Extended Data Fig. 2: Comparison in catalytic performances of the FL-MoS₂ and the Cu/ZnO/Al₂O₃ (CuZnAl) and other catalysts.

a, Comparison in net STY_methanol over the Cu/ZnO/Al₂O₃ (CuZnAl) and the FL-MoS₂ at 60 bar (Supplementary Table 1 for more details, ^# represents data of this work). b, Comparison in the forward TOF for methanol formation (calculated on the basis of the amount of exposed Cu, Mo or Sv sites) over the Cu/ZnO/Al₂O₃ (CuZnAl) and the FL-MoS₂ at 50 bar and iso-conversion levels. It was reported that for the Cu/ZnO/Al₂O₃ catalyst only small fractions of surface synergetic sites are considered to be highly active for the CO₂ conversion.^{25,26,27,28,29,30} However, the real high-active sites can hardly be precisely quantified in the actual systems owing to the difficulty in identifying them based on the currently reported characterization techniques. Thus, in the calculation of the TOF, all surface Cu atoms are included in the amount of the active sites, as typically done in previous works^{74,75,76,77,78}. The TOF on the Cu/ZnO/Al₂O₃ catalyst calculated in this way should represent an average activity level of the active sites^31,79. c, Comparison in the net TOF for methanol formation over the FL-MoS₂ and other state-of-the-art catalysts calculated on the basis of the amount of exposed metal (Supplementary Table 2 for more details, the order of catalysts in (c) corresponding to that in Supplementary Table 2). Reaction activity tests of the FL-MoS₂ were performed at 50 bar with a GHSV of 36000 mL g_cat.⁻¹ h⁻¹. d, The catalytic performances of the Cu/ZnO/Al₂O₃ (CuZnAl) and the FL-MoS₂ under identical reaction conditions, which were tested at 180 °C, 50 bar and 3000 mL g_cat.⁻¹ h⁻¹. e, Selectivity to methanol as a function of CO₂ conversion over the FL-MoS₂ and the Cu/ZnO/Al₂O₃ (CuZnAl) obtained by varying the GHSV in the range of 3000 to 36000 mL g_cat.⁻¹ h⁻¹ at 50 bar and different temperatures. Catalysts were pretreated in-situ by H₂ at 300 °C for 3 hours. Reaction activity tests were performed using a tubular fixed-bed reactor with a H₂/CO₂ ratio of 3. TOFs of the FL-MoS₂ were calculated on the basis of NO adsorption capacities.