論文提要內容：薄膜蒸餾海水淡化用來製造純水提供民生及工業使用，因其優點特色為具有裝置簡潔、低成本、可模組化、高介面面積等，為近來廣受重視的一種技術。然而，薄膜蒸餾因模組通道限制，對於系統產能有相當顯著的影響，此現象越明顯則產能相對低落。本研究針對薄膜蒸餾之主要設備進行效率改善的研究，目的為：(1)設計新型紊流促進因子(Eddy promoter) ，以求有效改善系統內部的溫度極化現象進而提升系統產能，並歸納出一經驗公式，描述此型式的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研究，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，網格型直接接觸式薄膜蒸餾系統之理論值與實驗值的相對誤差總平均為4.78 %，而本研究設定新型擾流因子能夠有效的提升系統透膜通量，最高可達到單位面積的45%的增益。本研究以操作在低體積流率之設備為主，除了有效利用通道內熱側流體以降低操作成本外，經由改善後的設計可提升設備效能並得到增加透膜通量總產量的效果。

Abstract:
    A new design of direct contact membrane distillation (DCMD) with various hydrodynamic angles of inserting carbon-fiber spacers in flow channels was proposed to increase the pure water productivity in saline water desalination. Temperature polarization causes the reduction of effection temperature driving force for membrane distillation. Attempts to reduce the temperature polarization were made by implementing the spacer-filled channel to create wakes and eddy in the flow characteristic. Experimental study has demonstrated its feasibility, and sustainable performance enhancement was obtained for the experimental system. The purposes of this study are (1) to develop the heat-transfer coefficient correlation for the carbon fiber channel; (2) to develop a one-dimensional mathematical model and propose a general numerical method for predicting pure water productivity of DCMD systems; (3) to study the effects of various operation parameters including the inlet fluid temperatures, volumetric flow rate, spacer-filled channel on the pure water productivity improvement. A correlated equation for estimating heat-transfer coefficient for spacer-filled channels with different hydrodynamic angles was obtained, and the results show that the agreement between the experimental results and the theoretical predictions is fairly good. The new design of eddy promoter can effectively enhance the mass flux, among the operating conditions set in this study, up to 45%.

目錄
中文摘要I
英文摘要II
目錄III
圖目錄VI
表目錄XII
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11
2-1薄膜蒸餾11
2-2紊流促進因子14
第三章理論分析16
3-1直接接觸式薄膜蒸餾之熱量、質量傳送機制分析16
3-1-1直接接觸式薄膜蒸餾質傳機制之理論分析18
3-1-2直接接觸式薄膜蒸餾熱傳機制之理論分析23
3-1-3溫度極化現象與溫度極化係數26
3-2納賽數經驗公式建立與模型28
3-3直接接觸式薄膜蒸餾系統一維理論模型之建立31
3-3-1直接接觸式薄膜蒸餾系統一維理論模型31
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	36
3-3-3實驗數據之取得與分析計算流程39
3-4系統水力損耗45
3-5數學模擬參數之設定47
第四章實驗分析50
4-1網格型直接接觸式薄膜蒸餾系統50
4-2實驗步驟60
第五章結果與討論61
5-1 新型擾流直接接觸式薄膜蒸餾系統之納賽數經驗公式迴歸分析61
5-2 平板型直接接觸式薄膜蒸餾系統65
5-2-1 系統操作變因對於透膜通量之影響65
5-2-2 溫度分佈與溫度極化現象65
5-3 添加紊流促進因子之平板型直接接觸式薄膜蒸餾系統79
5-3-1 紊流促進因子對於透膜通量之影響79
5-3-2 溫度分佈與溫度極化現象80
5-4 模組設計參數於透膜通量與水力損耗之影響114
5-4-1 透膜通量增益程度與水力損耗提升程度114
5-4-2 透膜通量與水力損耗提升程度之比較116
第六章結論124
6-1 新型紊流促進因子之納賽數經驗公式124
6-2 平板型直接接觸式薄膜蒸餾系統125
6-3 添加紊流促進因子之平板型直接接觸式薄膜蒸餾系統125
6-4 模組設計參數於透膜通量與水力損耗之影響126
符號說明127
參考文獻132
圖目錄
圖1-1-1世界海水淡化使用技術比例2
圖1-1-2海水淡化成本3
圖1-2-1薄膜蒸餾之操作型態6
圖1-2-2薄膜蒸餾之模組型式	6
圖1-3-1研究架構圖10
圖3-1-1薄膜蒸餾系統熱量及質量傳送機制示意圖	17
圖3-1-2薄膜蒸餾於薄膜內之質量傳送阻力模式20
圖3-1-3薄膜蒸餾之質量傳送阻力示意圖23
圖3-1-4熱量傳送之阻力串聯模式23
圖3-1-5溫度極化示意圖26
圖3-3-1順流操作之平板型直接接觸式薄膜蒸餾系統示意圖32
圖3-3-2逆流操作之平板型直接接觸式薄膜蒸餾系統示意圖34
圖3-3-3朗吉庫塔法求解聯立方程組之計算示意圖38
圖3-3-4順流平板型薄膜蒸餾系統運算流程圖39
圖3-3-5逆流平板型薄膜蒸餾系統運算流程圖40
圖3-3-6不同操作流態之溫度分佈示意圖	41
圖3-3-7熱對流係數運算流程圖44
圖4-1-1順流平板型直接接觸式薄膜蒸餾系統簡圖51
圖4-1-2逆流平板型直接接觸式薄膜蒸餾系統簡圖52
圖4-1-3網格型直接接觸式薄膜蒸餾系統實驗設備圖53
圖4-1-4溢流桶實際圖54
圖4-1-6尼龍纖維支撐層示意圖57
圖4-1-7碳纖維板規格圖57
圖4-1-5網格型直接接觸式薄膜蒸餾模組分解圖59
圖5-1-1納賽數理論值與實驗值比較圖64
圖5-2-1順流操作下且熱側流體為純水時，不同操作參數對於透膜通量之影響68
圖5-2-2順流操作下且熱側流體為鹽水時，不同操作參數對於透膜通量之影響69
圖5-2-3逆流操作下且熱側流體為純水時，不同操作參數對於透膜通量之影響70
圖5-2-4逆流操作下且熱側流體為鹽水時，不同操作參數對於透膜通量之影響71
圖5-2-5順流狀態下且熱側流體為鹽水時，不同體積流率於主流區域與薄膜表面溫度分佈之影響74
圖5-2-6逆流狀態下且熱側流體為鹽水時，不同體積流率於主流區域與薄膜表面溫度分佈之影響75
圖5-2-7順流狀態下且熱側流體為鹽水時，不同操作參數於溫度極化係數之影響76
圖5-2-8逆流狀態下且熱側流體為鹽水時，不同操作參數於溫度極化係數之影響77
圖5-3-1順流操作下且熱側流體為鹽水時，裝載寬度2 mm 60。之碳纖維板支撐條，不同操作參數對於透膜通量之關係圖81
圖5-3-2順流操作下且熱側流體為鹽水時，裝載寬度2 mm 90。之碳纖維支撐條，不同操作參數對於透膜通量之關係圖82
圖5-3-3順流操作下且熱側流體為鹽水時，裝載寬度2 mm 120。之碳纖維支撐條，不同操作參數對於透膜通量之關係圖83
圖5-3-4順流操作下且熱側流體為鹽水時，裝載寬度3 mm 60。之碳纖維板支撐條，不同操作參數對於透膜通量之關係圖84
圖5-3-5	順流操作下且熱側流體為鹽水時，裝載寬度3 mm 90。之碳纖維板支撐條，不同操作參數對於透膜通量之關係圖85
圖5-3-6順流操作下且熱側流體為鹽水時，裝載寬度3 mm 120。之碳纖維支撐條，不同操作參數對於透膜通量之關係圖86
圖5-3-7逆流操作下且熱側流體為鹽水時，裝載寬度2 mm 60。之碳纖維板支撐條，不同操作參數對於透膜通量之關係圖87
圖5-3-8逆流操作下且熱側流體為鹽水時，裝載寬度2 mm 90。之碳纖維支撐條，不同操作參數對於透膜通量之關係圖88
圖5-3-9逆流操作下且熱側流體為鹽水時，裝載寬度2 mm 120。之碳纖維支撐條，不同操作參數對於透膜通量之關係圖89
圖5-3-10	逆流操作下且熱側流體為鹽水時，裝載寬度3 mm 60。之碳纖維板支撐條，不同操作參數對於透膜通量之關係圖90
圖5-3-11	逆流操作下且熱側流體為鹽水時，裝載寬度3 mm 90。之碳纖維板支撐條，不同操作參數對於透膜通量之關係圖91
圖5-3-12	逆流操作下且熱側流體為鹽水時，裝載寬度3 mm 120。之碳纖維支撐條，不同操作參數對於透膜通量之關係圖92
圖5-3-13	順流操作下且熱側流體為鹽水時，不同碳纖維支撐條寬度與操作參數對於透膜通量之關係圖93
圖5-3-14	逆流操作下且熱側流體為鹽水時，不同碳纖維支撐條寬度與操作參數對於透膜通量之關係圖94
圖5-3-15	順流操作下且熱側流體為鹽水時，不同水力角度與操作參數對於透膜通量之關係圖	95
圖5-3-16	逆流操作下且熱側流體為鹽水時，不同水力角度與操作參數對於透膜通量之關係圖	96
圖5-3-17	
順流狀態下且熱側流體為鹽水時，不同碳纖維度支撐條寬度於主流區域與薄膜表面溫度分佈之影響105
圖5-3-18	順流狀態下且熱側流體為鹽水時，不同水力角度於主流區域與薄膜表面溫度分佈之影響106
圖5-3-19	逆流狀態下且熱側流體為鹽水時，不同碳纖維度支撐條寬度於主流區域與薄膜表面溫度分佈之影響107
圖5-3-20	逆流狀態下且熱側流體為鹽水時，不同水力角度於主流區域與薄膜表面溫度分佈之影響108
圖5-3-21	順流狀態下且熱側流體為鹽水時，不同碳纖維板支撐條寬度與操作參數於溫度極化係數之影響109
圖5-3-22	順流狀態下且熱側流體為鹽水時，不同水力角度與操作參數於溫度極化係數之影響	110
圖5-3-23	逆流狀態下且熱側流體為鹽水時，不同碳纖維板支撐條寬度與操作參數於溫度極化係數之影響111
圖5-3-24	逆流狀態下且熱側流體為鹽水時，不同水力角度與操作參數於溫度極化係數之影響	112
圖5-4-1	順流鹽水操作下，不同模組設計參數之理論透膜通量增益程度與水力耗損提升程度比較圖121
圖5-4-2順流鹽水操作下，不同模組設計參數之理論透膜通量增益程度與水力耗損提升程度比較圖122
表目錄
表1-2-1不同操作型態之薄膜蒸餾應用領域7
表3-2-1經驗式參數表28
表3-5-1模組相關參數47
表3-5-2疏水性薄膜(聚四氟乙烯+聚丙烯複合膜)相關參數47
表3-5-3流體相關參數48
表3-5-4流體相關參數式49
表4-1-1PTFE/PP複合膜之薄膜性質58
表5-1-1	納賽數經驗公式所需實驗數據之操作變因表62
表5-2-1	順流操作下平板型直接接觸式薄膜蒸餾系統實驗值與理論值之相對誤差比較表72
表5-2-2逆流操作下平板型直接接觸式薄膜蒸餾系統實驗值與理論值之相對誤差比較表73
表5-2-3不同操作流向對於平均溫度極化係數之影響比較表78
表5-3-1順流純水操作下網格型(2mm)直接接觸式薄膜蒸餾系統，實驗值與理論值之相對誤差比較表97
表5-3-2順流純水操作下網格型(3mm)直接接觸式薄膜蒸餾系統，實驗值與理論值之相對誤差比較表98
表5-3-3逆流純水操作下網格型(2mm)直接接觸式薄膜蒸餾系統，實驗值與理論值之相對誤差比較表99
表5-3-4	逆流純水操作下網格型(3mm)直接接觸式薄膜蒸餾系統，實驗值與理論值之相對誤差比較表100
表5-3-5順流鹽水操作下網格型(2mm)直接接觸式薄膜蒸餾系統，實驗值與理論值之相對誤差比較表101
表5-3-6順流鹽水操作下網格型(3mm)直接接觸式薄膜蒸餾系統，實驗值與理論值之相對誤差比較表102
表5-3-7逆流鹽水操作下網格型(2mm)直接接觸式薄膜蒸餾系統，實驗值與理論值之相對誤差比較表	103
表5-3-8逆流鹽水操作下網格型(3mm)直接接觸式薄膜蒸餾系統，實驗值與理論值之相對誤差比較表	104
表5-3-9不同操作流向與模組於平均溫度極化係數之影響比較表113
表5-4-1順流鹽水操作下網格型直接接觸式薄膜蒸餾模組，不同碳纖維板支撐條寬度之理論透膜通量增益比例表117
表5-4-2	逆流鹽水操作下網格型直接接觸式薄膜蒸餾模組，不同碳纖維板支撐條寬度之理論透膜通量增益比例表	117
表5-4-3順流鹽水操作下網格型直接接觸式薄膜蒸餾模組，不同水力角度之理論透膜通量增益比例表118
表5-4-4	逆流鹽水操作下網格型直接接觸式薄膜蒸餾模組，不同水力角度之理論透膜通量增益比例表	119
表5-4-5不同碳纖維板支撐條寬度之水力損耗提升程度比較表120
表5-4-6順流鹽水操作下，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值表123
表5-4-7逆流鹽水操作下，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值表123

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