## 1 Introduction  
Due tothe influence of greenhouse gases, in which CO2 is the major component, climate change is becoming gradually serious in the global world. Therefore, COP26 passed a resolution to control global warming below 1.5 \({}^{\circ}\)C before 2050 [1]. The emission amount of CO2 was about 35 Gt in 2022, and the baseline emission is estimated to be 57 Gt in 2050. To keep the temperature rise below 1.5 \({}^{\circ}\)C before 2050, the emission of CO2 needs to be maintained at 14 Gt; this means that a total amount of 43 Gt CO2 needs to be reduced. According to the roadmap of the International Energy Agency, the reduction contribution in CO2 emission using CCSU (Carbon Capture, Storage and Utilization) technology is at least 8 Gt. This shows that CCSU will be important in the coming 30-40 years. Recently, a Net-Zero-CO2 emission between 2040 and 2060 was also addressed through three routes: carbon capture and storage (CCS), carbon capture, and utilization (CCU), and the use of biomass grown and processed for the specific purpose of making chemicals (BIO) [2]. This impact was largely for some CO2 emissions sectors in the industry such as coal-fired plants, the petroleum industry, the cement industry, and the steel mill industry. To reduce CO2 emission, several technologies are used, such as absorption, adsorption, membrane separation, freezing technology, and chemical looping [3], in which absorption was found to be more effective in the CO\({}_{2}\) concentration range of 0-20% under 10 atm [4]. Recently, competing methods for the absorption and utilization of CO\({}_{2}\), such as the capture of CO\({}_{2}\) in molten salts, were reported in the literature [5; 6]. The method used molten salt CO\({}_{2}\) capture and an electrochemical transformation process to obtain carbon at the cathode and oxygen at the anode. In addition, synthesizing oxygen reduction reaction catalysts from CO\({}_{2}\), connecting the fields of carbon capture and fuel cell research was reported in the literature [7]. Generally speaking, a double-unit process including a combination of scrubber and stripper is required when using the absorption method, in which the alkanolamine solutions were proposed as the absorption solvents for CO\({}_{2}\) capture before 2030 [8; 9; 10; 11]. However, the capture cost in the stripping step in CCS is about 60-70%, making the selection of strippers and solvents pivotal. Due to this, several solvents have been adopted, such as amines [11; 12; 13; 14; 15], amino salts [16; 17], ammonia water [18; 19], sodium hydroxide [20], potassium carbonate [21], piperazines [22], ionic liquids, and physical solvents [10], with amines being the most popular solvents in these capture processes. The drawbacks of a single solvent, such as loading, corrosion rate, degradation rate, and regeneration energy, were improved by adopting new solvents, including mixed amines and non-aqueous solvents [23; 24; 25; 26; 27; 28]. There are four kinds of amines, basically classified as primary amines (such as monoethanolamine, MEA) [29; 30], secondary amines (such as diisopropanolamine, DIPA) [31; 32; 33], tertiary amines (such as triethanolamine, TEA) [34; 35; 36], and steric amine (such as 2-amino-2-methyl-1-propanol, AMP) [37; 38; 39]. Structurally, these amines have at least one hydroxyl group and one amino group, as shown in Figure 1. The presented hydroxyl group can reduce the vapor pressure, and the amino group can absorb acidic gases; therefore, it affects the physical properties of amines (Table 1). The vapor pressures at 20 \({}^{\circ}\)C for MEA, DIPA, and TEA are 64 Pa, 2 Pa, and 1 Pa, respectively. The vapor pressure of amine decreases with an increase in the -OH group. The loadings of various amines are affected by the functional groups. For instance, theoretically, the loading of MEA is limited stoichiometrically to 0.5 moles CO\({}_{2}\) per mole amine. However, the loading is higher for secondary and tertiary amines, with loadings of up to 1 mole of CO\({}_{2}\) per mole of amine.