氣隔式薄膜蒸餾(air gap membrane distillation)原理乃是利用薄膜兩側之飽和蒸汽壓差為驅動力促使水蒸氣通過薄膜及其氣隔層後，在冷凝板上冷凝，進而達到分離的效果，然而，溫度極化對於系統產能會有相當顯著的影響。本研究針對氣隔式薄膜蒸餾之主要設備進行效率改善的研究，目標為：(1)設計新型紊流促進因子(Eddy promoter)，以有效的改善系統內部之溫度極化現象進而提升系統產能，並歸納出一納賽數經驗公式，描述紊流促進因子對於通道內部熱對流效應的影響；(2)藉由一維數學模型針對薄膜蒸餾設備的熱量與質量傳送機制進行分析，配合實驗分析以驗證經驗公式與數學模型的正確性，並探討在不同之設計參數及操作條件對於薄膜蒸餾系統之流體溫度分佈、溫度極化現象、純水透膜通量增加百分率與水力損耗提升百分率的影響。研究結果顯示，平板型氣隔式薄膜蒸餾系統之理論值與實驗值的相對誤差總平均為8.06 %，而新型紊流促進因子能夠有效的提升系統透膜通量，在本研究設定的操作條件之中，最高可達到約18%的增益。

A new design of air gap membrane distillation (AGMD) with inserting carbon-fiber open slot separators of various hydrodynamic angles in flow channels for eddy promotion under concurrent-flow operation was developed and studied theoretically and experimentally.  Some studies showed that the eddy flow in aiming to reduce the temperature polarization were achieved implementing the carbon-fiber separators in the flow channel, and thus, heat- and mass-transfer rates were enhanced and the distillate flux enhancement was obtained.  A mathematical model considering heat and mass transfer mechanisms has been developed and a correlation of Nusselt numbers to calculate the heat transfer coefficient in the present AGMD device was correlated with the aid of the experimental data under various hydrodynamic angles of carbon-fiber separators.  The effects of various operation parameters were including the fluid inlet temperature, volumetric flow rate and hydrodynamic angles on the distillate flux enhancement of concurrent-flow operations for saline water desalination as compared that to the modules using empty channels.

目錄
中文摘要Ⅰ
英文摘要Ⅱ
目錄Ⅲ
圖目錄VI
表目錄IX
第一章緒論1
1-1引言1
1-2 薄膜蒸餾系統簡介5
1-3研究動機與方向8
第二章文獻回顧10
2-1薄膜蒸餾10
2-2紊流促進因子15
第三章理論分析18
3-1氣隔式薄膜蒸餾之熱量、質量傳送機制分析18
3-1-1氣隔式薄膜蒸餾質傳機制之理論分析21
3-1-2氣隔式薄膜蒸餾熱傳機制之理論分析28
3-1-3 溫度極化現象34
3-2紊流促進因子納賽數經驗公式之建立37
3-2-1 納賽數經驗公式模型38
3-2-2實驗數據之取得與分析計算流程41
3-3平板型氣隔式薄膜蒸餾系統一維理論模型之建立45
3-3-1平板型薄膜蒸餾系統一維理論模型46
3-3-2理論數據取得與計算分析流程-朗吉庫塔數值解析方法49
3-3-3系統水力損耗	53
3-4數學模擬參數之設定55
第四章實驗分析58
4-1平板型氣隔式薄膜蒸餾系統58
4-2實驗步驟65
第五章結果與討論66
5-1新型紊流促進因子之納賽數經驗公式迴歸分析66
5-2平板型氣隔式薄膜蒸餾系統69
5-2-1系統操作變因對於透膜通量之影響69
5-2-2溫度分佈與溫度極化現象70
5-3添加紊流促進因子之平板型氣隔式薄膜蒸餾系統75
5-3-1紊流促進因子對於透膜通量之影響75
5-3-2溫度分佈與溫度極化現象77
5-4設計參數於透膜通量與水力損耗之影響84
5-4-1透膜通量增益程度與水力損耗提升程度85
5-4-2透膜通量與水力損耗提升程度之比較86
第六章結論92
6-1紊流促進因子之納賽數經驗公式92
6-2平板型氣隔式薄膜蒸餾系統93
6-3添加紊流促進因子之平板型氣隔式薄膜蒸餾系統93
6-4模組設計參數於透膜通量與水力損耗之影響94
符號說明95
參考文獻102
圖目錄
圖1-1世界水資源分佈圖2
圖1-2世界海水淡化使用技術比例3
圖1-3青島市不同水源供水潛力與取水、製水之能耗比較圖4
圖1-4薄膜蒸餾之操作型態6 
圖1-5薄膜蒸餾之模組型式圖7
圖1-6研究架構圖9
圖3-1薄膜蒸餾系統熱量及質量傳送機制示意圖19
圖3-2薄膜蒸餾於薄膜內部之質量傳送阻力模式23
圖3-3氣隔式薄膜蒸餾之質量傳送阻力示意圖27
圖3-4氣隔式薄膜蒸餾之熱量傳送阻力串聯模式28
圖3-5薄膜蒸餾於薄膜內部熱量傳送之阻力模式29
圖3-6溫度極化示意圖34
圖3-7溫度極化現象改善示意圖37
圖3-8不同操作流態之溫度分佈示意圖41
圖3-9熱對流係數運算流程圖44
圖3-10順流操作之平板型氣隔式薄膜蒸餾系統示意圖47
圖3-11朗吉庫塔法求聯立方程組之計算示意圖51
圖3-12氣隔式薄膜蒸餾系統運算流程圖52
圖4-1平板型氣隔式薄膜蒸餾系統簡圖59
圖4-2平板型氣隔式薄膜蒸餾系統實驗設備圖(a)側視圖(b)正視圖59
圖4-3氣隔式薄膜蒸餾模組分解圖61
圖4-4壓克力頂板嵌入碳纖維板之實際圖62
圖4-5纖維板示意圖(a) 60 o (b) 90 o (c) 120 o62
圖4-6碳纖維板實際圖(a) 60 o (b) 90 o (c) 120 o62
圖4-7碳纖維支撐層實際圖(a)上視圖(b)下視圖63
圖5-1納賽數理論值與實驗值比較圖68
圖5-2冷流層固定25℃進口溫度且熱流層流體為純水下，未嵌入碳纖維板，不同操作參數對於透膜通量之影響72
圖5-3冷流層固定25℃進口溫度且進料端流體為鹽水下，未嵌入碳纖維板，不同操作參數對於透膜通量之影響72
圖5-4冷流層固定25℃進口溫度且熱流層流體為鹽水下，不同體積流對於主流區域、熱流層薄膜表面與冷凝液表面溫度分佈之影響74
圖5-5冷流層固定25℃進口溫度且熱流層流體為鹽水時，不同操作參數於溫度極化係數之影響74
圖5-6熱側流體為鹽水，碳纖維板之水力角度為60o，透膜通量之關係圖78
圖5-7熱側流體為鹽水，碳纖維板之水力角度為90o，透膜通量之關係圖79
圖5-8熱側流體為鹽水，碳纖維板之水力角度為120o，透膜通量之關係圖79
圖5-9冷流層固定25℃進口溫度且熱流層流體為純水下，不同水力角度之碳纖維板與操作參數對於透膜通量影響之比較80
圖5-10冷流層固定25℃進口溫度且熱流層流體為鹽水下，不同水力角度之碳纖維板與操作參數對於透膜通量影響之比較80
圖5-11冷流層固定25℃進口溫度且熱流層流體為鹽水下，不同水力角度對於主流區、熱流層薄膜表面與冷凝液表面溫度分佈之影響83
圖5-12冷流層固定25℃進口溫度且熱流層流體為鹽水下，不同水力角度與操作參數於溫度極化係數之影響83
圖5-13鹽水操作下，不同模組設計參數之理論透膜通量增益程度與水力損耗提升程度比較圖91
表目錄
表1-1不同操作型態之薄膜蒸餾應用領域7
表3-1經驗式參數表38
表3-2模組相關參數55
表3-3疏水性薄膜(聚四氟乙烯+聚丙烯複合膜)相關參數55
表3-4流體相關參數56
表3-5流體相關參數式57
表4-1PTFE/PP複合膜之薄膜性質63
表5-1納賽數經驗公式所需實驗數據之操作變因表66
表5-2冷流層固定25℃度進口溫度下，平板型氣隔式薄膜蒸餾系統實驗值與理論值之相對誤差比較表73
表5-3冷流進口25℃且熱流流體為純水下，不同水力角度之碳纖維板與操作參數之實驗與理論值相對誤差比較表81
表5-4冷流進口25℃且熱流流體為鹽水下，不同水力角度與操作參數之實驗與理論值相對誤差比較表82
表5-5不同水力角度與操作參數下之純水理論透膜通量增益比例表87
表5-6不同水力角度與操作參數下之鹽水理論透膜通量增益比例表88
表5-7碳纖維板支撐條寬度之水力損耗提升程度比較表89
表5-8不同水力角度與操作參數下，理論透膜通量增益程度與水力損耗提升程度比值90

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