臺灣博碩士論文加值系統

本研究主要探討丁酸乙酯反應蒸餾製程之可行性，設計目標為年產3000公噸的丁酸乙酯，採丁酸與乙醇酯化之連續式反應蒸餾製程。研究方式為利用商用模擬軟體AspenPlus來進行反應蒸餾製程之模擬分析。
丁酸乙酯反應蒸餾之製程可分為兩類，製程1為反應物由反應蒸餾塔進料，酯化產物分別由反應蒸餾塔之塔底與塔頂取出；製程2 則是反應物完全由塔底進料，所有產物由塔頂餾出，冷凝後經沉降槽分為有機相與水相產物。本研究首先探討反應蒸餾塔之最佳設計參數，然後進行製程之設備成本與能源成本分析。
比較製程1與製程2之成本，製程1的設備成本較高但是能源成本較低，總年成本則是製程1最低。就經濟評估之結果而言，製程1之總年成本較製程2約低8.7%。但是製程2之反應完全在塔底(反應釜)，製程較簡單，不需複雜之反應板，操作維修較容易。整體而言，就製程之簡單性考慮，製程2是不錯之選擇。

The purpose of this work is to study the process of synthesizing ethyl butyrate 3000 ton annually, by continuous reactive distillation. The commercial simulation software Aspen Plus® is used in this study.
Two processes are proposed. The first process (Process 1) is utilizing one single reactive distillation column, where two feeds are fed into the middle reaction section of the column and two products are withdrawn from the top and bottom of the column. The second process (Process 2) consists of two columns, where one is the main reactive distillation column and another is a stripper. The acid and alcohol feeds are fed into the bottom of the reactive distillation column and all products are withdrawn from top. The distillate is condensed into a decanter. The aqueous phase product is recycled into reactive distillation column and organic phase product is fed into the stripper to get the desired ethyl butyrate.
The analysis results show that the total annual cost of Process 1 is lower than Process 2 about by 8.7%, though the equipment cost of process 1 is higher but the energy cost is lower than Process 1. However, by considering the simplicity of the process, maintenance and operability, the process 2 is a good consideration.

第一章前言
1.1反應蒸餾
1.2酯化反應之反應蒸餾製程
1.3研究目的
第二章熱力學與動力學模式
2.1熱力學模式
2.1.1NRTL模式與參數
2.1.1氣液平衡
2.1.2液液平衡
2.2動力學模式
第三章反應蒸餾塔模擬設計
3.1反應蒸餾製程1
3.1.1乙醇進料位置之影響
3.1.2丁酸進料位置之影響
3.1.3精餾段與汽提段之影響
3.1.4反應段之影響
3.1.5 反應蒸餾製程1設計參數
3.2反應蒸餾製程2
3.2.1水相回流之效應
3.2.2 反應蒸餾製程2-1
3.2.3 反應蒸餾製程2-2
第四章結果與討論
4.1 成本分析
4.1.1設備成本估算
4.1.2能源成本估算
4-2 經濟評估結果
第五章結論
參考文獻
附錄A 計算年度總成本之公式

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