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Optimum synthesis of solvent-based post-combustion CO2 capture flowsheets through a generalized modeling framework

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Abstract

A generalized framework for the optimal design of post-combustion CO2 capture processes based on a systemic and flexible equilibrium separation model that employs orthogonal collocation on finite elements techniques is proposed. Within this context, a column section of adaptive separation capability and functionality serves as the fundamental structural block for the identification of efficient separation schemes. Separation column sections in combination with heat transfer blocks, as well as stream splitters and mixers enable the generation and evaluation of alternative flowsheet configurations within a nonlinear optimization program. The main objectives for the flowsheet evaluation involve separation and thermal efficiency that eventually impact the economics of the overall process. Vapor–liquid equilibrium calculations are performed using statistical associating fluid theory for potentials of variable range (Mac Dowell et al., Ind Eng Chem Res 49:1883–1899, 2010). The proposed design framework is used for the optimal design of five alternative flowsheet configurations for the separation of CO2 from a flue gas stream using a 30 % weight monoethanolamine aqueous solution. These flowsheets illustrate the various connection patterns between the process units and indicate suitable distribution of process-driving forces through which the overall efficiency can be drastically enhanced.

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Abbreviations

a :

Liquid loading (–)

A HEX :

Heat exchanger area (m2)

AMP:

2-Amino-2-methyl-1-propanol

DEA:

Diethanolamine

DGA:

Diglycolamine

F :

Molar flow rate (mol s−1)

H :

Stream molar enthalpy (J mol−1)

H c :

Column packing height (m)

k :

Process association coefficient (adjacency matrix element)

L :

Liquid molar flow rate (mol s−1)

LMTD:

Logarithmic mean temperature difference (–)

MDEA:

Methyl-diethanolamine

MEA:

Monoethanolamine

ncp:

Number of collocation points in a finite element (–)

NC:

Number of components (–)

NM:

Number of modules (–)

NP:

Number of phases

NS:

Number of sub-streams

NSS:

Number of side-streams

P:

Pressure (kPa)

p :

Split ratio in splitter block (–)

P i :

Vapor pressure of component i (kPa)

PZ:

Piperazine

Q :

Rate of heat loss/heat duty (Watt)

R :

Rate of generation/consumption (mol s−1 m−3)

SF:

Side-feed stream flow (mol s−1)

s :

Column position coordinate (–)

T :

Temperature (K)

TEA:

Triethanolamine

U :

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

V :

Vapor molar flow rate (mol s−1)

W :

Langrange interpolating polynomial (–)

x :

Liquid phase mole fraction (–)

y :

Gas phase mole fraction (–)

φ :

Liquid phase holdup (m3)

b:

Reboiler

in:

Inlet stream

l:

CO2 lean stream

out:

Outlet stream

r:

CO2 rich stream

solv:

Solvent

t:

Total

dep:

Departure

in:

Inlet stream

L:

Liquid phase

out:

Outlet stream

t:

Total

V:

Vapor phase

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Acknowledgments

The authors would like to thank Prof. Claire Adjiman, Prof. Amparo Galindo, Prof. George Jackson, and Dr. Alexandros Chremos, of Imperial College London for providing the SAFT-VR thermodynamic models. The financial support of the European Commission under contract FP7-ENERGY-2011-282789 is gratefully acknowledged.

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Authors and Affiliations

  1. Chemical Process and Energy Resources Institute (CPERI), Centre for Research and Technology-Hellas (CERTH), Thermi, 57001, Thessaloniki, Greece

    Theodoros Damartzis, Athanasios I. Papadopoulos & Panos Seferlis

  2. Department of Mechanical Engineering, Aristotle University of Thessaloniki, 54124, Thessaloniki, Greece

    Theodoros Damartzis & Panos Seferlis

Authors
  1. Theodoros Damartzis
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  2. Athanasios I. Papadopoulos
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  3. Panos Seferlis
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Corresponding author

Correspondence to Panos Seferlis.

Appendix 1

Appendix 1

The parameters A m,k and B m,k for the polynomial approximation of the component partial pressures and the liquid phase enthalpy departure with CO2 loading and temperature as calculated using the SAFT-VR equation of state (Eqs. 25 and 26) are listed in the following Tables 4, 5, 6, and 7.

Table 4 Parameters for the polynomial approximation of CO2 partial pressure in the 30 wt% MEA aqueous solution
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Table 5 Parameters for the polynomial approximation of H2O partial pressure in the 30 wt% MEA aqueous solution
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Table 6 Parameters for the polynomial approximation of MEA partial pressure in the 30 wt% MEA aqueous solution
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Table 7 Parameters for the polynomial approximation of H dep in the 30 wt% MEA aqueous solution
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Damartzis, T., Papadopoulos, A.I. & Seferlis, P. Optimum synthesis of solvent-based post-combustion CO2 capture flowsheets through a generalized modeling framework. Clean Techn Environ Policy 16, 1363–1380 (2014). https://doi.org/10.1007/s10098-014-0747-2

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