Improved rate-based modeling of carbon dioxide absorption with aqueous monoethanolamine solution

Abstract

This paper focuses on modeling and simulation of a post-combustion carbon dioxide capture in a coal-fired power plant by chemical absorption using monoethanolamine. The aim is to obtain a reliable tool for process simulation: a customized rate-based model has been developed and implemented in the ASPEN Plus^® software, along with regressed parameters for the Electrolyte-NRTL model worked out in a previous research. The model is validated by comparison with experimental data of a pilot plant and can provide simulation results very close to experimental data.

Graphical abstract

Keywords

Absorption / carbon dioxide capture / rate-based model / monoethanolamine scrubbing

References

[1] NOAA. 2013. NOAA website

[2] UNO. Kyoto Protocol to the United Nations Framework Convention on Climate Change, 1998

[3] Kohl A L, Nielsen R. Gas Purification, 5th ed. Texas: Gulf Publishing Company, Book Division, 1997

[4] Wang M, Lawal A, Stephenson P, Sidders J, Ramshaw C. Post-combustion CO₂ capture with chemical absorption: A state-of-the-art review. Chemical Engineering Research & Design, 2011, 89(9): 1609−1624

[5] Bergman D F, Yarborough L. In: 71st Annual Meeting of AIChE, Miami Beach, Florida, 1978

[6] Moioli S, Pellegrini L A. Regeneration section of CO₂ capture plant by MEA scrubbing with a rate-based model. Chemical Engineering Transactions, 2013, 32: 1849−1854

[7] Kent R L, Eisenberg B. Better data for amine treating. Hydrocarbon Processing, 1976, 55: 87−90

[8] Al-Baghli N A, Pruess S A, Yesavage V F, Selim M S. A rate-based model for the design of gas absorbers for the removal of CO₂ and H₂S using aqueous solutions of MEA and DEA. Fluid Phase Equilibria, 2001, 185(1−2): 31−43

[9] Mangalapally H P, Notz R, Hoch S, Asprion N, Sieder G, Garcia H, Hasse H. Pilot plant experimental studies of post combustion CO₂ capture by reactive absorption with MEA and new solvents. Energy Procedia, 2009, 1(1): 963−970

[10] Kucka L, Müller I, Kenig E Y, Górak A. On the modelling and simulation of sour gas absorption by aqueous amine solutions. Chemical Engineering Science, 2003, 58(16): 3571−3578

[11] Freguia S, Rochelle G T. Modeling of CO₂ capture by aqueous monoethanolamine. AIChE Journal. American Institute of Chemical Engineers, 2003, 49(7): 1676−1686

[12] King C J. Turbolent liquid phase mass transfer at a free gas-liquid interface. Industrial & Engineering Chemistry Fundamentals, 1966, 5(1): 1−8

[13] AspenTech. ASPEN Plus^®, Burlington. MA: AspenTech, 2010

[14] Pellegrini L A, Moioli S, Gamba S. Energy saving in a CO₂ capture plant by MEA scrubbing. Chemical Engineering Research & Design, 2011, 89(9 9A): 1676−1683

[15] Edwards T J, Maurer G, Newman J, Prausnitz J M. Vapor-liquid equilibria in multicomponent aqueous solutions of volatile weak electrolytes. AIChE Journal. American Institute of Chemical Engineers, 1978, 24(6): 966−976

[16] Hikita H, Asai S, Ishikawa H, Honda M. The kinetics of reactions of carbon dioxide with monoethanolamine, diethanolamine and triethanolamine by a rapid mixing method. Chemical Engineering Journal, 1977, 13(1): 7−12

[17] Pinsent B R W, Pearson L, Roughton F W J. The kinetics of combination of carbon dioxide with hydroxide ions. Transactions of the Faraday Society, 1956, 52: 1512−1518

[18] Pellegrini L A, Moioli S, Picutti B, Vergani P, Gamba S. Design of an acidic natural gas purification plant by means of a process simulator. Chemical Engineering Transactions, 2011, 24: 271−276

[19] Pellegrini L A, Moioli S, Gamba S, Ceragioli P. Prediction of vapor–liquid equilibrium for reservoir mixtures with cubic equations of state: binary interaction parameters for acidic gases. Fluid Phase Equilibria, 2012, 326: 45−49

[20] De Guido G, Langè S, Moioli S, Pellegrini L A. Thermodynamic method for the prediction of solid CO₂ formation from multicomponent mixtures. Process Safety and Environmental Protection, 2014, 92(1): 70−79

[21] Pellegrini L A, Langé S, Moioli S, Picutti B, Vergani P. Influence of gas impurities on thermodynamics of amine solutions. 1. Aromatics. Industrial & Engineering Chemistry Research, 2013, 52(5): 2018−2024

[22] Langé S, Pellegrini L A, Moioli S, Picutti B, Vergani P. Influence of gas impurities on thermodynamics of amine solutions. 2. Mercaptans. Industrial & Engineering Chemistry Research, 2013, 52(5): 2025−2031

[23] Gamba S, Soave G S, Pellegrini L A. Use of normal boiling point correlations for predicting critical parameters of paraffins for vapour-liquid equilibrium calculations with the SRK equation of state. Fluid Phase Equilibria, 2009, 276(2): 133−141

[24] Pellegrini L A, Gamba S, Bonomi S, Calemma V. Equilibrium constants for isomerization of n-paraffins. Industrial & Engineering Chemistry Research, 2007, 46(16): 5446−5452

[25] Pellegrini L A, Gamba S, Moioli S. Using an adaptive parameter method for process simulation of nonideal systems. Industrial & Engineering Chemistry Research, 2010, 49(10): 4923−4932

[26] Oyenekan B A, Rochelle G T. Energy performance of stripper configurations for CO₂ capture by aqueous amines. Industrial & Engineering Chemistry Research, 2005, 45(8): 2457−2464

[27] Moioli S, Pellegrini L A, Gamba S. Simulation of CO₂ capture by MEA scrubbing with a rate-based model. In: 20^th International Congress of Chemical and Process Engineering CHISA 2012, Prague, Czech Republic, 2012

[28] Soave G. Equilibrium constants from a modified Redlich-Kwong equation of state. Chemical Engineering Science, 1972, 27(6): 1197−1203

[29] Chen C C, Britt H I, Boston J F, Evans L B. Extension and application of the Pitzer equation for vapor-liquid equilibrium of aqueous electrolyte systems with molecular solutes. AIChE Journal. American Institute of Chemical Engineers, 1979, 25(5): 820−831

[30] Chen C C, Britt H I, Boston J F, Evans L B. Local composition model for excess Gibbs energy of electrolyte systems. Part I: Single solvent, single completely dissociated electrolyte systems. AIChE Journal. American Institute of Chemical Engineers, 1982, 28(4): 588−596

[31] Chen C C, Evans L B. A local composition model for the excess Gibbs energy of aqueous electrolyte systems. AIChE Journal. American Institute of Chemical Engineers, 1986, 32(3): 444−454

[32] Mock B, Evans L B, Chen C C. Thermodynamic representation of phase equilibria of mixed-solvent electrolyte systems. AIChE Journal. American Institute of Chemical Engineers, 1986, 32(10): 1655−1664

[33] Jou F Y, Mather A E, Otto F D. The Solubility of CO₂ in a 30-mass-percent monoethanolamine solution. Canadian Journal of Chemical Engineering, 1995, 73(1): 140−147

[34] Ma'mun S, Nilsen R, Svendsen H F, Juliussen O. Solubility of carbon dioxide in 30 mass % monoethanolamine and 50 mass % methyldiethanolamine solutions. Journal of Chemical & Engineering Data, 2005, 50(2): 630−634

[35] Gamba S, Pellegrini L A. Biogas upgrading: Analysis and comparison between water and chemical scrubbings. Chemical Engineering Transactions, 2013, 32: 1273−1278

[36] Lewis W K, Whitman W G. Principles of gas absorption. Industrial & Engineering Chemistry, 1924, 16(12): 1215−1220

[37] Moioli S, Pellegrini L A, Picutti B, Vergani P. Improved rate-based modeling of H₂S and CO₂ removal by MDEA scrubbing. Industrial & Engineering Chemistry Research, 2013, 52(5): 2056−2065

[38] Austgen D M A. Model of vapor-liquid equilibria for acid gas-alkanolamine-H₂O systems. Dissertation for the Doctoral Degree. Texas: University of Texas, 1989

[39] Dugas R E. Pilot plant study of carbon dioxide capture by aqueous monoethanolamine. Dissertation for the Master Degree. Texas: The University of Texas, 2006

[40] TRC. Selected Values of Properties of Chemical Compounds. Texas: Texas A&M University, College Station, 1980

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