## 2 Materials and Methods
### Reactivity Evaluation  
The catalytic activity was assessed in a fixed-bed reactor (I.D. = 10 mm). With each batch tested, 0.3 g of the prepared catalysts (40-60 mesh) was put at the center of a quartz reactor. Moreover, 1000 ppm of 1,2-DCE diluted in air with a flow rate of 300 mL/min was used as the inlet reaction stream, recalculated as a gas hourly space velocity (GHSV) of approximately 36,000 mL\(\cdot\)g\({}^{-1}\cdot\)h\({}^{-1}\). The concentration of 1,2-DCE and the organic by-products was measured using an online gas chromatograph (GC9890, China) equipped with an electron capture detector (ECD). The content of CO and CO\({}_{2}\) from the outlet gas flow was analyzed by an online gas chromatograph (GC9890A, China) equipped with a flame ionization detector (FID) and nickel converting equipment, similar to that reported by our group previously [38; 39; 40]. The 1,2-DCE conversion efficiency and the yield of CO and CO\({}_{2}\) were determined using the following equations:  
\[X_{1,2-\text{DCE}}=\frac{C_{\text{in}}-C_{\text{out}}}{C_{\text{in}}}\times 1 00\% \tag{1}\]  
\[Y_{\text{CO}}=\frac{C_{\text{CO}}}{2C_{\text{in}}\times X_{1,2-\text{DCE}}} \times 100\% \tag{2}\]  
\[Y_{\text{CO}_{2}}=\frac{C_{\text{CO}_{2}}}{2C_{\text{in}}\times X_{1,2-\text{ DCE}}}\times 100\% \tag{3}\]  
where \(C_{\text{in}}\), \(C_{\text{out}}\) are the 1,2-DCE concentration before and after the reaction, respectively, and \(C_{\text{CO}}\) and \(C_{\text{CO}_{2}}\) are the outlet consistent of CO and CO\({}_{2}\), respectively.  
The normalized reaction rate (\(r_{1,2-\text{DCE}}\), mmol\(\cdot\)g\({}^{-1}\cdot\)s\({}^{-1}\)) was derived using Equation (4):  
\[r_{1,2-\text{DCE}}=\frac{X_{1,2-\text{DCE}}\times V_{1,2-\text{DCE}}}{W_{\text {cat}}(wt\%\text{NM})} \tag{4}\]  
where \(W_{\text{cat}}\) is the amount of catalyst (g). \(wt\%\) NM is the weight ratio of noble metal in the catalyst (%), while V\({}_{1,2-\text{DCE}}\) is the 1,2-DCE gas flow rate (mol s\({}^{-1}\)).  
When the reaction efficiency of 1,2-DCE is below 15%, the reaction rate would be described as an alternative formula, as follows:  
\[r_{1,2-\text{DCE}}=A\exp(\frac{E_{a}}{RT})P_{1,2-\text{DCE}}^{\text{g}}P_{0_{ 2}} \tag{5}\]where \(E_{a}\) represents the apparent activation energy (J mol\({}^{-1}\)), \(R\) delegates the ideal gas constant (J mol\({}^{-1}\) K\({}^{-1}\)), \(T\) is the test temperature (K), \(P^{a}\) represents the fractional pressure of 1,2-DCE (Pa), and \(P^{\beta}\) is fractional pressure of O\({}_{2}\) (Pa).  
Activation energies were calculated at low temperatures for 1,2-DCE conversion efficiencies lower than 15%, which is determined by the Arrhenius relationship via Equation (5) simplified into Equation (6):  
\[\ln r=\frac{-E_{a}}{RT}+C \tag{6}\]  
The turnover frequency was calculated using the following equation:  
\[TOF=\frac{C_{\rm DCE}\times X_{i}\times v}{\frac{m_{NM}}{M_{NM}}\times D_{i}} \tag{7}\]  
where \(X_{\rm i}\) represents the 1,2-DCE conversion efficiencies of different catalysts at certain temperatures; \(C_{\rm DCE}\) is the feed concentration of 1,2-DCE (mol L\({}^{-1}\)), \(v\) is the volumetric flow rate (L s\({}^{-1}\)), \(M_{\rm NM}\) is the molecular weight of NM (g mol-1), \(m_{\rm NM}\) is the NM loading on the catalyst (g), and \(D_{\rm i}\) is the NM dispersion (%) on the catalyst surface obtained from the CO-chemisorption results.