# No-CH4-SCR Over Core-Shell MnH-Zeolite Composites
## 2 Materials and Methods
### Catalytic Activity Measurements  
The NO-CH\({}_{4}\)-SCR test was carried out in a fixed-bed micro-reactor system consisting of a 6 mm I.D. quartz reactor tube, a temperature controller with K mode thermoelectric couple, four mass flowing controllers, and a gas chromatograph (GC 9A) equipped with a TCD. The catalyst samples were palletized, crushed, and sieved to 40-60 mesh for the catalytic tests. The 0.3 g particular catalyst was packed into the micro-reactor and pretreated in He flow (40 mL-min\({}^{-1}\)) at a ramp of 1 K-min\({}^{-1}\) from room temperature to 673 K and kept for 1 h. Then, the sample was cooled down to 473-573 K and \begin{table}
\begin{tabular}{c c c c c c c c c c} \hline \multirow{2}{*}{**Catalyst**} & \multirow{2}{*}{**Si/Al**} & \multicolumn{4}{c}{**Ion-Exchange Condition 1** **} & & \multirow{2}{*}{**Mn**} & \multirow{2}{*}{**Mn/Al**} & \multirow{2}{*}{**S\({}_{\text{SET}}\)**} \\  & & & & & & & & & **(m\({}^{2}\)g\({}^{-1}\))** \\ \hline MnH-Y & 2.0 & 353 & 0.01 & 20 & 24 & 3 & 2.55 & 0.12 & 576 \\ MnH-Beta & 15.0 & 353 & 0.01 & 20 & 24 & 3 & 2.12 & 0.38 & 405 \\ H-ZZs-0.5 & 12.2 & 353 & — & — & — & — & 0 & 0 & 420 \\ MnNa-ZZs-0.5 & 12.2 & 353 & 0.01 & 20 & 24 & 3 & 2.07 & 0.37 & 428 \\ MnH-ZZs-1.0 & 10.8 & 353 & 0.01 & 20 & 24 & 3 & 2.27 & 0.31 & 379 \\ MnH-ZZs-0.5 & 12.2 & 353 & 0.01 & 20 & 24 & 3 & 2.15 & 0.38 & 359 \\ MnH-ZZs-0.3 & 13.1 & 353 & 0.01 & 20 & 24 & 3 & 2.16 & 0.38 & 365 \\ MnH-ZZs-0.2 & 14.5 & 353 & 0.01 & 20 & 24 & 3 & 2.23 & 0.39 & 363 \\ MnH-ZZs-0.5-1 & 12.2 & 353 & 0.01 & 20 & 24 & 2 & 1.82 & 0.32 & 359 \\ MnH-ZZs-0.5-2 & 12.2 & 353 & 0.01 & 20 & 24 & 1 & 1.27 & 0.25 & 356 \\ MnH-ZZs-0.5-3 & 12.2 & 353 & 0.008 & 20 & 24 & 1 & 0.92 & 0.17 & 354 \\ \hline \end{tabular}
\end{table} 
Table 1: Preparation catalyst and the selected physical properties. the reaction mixture containing 2180 ppm NO, 2050 ppm CH\({}_{4}\), 2% O\({}_{2}\), balanced by He flowed through the catalyst at 75 mL\(\cdot\)min\({}^{-1}\) (GHSV 7500 h\({}^{-1}\) by assuming the bulk density of the catalyst 0.5 g\(\cdot\)cm\({}^{-3}\)). Under oxidizing conditions, sulfur compounds end up mainly as SO\({}_{2}\); therefore, SO\({}_{2}\) was chosen as model sulfur compound. For reactions involving SO\({}_{2}\), a reactor with two-inlets was used to minimize contamination of the system by SO\({}_{2}\) exposure. SO\({}_{2}\)/He (294 ppm) was added to the reactor via a separate inlet. The final concentration in the feed was 78 ppm. Water vapor was added to the feed using an H\({}_{2}\)O saturator comprised of a sealed glass bubbler with a medium-pore frit immersed in distilled water. Helium (20 mL\(\cdot\)min\({}^{-1}\)) flowed through the bubbler, carrying H\({}_{2}\)O vapor to the feed. The bubbler was placed in a constant temperature tank. Different amounts of H\({}_{2}\)O vapor could be added to the feed by adjusting temperature of the bubbler. The gas line containing H\({}_{2}\)O vapor was heated traced to a temperature higher than the saturation temperature. An ice-cooled H\({}_{2}\)O condenser was incorporated downstream of the reactor before effluent gas entering gas chromatograph. The compositions of the effluent gas were analyzed by using the GC with molecular sieve-5A column for N\({}_{2}\), O\({}_{2}\), CH\({}_{4}\), CO, and Porapak Q column for CO\({}_{2}\) and N\({}_{2}\)O. Negligible N\({}_{2}\)O was formed in the effluent gas. NO and NO\({}_{2}\) were quantified by using a flue gas analyzer ([PERSON], UK). The catalytic activity was evaluated based on the NO to N\({}_{2}\) conversion C\({}_{\rm NO}\): C\({}_{\rm NO}\) = 2 \(\times\) ([N\({}_{2}\)]\({}^{\rm o}\)/[NO]\({}^{\rm i}\)) \(\times\) 100% where [N\({}_{2}\)]\({}^{\rm o}\) and [NO]\({}^{\rm i}\) represent concentration of outlet N\({}_{2}\) and inlet NO, respectively.