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The current study aimed to investigate the CO2 absorption capacity of the aqueous alkanolamine, including primary, secondary, tertiary, and sterically hindered amines and polyamines, i.e., monoethanolamine (MEA), diethanolamine (DEA), triethanolamine (TEA) and 2-amino-2-methyl-1-propanol (AMP), tetraethylenepentamine (TEPA), triethylenetetramine (TETA), 3-(Methylamino)propylamine (MAPA), and diethylenetriamine (DETA) at 40, 60, and 80 °C at 1.1 bar. An increase in reaction temperature caused a decrement in CO2 loading across the board for all solvents. The trend of CO2 loading was TEA < MEA < DEA < AMP < MAPA < DETA < TETA < TEPA at 40 ºC, TEA < DEA < MEA < AMP < MAPA < DETA < TETA < TEPA, at 60 ºC and TEA < DEA < AMP < MEA < MAPA < DETA < TETA < TEPA at 80 ºC. The results indicated that TEPA has great potential to be utilized as an energy-efficient and non-corrosive solvent for CO2 capture since it has outperformed all other aqueous amine solvents in this present study. Furthermore, the CO2 loading of sterically hindered amine (AMP) at the same temperature was found to be higher than primary, secondary, and tertiary amines. Heat of absorption〖 (∆H〗_abs) was also determined to gauge the energy requirement to regenerate absorbents for cyclic loading from an economic viewpoint. DETA has the highest 〖∆H〗_abs = 84.48 kJ/mol. On the contrary, the long-chain tertiary amine TEA resulted in the least 〖∆H〗_abs = 40.21 kJ/mol, among all other solvents. Whereas the sterically hindered amine (AMP) was reported to possess mid-range 〖∆H〗_abs, i.e., 58.76 kJ/mol. Among all selected solvents, polyamines showed higher 〖∆H〗_abs than other conventional amines pertaining to the precedence of TEA<AMP<DEA< MEA<TETA<TEPA<MAPA<DETA.

aims: Optimize the process parameters for low concentration blended tri-solvent background: This experimental work has studied the effect of various operating factors (such as MEA/DEA/PZ concentration, temperature, operating pressure, agitation speed, and time) on absorption capacity from stored gas reservoir. As the current approach has a significant application to the bio-gas reservoirs to enhance the purity of CH4 and elimination of CO2 from the gas. The RSM has been used to model and optimize the CO2 capture process relating to low-pressure operating conditions. objective: Maximize rapid CO2 absorption method: The CO2 absorption was performed for the total solvent (5, 10, and 15 %v/v) under the temperature range of (20, 25, and 30 °C) having reservoir pressure (1.5, 2, and 2.5 bar). The fraction of DEA: MEA was restricted to (0.2, 0.5, and 0.8) with simultaneous loading of anhydrous PZ range from 0 to 2 gms; and agitation speed for step intervals of (300, 600, and 900 rpm). result: The relative error was found to be within ±1.93% and ± 2.25% for the initial absorption rate and CO2 absorption (at t=15 min.) respectively. According to this evidence, the process statistical model suits to be appropriate and accomplishes the goal of optimization. conclusion: The findings of the analysis of variance (ANOVA) illustrates good agreement between the experimental and statistical model confirming the potential of blended tri-solvent by aggressive initial rate of absorption and rapid CO2 absorption of 3.415 gm. CO2/min. & 17.779 gm. CO2 respectively. other: RSM has successfully optimised the CO2 absorption by blended tri-solvent (MEA/DEA/PZ) for stored gas reservoir. For the initial absorption rate and CO2 absorption (at t=15 min.), the experimental design, quadratic models, and regression analysis developed for these variables were found to be reasonably accurate and efficient in forecasting response values in a range of the variables, with a relative error of ±1.93% and ± 2.25%, respectively. The potential of blended tri-solvent to attain a very high degree of absorption in a relatively short amount of time was proved by the optimum value of initial absorption rate, which was calculated to be 3.415 gm. CO2/min. and rapid CO2 absorption, which was calculated to be 17.779 gm. CO2. The 3D surface plots have shed light on the interactive effects that the process parameters have on the CO2 absorption while the synergistic effects of MEA/DEA/PZ have been taken into consideration.

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