## 1 Introduction
During the thermal step, H\({}_{2}\)S is brought into contact with air at a temperature between 1400 and 1600 K. One-third of the H\({}_{2}\)S undergoes partial oxidation and is converted into SO\({}_{2}\):  
\[H_{2}S+3/2O_{2}\to SO_{2}+H_{2}O \tag{4}\]  
The products of the thermal step are then cooled to \(\sim\)400 K. During the catalytic step, the remaining H\({}_{2}\)S and SO\({}_{2}\) react at temperatures between 460 and 650 K and in the presence of a catalyst, which can be an aluminum or titanium oxide, to form solid sulfur in its S\({}_{8}\) form:  
\[2\ H_{2}S+SO_{2}\to 3/8S_{8} \tag{5}\]  
Downstream, the Claus unit is a tail gas treatment unit (TGTU), which removes the remaining sulfur compounds. Despite being the most competitive process today, there are some significant drawbacks to the acid gas removal process with aqueous amines, namely the solvent regeneration step consumes a lot of energy (if thermal integration is not possible); the high regeneration temperatures tend to degrade the amine, resulting in performance and solvent losses; and there are corrosion issues. Because there is currently no solvent that is ultra-selective with respect to H\({}_{2}\)S at high pressure, the CO\({}_{2}\) is simultaneously captured. Therefore, in the H\({}_{2}\)S conversion process, the CO\({}_{2}\) also goes through the Claus units, resulting in larger units and higher energy consumption. Moreover, if one wants to capture this CO\({}_{2}\) for storage or reuse (today, the CO\({}_{2}\) is most often sent to the atmosphere), one needs to add a second AGRU downstream the Claus unit. This is shown in Figure 1A. The team of [PERSON] et al. [11; 12; 13; 14; 15; 16; 17; 18; 19; 20] at MIT developed a post-combustion CO\({}_{2}\) capture scheme with an electrochemistry mediated aqueous amine regeneration (EMAR). Here, instead of thermally regenerating the solvent to capture CO\({}_{2}\), electrochemistry is used. In the electrochemical cell, the CO\({}_{2}\) is detached from the carbamate over a copper anode. An amine-Cu complex is formed, and the amine is regenerated over the cathode. The Cu- and CO\({}_{2}\)-rich stream is sent from the anode to a flash tank to separate the CO\({}_{2}\) from the Cu-rich stream, which is recycled to the cathode. The advantage of this early-stage technology is that the regeneration does not require heating and steam, thereby potentially reducing degradation of the amine. Moreover, it might take place at higher pressure, thus avoiding repressurization of the CO\({}_{2}\) for reuse or storage. The main challenges are the overpotential intrinsic to electrochemical systems, efficiency losses due to ion migration, and a stable cyclic operation. The feasibility of the technology has been demonstrated with a continuous bench scale EMAR unit. In this paper, we present a theoretical process adapted from the work of [PERSON] et al. to capture CO\({}_{2}\) from gas when H\({}_{2}\)S is also present. The technology is also suitable for CO\({}_{2}\) removal from gases in the absence of H\({}_{2}\)S. The key idea of this work is to regenerate the solvent in an electrochemical cell, namely, to desorb CO\({}_{2}\) and H\({}_{2}\)S so that the solvent can be recycled back to the absorption column and CO\({}_{2}\) and H\({}_{2}\)S can be separated simultaneously. This is shown in Figure 1B. Moreover, the H\({}_{2}\)S is converted into H\({}_{2}\) and solid S during this process. Hence, the electrochemical regeneration cell replaces both the thermal regeneration column of the first AGRU as well as the Claus unit, the TGTU unit, the second AGRU, and the incineration unit.