本研究以三酸甘油脂為原料，建立經由脂肪酸和脂類加氫處理（Hydroprocessed Esters and Fatty Acids, HEFA）途徑生產永續航空燃料（Sustainable Aviation Fuel, SAF）之製程模型，並比較不同SAF摻混比例目標下之製程表現。研究中使用 Aspen Plus 建立包含加氫脫氧、異構化／裂解與後續分離程序之穩態模型，並參考文獻動力學模型進行反應段驗證。後續結合MATLAB與模擬退火演算法，針對反應溫度、蒸餾塔塔板數、進料板位置、操作溫度與壓力等變數進行最佳化，以評估混合10%與混合50%兩種案例之操作條件、產品分布、物理性質與經濟表現。
結果顯示，混合10%案例因所需異構化程度較低，裂解反應較不明顯，因此反應段設備需求與年總成本較低，TAC約為967 kUSD/y；其SAF產量為320.27 kg/hr，質量產率為0.391，凝固點為−33.571°C。相較之下，混合50%案例需較深度異構化以滿足較高摻混比例需求，使SAF產量提升至380.436 kg/hr，質量產率提高至0.464，凝固點降低至 −46.497°C，但也伴隨較高裂解程度，使石油腦產量增加、柴油產量下降，並使TAC上升至約2648 kUSD/y。經濟分析結果顯示，雖然混合50%案例之設備成本較高，但因SAF產量較高，其最低售價低於混合10%案例，兩者分別為6.66與6.29USD/L。混合10%案例適合低投資與保留柴油餾分之生產策略；混合50%案例則較適合以提高SAF產率、改善低溫性質與降低單位產品成本為主要目標之製程策略。

Sustainable aviation fuel (SAF) is considered an important option for reducing greenhouse gas emissions from the aviation sector. Among the available SAF production pathways, hydroprocessed esters and fatty acids (HEFA) is one of the most mature technologies and can utilize triglyceride-based feedstocks such as vegetable oils, waste oils, animal fats, and microalgal lipids. In this study, a triglyceride-based HEFA process was developed in Aspen Plus to investigate SAF production under two blending targets, 10% and 50%. The process includes hydrodeoxygenation (HDO), hydroisomerization hydrocracking, and downstream separation. Literature-based kinetic models were implemented and validated before being applied to the process simulation. Sensitivity analysis was used to determine a suitable hydrogen feed ratio and reactor specifications. The separation section was first designed using DSTWU and then rigorously simulated using RadFrac. MATLAB was linked with Aspen Plus, and simulated annealing was applied to optimize the overall process based on total annual cost.The results showed that the optimal H₂-to-oil molar ratio for the HDO section was approximately 2.2. The 10% blending case achieved a SAF mass yield of about 39.1% with a TAC of approximately 967 kUSD/y, while the 50% blending case achieved a higher SAF mass yield of about 46.4% but required a higher TAC of approximately 2648 kUSD/y because of the more severe isomerization requirement. Despite the higher TAC, the 50% case achieved a lower estimated minimum selling price due to its higher SAF production rate. Overall, the two cases represent different process strategies depending on whether lower investment or higher SAF yield is prioritized.

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