High-Pressure Vapor–Liquid Equilibrium Measurement of CO₂ Solubility into Aqueous Solvents of (Diisopropylamine + L-Lysine) and (Diisopropylamine + Piperazine + L-Lysine) at Different Temperatures and Compositions

Abstract

The new experimental vapor−liquid equilibrium data for CO 2 solubility into two different combinations of alkanolamine + amino acid, alkanolamine + chemical additive, and one aqueous alkanolamine were attained at 328.15, 343.15, and 363.15 K and in the CO 2 partial pressure range from 40 to 3800 kPa. The measurements are performed for the mixture of diisopropylamine (DIPA) + L-lysine with the compositions of (37.5−2.19) wt %, (35.0−4.38) wt %, and (30−8.77) wt %, and a blend of DIPA + piperazine (PZ) + L-lysine with the compositions (30.0−7.5−2.19) wt % and (30.0−5−4.38) wt %. Besides, the CO 2 partial pressure against its loading was acquired for the aqueous systems of DIPA + PZ (30.0−10.0) wt % and DIPA (40.0) wt %. The results illustrate that the CO 2 loading in the solvents was enlarged with declining temperature and increasing pressure. For the system of DIPA (40.0) wt %, it was deduced that CO 2 solubility improves by substituting the 10 wt % of DIPA with PZ. In other comparisons, we found that, at a constant weight percentage of L-lysine and water and total alkanolamines, the degree of selectivity toward CO 2 solubility is as follows: DIPA + PZ + L-lysine + H 2 O > DIPA + L-lysine + H 2 O. Accordingly, the ability of PZ to remove CO 2 is more than DIPA. Besides, a quadratic equation is employed to correlate the CO 2 partial pressure versus its loading so that the calculated values reveal a great agreement with the experimental data. Lastly, the Clausius−Clapeyron equation is applied to compute and compare the enthalpy of CO 2 absorption for the current systems. We found that, among the utilized solvents, the aqueous systems of DIPA + L-lysine + water (30−10−60) wt % and DIPA+ water (40.0-60.0) wt % have the maximum and minimum heats of absorption, respectively.

Modeling CO2 solubility in water using gradient boosting and light gradient boosting machine

“…They determined Henry's constant by fitting the experimental CO 2 solubility in pure water at the same pressure and temperature range. Moreover, multiple thermodynamic models of CO 2 solubility have been constructed based on various pressures, temperatures, and water salinity conditions 25 , 35 , 36 . Table 2 provides an informative summary of theoretical models found in the literature.…”

Physicochemical Properties and Applications of Deep Eutectic Solvents for CO2 Capture

“…Furthermore, greenhouse gases are a significant by-product of fossil fuel combustion. CO 2 is a major pollutant responsible for more than 60 % of greenhouse gas emissions, which contribute to global warming [3]. For these reasons, carbon sequestration and storage methods have been studied in recent decades.…”

The Ratio of Chemical and Physical CO2 Absorption Capacity in Triethanolamine and Methyl-diethanolamine Solution Systems

“…Recently, in response to climate change, researchers have reported on many carbon capture and storage (CCS) technologies intended for practical use. − Among them, the chemical absorption process using amine-based solutions as the solvent has been commercialized due to its advantages such as its relatively high economic feasibility and fast reaction rate. − Monoethanolamine (MEA), one of the primary amines, reacts directly with CO 2 to generate protonated amine and carbamate ions, and it is currently considered to be the most optimum solvent for chemical absorption because of its high absorption rate and low solvent price; therefore, several CCS plants employing MEA as the solvent have been commercially operated in the USA, Canada, and China. − However, MEA aqueous systems can still be improved upon; for example, they can be made more economical by improving their utilization limit (lower than 0.5 mol of CO 2 /mol of MEA in a high-concentration solution) and substantial energy consumption for solvent regeneration. Therefore, some MEA–organic solvent (water-free or water-lean) systems using monoethylene glycol, methanol, acetone, and tetrahydrofurfuryl alcohol as the organics are an alternative to enhance the amine utilization increasing the physical absorption capacity of the systems. − …”