## 3 Results
### Integration with Plate Reformer  
The integration of the plate reformer system with the burner is shown in Figures S3 and S7. Figure 6 shows the hydrogen production performance of the self-thermal methanol steam reforming microreactor, integrated with the clover plate burner, using different catalyst arrangements under various methanol flow rates (2-6 mL/min) at a fixed temperature of 250 \({}^{\circ}\)C. Compared with the 50/50 type (A type in the figure) design, the reaction chamber plate for the 30/70 type (C type in the figure) exhibited a better methanol steam reforming reaction performance. Especially compared with the 50/50 type, the 30/70 type not only increases the methanol conversion rate by 10.2%, but also increases the H2 flow rate by 10% at a methanol-water mixed injection rate of 6 mL/min and 250\({}^{\circ}\) operation temperature, while CO selectivity decreased by 1.7%. The results show that when the heat distribution \(\Delta\)T\({}_{\text{max}}\) of the burner plate is small (or more uniform), it is more conducive to improving the methanol steam reforming reaction efficiency of the SRM reformer.  
Figure 5: Temperature monitoring of the burners with different catalyst arrangements. (**a**) The locations for thermal couple measurements, and temperature measured results of burner startup process for, the colored dots in the figure represent the lines of the corresponding colors in subfigures (**b**)-(**d**); (**b**) 50/50 type; (**c**) 40/60 type; (**d**) 30/70 type; (**e**) the comparison of the maximum temperature differences \(\Delta\)T\({}_{\text{max}}\) among different burner types.  
Figure 6: Reaction performance of the ATMSR integrated with burners of different catalyst arrangements under various fueling rates (2, 4, and 6 mL/min of methanol solution). (**a**) Methanol conversion; (**b**) H\({}_{2}\) flow rate; (**c**) CO selectivity.  
Figure 7 shows the 30 h long-term performance of the ATMSR system integrated with the 30/70 type burner. After optimizing the heating system, it can be observed that it provides heat more evenly to the reformer for the reforming reaction, thus reducing the occurrence of local hotspots. When continuously supplying 4 mL/min of methanol solution for 30 h, the methanol conversion rate of the reformer decreased from an initial 97.1% to 92.3%, and hydrogen conversion rate of the burner decreased from 99.9% to 97.5%, providing a degradation rate of 0.16%/h and 0.08%/h for reformer and burner, respectively. This is much lower than our previous reformer systems containing similar catalysts and integrated with 50/50 type burner (reformers: ranging from 97 to 89.3%, burners: ranging from 98.6 to 95.6%) [22]. The hydrogen conversion rate of the burner system remained above 95% even after 30 h of continuous operation, demonstrating decent long-term performance.  
Figure 8 shows the particle agglomeration situations after long-term reactions with different catalyst arrangements in the combustor. As shown in Figure 8, the particle size of the catalyst at the front and back end of the 50/50 Type combustor reaction is 24.9 nm and 3. 0 nm, respectively, with more severe sintering and aggregation at the front end, but not much utilization of catalyst at the back end. However, for the 30/70 type combustor, the particle size of the catalyst at the front and back ends is 19.9 nm and 13.2 nm, respectively, demonstrating a more uniform catalyst preservation/utilization throughout the reaction channel for long term operation.  
Figure 7: Long-term HP performance of an ATMSR reactor integrated with a 30/70 type burner for 30 h reaction.