Feasibility study, simulation and economical evaluation of natural gas sweetening processes – Part 1: A case study on a low capacity plant in iran

Oxidative Absorption of Hydrogen Sulfide by Iron-Containing Ionic Liquids

“…As has been discussed in Figure 2 and Figure Meanwhile, it was sure that the absorbed H 2 S was all oxidized by iron-containing ionic liquids at M=0.4-2 due to a fast chemical reaction between H 2 S and Fe 3+ . 19,20 Especially for M=0.3 and pH=2.78, the measured concentration of H 2 S is greater than the theoretical value, which demonstrates that only physical absorption of H 2 S also exists in ionic liquids even at 333.15 K and available iron(III) has been depleted which is also confirmed by Raman spectra of Figure 6 below. So, it was possible that the oxidative 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60 11 the acidity was the leading factor controlling the H 2 S oxidation in the studied ionic liquids at pH<2.78, whereas the iron(III) concentration was the major influence at pH≥2.78.…”

“…concentration varied with temperature due to the decrease of hydrogen sulfide solubility in ionic liquids with the increase of temperature 20,[26][27][28][29][30]. Based on these results, it was clear that an optimal iron(III) ionic liquids system should possess high Fe 3+ and low pH at low temperature, while lower Fe 3+ and higher pH were suitable when the temperature increased, in order to have the largest utilization of Fe 3+ .…”

Economic analysis of microaerobic removal of H2S from biogas in full-scale sludge digesters

“…Obviously, any other specific equipment required to implement the aforementioned technologies would increase the investment cost. Kazemi et al (2014) performed a simulation in order to calculate the cost arising from the implementation of four different commercial alternatives for H 2 S removal in a plant treating sour in Iran: the mixed amine, Sulfinol-M, Chelated iron (LO CAT), and Shell Paques processes. By applying Eq.…”

“…Nevertheless, and although the operating cost in ISF included only the expense on the iron-sponge, the operating cost of MA O2 was lower than that of the ISF scenario (18,277 against 23,322 €/yr, or equivalently, 0.0039 against 0.0049 €/m 3 biogas). The operating cost of the different alternatives for H 2 S removal considered by Kazemi et al (2014) and Abatzoglou and Boivin (2009) was estimated with Eq. (4).…”

Conceptual design of a new SF6 abatement technology using a multi‐bed series reactor for the production of valuable chemicals free of toxic wastes

“…In addition, the Peng–Robinson fluid property package was opted as an appropriate equation of state and a steady‐state condition was assumed. Since thermodynamic properties of some components (SF 6 , SO 3 , CaO, CaF 2 , and CaSO 4 ) are not in the component library of Aspen HYSYS ® , hypothetical components were created using some important thermodynamic properties of each component like molecular weight, normal boiling point, and ideal liquid density . In particular, thermodynamic properties for the utilized adsorbent, CaO with molecular weight of 56.08 g mol −1 , normal boiling point of 3123 K, and ideal liquid density of 3,340 kg m −3 were used in this study.…”