numerous studies have focused on developing reaction schemes for the isomerization of this series, as well as kinetic modeling to replicate experimental or plant data. In refineries, the typical operating conditions for the isomerization process depend on the catalyst and reactor design, with temperatures ranging from 120 to 300 \({}^{\circ}\)C and pressures between 20 and 30 bar [7; 8; 9; 10; 11; 12; 13; 14; 15; 16; 17], which determine whether the reaction occurs in the vapor phase, liquid phase, or a vapor-liquid mixture [17]. The reactions in the isomerization process are governed by chemical equilibrium, which imposes a limit on the conversion of reactants into products, with temperature being the main controlling variable. Increasing the temperature can enhance conversion; however, once the equilibrium composition is reached, no further isomerization occurs. Instead, the reaction shifts, favoring the reverse process, where product reconversion into reactants becomes dominant [7; 8]. Several authors have conducted experimental studies on the isomerization of the C\({}_{6}\) fraction to gain a deeper understanding of the process and establish the most suitable reaction scheme to describe it, using various catalysts [7; 8; 9; 10; 11; 12; 13; 14; 15; 16]. Authors such as [PERSON] et al. [9] and [PERSON] et al. [10] agree on a reaction scheme consisting of four reversible reactions, despite using different catalysts in their experimental studies. [PERSON] et al. [6] proposed a reaction scheme, based on their experimental study, that includes four reversible and three irreversible reactions, despite the generally reversible nature of isomerization reactions. Multiple experimental studies have employed reaction schemes from the literature to model their data, validating and comparing their results with already established theoretical models. For instance, [PERSON] et al. [11], [PERSON] et al. [12], and [PERSON] et al. [13] used reaction schemes consisting of two, four, and five reversible reactions, respectively, in their investigations on the isomerization of the C\({}_{6}\) series. In modeling the industrial isomerization process, reaction schemes can be adapted to different cases. For instance, [PERSON] et al. [7] utilized the reaction scheme proposed by [PERSON] et al. [14], which consists of five reversible reactions applied to distinct industrial processes. Similarly, [PERSON] et al. [15] adopted the scheme of [PERSON] et al. [16], which comprises 16 irreversible reactions, to adjust the plant reactors used in the industrial case presented by the latter. Although the studies mentioned [6; 7; 9; 10; 11; 12; 13; 14] initially consider the reaction schemes for the C6 fraction as reversible, in the solution of kinetic models, these reactions are often treated as irreversible, as is the case in the works of [PERSON] et al. [15] and [PERSON] et al. [16]. For their part, [PERSON] et al. [8] considered the reversible nature both in the model and its solution, using a scheme of four reactions. However, their study lacks a detailed analysis of the impact of chemical equilibrium on the reaction kinetics, which limits a comprehensive understanding of the process. Despite the diversity of reaction schemes available in the literature for the C\({}_{6}\) series and their application in numerous studies, to our knowledge, it has not been assessed whether they lead to virtually identical predictions in the isomerization process. This lack of comparison raises the question of whether certain schemes are more suitable than others for modeling the C\({}_{6}\) series. Based on this approach, a comparative study was conducted on eight reaction schemes for the C\({}_{6}\) series: five extracted from the literature, two derived from these by eliminating redundant reactions, and the one proposed. These schemes were evaluated through the modeling of the case study presented by [PERSON] et al. [15].