CO2 capture in power plants: Minimization of the investment and operating cost of the post-combustion process using MEA aqueous solution

Mores, Patricia Liliana; Rodríguez, Néstor Eduardo Rodríguez; Scenna, Nicolás J.; Mussati, Sergio F.

doi:10.1016/j.ijggc.2012.06.002

Cited by 117 publications

(73 citation statements)

References 36 publications

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“…One of the proposed alternatives for amine solvent improvement considers the use of piperazine (PZ) activated amine and advanced formulated amines that consists of blend of different amine classes. These solvents are expected to combine the merits of each amine and they are characterized with superior absorption capacity and rate due to the addition of PZ activator [13][14][15]. Another remarkable development is the use of amines and room temperature ionic liquids…”

Section: Accepted Manuscriptmentioning

confidence: 99%

High-pressure absorption study of CO 2 in aqueous N -methyldiethanolamine (MDEA) and MDEA-piperazine (PZ)-1-butyl-3-methylimidazolium trifluoromethanesulfonate [bmim][OTf] hybrid solvents

Khan

Hailegiorgis

Man

et al. 2018

Journal of Molecular Liquids

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High-pressure absorption study of CO2 in aqueous N-methyldiethanolamine (MDEA) and MDEA-piperazine (PZ)-1-butyl-3-methylimidazolium trifluoromethanesulfonate [bmim][OTf] hybrid solvents. Abstract:In present study, high pressure CO2 absorption performance of aqueous N-methyldiethanolamine (MDEA) and its hybrid solvents with anhydrous piperazine (PZ) and ionic liquid (IL) 1-butyl-3-methylimidazolium trifluoromethanesulfonate [bmim][OTf] were investigated. The absorption performance of hybrid solvents were carried out to investigate CO2 loading capacity (mol of CO2/mol of solvent), and apparent absorption rate (CO2 capture efficiency, overall rate constant). The CO2 loading capacity of aqueous MDEA and its hybrid solvents were experimentally investigated for a wide range of compositions between pressure ranges of 2 to 50 bar and at three different temperatures (303.15, 313.15, and 333.15 K). Furthermore, apparent absorption rate performance of hybrid solvents were determined at 303.15 K temperature and 2 bar pressure. The effect of temperature, CO2 partial pressure, and ionic liquid (IL) concentrations on CO2 loading of aqueous IL-amines hybrid solvent were also investigated. The results indicated that CO2 loading of hybrid solvents were increased with ACCEPTED MANUSCRIPTA C C E P T E D M A N U S C R I P T 2 increase in CO2 partial pressure and IL concentration (up to 10 wt. %), further increased concentration of IL suppressed CO2 loading capacity. The CO2 loading capacity of hybrid solvents were also reduced with rise in system's temperature. The addition of IL and anhydrous PZ significantly enhanced CO2 capture efficiency (nCO2) and overall absorption rate constant (k) of aqueous MDEA solvent.

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Section: Accepted Manuscriptmentioning

confidence: 99%

High-pressure absorption study of CO 2 in aqueous N -methyldiethanolamine (MDEA) and MDEA-piperazine (PZ)-1-butyl-3-methylimidazolium trifluoromethanesulfonate [bmim][OTf] hybrid solvents

Khan

Hailegiorgis

Man

et al. 2018

Journal of Molecular Liquids

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“…The solution is then introduced in the stripper, where the weak chemical bonds between the CO 2 and the solution are broken by applying hot steam. Regeneration of the amine solution constitutes normally the highest energy penalty of the system; accounting for as much as 80% of the operational cost (Mores et al, 2012;Raynal et al, 2011). At the present time CCS has been successfully tested at pilot-plant scale (e.g.…”

Section: Introductionmentioning

confidence: 99%

Micro-scale CFD modeling of reactive mass transfer in falling liquid films within structured packing materials

Sebastia‐Saez

Ranganathan

et al. 2015

International Journal of Greenhouse Gas Control

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Post-combustion carbon capture in structured packing columns is considered as a promising technology to reduce greenhouse gas (GHG) emissions because of its maturity and the possibility of being retrofitted to existing power plants. CFD plays an important role in the optimization of this technology. However, due to the current computational capacity limitations, the simulations need to be divided into three scales (i.e. micro-, meso- and macro-scale) depending on the flow characteristics to be analyzed. This study presents a 3D micro-scale approach to describe the hydrodynamics and reactive mass transfer of the CO2-MEA chemical system within structured packing materials. Higbie's penetration theory is used to describe the mass transfer characteristics whereas enhancement factors are implemented to represent the gain in the absorption rate attributable to the chemical reaction. The results show a detrimental effect of the liquid load on the absorption rate via a decrease in the enhancement factor. The evolution of the wetted area for MEA solutions is compared to the case of pure water highlighting the differences in the transient behavior. The CO2 concentration profiles are examined showing the capability of the model to reproduce the depletion of the solute within the bulk liquid ascribed to the high value of the Hatta number. Also, several approaches on the reaction mechanism such as reversibility and instantaneous behavior are assessed. The results from micro-scale are to be used in meso-scale analysis in future studies to optimize the reactive absorption characteristics of structured packing materials

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“…The application of the here proposed model-based optimization approach has been successfully applied by the authors in other processes such as single-purpose seawater desalination plants [34][35][36], dual-purpose desalination plants [37,38], combined cycle power plants [39,40], amine-based CO 2 capture processes [41,42], biological wastewater treatment plants [43,44], real-time optimization in energy systems [45], liquid biofuel processors for H 2 production coupled to stationary fuel cells [46,47] and its associated heat exchanger network for optimal energy integration [48]. For instance, based on process models, this approach allowed to find a new cost-effective configuration for multi-stage flash desalination processes [35,36], which differ from the conventional configuration in the locations of distillate, recycle, and discharge streams.…”

Section: Sensitivity Of the Optimal Solution To The H 2 Product Puritmentioning

confidence: 99%

Optimal Design of a Two-Stage Membrane System for Hydrogen Separation in Refining Processes

Arias¹,

Scenna

et al. 2018

Processes

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This paper fits into the process system engineering field by addressing the optimization of a two-stage membrane system for H 2 separation in refinery processes. To this end, a nonlinear mathematical programming (NLP) model is developed to simultaneously optimize the size of each membrane stage (membrane area, heat transfer area, and installed power for compressors and vacuum pumps) and operating conditions (flow rates, pressures, temperatures, and compositions) to achieve desired target levels of H 2 product purity and H 2 recovery at a minimum total annual cost. Optimal configuration and process design are obtained from a model which embeds different operating modes and process configurations. For instance, the following candidate ways to create the driving force across the membrane are embedded: (a) compression of both feed and/or permeate streams, or (b) vacuum application in permeate streams, or (c) a combination of (a) and (b). In addition, the potential selection of an expansion turbine to recover energy from the retentate stream (energy recovery system) is also embedded. For a H 2 product purity of 0.90 and H 2 recovery of 90%, a minimum total annual cost of 1.764 M$·year −1 was obtained for treating 100 kmol·h −1 with 0.18, 0.16, 0.62, and 0.04 mole fraction of H 2 , CO, N 2 , CO 2 , respectively. The optimal solution selected a combination of compression and vacuum to create the driving force and removed the expansion turbine. Afterwards, this optimal solution was compared in terms of costs, process-unit sizes, and operating conditions to the following two sub-optimal solutions: (i) no vacuum in permeate stream is applied, and (ii) the expansion turbine is included into the process. The comparison showed that the latter (ii) has the highest total annual cost (TAC) value, which is around 7% higher than the former (i) and 24% higher than the found optimal solution. Finally, a sensitivity analysis to investigate the influence of the desired H 2 product purity and H 2 recovery is presented. Opposite cost-based trade-offs between total membrane area and total electric power were observed with the variations of these two model parameters. This paper contributes a valuable decision-support tool in the process system engineering field for designing, simulating, and optimizing membrane-based systems for H 2 separation in a particular industrial case; and the presented optimization results provide useful guidelines to assist in selecting the optimal configuration and operating mode.

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CO2 capture in power plants: Minimization of the investment and operating cost of the post-combustion process using MEA aqueous solution

Cited by 117 publications

References 36 publications

High-pressure absorption study of CO 2 in aqueous N -methyldiethanolamine (MDEA) and MDEA-piperazine (PZ)-1-butyl-3-methylimidazolium trifluoromethanesulfonate [bmim][OTf] hybrid solvents

High-pressure absorption study of CO 2 in aqueous N -methyldiethanolamine (MDEA) and MDEA-piperazine (PZ)-1-butyl-3-methylimidazolium trifluoromethanesulfonate [bmim][OTf] hybrid solvents

Micro-scale CFD modeling of reactive mass transfer in falling liquid films within structured packing materials

Optimal Design of a Two-Stage Membrane System for Hydrogen Separation in Refining Processes

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