

separation but its major disadvantage is the large amountof energy required to provide the refrigeration Many newprocesses have been proposed for using cryogenic but

generally this technology is not suitable for post-combustioncapture and is appropriate for oxy-fuel combustion methodand CO

2separation from exhaust of cement industry (stream

with high CO2concentration)

The membrane separation method is a continuoussteady-state clean and simple process for CO

2recovery Since

the pressure drop is driving force for membrane processthe flue gas stream must compress Since compressing fluegas is very difficult and expensive membrane separation issuitable for high pressure stream with high concentration(gt10 vol) Inorganic membrane have high thermal andchemical stability but their selectivity is lower than polymericmembranes Although Y (FAU) with 120572-Al

2O3support and

arginine salt chitosan are the best inorganic membranezeolite mambranes are suitable ones for CO

2separation

Polymeric membranes are very selective for CO2separation

but they have low thermal stability Therefore polymericmembranes are suitable for application in pre-combustionprocesses Glassy polymeric membranes have higher selec-tivity while the rubbery polymeric membranes have higherthermal stability Perfect membrane with high performancefor CO



be prepared by mixing various membranesBecause of operating problems andhigh cost of compress-

ingmembrane separation is not suitable for post-combustioncapture but membrane technology is suitable for producingoxygen-enriched streams from air in oxy-fuel combustionsystems

Electrochemical pumps and chemical looping are twonew technologies suggested for CO

2capture Now these

technologies are not effective in comparison with other tech-nologies Therefore application of electrochemical pumpsand chemical looping in CCS needs more research

3 Conclusion

Because of economical and environmental incentivesresearchers have mainly focused on CO

2separation from

different process streams especially from the flue gases Inrecent years post-combustion capture has been the topic ofmany researches because it is more flexible and can be easilyadded to the fossil fuel power plants

Based on above findings it can be concluded that fluegases properties (mainly concentration of CO

2 temperature

and pressure) are the most effective factors for selection ofsuitable process for CO

2separation

Since flue gases have high temperature (about 373K)low pressure and low CO

2concentration (1 atm and 10ndash15

moL) bulk absorption and adsorption processes may be thebest suitable process for CO

2separation from these streams

Due to simplicity of absorption process this process has beenapplied in industrial plants although many researches havebeen focused on preparation of adsorbents with high selec-tivity and capacity in recent years For industrial applicationmore studies about adsorbents are necessary Cryogenic dis-tillation andmembrane processes are efficient for gas streamswith high CO

2concentration Therefore these process are

economically efficient for pre-combustion capture In recent


years different studies have been performed to optimizecryogenic cycles and preparation of suitable membrane forCO2separation from post-combustion flue gases

By the result of this study future research direction on thescale-up and industrialization of adsorption (with modifiedadsorbent) andmembrane process forCO

2separation is sug-

gested Therefore more studies must be focused on modelingand simulation of these processes (membrane and adsorp-tion) although research for finding new adsorbent suitablemambrane (with mixed or modified present membrane) andblending amine solvents can reduce CCS cost

Conflict of Interests

The authors declare that there is no conflict of interests re-garding the publication of this paper

References

[1] S Q Solomon S Q DMManning et al ldquoBook reviewsrdquo SouthAfrican Geographical Journal vol 91 pp 103ndash104 2009

[2] C A McMillan G A Keoleian and D V Spitzley GreenhouseGases University of Michigan Ann Arbor Mich USA 2005

[3] T J BlasingRecent Greenhouse Gas Concentrations USDepart-ment of Energy 32 edition 2012

[4] C H Chiao J L Chen C R Lan S Chen and H WHsu ldquoDevelopment of carbon dioxide capture and storagetechnology taiwan power company perspectiverdquo SustainableEnvironment Research vol 21 pp 1ndash8 2011

[5] T L P Dantas F M T Luna I J Silva et al ldquoCarbon dioxide-nitrogen separation through pressure swing adsorptionrdquoChem-ical Engineering Journal vol 172 no 2-3 pp 698ndash704 2011

[6] K E Zanganeh A Shafeen and C Salvador ldquoCO2capture and

development of an advanced pilot-scale cryogenic separationand compression unitrdquo Energy Procedia vol 1 pp 247ndash2522009

[7] A T A oCaNACo ldquoCanadian aviation industry reporton greenhouse gas emissions reductionsrdquo Tech Rep OttawaCanda 2012

[8] D Berstad R Anantharaman and P Neksa ldquoLow-temperatureCO2capture technologies-applications and potentialrdquo Interna-

tional Journal of Refrigeration vol 36 pp 1403ndash1416 2013[9] IEAIGGRD Programme ldquoCO

2abatement in oil refineries

fired heatersrdquo I E A IGGRD PH331 edition 2000[10] L Zhao E Riensche R Menzer L Blum and D Stolten

ldquoA parametric study of CO2N2gas separation membrane

processes for post-combustion capturerdquo Journal of MembraneScience vol 325 no 1 pp 284ndash294 2008

[11] A Hussain and M-B Hagg ldquoA feasibility study of CO2capture

from flue gas by a facilitated transport membranerdquo Journal ofMembrane Science vol 359 no 1-2 pp 140ndash148 2010

[12] I T Forum ldquoReducing transport greenhouse gas emissionstrends amp datardquo 2010

[13] N Mahasenan S Smith K Humphreys and Y Kaya ldquoThecement industry and global climate change current and poten-tial future cement industry CO

2emissionsrdquo in Proceedings

of the Greenhouse Gas Control Technologies-6th InternationalConference p 995 Pergamon Turkey 2003

[14] K S Lackner A H A Park and B G Miller ldquoEliminating CO2

emissions from coal-fired power plantsrdquo in Generating Electric-ity in aCarbon-ConstrainedWorld pp 127ndash173 Academic PressBoston 2010

[15] A Mohammadi M Soltanieh M Abbaspour and F AtabildquoWhat is energy efficiency and emission reduction potential inthe Iranian petrochemical industryrdquo International Journal ofGreenhouse Gas Control vol 12 pp 460ndash471 2013

[16] E Worrell L Price N Martin C Hendriks and L O MeidaldquoCarbon dioxide emissions from the global cement industryrdquoAnnual Review of Energy and the Environment vol 26 pp 303ndash329 2001

[17] H Yang Z Xu M Fan et al ldquoProgress in carbon dioxideseparation and capture a reviewrdquo Journal of EnvironmentalSciences vol 20 no 1 pp 14ndash27 2008

[18] J Barnett S Dessai and M Webber ldquoWill OPEC lose from theKyoto Protocolrdquo Energy Policy vol 32 no 18 pp 2077ndash20882004

[19] H Li R P Berrens A K Bohara H C Jenkins-Smith CL Silva and D L Weimer ldquoWould developing country com-mitments affect US householdsrsquo support for a modified KyotoProtocolrdquo Ecological Economics vol 48 no 3 pp 329ndash3432004

[20] M Crombie S Imbus and I Miracca ldquoCO2capture project

phase 3-demonstration phaserdquo Energy Procedia vol 4 pp6104ndash6108 2011

[21] U Springer ldquoThe market for tradable GHG permits under theKyoto Protocol a survey of model studiesrdquo Energy Economicsvol 25 no 5 pp 527ndash551 2003

[22] A Pridmore A Bristow TMay andM Tight ldquoClimate changeimpacts future scenarios and the role of transportrdquo Report ofUniversity of Leeds Institute for Transport Studies 2003

[23] J G J Olivier G Janssens-Maenhout and J A H W PetersldquoTrends in global CO

2emissionsrdquo Tech Rep PBL Netherlands

Environmental Assessment Agency Ispra Italy 2012[24] H Herzog J Meldon and A Hatton ldquoAdvanced post-com-

bustion CO2capturerdquo Tech Rep Clean Air Task Force Doris

Duke Foundation 2009[25] J C M Pires F G Martins M C M Alvim-Ferraz and M

Simoes ldquoRecent developments on carbon capture and storagean overviewrdquoChemical Engineering Research andDesign vol 89no 9 pp 1446ndash1460 2011

[26] D G Chapel C L Mariz and J Ernest ldquoRecovery of CO2from

flue gases commercial trendsrdquo in Proceedings of the CanadianSociety of Chemical Engineers Annual Meeting pp 1ndash16 1999

[27] F T Zangeneh S Sahebdelfar andM T Ravanchi ldquoConversionof carbon dioxide to valuable petrochemicals an approachto clean development mechanismrdquo Journal of Natural GasChemistry vol 20 no 3 pp 219ndash231 2011

[28] N Dave T Do G Puxty R Rowland P H M Feron andM I Attalla ldquoCO

2capture by aqueous amines and aqueous

ammonia-A Comparisonrdquo Energy Procedia vol 1 pp 949ndash9542009

[29] R Thiruvenkatachari S Su H An and X X Yu ldquoPost com-bustion CO

2capture by carbon fibre monolithic adsorbentsrdquo

Progress in Energy and Combustion Science vol 35 no 5 pp438ndash455 2009

[30] J Gibbins and H Chalmers ldquoCarbon capture and storagerdquoEnergy Policy vol 36 no 12 pp 4317ndash4322 2008

[31] BMetz ldquoCarbonDioxide Capture and Storagerdquo Special Reportof the Intergovernmental Panel on Climate Change 2005


[32] T F Wall ldquoCombustion processes for carbon capturerdquo Proceed-ings of the Combustion Institute vol 31 pp 31ndash47 2007

[33] E Rubin and H de Coninck ldquoIPCC special report on carbondioxide capture and storagerdquo Tech Rep Cambridge UniversityPress UK 2005 TNO Cost Curves for CO

2Storage part 2

2004[34] V R Choudhary S Mayadevi and A P Singh ldquoSorption

isotherms of methane ethane ethene and carbon dioxide onNaX NaY and Na-mordenite zeolitesrdquo Journal of the ChemicalSociety Faraday Transactions vol 91 no 17 pp 2935ndash29441995

[35] P Dechamps ldquoEuropean CO2capture and storage projectsrdquo

Tech Rep European Commission Brussels Belgium 2007[36] B J P Buhre L K Elliott C D Sheng R P Gupta and T

F Wall ldquoOxy-fuel combustion technology for coal-fired powergenerationrdquo Progress in Energy and Combustion Science vol 31no 4 pp 283ndash307 2005

[37] M Glazer C Bertrand L Fryda and W de Jong ldquoEOSLTconsortiumbiomass co-firingWP4mdashbiomass co-firing in oxy-fuel combustion Part II ash deposition modelling of coal andbiomass blends under air and oxygen combustion conditionsrdquoTech Rep Energy research Center of the Neterland 2010

[38] SAGE Publications I Green Issues and Debates an A-to-ZGuide Green Issues and Debates an A-to-Z Guide SAGEPublications Oaks Calif USA

[39] AAOlajire ldquoCO2capture and separation technologies for end-

of-pipe applicationsmdasha reviewrdquo Energy vol 35 no 6 pp 2610ndash2628 2010

[40] A Samanta A Zhao G K H Shimizu P Sarkar and R GuptaldquoPost-combustion CO

2capture using solid sorbents a reviewrdquo

Industrial and Engineering Chemistry Research vol 51 no 4 pp1438ndash1463 2012

[41] J S Rhodes andDW Keith ldquoEngineering economic analysis ofbiomass IGCC with carbon capture and storagerdquo Biomass andBioenergy vol 29 no 6 pp 440ndash450 2005

[42] T L Dantas A E Rodrigues and R F Moreira ldquoSeparationof carbon dioxide from flue gas using adsorption on poroussolidsrdquo Tech Greenhouse GasesmdashCapturing Utilization andReduction 2012

[43] G S Esber III ldquoCarbon dioxide capture technology for thecoal-powered electricity industry a systematic prioritization ofresearch needsrdquo Tech Rep Massachusetts Institute of Technol-ogy 2006

[44] Y Lv X Yu J Jia S-T Tu J Yan and E Dahlquist ldquoFabricationand characterization of superhydrophobic polypropylene hol-low fiber membranes for carbon dioxide absorptionrdquo AppliedEnergy vol 90 no 1 pp 167ndash174 2012

[45] E J Granite and T OrsquoBrien ldquoReview of novel methods forcarbon dioxide separation from flue and fuel gasesrdquo FuelProcessing Technology vol 86 no 14-15 pp 1423ndash1434 2005

[46] T Nguyen M Hilliard and G T Rochelle ldquoAmine volatility inCO2capturerdquo International Journal of Greenhouse Gas Control

vol 4 no 5 pp 707ndash715 2010[47] M Gupta I Coyle and K Thambimuthu ldquoCO2capture tech-

nologies and opportunities in Canadardquo in Proceedings of the 1stCanadian CCampS Technology Roadmap Workshop CO2 capturetechnologies and opportunities in Canada CANMET EnergyTechnology Centre Natural Resources Canada 2003

[48] H J Herzog ldquoThe economics of CO2separation and capturerdquo

Journal of the Franklin Institute vol 7 pp 13ndash24 2000

[49] G Pellegrini R Strube andGManfrida ldquoComparative study ofchemical absorbents in postcombustion CO

2capturerdquo Energy

vol 35 no 2 pp 851ndash857 2010[50] NMacDowell N Florin A Buchard et al ldquoAnoverviewofCO

2

capture technologiesrdquo Energy and Environmental Science vol 3no 11 pp 1645ndash1669 2010

[51] X P Li Gang A Webley Paul Zhang Jun and R SinghldquoCompetition of CO

2H2O in adsorption based CO

2capturerdquo

Energy Procedia vol 1 pp 1123ndash1130[52] P Singh J P M Niederer and G F Versteeg ldquoStructure

and activity relationships for amine based CO2absorbents-Irdquo

International Journal of Greenhouse Gas Control vol 1 no 1 pp5ndash10 2007

[53] S Marsquomun ldquoSelection and characterization of new absorbentsfor carbon dioxide capturerdquo inChemical Engineering Faculty ofNatural Science and Technology 2005

[54] S Cavenati C A Grande and A E Rodrigues ldquoRemoval ofcarbon dioxide from natural gas by vacuum pressure swingadsorptionrdquo Energy and Fuels vol 20 no 6 pp 2648ndash26592006

[55] J David Economic evaluation of leading technology options23 for sequestration of carbon dioxide [MS thesis] ChemicalEngineering Practice Massachusetts Institute of Technology2000

[56] D L Albritton T Barker I A Bashmakov et alClimate Change2001 Synthesis Report edited by D J Dokken M Noguer P Vd LindenC Johnson J Pan Cambridge University Press 2001

[57] M Wang A Lawal P Stephenson J Sidders and C RamshawldquoPost-combustion CO

2capture with chemical absorption a

state-of-the-art reviewrdquo Chemical Engineering Research andDesign vol 89 no 9 pp 1609ndash1624 2011

[58] J Gabrielsen H F Svendsen M L Michelsen E H Stenbyand G M Kontogeorgis ldquoExperimental validation of a rate-basedmodel for CO

2capture using anAMP solutionrdquoChemical

Engineering Science vol 62 no 9 pp 2397ndash2413 2007[59] R Idem M Wilson P Tontiwachwuthikul et al ldquoPilot plant

studies of the CO2capture performance of aqueous MEA and

mixed MEAMDEA solvents at the University of Regina CO2

capture technology development plant and the boundary damCO2capture demonstration plantrdquo Industrial and Engineering

Chemistry Research vol 45 no 8 pp 2414ndash2420 2006[60] M Lucquiaud and J Gibbins ldquoOn the integration of CO

2

capture with coal-fired power plants a methodology to assessand optimise solvent-based post-combustion capture systemsrdquoChemical Engineering Research and Design vol 89 no 9 pp1553ndash1571 2011

[61] J N Knudsen J N Jensen P J Vilhelmsen and O BiedeldquoExperience with CO

2capture from coal flue gas in pilot-scale

testing of different amine solventsrdquo Energy Procedia vol 1 no1 pp 783ndash790 2009

[62] P H M Feron ldquoExploring the potential for improvement ofthe energy performance of coal fired power plants with post-combustion capture of carbon dioxiderdquo International Journal ofGreenhouse Gas Control vol 4 no 2 pp 152ndash160 2010

[63] F Qin S Wang A Hartono H F Svendsen and C ChenldquoKinetics of CO

2absorption in aqueous ammonia solutionrdquo

International Journal of Greenhouse Gas Control vol 4 no 5pp 729ndash738 2010

[64] H P Mangalapally R Notz S Hoch et al ldquoPilot plant exper-imental studies of post combustion CO

2capture by reactive

absorption with MEA and new solventsrdquo Energy Procedia vol1 pp 963ndash970 2009


[65] P S Kumar J A Hogendoorn G F Versteeg and P H MFeron ldquoKinetics of the reaction of CO

2with aqueous potassium

salt of taurine and glycinerdquo AIChE Journal vol 49 no 1 pp203ndash213 2003

[66] S A Freeman R Dugas D van Wagener T Nguyen and G TRochelle ldquoCarbon dioxide capture with concentrated aqueouspiperazinerdquo Energy Procedia vol 1 pp 1489ndash1496 2009

[67] J V Holst G F Versteeg D W F Brilman and J A Hogen-doorn ldquoKinetic study of CO

2with various amino acid salts in

aqueous solutionrdquo Chemical Engineering Science vol 64 no 1pp 59ndash68 2009

[68] E S Hamborg J P M Niederer and G F Versteeg ldquoDis-sociation constants and thermodynamic properties of aminoacids used in CO

2absorption from (293 to 353) Krdquo Journal of

Chemical and Engineering Data vol 52 no 6 pp 2491ndash25022007

[69] U E Aronu H F Svendsen and K A Hoff ldquoInvestigationof amine amino acid salts for carbon dioxide absorptionrdquoInternational Journal of Greenhouse Gas Control vol 4 no 5pp 771ndash775 2010

[70] J T Yeh K P Resnik K Rygle and H W Pennline ldquoSemi-batch absorption and regeneration studies for CO

2capture by

aqueous ammoniardquo Fuel Processing Technology vol 86 no 14-15 pp 1533ndash1546 2005

[71] C H Yu C H Huang and C S Tan ldquoA Review of CO2

Capture by Absorption and Adsorptionrdquo Aerosol and AirQuality Research vol 12 pp 745ndash769 2012

[72] B E Gurkan C Juan E M Mindrup et al ldquoChemicallycomplexing ionic liquids for post-combustion CO

2capturerdquo in

Clearwater Clean Coal Conference pp 6ndash10 Clearwater FlaUSA 2010

[73] E D Bates R D Mayton I Ntai and J H Davis Jr ldquoCO2

capture by a task-specific ionic liquidrdquo Journal of the AmericanChemical Society vol 124 no 6 pp 926ndash927 2002

[74] S Baj A Siewniak A Chrobok T Krawczyk and A Sob-olewski ldquoMonoethanolamine and ionic liquid aqueous solu-tions as effective systems for CO

2capturerdquo Journal of Chemical

Technology and Biotechnology vol 88 pp 1220ndash1227 2012[75] J P Ciferno D Lang and G T Rochelle Carbon Dioxide

Capture by Absorption with Potassium Carbonate University ofTexas 2010

[76] J T Cullinane andG T Rochelle ldquoThermodynamics of aqueouspotassium carbonate piperazine and carbon dioxiderdquo FluidPhase Equilibria vol 227 no 2 pp 197ndash213 2005

[77] H P Mangalapally and H Hasse ldquoPilot plant experiments withmea and new solvents for post combustion CO

2capture by

reactive absorptionrdquo Energy Procedia vol 4 pp 1ndash8 2011[78] J Brouwer P Feron and N Ten Asbroek ldquoAmino-acid salts for

CO2capture from flue gasesrdquo in Proceedings of the 4th Annual

Conference on Carbon Capture amp Sequestration 2009[79] D Kang S Park H Jo J Min and J Park ldquoSolubility of

CO2in amino-acid-based solutions of (potassium sarcosinate)

(potassium alaninate + piperazine) and (potassium serinate +piperazine)rdquo Journal of Chemical amp Engineering Data vol 58pp 1787ndash1791 2013

[80] B Farid and E Fadwa ldquoFront matterrdquo in Proceedings of the 2ndAnnualGas Processing Symposium p 488 ElsevierDohaQatar2010

[81] R M Davidson Post-Combustion Carbon Capture from CoalFired Plants Solvent Scrubbing IEA Clean Coal Centre 2007

[82] V Darde KThomsenW J vanWell and E H Stenby ldquoChilledammonia process for CO

2capturerdquo Energy Procedia vol 1 pp

1035ndash1042 2009[83] S Bishnoi and G T Rochelle ldquoThermodynamics of piper-

azinemethyldiethanolaminewatercarbon dioxiderdquo Industrialand Engineering Chemistry Research vol 41 no 3 pp 604ndash6122002

[84] A Bajpai and M K Mondal ldquoEquilibrium solubility of CO2in

aqueous mixtures of DEA and AEEArdquo Journal of Chemical ampEngineering Data vol 58 pp 1490ndash1495 2013

[85] A L Chaffee G P Knowles Z Liang J Zhang P Xiao and PA Webley ldquoCO

2capture by adsorption materials and process

developmentrdquo International Journal of Greenhouse Gas Controlvol 1 no 1 pp 11ndash18 2007

[86] J-R Li Y Ma M C McCarthy et al ldquoCarbon dioxidecapture-related gas adsorption and separation in metal-organicframeworksrdquo Coordination Chemistry Reviews vol 255 no 15-16 pp 1791ndash1823 2011

[87] L-Y Meng and S-J Park ldquoInfluence of MgO template oncarbon dioxide adsorption of cation exchange resin-basednanoporous carbonrdquo Journal of Colloid and Interface Sciencevol 366 no 1 pp 135ndash140 2012

[88] M Sevilla and A B Fuertes ldquoCO2adsorption by activated

templated carbonsrdquo Journal of Colloid and Interface Science vol366 no 1 pp 147ndash154 2012

[89] M Martunus Z Helwani A D Wiheeb J Kim and MR Othman ldquoImproved carbon dioxide capture using metalreinforced hydrotalcite under wet conditionsrdquo InternationalJournal of Greenhouse Gas Control vol 7 pp 127ndash136 2012

[90] B Dou Y Song Y Liu and C Feng ldquoHigh temperature CO2

capture using calcium oxide sorbent in a fixed-bed reactorrdquoJournal of Hazardous Materials vol 183 no 1ndash3 pp 759ndash7652010

[91] M Kotyczka-moranska G Tomaszewicz and G LabojkoldquoComparison of different methods for enhancing CO

2capture

by CaO-based sorbents Reviewrdquo Physicochemical Problems ofMineral Processing vol 48 pp 77ndash90 2012

[92] G Valenti D Bonalumi and E Macchi ldquoA parametric inves-tigation of the chilled ammonia process from energy andeconomic perspectivesrdquo Fuel vol 101 pp 74ndash83 2011

[93] Z H Lee K T Lee S Bhatia and A R Mohamed ldquoPost-combustion carbon dioxide capture evolution towards uti-lization of nanomaterialsrdquo Renewable and Sustainable EnergyReviews vol 16 no 5 pp 2599ndash2609 2012

[94] Z Xiang Z Hu D Cao et al ldquoMetal-organic frameworkswith incorporated carbonnanotubes improving carbondioxideandmethane storage capacities by lithium dopingrdquoAngewandteChemie vol 50 no 2 pp 491ndash494 2011

[95] K Essaki M Kato and K Nakagawa ldquoCO2removal at high

temperature using packed bed of lithium silicate pelletsrdquo Jour-nal of the Ceramic Society of Japan vol 114 no 1333 pp 739ndash7422006

[96] C S Martavaltzi and A A Lemonidou ldquoDevelopment ofnew CaO based sorbent materials for CO

2removal at high

temperaturerdquo Microporous and Mesoporous Materials vol 110no 1 pp 119ndash127 2008

[97] R BessonM RochaVargas and L Favergeon ldquoCO2adsorption

on calcium oxide an atomic-scale simulation studyrdquo SurfaceScience vol 606 no 3-4 pp 490ndash495 2012

[98] SMiyata ldquoAnion-exchange properties of hydrotalcite-like com-poundsrdquo Clays amp Clay Minerals vol 31 no 4 pp 305ndash311 1983


[99] A RMohamed S Bhatia K T Lee C Y H Foo Z H Lee andN A Razali ldquoNanomaterials as environmentally compatiblenext generation green carbon capture and utilizationmaterialsrdquoTransactions on GIGAKU vol 1 Article ID 01006 pp 1ndash7 2012

[100] M Songolzadeh M Takht Ravanchi and M Soleimani ldquoCar-bon dioxide capture and storage a general review on adsor-bentsrdquo World Academy of Science Engineering and Technologyvol 70 pp 225ndash232 2012

[101] M Anbia and V Hoseini ldquoDevelopment of MWCNTMIL-101 hybrid composite with enhanced adsorption capacity forcarbon dioxiderdquoChemical Engineering Journal vol 191 pp 326ndash330 2012

[102] L-Y Lin and H Bai ldquoContinuous generation of mesoporoussilica particles via the use of sodiummetasilicate precursor andtheir potential for CO

2capturerdquo Microporous and Mesoporous

Materials vol 136 no 1ndash3 pp 25ndash32 2010[103] D M DrsquoAlessandro B Smit and J R Long ldquoCarbon dioxide

capture prospects for new materialsrdquo Angewandte Chemie vol49 no 35 pp 6058ndash6082 2010

[104] D I Jang and S J Park ldquoInfluence of nickel oxide on carbondioxide adsorption behaviors of activated carbonsrdquo Fuel vol102 pp 439ndash444 2012

[105] S Choi J H Drese and C W Jones ldquoAdsorbent materialsfor carbon dioxide capture from large anthropogenic pointsourcesrdquo ChemSusChem vol 2 no 9 pp 796ndash854 2009

[106] J A Delgado M A Uguina J L Sotelo and B Ruız ldquoFixed-bed adsorption of carbon dioxide-helium nitrogen-heliumand carbon dioxide-nitrogen mixtures onto silicalite pelletsrdquoSeparation and Purification Technology vol 49 no 1 pp 91ndash1002006

[107] H R Abid G H Pham H-M Ang M O Tade and S WangldquoAdsorption of CH

4andCO

2on Zr-metal organic frameworksrdquo

Journal of Colloid and Interface Science vol 366 no 1 pp 120ndash124 2012

[108] J Wang L A Stevens T C Drage and J Wood ldquoPreparationand CO

2adsorption of amine modified Mg-Al LDH via

exfoliation routerdquo Chemical Engineering Science vol 68 no 1pp 424ndash431 2012

[109] A K Mishra and S Ramaprabhu ldquoPalladium nanoparticlesdecorated graphite nanoplatelets for room temperature carbondioxide adsorptionrdquo Chemical Engineering Journal vol 187 pp10ndash15 2012

[110] G Finos S Collins G Blanco et al ldquoInfrared spectroscopicstudy of carbon dioxide adsorption on the surface of cerium-gallium mixed oxidesrdquo Catalysis Today vol 180 no 1 pp 9ndash182012

[111] R P Grimm K A Eriksson N Ripepi C Eble and SF Greb ldquoSeal evaluation and confinement screening criteriafor beneficial carbon dioxide storage with enhanced coal bedmethane recovery in the Pocahontas Basin Virginiardquo Interna-tional Journal of Coal Geology vol 90-91 pp 110ndash125 2012

[112] B Guo L Chang and K Xie ldquoAdsorption of carbon dioxide onactivated carbonrdquo Journal of Natural Gas Chemistry vol 15 no3 pp 223ndash229 2006

[113] R Sakurovs S Day and S Weir ldquoRelationships between thesorption behaviour of methane carbon dioxide nitrogen andethane on coalsrdquo Fuel vol 97 pp 725ndash729 2012

[114] P Weniger J Francu P Hemza and B M Krooss ldquoInvestiga-tions on the methane and carbon dioxide sorption capacity ofcoals from the SWUpper Silesian Coal Basin Czech RepublicrdquoInternational Journal of Coal Geology vol 93 pp 23ndash39 2012

[115] C Garnier G Finqueneisel T Zimny et al ldquoSelection of coalsof different maturities for CO

2Storage by modelling of CH

4

and CO2adsorption isothermsrdquo International Journal of Coal

Geology vol 87 no 2 pp 80ndash86 2011[116] J C Abanades E S Rubin and E J Anthony ldquoSorbent

cost and performance in CO2capture systemsrdquo Industrial and

Engineering Chemistry Research vol 43 no 13 pp 3462ndash34662004

[117] T C Drage J M Blackman C Pevida and C E SnapeldquoEvaluation of activated carbon adsorbents for CO

2capture in

gasificationrdquo Energy and Fuels vol 23 no 5 pp 2790ndash27962009

[118] W Shen S Zhang Y He J Li and W Fan ldquoHierarchicalporous polyacrylonitrile-based activated carbon fibers for CO

2

capturerdquo Journal of Materials Chemistry vol 21 no 36 pp14036ndash14040 2011

[119] M Gray Y Soong K Champagne R Stevens Jr P Toochindaand S Chuang ldquoSolid amine CO2capture sorbentsrdquo Fuel vol80 pp 867ndash871 2001

[120] C Pevida M G Plaza B Arias J Fermoso F Rubiera andJ J Pis ldquoSurface modification of activated carbons for CO

2

capturerdquoApplied Surface Science vol 254 no 22 pp 7165ndash71722008

[121] M G Plaza C Pevida B Arias J Fermoso F Rubiera and J JPis ldquoA comparison of two methods for producing CO

2capture

adsorbentsrdquo Energy Procedia vol 1 pp 1107ndash1113 2009[122] M G Plaza S Garcıa F Rubiera J J Pis and C Pevida ldquoPost-

combustion CO2capture with a commercial activated carbon

comparison of different regeneration strategiesrdquoChemical Engi-neering Journal vol 163 no 1-2 pp 41ndash47 2010

[123] K S Nor Kamarudin and H Mat ldquoSynthesis and modificationof micro and mesoporous materials as CO

2adsorbentrdquo Tech

Rep Faculty of Chemical and Natural Resources EngineeringUniversity of Technology Johor Malaysia 2009

[124] M Radosz X Hu K Krutkramelis and Y Shen ldquoFlue-gascarbon capture on carbonaceous sorbents toward a low-costmultifunctional carbon filter for ldquogreenrdquo energy producersrdquoIndustrial and Engineering Chemistry Research vol 47 no 10pp 3783ndash3794 2008

[125] J M Rosas J Bedia J Rodrıguez-Mirasol and T CorderoldquoPreparation of hemp-derived activated carbon monolithsAdsorption of water vaporrdquo Industrial and Engineering Chem-istry Research vol 47 no 4 pp 1288ndash1296 2008

[126] R Yang G Liu M Li J Zhang and X Hao ldquoPreparationand N2 CO

2and H

2adsorption of super activated carbon

derived from biomass source hemp (Cannabis sativa L) stemrdquoMicroporous and Mesoporous Materials vol 158 pp 108ndash1162012

[127] R V Siriwardane M-S Shen E P Fisher and J A PostonldquoAdsorption of CO

2on molecular sieves and activated carbonrdquo

Energy and Fuels vol 15 no 2 pp 279ndash284 2001[128] K I Vatalis A Laaksonen G Charalampides andN P Benetis

ldquoIntermediate technologies towards low-carbon economy theGreek zeolite CCS outlook into the EU commitmentsrdquo Renew-able and Sustainable Energy Reviews vol 16 no 5 pp 3391ndash3400 2012

[129] Z Liu C AGrande P Li J Yu andA E Rodrigues ldquoMulti-bedvacuum pressure swing adsorption for carbon dioxide capturefrom flue gasrdquo Separation and Purification Technology vol 81pp 307ndash317 2011

[130] J Zhang P Xiao G Li and P A Webley ldquoEffect of fluegas impurities on CO

2capture performance from flue gas at


coal-fired power stations by vacuum swing adsorptionrdquo EnergyProcedia vol 1 pp 1115ndash1122 2009

[131] X Cui RM Bustin andGDipple ldquoSelective transport of CO2

CH4 and N

2in coals insights from modeling of experimental

gas adsorption datardquo Fuel vol 83 no 3 pp 293ndash303 2004[132] C J Anderson W Tao J Jiang S I Sandler G W Stevens

and S E Kentish ldquoAn experimental evaluation and molecularsimulation of high temperature gas adsorption on nanoporouscarbonrdquo Carbon vol 49 no 1 pp 117ndash125 2011

[133] M Kumar and Y Ando ldquoChemical vapor deposition of carbonnanotubes a review on growth mechanism and mass produc-tionrdquo Journal of Nanoscience and Nanotechnology vol 10 no 6pp 3739ndash3758 2010

[134] M Cinke J Li C W Bauschlicher Jr A Ricca and MMeyyappan ldquoCO

2adsorption in single-walled carbon nan-

otubesrdquo Chemical Physics Letters vol 376 no 5-6 pp 761ndash7662003

[135] A F Portugal PW J Derks G F Versteeg F DMagalhaes andAMendes ldquoCharacterization of potassium glycinate for carbondioxide absorption purposesrdquo Chemical Engineering Sciencevol 62 no 23 pp 6534ndash6547 2007

[136] R Banerjee A Phan B Wang et al ldquoHigh-throughput synthe-sis of zeolitic imidazolate frameworks and application to CO

2

capturerdquo Science vol 319 no 5865 pp 939ndash943 2008[137] K S Park Z Ni A P Cote et al ldquoExceptional chemical and

thermal stability of zeolitic imidazolate frameworksrdquo Proceed-ings of the National Academy of Sciences of the United States ofAmerica vol 103 no 27 pp 10186ndash10191 2006

[138] T D Burchell and R R Judkins ldquoPassive CO2removal using a

carbon fiber compositemolecular sieverdquo Energy Conversion andManagement vol 37 no 6ndash8 pp 947ndash954 1996

[139] Z Yong V Mata and A E Rodrigues ldquoAdsorption of carbondioxide at high temperaturemdasha reviewrdquo Separation and Purifi-cation Technology vol 26 no 2-3 pp 195ndash205 2002

[140] G M Kimber M Jagtoyen Y Q Fei and F J DerbyshireldquoFabrication of carbon fibre composites for gas separationrdquoGasSeparation and Purification vol 10 no 2 pp 131ndash136 1996

[141] L M Viculis J J Mack O M Mayer H T Hahn andR B Kaner ldquoIntercalation and exfoliation routes to graphitenanoplateletsrdquo Journal of Materials Chemistry vol 15 no 9 pp974ndash978 2005

[142] A K Mishra and S Ramaprabhu ldquoStudy of CO2adsorption

in low cost graphite nanoplateletsrdquo International Journal ofChemical Engineering andApplications vol 1 pp 266ndash269 2010

[143] R Du X Feng and A Chakma ldquoPoly(NN-dimethylaminoethyl methacrylate)polysulfone compositemembranes for gas separationsrdquo Journal of Membrane Sciencevol 279 no 1-2 pp 76ndash85 2006

[144] K Kumar C N Dasgupta B Nayak P Lindblad and D DasldquoDevelopment of suitable photobioreactors for CO

2seques-

tration addressing global warming using green algae andcyanobacteriardquoBioresource Technology vol 102 no 8 pp 4945ndash4953 2011

[145] H Deng H Yi X Tang Q Yu P Ning and L YangldquoAdsorption equilibrium for sulfur dioxide nitric oxide carbondioxide nitrogen on 13X and 5A zeolitesrdquoChemical EngineeringJournal vol 188 pp 77ndash85 2012

[146] N Gargiulo F Pepe and D Caputo ldquoModeling carbon dioxideadsorption on polyethylenimine-functionalized TUD-1 meso-porous silicardquo Journal of Colloid and Interface Science vol 367no 1 pp 348ndash354 2012

[147] A R Millward and O M Yaghi ldquoMetal-organic frameworkswith exceptionally high capacity for storage of carbon dioxideat room temperaturerdquo Journal of the American Chemical Societyvol 127 no 51 pp 17998ndash17999 2005

[148] C Lu H Bai F Su W Chen J F Hwang and H-H LeeldquoAdsorption of carbondioxide fromgas streams viamesoporousspherical-silica particlesrdquo Journal of the Air andWaste Manage-ment Association vol 60 no 4 pp 489ndash496 2010

[149] A Boonpoke S Chiarakorn N Laosiripojana S Towprayoonand A Chidthaisong ldquosynthesis of activated carbon andMCM-41 from bagasse and rice husk and their carbon dioxide adsorp-tion capacityrdquo Journal of Sustainable Energy amp Environmentnvol 2 pp 77ndash81 2011

[150] J Wei L Liao Y Xiao P Zhang and Y Shi ldquoCapture ofcarbon dioxide by amine-impregnated as-synthesized MCM-41rdquo Journal of Environmental Sciences vol 22 no 10 pp 1558ndash1563 2010

[151] QWang H H Tay Z Zhong J Luo and A Borgna ldquoSynthesisof high-temperature CO

2adsorbents from organo-layered dou-

ble hydroxides with markedly improved CO2capture capacityrdquo

Energy amp Environmental Science vol 5 pp 7526ndash7530 2012[152] H Lin and B D Freeman ldquoGas solubility diffusivity and

permeability in poly(ethylene oxide)rdquo Journal of MembraneScience vol 239 no 1 pp 105ndash117 2004

[153] P Chowdhury C Bikkina and S Gumma ldquoGas adsorptionproperties of the chromium-based metal organic frameworkMIL-101rdquo The Journal of Physical Chemistry C vol 113 no 16pp 6616ndash6621 2009

[154] P Li B Ge S Zhang S Chen Q Zhang and Y ZhaoldquoCO2capture by polyethylenimine-modified fibrous adsor-

bentrdquo Langmuir vol 24 no 13 pp 6567ndash6574 2008[155] B Aziz N Hedin and Z Bacsik ldquoQuantification of chemisorp-

tion and physisorption of carbon dioxide on porous silicamodified by propylamines effect of amine densityrdquoMicroporousand Mesoporous Materials vol 159 pp 42ndash49 2012

[156] M M Maroto-Valer Z Tang and Y Zhang ldquoCO2capture

by activated and impregnated anthracitesrdquo Fuel ProcessingTechnology vol 86 no 14-15 pp 1487ndash1502 2005

[157] X Xu C Song B G Miller and A W Scaroni ldquoAdsorptionseparation of carbon dioxide from flue gas of natural gas-firedboiler by a novel nanoporous ldquomolecular basketrdquo adsorbentrdquoFuel Processing Technology vol 86 no 14-15 pp 1457ndash14722005

[158] X Xu C Song J M Andresen B G Miller and A W Sca-roni ldquoNovel polyethylenimine-modified mesoporous molecu-lar sieve of MCM-41 type as high-capacity adsorbent for CO

2

capturerdquo Energy and Fuels vol 16 no 6 pp 1463ndash1469 2002[159] J Zhang R Singh and P A Webley ldquoAlkali and alkaline-earth

cation exchanged chabazite zeolites for adsorption based CO2

capturerdquoMicroporous and Mesoporous Materials vol 111 no 1ndash3 pp 478ndash487 2008

[160] H R Abid H Tian H-M Ang M O Tade C E Buckleyand S Wang ldquoNanosize Zr-metal organic framework (UiO-66)for hydrogen and carbon dioxide storagerdquoChemical EngineeringJournal vol 187 pp 415ndash420 2012

[161] C Chen J Kim and W-S Ahn ldquoEfficient carbon dioxidecapture over a nitrogen-rich carbon having a hierarchicalmicro-mesopore structurerdquo Fuel vol 95 pp 360ndash364 2012

[162] M G Plaza C Pevida B Arias et al ldquoApplication of ther-mogravimetric analysis to the evaluation of aminated solidsorbents for CO

2capturerdquo Journal of Thermal Analysis and

Calorimetry vol 92 no 2 pp 601ndash606 2008


[163] A-Y Park H Kwon A J Woo and S-J Kim ldquoLayered doublehydroxide surface modified with (3-aminopropyl) triethoxysi-lane by covalent bondingrdquoAdvancedMaterials vol 17 no 1 pp106ndash109 2005

[164] N S Nhlapo ldquoIntercalation of fatty acids into layered doublehydroxidesrdquo Tech Rep Department of Chemistery Faculty ofNatural and Agricultural sciences South Africa University ofPretoria 2008

[165] M S Shafeeyan W M A Wan Daud A Houshmand and AArami-Niya ldquoThe application of response surfacemethodologyto optimize the amination of activated carbon for the prepara-tion of carbon dioxide adsorbentsrdquo Fuel vol 94 pp 465ndash4722012

[166] M Clausse J Merel and F Meunier ldquoNumerical parametricstudy on CO

2capture by indirect thermal swing adsorptionrdquo


[167] L Wang Z Liu P Li J Yu and A E Rodrigues ldquoExperimentalandmodeling investigation onpost-combustion carbon dioxidecapture using zeolite 13X-APG by hybrid VTSA processrdquoChemical Engineering Journal vol 197 pp 151ndash161 2012

[168] A R Kulkarni and D S Sholl ldquoAnalysis of Equilibrium-BasedTSA Processes for Direct Capture of CO

2from Airrdquo Industrial

amp Engineering Chemistry Research vol 51 pp 8631ndash8645 2012[169] J Merel M Clausse and F Meunier ldquoExperimental investi-

gation on CO2post-combustion capture by indirect thermal

swing adsorption using 13X and 5A zeolitesrdquo Industrial andEngineering Chemistry Research vol 47 no 1 pp 209ndash215 2008

[170] S LucasM P Calvo C Palencia andM J Cocero ldquoMathemat-ical model of supercritical CO

2adsorption on activated carbon

effect of operating conditions and adsorption scale-uprdquo Journalof Supercritical Fluids vol 32 no 1ndash3 pp 193ndash201 2004

[171] C Hoeger C Bence S S Burt A Baxter and L BaxterldquoCryogenic CO

2capture for improved efficiency at reduced

costrdquo in Proceedings of the AIChE Annual Meeting November2010

[172] S Burt A Baxter and L Baxter ldquoCryogenic CO2capture

to control climate change emissionsrdquo in Proceedings of the34th International Technical Conference on Clean Coal amp FuelSystems May 2009

[173] M J TuinierH PHamers andM van SintAnnaland ldquoTechno-economic evaluation of cryogenic CO

2capture-A comparison

with absorption andmembrane technologyrdquo International Jour-nal of Greenhouse Gas Control vol 5 no 6 pp 1559ndash1565 2011

[174] AHart andNGnanendran ldquoCryogenic CO2capture in natural

gasrdquo Energy Procedia vol 1 pp 697ndash706 2009[175] G Xu L Li Y Yang L Tian T Liu and K Zhang ldquoA novel CO

2

cryogenic liquefaction and separation systemrdquo Energy vol 42pp 522ndash529 2012

[176] B Shimekit and H Mukhtar ldquoNatural gas purification tech-nologies-major advances for CO

2separation and future direc-

tionsrdquo inAdvances inNaturalGas Technology AMHamid Edpp 235ndash270 InTech China 2012

[177] M T Ravanchi S Sahebdelfar and F T Zangeneh ldquoCarbondioxide sequestration in petrochemical industries with the aimof reduction in greenhouse gas emissionsrdquo Frontiers of ChemicalEngineering in China vol 5 no 2 pp 173ndash178 2011

[178] R P LivelyW J Koros and J R Johnson ldquoEnhanced cryogenicCO2capture using dynamically operated low-cost fiber bedsrdquo

Chemical Engineering Science vol 71 pp 97ndash103 2012

[179] D Clodic R El Hitti M Younes A Bill and F CasierldquoCO2capture by anti-sublimation thermo-economic process

evaluationrdquo in Proceedings of the 4th Annual Conference onCarbon Capture amp Sequestration pp 2ndash5 Alexandria Va USA2005

[180] J-M Amann M Kanniche and C Bouallou ldquoNatural gascombined cycle power plant modified into an O

2CO2cycle for

CO2capturerdquo Energy Conversion and Management vol 50 no

3 pp 510ndash521 2009[181] C-F Song Y Kitamura S-H Li and K Ogasawara ldquoDesign

of a cryogenic CO2capture system based on Stirling coolersrdquo

International Journal of Greenhouse Gas Control vol 7 pp 107ndash114 2012

[182] M J Tuinier M van Sint Annaland and J A M KuipersldquoA novel process for cryogenic CO

2capture using dynamically

operated packed beds-An experimental and numerical studyrdquoInternational Journal of Greenhouse Gas Control vol 5 no 4pp 694ndash701 2011

[183] P Chiesa S Campanari andGManzolini ldquoCO2cryogenic sep-

aration from combined cycles integrated withmolten carbonatefuel cellsrdquo International Journal of Hydrogen Energy vol 36 no16 pp 10355ndash10365 2011

[184] E Favre ldquoMembrane processes and postcombustion carbondioxide capture challenges and prospectsrdquo Chemical Engineer-ing Journal vol 171 no 3 pp 782ndash793 2011

[185] B Freeman and Y YampolskiiMembrane Gas Separation JohnWiley amp Sons 2010

[186] R Bounaceur N Lape D Roizard C Vallieres and E FavreldquoMembrane processes for post-combustion carbon dioxidecapture a parametric studyrdquo Energy vol 31 no 14 pp 2220ndash2234 2006

[187] D Aaron and C Tsouris ldquoSeparation of CO2from flue gas a

reviewrdquo Separation Science and Technology vol 40 no 1ndash3 pp321ndash348 2005

[188] A Xu A Yang S Young D deMontigny and P Tonti-wachwuthikul ldquoEffect of internal coagulant on effectiveness ofpolyvinylidene fluoride membrane for carbon dioxide separa-tion and absorptionrdquo Journal of Membrane Science vol 311 no1-2 pp 153ndash158 2008

[189] T-L Chew A L Ahmad and S Bhatia ldquoOrdered mesoporoussilica (OMS) as an adsorbent and membrane for separationof carbon dioxide (CO

2)rdquo Advances in Colloid and Interface

Science vol 153 no 1-2 pp 43ndash57 2010[190] C A Scholes G Q Chen G W Stevens and S E Kentish

ldquoNitric oxide and carbon monoxide permeation through glassypolymericmembranes for carbon dioxide separationrdquoChemicalEngineering Research and Design vol 89 no 9 pp 1730ndash17362011

[191] C A Scholes S E Kentish and GW Stevens ldquoCarbon dioxideseparation through polymeric membrane systems for flue gasapplicationsrdquo Recent Patents on Chemical Engineering vol 1 pp52ndash66 2008

[192] L A El-Azzami and E A Grulke ldquoCarbon dioxide separationfrom hydrogen and nitrogen by fixed facilitated transport inswollen chitosanmembranesrdquo Journal ofMembrane Science vol323 no 2 pp 225ndash234 2008

[193] C E Powell and G G Qiao ldquoPolymeric CO2N2gas separation

membranes for the capture of carbon dioxide from power plantflue gasesrdquo Journal of Membrane Science vol 279 no 1-2 pp1ndash49 2006

[194] L A El-Azzami and E A Grulke ldquoCarbon dioxide separationfrom hydrogen and nitrogen facilitated transport in arginine


salt-chitosan membranesrdquo Journal of Membrane Science vol328 no 1-2 pp 15ndash22 2009

[195] G Xomeritakis C-Y Tsai and C J Brinker ldquoMicroporoussol-gel derived aminosilicate membrane for enhanced carbondioxide separationrdquo Separation and Purification Technology vol42 no 3 pp 249ndash257 2005

[196] E Favre ldquoCarbon dioxide recovery from post-combustion pro-cesses can gas permeation membranes compete with absorp-tionrdquo Journal of Membrane Science vol 294 no 1-2 pp 50ndash592007

[197] A Julbe ldquoChapter 6 Zeolite membranesmdashsynthesis characteri-zation and applicationrdquo Studies in Surface Science and Catalysisvol 168 pp 181ndash219 2007

[198] D W Shin S H Hyun C H Cho and M H Han ldquoSynthesisand CO

2N2gas permeation characteristics of ZSM-5 zeolite

membranesrdquo Microporous and Mesoporous Materials vol 85no 3 pp 313ndash323 2005

[199] M Anderson and Y S Lin ldquoCarbonate-ceramic dual-phasemembrane for carbon dioxide separationrdquo Journal ofMembraneScience vol 357 no 1-2 pp 122ndash129 2010

[200] D Shekhawat D R Luebke and H W Pennline ldquoA review ofcarbon dioxide selective membranesrdquo A Topical Report DOENETL-20031200 Department of Energy National EnergyTechnology Laboratory 2003

[201] P Kumar S Kim J Ida and V V Guliants ldquoPolyethyleneimine-modified MCM-48 membranes effect of water vapor and feedconcentration on N

2CO2selectivityrdquo Industrial and Engineer-

ing Chemistry Research vol 47 no 1 pp 201ndash208 2008[202] T C Merkel H Lin X Wei and R Baker ldquoPower plant

post-combustion carbon dioxide capture an opportunity formembranesrdquo Journal of Membrane Science vol 359 no 1-2 pp126ndash139 2010

[203] Y Cai Z Wang C Yi Y Bai J Wang and S WangldquoGas transport property of polyallylamine-poly(vinyl alco-hol)polysulfone composite membranesrdquo Journal of MembraneScience vol 310 no 1-2 pp 184ndash196 2008

[204] L Deng T-J Kim and M-B Hagg ldquoFacilitated transportof CO

2in novel PVAmPVA blend membranerdquo Journal of

Membrane Science vol 340 no 1-2 pp 154ndash163 2009[205] X Ren J Ren H Li S Feng and M Deng ldquoPoly (amide-6-

b-ethylene oxide) multilayer composite membrane for carbondioxide separationrdquo International Journal of Greenhouse GasControl vol 8 pp 111ndash120 2012

[206] L Liu A Chakma and X Feng ldquoPreparation of hollow fiberpoly(ether block amide)polysulfone composite membranesfor separation of carbon dioxide from nitrogenrdquo ChemicalEngineering Journal vol 105 no 1-2 pp 43ndash51 2004

[207] A Car C Stropnik W Yave and K-V Peinemann ldquoPEGmodified poly(amide-b-ethylene oxide) membranes for CO

2

separationrdquo Journal of Membrane Science vol 307 no 1 pp 88ndash95 2008

[208] W Yave A Car and K-V Peinemann ldquoNanostructured mem-brane material designed for carbon dioxide separationrdquo Journalof Membrane Science vol 350 no 1-2 pp 124ndash129 2010

[209] Y Gu and S T Oyama ldquoHigh molecular permeance in aporeless ceramic membranerdquo Advanced Materials vol 19 no12 pp 1636ndash1640 2007

[210] M Reif and R Dittmeyer ldquoPorous catalytically active ceramicmembranes for gas-liquid reactions a comparison betweencatalytic diffuser and forced through flow conceptrdquo CatalysisToday vol 82 no 1ndash4 pp 3ndash14 2003

[211] K Kusakabe T Kuroda and S Morooka ldquoSeparation ofcarbon dioxide from nitrogen using ion-exchanged faujasite-type zeolite membranes formed on porous support tubesrdquoJournal of Membrane Science vol 148 no 1 pp 13ndash23 1998

[212] J van den Bergh W Zhu J Gascon J A Moulijn and FKapteijn ldquoSeparation and permeation characteristics of aDD3Rzeolite membranerdquo Journal of Membrane Science vol 316 no 1-2 pp 35ndash45 2008

[213] M P Bernal J Coronas M Menendez and J SantamarıaldquoSeparation of CO

2N2mixtures using MFI-type zeolite mem-

branesrdquo AIChE Journal vol 50 no 1 pp 127ndash135 2004[214] Z Rui H Ji and Y S Lin ldquoModeling and analysis of ceramic-

carbonate dual-phase membrane reactor for carbon dioxidereforming with methanerdquo International Journal of HydrogenEnergy vol 36 no 14 pp 8292ndash8300 2011

[215] Z RuiM Anderson Y S Lin and Y Li ldquoModeling and analysisof carbon dioxide permeation through ceramic-carbonate dual-phase membranesrdquo Journal of Membrane Science vol 345 no1-2 pp 110ndash118 2009

[216] S J Metz M H V Mulder and M Wessling ldquoGas-permeationproperties of poly(ethylene oxide) poly(butylene terephthalate)block copolymersrdquo Macromolecules vol 37 no 12 pp 4590ndash4597 2004

[217] Z Xu J Wang W Chen and Y Xu ldquoSeparation and fixation ofcarbon dioxide using polymeric membrane contactorrdquo in Pro-ceedings of the 1st National Conference on Carbon Sequestration2001

[218] D Dortmundt and K Doshi Recent Developments in CO2

Removal Membrane Technology UOP LLC 1999[219] C A Scholes S E Kentish and G W Stevens ldquoThe effect of

condensable minor components on the gas separation perfor-mance of polymeric membranes for carbon dioxide capturerdquoEnergy Procedia vol 1 pp 311ndash317 2009

[220] K Hunger N Schmeling H B Jeazet C Janiak C Staudt andK Kleinermanns ldquoInvestigation of cross-linked and additivecontaining polymer materials for membranes with improvedperformance in pervaporation and gas separationrdquoMembranevol 2 pp 727ndash763 2012

[221] S R Reijerkerk ldquoPolyether based block copolymer membranesfor CO

2separationrdquo in Science and Technology University of

Twente Enschede The Netherlands 2010[222] A L B Ahmad Z A Jawad S C Low andH S Zein ldquoProspect

of mixedmatrix membrane towards CO2Separationrdquo Journal of

Membrane Science amp Technology vol 2 article e110 2012[223] C A Scholes G Q Chen G W Stevens and S E Kentish

ldquoPlasticization of ultra-thin polysulfone membranes by carbondioxiderdquo Journal of Membrane Science vol 346 no 1 pp 208ndash214 2010

[224] N Du H B Park G P Robertson et al ldquoPolymer nanosievemembranes for CO

2-capture applicationsrdquo Nature Materials

vol 10 no 5 pp 372ndash375 2011[225] P Uchytil J Schauer R Petrychkovych K Setnickova and S

Y Suen ldquoIonic liquid membranes for carbon dioxide-methaneseparationrdquo Journal of Membrane Science vol 383 no 1-2 pp262ndash271 2011

[226] O G Nik X Y Chen and S Kaliaguine ldquoAmine-functionalizedzeolite FAUEMT-polyimide mixed matrix membranes forCO2CH4separationrdquo Journal of Membrane Science vol 379

no 1-2 pp 468ndash478 2011[227] Y C Hudiono T K Carlisle J E Bara Y Zhang D L Gin

and R D Noble ldquoA three-component mixed-matrix membrane


with enhanced CO2separation properties based on zeolites and

ionic liquid materialsrdquo Journal of Membrane Science vol 350no 1-2 pp 117ndash123 2010

[228] A Kovvali and G Obuskovic ldquoImmobilized liquid membranesfor CO

2separationrsquordquo in Proceedings of the Preprints of Symposia-

American Chemical Society pp 665ndash667 Division of FuelChemistry American Chemical Society 2000

[229] Z Wang L E K Achenie S J Khativ and S T OyamaldquoSimulation study of single-gas permeation of carbon dioxideand methane in hybrid inorganic-organic membranerdquo Journalof Membrane Science vol 387-388 no 1 pp 30ndash39 2012

[230] S-P Yan M-X Fang W-F Zhang et al ldquoExperimental studyon the separation of CO

2from flue gas using hollow fibermem-

brane contactors without wettingrdquo Fuel Processing Technologyvol 88 no 5 pp 501ndash511 2007

[231] J-L Li andB-HChen ldquoReviewofCO2absorption using chem-

ical solvents in hollow fiber membrane contactorsrdquo Separationand Purification Technology vol 41 no 2 pp 109ndash122 2005

[232] Y-S Kim and S-M Yang ldquoAbsorption of carbon diox-ide through hollow fiber membranes using various aqueousabsorbentsrdquo Separation and Purification Technology vol 21 no1-2 pp 101ndash109 2000

[233] K Sugiura K Takei K Tanimoto and YMiyazaki ldquoThe carbondioxide concentrator by usingMCFCrdquo Journal of Power Sourcesvol 118 no 1-2 pp 218ndash227 2003

[234] H Herzog ldquoAssessing the feasibility of capturing CO2from the

airrdquo Tech Rep MIT Laboratory for Energy and the Environ-ment Massachusetts Institute of Techology Cambridge MassUSA 2003

[235] M R M Abu-Zahra J P M Niederer P H M Feron andG F Versteeg ldquoCO

2capture from power plants Part II A

parametric study of the economical performance based onmono-ethanolaminerdquo International Journal of Greenhouse GasControl vol 1 no 2 pp 135ndash142 2007


Table 1 The main greenhouse gases and their concentration [2 3]

Compound Preindustrialconcentration (ppmv)

Concentrationin 2011 (ppmv)

Atmosphericlifetime (years) Main human activity source GWPlowastlowast

Carbon dioxide (CO2) 280 3885 sim100 Fossil fuels cement production land use 1

Methane (CH4) 0715 1871748 12 Fossil fuels rice paddies waste dumpslivestock 25

Nitrous oxide (N2O) 027 0323 114 Fertilizers combustion industrial processes 298CFC-12 (CCL2F2) 0 0000533 100 Liquid coolants foams 10900CF-113 (CCl2CClF2) 0 000000075 85 na 6130HFC 23 (CHF3) 0 0000018 270 Electronics refrigerants 11700HCFC-22 (CCl2F2) 0 0000218 12 Refrigerants 1810HFC 134 (CF3CH2F) 0 0000035 14 Refrigerants 1300HCFC-141b (CH3CCl2F) 0 000000022 93 na 725HCFC-142b (CH3CClF2) 0 000000020 179 na 2310HFC 152 (CH3CHF2) 0 00000039 14 Industrial processes 140Perfluoromethane (CF4) 000004 000008lowast 50000 Aluminum production 6500Perfluoroethane (C2F6) 0 0000003lowast 10000 Aluminum production 9200Sulfur hexafluoride (SF6) 0 000000712lowast 3200 Dielectric fluid 22800lowastConcentration in 2011lowastlowastGlobal warming potentials (GWPs) measure the relative effectiveness of GHGs in trapping the Earthrsquos heat

05

10152025303540

Year1990 1993 1996 1999 2002 2005 2008 2011

1000

mill

ion

tonn

es C

O2

Figure 1 Global CO2emissions from fossil fuel combustion and

cement production [23]

Kyoto protocol therefore in 2011 Durban COP meetingthis protocol was extended until 2017 Several countries withhigh GHGs emission like China India Brazil and evenIran have added to this Protocol Intergovernmental Panelon Climate Change (IPCC) predicted the atmosphere maycontain up to 570 ppmv CO

2by the year 2100 causing a rise

of mean global temperature and sea level around 19∘C and38m respectively [15 17ndash20] Given that the earthrsquos averagetemperature continues to rise Intergovernmental Panel onClimate Change (IPCC) stated global GHG emissions mustbe reduced by 50 to 80 percent by 2050 to avoid dramaticconsequences of global warming [21ndash23]

Carbon capture and storage (CCS) is the most indi-cated technology to decrease CO

2emission from fossil fuels

sources to atmosphere Also CO2separated from flue gases

can be used in enhanced oil recovery (EOR) operationswhereCO2is injected into oil reservoirs to increase mobility of

oil and reservoir recovery [24 25] Pure CO2has many

applications in foodbeverage and different chemical indus-tries such as urea and fertilizer production foam blowing

0

500

1000

1500

2000

2500

3000

1990

1992

1994

1996

1998

2000

2002

2004

2006

2008

Year

Tone

gas

CO2

equi

vale

nt Electric powerindustry

Transportation

Industry

AgricultureCommercialResidential

Figure 2 US GHG Emissions Allocated to Economic Sectors [2]

carbonation of beverages and dry ice production or even inthe supercritical state as supercritical solvent [26ndash28]

From this definition CCS consists of three basic stages(a) separation of CO

2 (b) transportation and (c) storage

Operating costs of these stages have been estimated in 2008

(i) CO2separation from exhausting gases 24 to 52 C

ton-CO2

(ii) transportation to storage location 1 to 6 Cton-CO2

per 100 km

(iii) storage minus28 to 42 Cton-CO2

Therefore CO2separation is a major stage in CCS The

CCS total costs can vary from minus3 to 106 Cton-CO2(negative

values are expected for the injection of CO2in EOR) There

are threemajor approaches for CCS pre-combustion captureoxy-fuel process and post-combustion capture (Figure 3)[25 30 31]


FuelCombustionAir

flue gas


FuelCombustion

Oxy fuel combustion

FuelCombustion


CO2 for storage

CO2 for storage

CO2 for storage

CO2 containing

CO2 capture

CO2 capture

O2

H2O2air




2is





2and H
















2


2separation Granite


2separation






2 The CO



2 The released CO

2is




2for a given



2is absorbed











capture

Absorption

Chemical

Physical



Adsorption


Cryogenic

Membrane

Gas separation

Ceramic membrane


Gas absorption

Polypropylene



Condenser

Feed gas cooler

Feed gas

Exhaust gas

Absorber Heater

Liquidstorage tank

Cooler Reboiler

Stripper

gas CO2 product



2absorption







3 and 5NH

3)







2





2[71]







Physical









Fluorinated solvent


Chemical





[58 60 6164ndash66]





[65 67ndash69]

Ammonia




Ionic liquid (IL)





Table 2 Continued






[29 66 7576]



2





2is absorbed in



2absorp-


3

2minusHCO3



2in post-


2

















2adsorption



FGD

HX1

AC1

A PM1

CC1

HX2 HX3

A PM2

CC2

FN1

A PM3

CC3HC

PM5PM4

HX4HX6

HX5

PM6

PR1

HX7

FN2PR2

A

Chilmine Y

WT3 WT1WT2

AC2

PM7

RBRGAB

Steam

Condensate

CM1

AC3

CM2

AC4

PR3

CM3

AC4 PM8PIPE

Exhausts chilling

Ammonia removal


gas wash

CO2 compression

CH1 CH2CH3

CH4

CH5

H2ONH3

HCl




(K)



CO2kg sorbent)



Reference



2ZrO3is reversible














2





2and








(K)



CO2kg sorbent)



cycles ()Reference





4

minus 406 1 355 na na [108]


Table 4 Continued


(K)



CO2kg sorbent)



cycles ()Reference











2capture [126]










2

over CH4[131 132]


2better than unpu-



2capacities of





2











2gt CO

2gt NO gt N

2on both



2adsorption


















2 heat


2adsorbents [24 104 155 156]



2and CH














2capacity) are



2adsorbent




2capture














Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)




CO2purity ()

CO2recovery ()


VTSA 17 na 97


2is 1955 K



2that can be stored


follows [6 8 174]









2



2as



S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































FuelCombustionAir

flue gas


FuelCombustion

Oxy fuel combustion

FuelCombustion


CO2 for storage

CO2 for storage

CO2 for storage

CO2 containing

CO2 capture

CO2 capture

O2

H2O2air




2is





2and H
















2


2separation Granite


2separation






2 The CO



2 The released CO

2is




2for a given



2is absorbed











capture

Absorption

Chemical

Physical



Adsorption


Cryogenic

Membrane

Gas separation

Ceramic membrane


Gas absorption

Polypropylene



Condenser

Feed gas cooler

Feed gas

Exhaust gas

Absorber Heater

Liquidstorage tank

Cooler Reboiler

Stripper

gas CO2 product



2absorption







3 and 5NH

3)







2





2[71]







Physical









Fluorinated solvent


Chemical





[58 60 6164ndash66]





[65 67ndash69]

Ammonia




Ionic liquid (IL)





Table 2 Continued






[29 66 7576]



2





2is absorbed in



2absorp-


3

2minusHCO3



2in post-


2

















2adsorption



FGD

HX1

AC1

A PM1

CC1

HX2 HX3

A PM2

CC2

FN1

A PM3

CC3HC

PM5PM4

HX4HX6

HX5

PM6

PR1

HX7

FN2PR2

A

Chilmine Y

WT3 WT1WT2

AC2

PM7

RBRGAB

Steam

Condensate

CM1

AC3

CM2

AC4

PR3

CM3

AC4 PM8PIPE

Exhausts chilling

Ammonia removal


gas wash

CO2 compression

CH1 CH2CH3

CH4

CH5

H2ONH3

HCl




(K)



CO2kg sorbent)



Reference



2ZrO3is reversible














2





2and








(K)



CO2kg sorbent)



cycles ()Reference





4

minus 406 1 355 na na [108]


Table 4 Continued


(K)



CO2kg sorbent)



cycles ()Reference











2capture [126]










2

over CH4[131 132]


2better than unpu-



2capacities of





2











2gt CO

2gt NO gt N

2on both



2adsorption


















2 heat


2adsorbents [24 104 155 156]



2and CH














2capacity) are



2adsorbent




2capture














Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)




CO2purity ()

CO2recovery ()


VTSA 17 na 97


2is 1955 K



2that can be stored


follows [6 8 174]









2



2as



S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































capture

Absorption

Chemical

Physical



Adsorption


Cryogenic

Membrane

Gas separation

Ceramic membrane


Gas absorption

Polypropylene



Condenser

Feed gas cooler

Feed gas

Exhaust gas

Absorber Heater

Liquidstorage tank

Cooler Reboiler

Stripper

gas CO2 product



2absorption







3 and 5NH

3)







2





2[71]







Physical









Fluorinated solvent


Chemical





[58 60 6164ndash66]





[65 67ndash69]

Ammonia




Ionic liquid (IL)





Table 2 Continued






[29 66 7576]



2





2is absorbed in



2absorp-


3

2minusHCO3



2in post-


2

















2adsorption



FGD

HX1

AC1

A PM1

CC1

HX2 HX3

A PM2

CC2

FN1

A PM3

CC3HC

PM5PM4

HX4HX6

HX5

PM6

PR1

HX7

FN2PR2

A

Chilmine Y

WT3 WT1WT2

AC2

PM7

RBRGAB

Steam

Condensate

CM1

AC3

CM2

AC4

PR3

CM3

AC4 PM8PIPE

Exhausts chilling

Ammonia removal


gas wash

CO2 compression

CH1 CH2CH3

CH4

CH5

H2ONH3

HCl




(K)



CO2kg sorbent)



Reference



2ZrO3is reversible














2





2and








(K)



CO2kg sorbent)



cycles ()Reference





4

minus 406 1 355 na na [108]


Table 4 Continued


(K)



CO2kg sorbent)



cycles ()Reference











2capture [126]










2

over CH4[131 132]


2better than unpu-



2capacities of





2











2gt CO

2gt NO gt N

2on both



2adsorption


















2 heat


2adsorbents [24 104 155 156]



2and CH














2capacity) are



2adsorbent




2capture














Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)




CO2purity ()

CO2recovery ()


VTSA 17 na 97


2is 1955 K



2that can be stored


follows [6 8 174]









2



2as



S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2





















































Physical









Fluorinated solvent


Chemical





[58 60 6164ndash66]





[65 67ndash69]

Ammonia




Ionic liquid (IL)





Table 2 Continued






[29 66 7576]



2





2is absorbed in



2absorp-


3

2minusHCO3



2in post-


2

















2adsorption



FGD

HX1

AC1

A PM1

CC1

HX2 HX3

A PM2

CC2

FN1

A PM3

CC3HC

PM5PM4

HX4HX6

HX5

PM6

PR1

HX7

FN2PR2

A

Chilmine Y

WT3 WT1WT2

AC2

PM7

RBRGAB

Steam

Condensate

CM1

AC3

CM2

AC4

PR3

CM3

AC4 PM8PIPE

Exhausts chilling

Ammonia removal


gas wash

CO2 compression

CH1 CH2CH3

CH4

CH5

H2ONH3

HCl




(K)



CO2kg sorbent)



Reference



2ZrO3is reversible














2





2and








(K)



CO2kg sorbent)



cycles ()Reference





4

minus 406 1 355 na na [108]


Table 4 Continued


(K)



CO2kg sorbent)



cycles ()Reference











2capture [126]










2

over CH4[131 132]


2better than unpu-



2capacities of





2











2gt CO

2gt NO gt N

2on both



2adsorption


















2 heat


2adsorbents [24 104 155 156]



2and CH














2capacity) are



2adsorbent




2capture














Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)




CO2purity ()

CO2recovery ()


VTSA 17 na 97


2is 1955 K



2that can be stored


follows [6 8 174]









2



2as



S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 2 Continued






[29 66 7576]



2





2is absorbed in



2absorp-


3

2minusHCO3



2in post-


2

















2adsorption



FGD

HX1

AC1

A PM1

CC1

HX2 HX3

A PM2

CC2

FN1

A PM3

CC3HC

PM5PM4

HX4HX6

HX5

PM6

PR1

HX7

FN2PR2

A

Chilmine Y

WT3 WT1WT2

AC2

PM7

RBRGAB

Steam

Condensate

CM1

AC3

CM2

AC4

PR3

CM3

AC4 PM8PIPE

Exhausts chilling

Ammonia removal


gas wash

CO2 compression

CH1 CH2CH3

CH4

CH5

H2ONH3

HCl




(K)



CO2kg sorbent)



Reference



2ZrO3is reversible














2





2and








(K)



CO2kg sorbent)



cycles ()Reference





4

minus 406 1 355 na na [108]


Table 4 Continued


(K)



CO2kg sorbent)



cycles ()Reference











2capture [126]










2

over CH4[131 132]


2better than unpu-



2capacities of





2











2gt CO

2gt NO gt N

2on both



2adsorption


















2 heat


2adsorbents [24 104 155 156]



2and CH














2capacity) are



2adsorbent




2capture














Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)




CO2purity ()

CO2recovery ()


VTSA 17 na 97


2is 1955 K



2that can be stored


follows [6 8 174]









2



2as



S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































FGD

HX1

AC1

A PM1

CC1

HX2 HX3

A PM2

CC2

FN1

A PM3

CC3HC

PM5PM4

HX4HX6

HX5

PM6

PR1

HX7

FN2PR2

A

Chilmine Y

WT3 WT1WT2

AC2

PM7

RBRGAB

Steam

Condensate

CM1

AC3

CM2

AC4

PR3

CM3

AC4 PM8PIPE

Exhausts chilling

Ammonia removal


gas wash

CO2 compression

CH1 CH2CH3

CH4

CH5

H2ONH3

HCl




(K)



CO2kg sorbent)



Reference



2ZrO3is reversible














2





2and








(K)



CO2kg sorbent)



cycles ()Reference





4

minus 406 1 355 na na [108]


Table 4 Continued


(K)



CO2kg sorbent)



cycles ()Reference











2capture [126]










2

over CH4[131 132]


2better than unpu-



2capacities of





2











2gt CO

2gt NO gt N

2on both



2adsorption


















2 heat


2adsorbents [24 104 155 156]



2and CH














2capacity) are



2adsorbent




2capture














Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)




CO2purity ()

CO2recovery ()


VTSA 17 na 97


2is 1955 K



2that can be stored


follows [6 8 174]









2



2as



S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2





















































(K)



CO2kg sorbent)



cycles ()Reference





4

minus 406 1 355 na na [108]


Table 4 Continued


(K)



CO2kg sorbent)



cycles ()Reference











2capture [126]










2

over CH4[131 132]


2better than unpu-



2capacities of





2











2gt CO

2gt NO gt N

2on both



2adsorption


















2 heat


2adsorbents [24 104 155 156]



2and CH














2capacity) are



2adsorbent




2capture














Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)




CO2purity ()

CO2recovery ()


VTSA 17 na 97


2is 1955 K



2that can be stored


follows [6 8 174]









2



2as



S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 4 Continued


(K)



CO2kg sorbent)



cycles ()Reference











2capture [126]










2

over CH4[131 132]


2better than unpu-



2capacities of





2











2gt CO

2gt NO gt N

2on both



2adsorption


















2 heat


2adsorbents [24 104 155 156]



2and CH














2capacity) are



2adsorbent




2capture














Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)




CO2purity ()

CO2recovery ()


VTSA 17 na 97


2is 1955 K



2that can be stored


follows [6 8 174]









2



2as



S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2




















































2gt CO

2gt NO gt N

2on both



2adsorption


















2 heat


2adsorbents [24 104 155 156]



2and CH














2capacity) are



2adsorbent




2capture














Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)




CO2purity ()

CO2recovery ()


VTSA 17 na 97


2is 1955 K



2that can be stored


follows [6 8 174]









2



2as



S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Steam

Cond

ensa

te

(a)

Adso

rben

t be

d

Adso

rben

t be

d

Flue gas

Adsorbed gas

(b)

Vacuum pump

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

(c)

Ads

orbe

nt

bed

Ads

orbe

nt

bed

Flue gas

Adsorbed gas

++

minusminus

(d)




CO2purity ()

CO2recovery ()


VTSA 17 na 97


2is 1955 K



2that can be stored


follows [6 8 174]









2



2as



S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































S1

C1

H1 S3 H2 Sep1 S4 C2 S7 H3 S8 H4

Sep2

S12 (purge gas) H5


C1 (intercooled

S2

P2



P1

Mixture

Step 1 Step 2

S6 (liquid CO2)


S10 (liquid CO2)

S15 (liquid CO2)

S11 (liquid CO2)















2O





2


2could








2is concentrated



2



2recovery Gas









2 Howevre





119909andNO








Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Flue gas in

Axial position

Tem

pera

ture

N2

TC in

T0

TH2O

TCO2

t1

t2

(a)

Axial position Te

mpe

ratu

re

CO2 in CO2 out

TC in

TR inTlowast

CO2

TH2O

TCO2

t0

t2

(b)

Axial position

Tem

pera

ture

N2 in N2 out

TC in

TR in

T0

Tlowast

CO2

TH2O

t0

t1

t2

(c)


Condensate

Cryogenic

separation

storageMake-up

water

Air

Cathode

Anode

ACDC

Natural gas

Sulfurremoval

CO2 to

CO2





2








Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2





















































Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference


na na na na 3 [197]


na 923 7780 na 16 [199]



na 298 310 21 148 [193]


na 298 150 14 107 [193]








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference











Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference






Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference








Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




10 308 187 117 160 [193]





Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference




















Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference





300 298 150 23 652 [193]


300 298 149 10 149 [193]


300 298 161 05 322 [193]



Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2



















































Table 6 Continued


Temperature(K)

119875


119875

lowast (N2)(barrer)

120572

(CO2N2)Reference



























its permeability






Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2























































Industrial








Experimental























2separation but




119909[45 233]


HC +metal oxide


(2)












2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2




















































2





2and are relatively



2




2absorption


2for absorption






2O4and nano







2than zeolite 13X




2



2






2recovery Since


2O3support and


2separation








2capture Now these


3 Conclusion


2separation from



2 temperature


2separation











2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2





















































2separation is sug-




References




















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2





















































2Storage part 2


























2




2capturerdquo


















2

























2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2































































2capture by





2capturerdquo in










2capture by

























2capture








2removal at high

















4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2






























































4andCO














4






2capture in



2




2



2capture










2and H













CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2





















































CH4 and N










2












2seques-





















2



































2











2CO2cycle for














































2












































































2











2CO2cycle for














































2







































































2


















































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