1. The capture of CO2 from flue gas using adsorption combined with membrane separation
Prof. Krzysztof Warmuzinski Polish Academy of Sciences Institute of Chemical Engineering
6th International Scientific Conference on Energy and Climate Change

2. Post-combustion systems Pre-combustion systems Oxyfuel combustion
CO2 CAPTURE
Post-combustion systems
Pre-combustion systems
Oxyfuel combustion
Post-combustion systems, which separate CO2 from flue gases produced by the combustion of a primary fossil fuel (coal, natural gas, oil) or biomass in air
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3. POST-COMBUSTION CO2 CAPTURE
Absorption
Membrane separation
Adsorption (PSA, TSA)
Hybrid systems
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4. HYBRID PROCESS FOR THE CAPTURE OF CO2 FROM FLUE GAS
SEPARATION PROPERTIES OF POLYMERIC MEMBRANES
MATHEMATICAL MODEL OF THE HYBRID PROCESS
DEMONSTRATION
HYBRID INSTALLATION
HYBRID PROCESS FOR CO2 REMOVAL FROM FLUE GAS
EFFECT OF GAS FLOW RATES IN THE REGENERATION AND PURGE STEPS ON CO2 PURITY AND RECOVERY
ADSORPTION EQUILIBRIA AND KINETICS ON ZMS 13X
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5. Demonstration hybrid installation
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6. Demonstration hybrid installation
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7. Objectives of the study
Theoretical and experimental determination of the principal parameters of product streams (i.e. the purified gas stream and the CO2-rich stream), especially from the standpoint of purity requirements associated with the transport and storage of CO2
Analysis of the effect of two crucial process parameters – gas flow rates in the regeneration and purge steps – on the recovery of CO2 and its concentration in the enriched stream
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8. The PSA cycle
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9. Basic parameters of the process
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10. Properties of the adsorbent
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11. Properties of the adsorbent
Multisite Langmuir isotherm
Gas qs b0 A n
mol/kg
Pa-1 K -
CO2
8.20
3.56∙10-11
4415.7
4.686 N2
5.45
5.77∙10-10
1909.5
1.952 O2
5.21
1.47∙10-9
1528.6
0.821
Mass transfer coefficients
CO2: 1.22∙10-2 s-1, N2: 7.01∙10-2 s-1 for N2, O2: 7.59∙10-2 s-1
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12. Properties of the membrane module
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13. Modelling of the hybrid separation of CO2 from flue gas streams
Model of the PSA separation
Model of the membrane separation
Integration of the PSA and membrane models into PSE gPROMS software package
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14. Model of the PSA separation
Plug flow with axial dispersion is assumed
The feed may contain N adsorbing species
Process is non-isothermal with thermal equilibrium between the gas and the solid phase
Pressure drop over the adsorbent bed is negligible
Adsorption equilibria are described by non-iterative isotherm equation (e.g. multisite Langmuir, Langmuir-Freundlich, etc.)
The fluid phase is modelled as an ideal gas
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15. Model of the membrane separation
Plug flow on the feed side and unhindered flow on the permeate side
The feed may contain N permeating species
There are no interactions between the permeating gases
Permeation coefficients are independent of pressure
Pressure drops are negligible on both sides of the membrane
The process is isothermal
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16. Numerical solver PSE gPROMS package
Built-in reliable and stable numerical methods
Flexibility in defining the complex network of interconnecting components for the whole system
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17. CO2 recovery and its concentration in the enriched gas
Gas flow rates in the purge step of the PSA cycle:
  6.4 m3(STP)/h
  6.8 m3(STP)/h
  7.2 m3(STP)/h
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18. CO2 concentration and gas flow rate in the membrane module
Gas flow rates in the purge step of the PSA cycle: 6.8 m3(STP)/h
  inlet to the membrane module
  permeate outlet
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19. Experimental results
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20. CONCLUSIONS
In the process analyzed, it is possible to raise CO2 concentration from 13.3 vol.% to over 97 vol.%, with a virtually total recovery
The CO2 concentrations obtained are sufficient from the standpoint of CO2 transportation and storage
For three different flow rates during purge with the enriched stream (6.4, 6.8 and 7.2 m3 (STP)/h) the limiting values were determined for the regenerating streams (0.7, 0.9 and 1.1 m3 (STP)/h, respectively). These values lead to the maximum CO2 concentrations in the enriched product without any CO2 breakthrough into the purified stream
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21. THANK YOU FOR YOUR ATTENTION
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