Assessment of advanced solvent-based post-combustion CO2 capture processes using a bi-objective optimization technique

Kang, Charles A.; Brandt, Adam R.; Durlofsky, Louis J.; Jayaweera, Indira

doi:10.1016/j.apenergy.2016.07.062

Cited by 17 publications

(6 citation statements)

References 29 publications

(75 reference statements)

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“…MEA, monoethanolamine 47 ; KS-1, KS-1 TM solvent 48 ; Adv. sol., advanced solvents 49 ; Selexol, Selexol TM physical absorption process 50 ; Membr., membrane separation using selective carbon membrane 51 ; Hydrate, hydrate crystallisation CO 2 capture process 24 …”

Section: Resultsmentioning

confidence: 99%

Inherent potential of steelmaking to contribute to decarbonisation targets via industrial carbon capture and storage

et al. 2018

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Accounting for ~8% of annual global CO2 emissions, the iron and steel industry is expected to undertake the largest contribution to industrial decarbonisation. Despite the launch of several national and regional programmes for low-carbon steelmaking, the techno-economically feasible options are still lacking. Here, based on the carbon capture and storage (CCS) strategy, we propose a new decarbonisation concept which exploits the inherent potential of the iron and steel industry through calcium-looping lime production. We find that this concept allows steel mills to reach the 2050 decarbonisation target by 2030. Moreover, only this concept is revealed to exhibit a CO2 avoidance cost (12.5–15.8 €2010/t) lower than the projected CO2 trading price in 2020, whilst the other considered options are not expected to be economically feasible until 2030. We conclude that the proposed concept is the best available option for decarbonisation of this industrial sector in the mid- to long-term.

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Section: Resultsmentioning

confidence: 99%

Inherent potential of steelmaking to contribute to decarbonisation targets via industrial carbon capture and storage

et al. 2018

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“…For this reason, the plant configuration was examined prior the process analysis. In different works dealing with the design problem [6,7,9,19,[21][22][23]65], the authors considered the possibility of sending part of the water recovered in the condenser back to the column top as reflux. The reflux would enter the column at a considerably lower temperature compared to the stripper feed, and this would decrease the temperature in the top of the column, leading to necessity to use a higher duty to heat the cold water reflux.…”

Section: Stripper Analysis and Design Implicationsmentioning

confidence: 99%

“…In the field of Carbon Capture & Storage (CCS) technologies, the post-combustion capture using amine-based solvents is nowadays recognized as the most mature and promising process, as it is retrofittable in already existing plants [1][2][3][4]. The main drawback for its implementation, at an industrial scale, is represented by the high energy consumption [4][5][6][7][8][9][10]. The process consists in the coupling of two main sections: the absorption, where the CO2 is captured, and the stripping, where the solvent is regenerated.…”

Section: Introductionmentioning

confidence: 99%

Process analysis for the carbon dioxide chemical absorption–regeneration system

2018

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The process analysis for the post-combustion CO2 capture using amine-based solvents is nowadays a fundamental step in its industrial scale design. In this work, the absorption-solvent regeneration system is deeply analyzed for different values of the loading in the solvent entering the absorber. The importance of the temperature and composition column profiles is highlighted for both the columns. In particular, the tight connection between the profiles and the L/G ratio is found to influence the choice of solvent flow rate for what concerns the absorber. On the other hand, an alternative configuration for the stripper is proposed together with a new criterion for the evaluation of the packing height. Finally, it is found that, in order to minimize the energy consumption in the stripper, the rich solvent must be sent at the highest possible temperature, taking into account the limitations imposed by the minimum temperature approach in the cross heat-exchanger and the solvent degradation.

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“…Main challenges for industrial implementation of post-combustion CO2 capture are high energy requirement for regeneration, aerosol formation and degradation of the amine. Due to the high-energy penalty and aerosols emissions challenge for successful implementation of CO2 capture technologies, a great number of researchers are working in developing the new low-energy penalty solvents, aerosols emissions control, optimization and integration and scale-up of the process [2][3][4][5][6][7][8][9][10][11][12][13][14][15]. Rate-based models have been used for the simulation of CO2 absorption process.…”

Section: Introductionmentioning

confidence: 99%

“…Third order kinetic rate constant of MEA, m6 •kmol -2 •s -2kOH -Second order kinetic rate constant of CO2-OHreaction, m3 •kmol -1 •s -2…”

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confidence: 99%

Applicability of enhancement factor models for CO2 absorption into aqueous MEA solutions

et al. 2017

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In many chemical industrial processes, mass transfer across gas-liquid interfaces accompanied by chemical reaction is the governing phenomena. In case of mass transfer accompanied by a chemical reaction in the liquid phase, the reaction will enhance mass transfer and generally the mass transfer enhancement is quantified in terms of an enhancement factor. Large number of enhancement factor models have been developed in literature and used without critical analysis for analyzing pilot data for CO2 absorption into aqueous amines. In order to perform such a critical analysis, 24 models are tested using lab-scale experimental data from four independent apparatuses for CO2 absorption into MEA solutions covering a range of different conditions such as short and long contact times, with and without gas phase resistance, high and low CO2 loadings and temperatures. Of the 24 enhancement factor models tested only six models were found to satisfactorily predict the experimental CO2 fluxes. These were the models based on the simple pseudo-first order reaction assumption, Emodels 1, 2 and 3 by Hatta [2] and Dankwerts [4] respectively, Emodel 20, the deCoursey and Thring [44] model based on Danckwert's surface renewal theory with unequal diffusivities, Emodel 24, the recently published generalized model by Gaspar and Fosbøl [51] and Emodel 21, the Tufano et al. [67] model based surface renewal theory. All these models were found to work equally well to the discretized penetration model. No significant difference was found between Emodels 1, 2 and 3, indicating that whether one uses as basis a film, penetration or surface renewal model, is of insignificant importance. The success of the simple models is attributed to the short contact times in the experiments used as basis and the accuracy of the kinetic model. Contact times of the same magnitude between mixing points is also encountered in industrial packings and it is believed that the simple enhancement factor models may work well also in these cases if an accurate kinetic model is used.

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Assessment of advanced solvent-based post-combustion CO2 capture processes using a bi-objective optimization technique

Cited by 17 publications

References 29 publications

Inherent potential of steelmaking to contribute to decarbonisation targets via industrial carbon capture and storage

Inherent potential of steelmaking to contribute to decarbonisation targets via industrial carbon capture and storage

Process analysis for the carbon dioxide chemical absorption–regeneration system

Applicability of enhancement factor models for CO2 absorption into aqueous MEA solutions

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