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CO2 capture by ethanolamines functionalized resins: amination and kinetics of adsorption in a fixed bed

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The main aim of this manuscript was to investigate the effect of amine (MEA, DEA and TEA) functionalization of high surface area supports (Amberlite IR120H, Ambersep 252H, Amberlite 200CNa and Amberlite XAD7HP) on adsorption of CO2 from gases streams. A saturated factorial design of experiments was initially applied to determine the influence of four amine impregnation variables on amine loading. Except for the amine concentration whose effect was significantly positive on the amount of ethanolamine impregnated in Amberlite XAD7HP (p ≤ 0.05), the other factors had negligible importance. Kinetic experiments of CO2 adsorption were performed in a fixed bed at different inlet concentrations of CO2 and temperatures. The amounts of adsorbed CO2 on the DEA enriched Ambersep 252H, Amberlite 200CNa and Amberlite XAD7HP at bed saturation were ~ 40–400 times as high as those obtained with the same adsorbents without impregnation. DEA enriched Amberlite IR120H and TEA functionalized resins presented small capacities to adsorb CO2 at the investigated conditions, while MEA enriched resins were effective as CO2 adsorbents in the case of impregnation in Amberlite 200CNa. A classical fundamental model described correctly the breakthrough curves for CO2 adsorption–desorption at concentrations of CO2 in the gas feed stream of 1%, 3% and 5% at 40 °C and 60 °C.

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C A :

Initial concentration of ethanolamine for resin amination (kg m3)

C :

Concentration of CO2 in the gas stream flowing in the fixed bed at t and z (kg m3)

C e :

Equilibrium concentration of CO2 in the gas phase (kg m3)

CL :

Outlet concentration of CO2 in the gas phase (kg m3)

C 0 :

Concentration of CO2 in the gas feed stream of the fixed bed (kg m3)

D L :

Axial dispersion coefficient (m2 s1)

e 0 :

Arithmetic mean of Y2 for amination of a specific resin (kg kg1)

e j :

Parameter in Eq. (1) (kg kg1)

k C a :

Effective coefficient of CO2 transfer between gas and solid phases (s1)

K :

Adsorption equilibrium constant for CO2 (m3 kg1)

k YN :

Parameter of the Yoon and Nelson model (Eq. 4) (s1)

m s :

Mass of resin packed in the bed (kg)

n OH :

Number of OH groups in the ethanolamine fixed in the examined resins

Q 0 :

Volumetric flow rate of gases in the feed stream of the fixed bed (m3 s1)

T :

Temperature (°C)

T high :

Highest temperature of amination (°C)

T low :

Lowest temperature of amination (°C)

T 0 :

Gas feed stream temperature in the bed (°C)

t :

Time (s)

u 0 :

Inlet superficial velocity of the gas in the bed (m s1)

W :

Concentration of CO2 in the solid phase in the bed at t and z (kg kg1)

W e :

Amount of CO2 adsorbed at equilibrium (kg kg1)

W s :

CO2 adsorbed on the resins at bed saturation (kg kg1)

W m :

CO2 adsorbed per mass of resin when all the surface of adsorbent is covered (kg kg1)

X j :

Dimensionless coded variable in Eq. (1)

X 0 :

Fraction of CO2 in the gas feed stream of the fixed bed (% in v/v)

Y 1 :

Mass loss of resin due to the pretreatment with methanol (kg kg1)

Y 2 :

Mass ratio of fixed amine and resin free of ethanolamine pretreated with methanol (kg kg1)

z :

Axial position in the bed (m)

ε :

Bed void fraction (m3 m3)

ρ s :

Adsorbent density (kg m3)

τ :

Parameter of the Yoon and Nelson model (Eq. 4) (s)


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The Brazilian Council for Scientific and Technological Development (CNPq) is acknowledged by the financial support (Research Project No. 401950/2016-6).

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Lopes, T.J., Benincá, C., Zanoelo, E.F. et al. CO2 capture by ethanolamines functionalized resins: amination and kinetics of adsorption in a fixed bed. Adsorption 27, 1237–1250 (2021).

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