## 4 Case Studies and Process Description
\begin{table}
\begin{tabular}{c c c c c c c c c} \hline \hline
**Stream** & **Units** & **1** & **2** & **3** & **4** & **5** & **6** & **7** & **8** \\ \hline \(\hat{m}\) & kg/s & 16.88 & 16.90 & 1.31 & 18.20 & 1634.26 & 40.22 & 26.19 & 1586.00 \\ \(t\) & \({}^{\circ}\)C & 15.00 & 124.57 & 550.00 & 509.55 & 884.75 & 117.10 & 15.00 & 15.00 \\ \(p\) & bar & 10.00 & 29.00 & 29.50 & 26.70 & 6.50 & 50.00 & 10.00 & 1.01 \\ \(x_{H_{2}}\) & \% (mole) & 0.00 & 0.00 & 0.00 & 0.00 & 0.00 & 75.74 & 0.00 & 0.00 \\ \(x_{CO}\) & \% (mole) & 0.00 & 0.00 & 0.00 & 0.96 & 0.00 & 15.59 & 0.00 & 0.00 \\ \(x_{CO_{2}}\) & \% (mole) & 0.70 & 0.72 & 0.00 & 0.68 & 3.68 & 7.60 & 0.70 & 0.00 \\ \(x_{CH_{4}}\) & \% (mole) & 94.90 & 94.81 & 0.00 & 91.17 & 0.00 & 0.69 & 94.90 & 0.00 \\ \(x_{Hb_{0}}\) & \% (mole) & 0.00 & 0.08 & 100.00 & 5.74 & 7.62 & 0.00 & 0.00 & 0.00 \\ \(x_{CH_{5}OH}\) & \% (mole) & 0.00 & 0.00 & 0.00 & 0.00 & 0.00 & 0.00 & 0.00 \\ \(e\) & MJ/kg & 49.66 & 49.79 & 1.49 & 46.85 & 0.73 & 25.07 & 49.66 & 0.00 \\ \hline
**Stream** & **Units** & **9** & **10** & **11** & **12** & **13** & **14** & **15** & **16** \\ \hline \(\hat{m}\) & kg/s & 13.50 & 351.62 & 351.62 & 276.06 & 2.40 & 58.62 & 31.32 & 1630.63 \\ \(t\) & \({}^{\circ}\)C & 45.00 & 250.00 & 38.00 & 38.52 & 38.00 & 38.00 & 70.97 & 100.00 \\ \(p\) & bar & 50.00 & 50.00 & 49.30 & 48.50 & 2.00 & 2.00 & 1.30 & 4.80 \\ \(x_{H_{2}}\) & \% (mole) & 0.00 & 67.99 & 63.84 & 69.46 & 3.03 & 0.00 & 0.00 & 0.00 \\ \(x_{CO}\) & \% (mole) & 0.00 & 10.18 & 8.81 & 9.58 & 0.99 & 0.00 & 0.00 & 0.00 \\ \(x_{CO}\) & \% (mole) & 100.00 & 15.88 & 15.40 & 16.50 & 81.24 & 0.65 & 0.00 & 3.67 \\ \(x_{CH_{4}}\) & \% (mole) & 0.00 & 2.09 & 2.25 & 2.45 & 1.33 & 0.00 & 0.00 & 0.00 \\ \(x_{H_{2}O}\) & \% (mole) & 0.00 & 0.05 & 1.75 & 0.05 & 0.95 & 21.65 & 0.08 & 7.55 \\ \(x_{CH_{5}OH}\) & \% (mole) & 0.00 & 2.65 & 6.70 & 0.62 & 12.08 & 77.69 & 99.92 & 0.00 \\ \(e\) & MJ/kg & 0.65 & 18.64 & 18.34 & 18.30 & 3.10 & 19.20 & 22.42 & 0.17 \\ \hline \end{tabular}
\end{table} 
Table 3: Stream data of the methanol plant with steam–methane reforming (Case I). Figure 3: Process flow sheet of the methanol plant with steam–methane reforming (Case I). Thereby, the configuration avoids the need for natural gas as a fuel. Additional heat is provided to the heat recovery steam generator by the combustion of a purge stream (stream 12) in R-07. The integration of the ATR reduces the load and the size of the SMR with a low S/C-ratio of 0.5. The conversion is completed by combustion with 45 kg/s oxygen (stream 15). The resulting syngas composition is in the range of high methanol yield in Figure 2--the H\({}_{2}\)/CO-ratio is 2.1 and the mole fraction of carbon dioxide is low (stream 6). Downstream, water is rejected in drum D-01 to shift the composition to the product side of WGS reaction and to initiate the reverse water gas shift reaction (RWGS). Accordingly, the small excess of hydrogen reacts with carbon dioxide to increase the carbon monoxide content. The application of a further syngas conditioning unit results in a methanol yield of 10.4 mole-% and an RTFR of 2.13. A stream of 55.1 kg/s methanol is produced corresponding to a methane intensity of 1.23 kgCH3 OH/kgCH4.