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New hybrid composite honeycomb monolith with 13X zeolite and activated carbon for CO2 capture

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Abstract

Due to the industrialization, it is urgent to reduce the carbon dioxide emissions. For that, diverse technologies can be applied. In adsorption processes, the development of new materials is an emerging challenge in order to increase the CO2 adsorption capacity of materials and the efficiency of the processes. In this work, a new hybrid honeycomb monolith composed by zeolite and activated carbon was produced by extrusion process. Single adsorption equilibrium isotherms of carbon dioxide and nitrogen were measured by a gravimetric method using a Rubotherm® magnetic suspension balance at three temperatures, 303, 333 and 373 K. The experimental points were well described by Dual-Site Langmuir model. The material presented a carbon dioxide adsorption capacity of 2.63 mol kg−1 at 1 bar and 303 K. Binary breakthrough curves were obtained at 298 K and 2.4 bar with different feed mixtures. The experimental results of adsorption equilibrium were validated with the Dual-Site Langmuir isotherm extended to multicomponent mixtures. A mathematical model was applied to predict the dynamic behaviour of the adsorption bed.

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(Adapted from Moreira et al. 2017)

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Abbreviations

\({a_m}\) :

Monolith channel specific area (m−1)

\({a_p}\) :

Particle external specific area (m−1)

\({b_{0i}}\) :

Affinity constant at infinite temperature (bar−1)

\({b_i}\) :

Affinity constant (bar−1)

\({C_{inlet}}\) :

Inlet gas phase concentration (mol m−3)

\({C_i}\) :

Gas phase concentration of component \(i\) (mol m−3)

\({C_p}\) :

Heat capacity of the mixture at constant pressure (J mol−1 K−1)

\({\hat {C}_p}\) :

Heat capacity at constant pressure (per mass unit) (J kg−1 K−1)

\({C_{p,i}}\) :

Heat capacity at constant pressure of component \(i\) (J mol−1 K−1)

\({\tilde {C}_{p,s}}\) :

Solid specific heat (per mass unit) (J kg−1 K−1)

\({\tilde {C}_{p,w}}\) :

Wall specific heat (per mass unit) (J kg−1 K−1)

\({C_s}\) :

Concentration at the solid interface (mol m−3)

\({C_t}\) :

Total gas phase concentration (mol m−3)

\({\tilde {C}_{v,ads,i}}\) :

Molar specific heat of component \(i\) in the adsorbed phase at constant volume (J mol−1 K−1)

\({C_{v,i}}\) :

Molar specific heat of component \(i\) at constant volume (J mol−1 K−1)

\(D\) :

Total diameter of channels (m)

\({D_{ax}}\) :

Mass axial dispersion coefficient (m2 s−1)

\({D_{k,i}}\) :

Knudsen diffusivity of component \(i\) (m2 s−1)

\({D_m}\) :

Molecular diffusivity (m2 s−1)

\({D_{m,i}}\) :

Molecular diffusivity of component \(i\) (m2 s−1)

\(e\) :

Column wall thickness (m)

\({h_f}\) :

Heat transfer coefficient between the gas and the particle (W m−2 K−1)

\({h_w}\) :

Heat transfer coefficient between the gas phase and the wall (W m−2 K−1)

\({k_g}\) :

Thermal conductivity of the gas mixture (W m−2 K−1)

\({k_{g,i}}\) :

Thermal conductivity of component \(i\) (W m−2 K−1)

\({k_f}\) :

Film mass transfer coefficient (m s−1)

\({k_{macro}}\) :

LDF coefficient for macropores (s−1)

\({k_{micro}}\) :

LDF coefficient for micropores (s−1)

\({L_c}\) :

Monolith length (m)

\({l_w}\) :

Monolith wall thickness (m)

\({m_S}\) :

Adsorbent mass (kg)

\({M_w}\) :

Adsorbate molecular weight (kg mol−1)

\(P\) :

Pressure (bar)

\({P_i}\) :

Partial pressure of component \(i\) (bar)

\({q_i}\) :

Adsorbed amount of component \(i\) (mol kg−1)

\({\bar {q}_i}\) :

Particle average adsorbed concentration (mol kg−1)

\(q_{i}^{*}\) :

Adsorbed concentration in equilibrium of component \(i\) (mol kg−1)

\({q_{sat,i}}\) :

Adsorbent saturation capacity of component \(i\) (mol kg−1)

Re:

Reynolds number

\({R_g}\) :

Universal gas constant (J mol−1 K−1)

\({R_c}\) :

Equivalent monolith radius (approximation of cylindrical monolith) (m)

\({R_{ch,e}}\) :

Equivalent channel radius (approximation of cylindrical channel) (m)

\(T\) :

Temperature (K)

\({T_g}\) :

Temperature of the gas phase (K)

\({T_{inlet}}\) :

Inlet temperature (K)

\({T_s}\) :

Temperature of the solid phase (K)

\({T_w}\) :

Wall temperature (K)

\({T_\infty }\) :

External temperature (K)

\(Sc\) :

Schmidt number

\(Sh\) :

Sherwood number

\({u_0}\) :

Superficial gas velocity (m s−1)

\({u_m}\) :

Intersticial gas velocity (m s−1)

\(U\) :

Overall heat transfer coefficient (W m−2 K−1)

\({V_C}\) :

Volume of the permanent magnet, of the sample basket and of the glass wool used to hold the sample (m3 mol−1)

\({V_S}\) :

Volume of the solid adsorbent (m3 mol−1)

\({y_i}\) :

Molar faction of component \(i\)

\(z\) :

Axial position (m)

\({{{\upalpha}}}\) :

Adsorption separation factor

\({{{{\upalpha}}}_{\text{w}}}\) :

Ratio of the internal surface area to the volume of the column wall (m−1)

\({{{{\upalpha}}}_{{\text{wl}}}}\) :

Ratio of the log mean surface area to the volume of the column wall (m−1)

\(\Delta {\text{H}}\) :

Heat of adsorption (kJ mol−1)

\(\Delta {{\text{H}}_{\text{i}}}\) :

Isosteric heat of adsorption of component \(i\) (kJ mol−1)

\(\Delta {\text{m}}\) :

Difference in weight between two measurements (kg)

\({{{{\upvarepsilon}}}_{\text{i}}}\) :

Energy parameter for interaction between molecules

\({{{{\upvarepsilon}}}_m}\) :

Monolith porosity

\({{{{\upvarepsilon}}}_w}\) :

Monolith wall porosity

λ:

Axial heat dispersion coefficient (W m−1 K−1)

\({{{{\upmu}}}_{\text{g}}}\) :

Gas viscosity (Pa s)

\({{{\uprho}}}\) :

Gas density (kg m−3)

\({{{{\uprho}}}_{{\text{ap}}}}\) :

Apparent density (kg m−3)

\({{{{\uprho}}}_{\text{b}}}\) :

Bulk density (kg m−3)

\({{{{\uprho}}}_{\text{G}}}\) :

Density of the gas phase at the measuring conditions (T,P) (kg m−3)

\({{{{\uprho}}}_{\text{L}}}\) :

Density of the adsorbed phase (kg m−3)

\({{{{\uprho}}}_{\text{w}}}\) :

Wall density (kg m−3)

\({{{{\uptau}}}_{\text{p}}}\) :

Particle tortuosity

BPR:

Back-pressure regulator

EDS:

Energy dispersive X-ray spectroscopy

GA:

Gas analyser

LDF:

Linear driving force model

MFC:

Mass flow controller

MFM:

Mass flow meter

RH:

Humidity sensor

SEM:

Scanning electron microscopy

References

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Acknowledgements

This work was financed by scholarship programme with reference PD/BD/105981/2014 by FCT – Fundação para a Ciência e Tecnologia. This work was financially supported by: Project POCI-01-0145-FEDER-006984 – Associate Laboratory LSRE-LCM funded by FEDER through COMPETE2020 Programa Operacional Competitividade e Internacionalização (POCI) – and by national funds through FCT – Fundação para a Ciência e Tecnologia. The support from Mr. Dabo Chen in Jingdezhen Jiayi advanced material Co. Ltd is highly appreciated.

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Authors and Affiliations

  1. LSRE-Laboratory of Separation and Reaction Engineering, Associate Laboratory LSRE/LCM, Faculdade de Engenharia, Universidade do Porto, Rua Dr. Roberto Frias, 4200-465, Porto, Portugal

    Maria João Regufe, Alexandre F. P. Ferreira, José Miguel Loureiro, Alírio Rodrigues & Ana Mafalda Ribeiro

  2. Key Laboratory for Thermal Science and Power Engineering of Ministry of Education, Department of Thermal Engineering, Tsinghua University, Beijing, 100084, China

    Yixiang Shi

Authors
  1. Maria João Regufe
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  2. Alexandre F. P. Ferreira
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  3. José Miguel Loureiro
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  4. Yixiang Shi
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  5. Alírio Rodrigues
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  6. Ana Mafalda Ribeiro
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Corresponding author

Correspondence to Ana Mafalda Ribeiro.

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Regufe, M.J., Ferreira, A.F.P., Loureiro, J.M. et al. New hybrid composite honeycomb monolith with 13X zeolite and activated carbon for CO2 capture. Adsorption 24, 249–265 (2018). https://doi.org/10.1007/s10450-018-9938-1

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