臺灣博碩士論文加值系統

Luyben於2013年研究變壓蒸餾分離丙酮-氯仿之二元勻相最大共沸混合物，主要是利用壓力變化使其共沸點偏移，使高壓塔蒸餾出高純度的丙酮，低壓塔蒸餾出高純度的氯仿。為了處理不同於Luyben的進料濃度50 mol %之丙酮和50 mol %之氯仿，本研究將自行設計之進料濃度為25.25 mol %之丙酮和74.75 mol %之氯仿，由原本高壓塔進料位置移至低壓塔進料，此為低壓塔進料設計之研究，並探討高壓塔進料設計與低壓塔進料設計之高壓塔壓力變化與成本差距，此為壓力最適化研究。由於傳統蒸餾使用冷凝器和再沸器會耗費大量能源，以結合熱交換器之外部熱整合與熱泵輔助蒸餾設計之概念，進而取代傳統型冷凝器及再沸器，將多餘之熱能整合再利用，以達節省能源為目的。本研究使用Aspen Plus V8.8商業用軟體，在穩定狀態下UNIQUAC之熱力學模式進行模擬，將高壓塔進料設計與低壓塔進料設計之壓力最適化、外部熱整合、熱泵輔助蒸餾設計之模擬結果用APEA 進行經濟評估，將其總年成本與二氧化碳排放量進行比較。
模擬結果顯示，壓力最適化之11 atm傳統蒸餾塔相對於Luyben 10 atm傳統蒸餾塔，總年成本節省了每年336,800美元，約節省了3.4 %。外部熱整合設計相對於傳統蒸餾塔可以節省總年成本每年2,029,133美元，約節省了21.2 %，而熱泵輔助蒸餾設計之底部驟沸設計與蒸氣再壓縮設計較傳統蒸餾塔分別可以減少操作成本為每年3,425,480美元、每年1,690,700美元，大約減少43.8 %、21.7 %的操作成本，但熱泵輔助蒸餾設計的壓縮機設備成本太昂貴，導致底部驟沸與蒸氣再壓縮之總年成本較傳統塔為高。最後比較二氧化碳碳排放量，高壓塔進料設計之11 atm 外部熱整合系統，相較於Luyben的設計減少了每年2.249×107公斤二氧化碳，降低了約45.7 %。

Pressure swing distillation,which is separation of acetone-chloroform of binary homogeneous maximum azeotropic mixture that mainly use its azeotropic point shift when the pressure changed by Luyben’s study in 2013. High purity acetone is distillated with the high pressure column, and high purity chloroform is distillated with low pressure column. This study is designed with feed of concentration of 25.25 mol %- acetone and 74.75 mol %- chloroform in order to compare the different with Luyben's feed of concentration of 50 mol %- acetone and 50 mol %- chloroform. This is a design of low pressure tower feed study that feed of high pressure column position will change to the lower pressure tower. This is the pressure which optimized of the study that explored the high pressure column pressure changed and cost gap. The traditional distillation consumed a lot of energy because of it used of condensers and reboilers. To replace the traditional condenser and reboiler with the concept of external thermal integration and heat pump assisting distillation, combined with the use of excess heat energy for the purpose of saving energy, may lead to save more energy. In this study, the commercial software of Aspen Plus V8.8 was used. The thermodynamic model,UNIQUAC,was used as in a steady state. The results were economically evaluated using APEA to the design of high pressure column feed and the design of the low pressure column feed with the simulation of pressure which optimized , external thermal integration,heat pump assisted distillation design. Make to compare its total annual cost with carbon dioxide emissions.
The simulation result shows that the pressure-optimized conventional distillation tower compared to Luyben 10 atm conventional distillation towers will save the annual cost of $ 336,800 per year, will save about 3.4 %. The design of external thermal integration relative to the traditional distillation towers that can save the total annual cost of $ 2,029,133 per year, saving about 21.2%. While the heat pump assisted distillation design of the bottom flashing design and vapor recompression compared to conventional distillation towers can reduce operating costs per year $ 3,425,480, $ 1,690,700 per year, approximately 43.8%, 21.7% operating costs of reduction. However, the cost of the compressor equipment design of heat pump assisted distillation is too expensive that resulting in a higher total cost of bottom flashing and vapor recompression than the traditional tower. Finally,it’s comparing the carbon dioxide emissions which the design of high pressure tower feed of 11 atm external thermal integration system that compared to Luyben's design reduced by 2.249 × 107 kg of carbon dioxide per year, reduced by about 45.7%.

目錄
摘要 I
ABSTRACT II
致謝 IV
目錄 VI
圖目錄 XII
表目錄 XVI
符號表 XX
第一章 緒論 1
1-1前言 1
1-2文獻回顧 3
1-2-1 共沸混合物 3
1-2-2 變壓蒸餾 4
1-2-3 低壓塔進料設計 8
1-2-4 外部熱整合 10
1-2-5 熱泵 14
1-3研究動機與目的 19
1-4組織章節 20
第二章 原理與架構 21
2-1前言 21
2-2原理 21
2-2-1 共沸混合物 21
2-2-2 變壓蒸餾 26
2-2-3 外部熱整合設計 31
2-2-4 熱泵設計 33
2-2-5 蒸餾塔質量平衡 35
2-2-6 熱力學模式 38
2-3經濟估算公式 42
2-3-1 設備成本 42
2-3-1-1 蒸餾塔 43
2-3-1-2 再沸器 44
2-3-1-3 冷凝器 45
2-3-1-4 壓縮機 46
2-3-2 操作成本 46
2-3-2-1 冷卻水成本 46
2-3-2-2 蒸汽成本 47
2-3-2-3 電力成本 47
2-3-3 總年成本 (TAC) 47
2-4研究架構 47
第三章 二元勻相最大共沸混合物之熱整合設計與模擬 49
3-1 前言 49
3-2 Luyben 文獻設計與模擬 52
3-2-1 Luyben 傳統變壓蒸餾 52
3-2-2 Luyben 外部熱整合之模擬設計 54
3-3 高壓塔壓力最適化之高壓塔進料設計與低壓塔進料設計 56
3-3-1 傳統變壓蒸餾之高壓塔進料設計高壓塔壓力最適化 57
3-3-2 傳統變壓蒸餾之低壓塔進料設計高壓塔壓力最適化 59
3-4 外部熱整合設計之高壓塔進料設計與低壓塔進料設計 62
3-4-1 外部熱整合設計之高壓塔進料設計 62
3-4-2 外部熱整合設計之低壓塔進料設計 64
3-5 熱泵設計與模擬之高壓塔進料設計與低壓塔進料設計 67
3-5-1 熱泵輔助蒸餾設計之底部驟沸於高壓塔 68
3-5-2 熱泵輔助蒸餾設計之蒸氣再壓縮於低壓塔 74
3-5-3 熱泵輔助蒸餾設計之合併底部驟沸與蒸氣再壓縮設計 79
第四章 結果與討論 84
4-1 高壓塔壓力最適化之高壓塔進料設計與低壓塔進料設計 84
4-1-1 傳統變壓蒸餾之高壓塔進料設計之高壓塔壓力最適化 84
4-1-1-1傳統變壓蒸餾之高壓塔進料設計之高壓塔壓力最適化 85
設備成本 85
4-1-1-2 傳統變壓蒸餾之高壓塔進料設計之高壓塔壓力最適化
操作成本 86
4-1-1-3 傳統變壓蒸餾之高壓塔進料設計之高壓塔壓力最適化
總年成本 88
4-1-2 傳統變壓蒸餾之低壓塔進料設計之高壓塔壓力最適化 88
4-1-2-1 傳統變壓蒸餾之低壓塔進料設計之高壓塔壓力最適化
設備成本 89
4-1-2-2 傳統變壓蒸餾之低壓塔進料設計之高壓塔壓力最適化
操作成本 90
4-1-2-3 傳統變壓蒸餾之低壓塔進料設計之高壓塔壓力最適化
總年成本 91
4-2 外部熱整合設計之高壓塔進料設計與低壓塔進料設計 92
4-2-1 外部熱整合設計之高壓塔進料設計 92
4-2-1-1 外部熱整合設計之高壓塔進料設計設備成本 93
4-2-1-2 外部熱整合設計之高壓塔進料設計操作成本 94
4-2-1-3 外部熱整合設計之高壓塔進料設計總年成本 95
4-2-2 外部熱整合設計之低壓塔進料設計 96
4-2-2-1 外部熱整合設計之低壓塔進料設計設備成本 96
4-2-2-2 外部熱整合設計之低壓塔進料設計操作成本 97
4-2-2-3 外部熱整合設計之低壓塔進料設計總年成本 98
4-3 熱泵輔助蒸餾設計之高壓塔進料設計與低壓塔進料設計 99
4-3-1 熱泵輔助蒸餾設計之高壓塔進料設計 99
4-3-1-1 熱泵輔助蒸餾設計之高壓塔進料設計設備成本 100
4-3-1-2 熱泵輔助蒸餾設計之高壓塔進料設計操作成本 101
4-3-1-3 熱泵輔助蒸餾設計之高壓塔進料設計總年成本 103
4-3-2 熱泵輔助蒸餾設計之低壓塔進料設計 104
4-3-2-1 熱泵輔助蒸餾設計之低壓塔進料設計設備成本 104
4-3-2-2 熱泵輔助蒸餾設計之低壓塔進料設計操作成本 105
4-3-2-3 熱泵輔助蒸餾設計之低壓塔進料設計總年成本 106
4-4 二氧化碳排放量 121
第五章 結論與未來展望 126
5-1 總設備成本 126
5-2 總操作成本 128
5-3 總年成本 131
5-4 二氧化碳排放量 133
5-5 未來展望 133
參考文獻 136
自述與著作發表 140

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