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)於模組之進料側增加螺旋型檔板之設計來增加流速以及總通道長度，以求有效改善系統進料側離開系統後之殘於能量，並歸納出一經驗公式，描述此型式的螺旋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，套管型與螺旋通道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7.61 %，而本研究設定螺旋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39.5%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。

A new design of the DCMD module winding a spiral wire within the annulus of the concentric circular tube was investigated theoretically and experimentally in aiming to increase the pure water productivity in saline water desalination.  The hot sea water stream flowing through the annulus of a concentric circular tube, which a tight fitting spiral wire in a small annular spacing is inserted, could enhance the improvement of device performance.  The purposes of this study are (1) to develop the heat-transfer coefficient correlation for the spiral wire 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 spiral wire pitch on the pure water productivity improvement.  The correlated equation of estimating heat-transfer coefficient for the wire helix by using spiral flow channel was obtained, and the results show that the agreement between the experimental results and the theoretical predictions are fairly good. The new design of DCMD module winding a spiral wire within the annulus of the concentric circular tube can effectively enhance the mass flux, among the operating conditions set in this study, up to 39.5% of the gain.

中文摘要＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿I 
英文摘要＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿II 
目錄＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿III 
圖目錄＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿VI 
表目錄＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿XI 
第一章　緒論＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿1 
1－1引言＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿1 
1－2薄膜蒸餾系統簡介＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿4 
1－3研究動機與方向＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿8 
第二章　文獻回顧＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿10 
2－1直接接觸式薄膜蒸餾＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿10 
2－2螺旋通道行系統設計＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿15 
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螺旋通道型系統之螺旋因子納賽數經驗公式建立與模型＿＿28 
3－3螺旋通道型直接接觸式薄膜蒸餾系統一維理論模型之建立＿31 
3-3-1 套管熊與螺旋通道型薄膜蒸餾系統一維理論模型＿＿＿＿32 
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與 
高斯正交轉換＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿36 
3-3-3 實驗數據之取得與分析計算流程＿＿＿＿＿＿＿＿＿＿＿43 
3－4系統水力損耗＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿52 
3－5數學模擬參數之設定＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿54 
第四章　實驗分析＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿57 
4－1螺旋通道型直接接觸式薄膜蒸餾系統＿＿＿＿＿＿＿＿＿＿57
4－2直接接觸式薄膜蒸餾模組＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿62
4－3實驗步驟＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿66
第五章　結果與討論＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿67
5－1螺旋通道型直接接觸式薄膜蒸餾系統之納賽數經驗公式迴歸
分析＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿67
5－2套管型直接接觸式薄膜蒸餾系統＿＿＿＿＿＿＿＿＿＿＿＿72
5-2-1 系統操作變因對於透膜通量之影響＿＿＿＿＿＿＿＿＿＿72
5-2-2 溫度分佈與溫度極化現象＿＿＿＿＿＿＿＿＿＿＿＿＿＿	72
5－3螺旋通道型直接接觸式薄膜蒸餾系統＿＿＿＿＿＿＿＿＿＿86
5-3-1 螺旋因子對於透膜通量之影響＿＿＿＿＿＿＿＿＿＿＿＿86
5-3-2 溫度分佈與溫度極化現象	＿＿＿＿＿＿＿＿＿＿＿＿＿＿87
5－4模組設計參數於透膜通量與水力損耗之影響＿＿＿＿＿＿＿107
5-4-1 透膜通量增益程度與水力損耗提升程度＿＿＿＿＿＿＿＿107
5-4-2 透膜通量與水力損耗提升程度之比較＿＿＿＿＿＿＿＿＿108
第六章　結論與未來展望＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿116
6－1新型擾流增益因子之納賽數經驗公式＿＿＿＿＿＿＿＿＿＿116
6－2套管型直接接觸式薄膜蒸餾系統＿＿＿＿＿＿＿＿＿＿＿＿117
6－3添加螺旋因子之螺旋通道型直接接觸式薄膜蒸餾系統＿＿＿117
6－4模組設計參數於透膜通量與水力損耗之影響＿＿＿＿＿＿＿118
6－5未來展望＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿118
符號說明＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿119
參考文獻＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿124

圖目錄
圖1-1-1	海水淡化成本＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿4
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＿＿＿＿＿＿＿＿＿＿＿＿＿＿7
圖1-3-1	研究架構圖＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿9
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	＿＿＿＿＿＿＿＿＿22
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	質接接觸式模組示意圖＿＿＿＿＿＿＿＿＿＿＿＿＿32
圖3-3-2	順流操作直接接觸式薄膜蒸餾系統示意圖＿＿＿＿＿33
圖3-3-3	逆流操作質接接觸式薄膜蒸餾系統示意圖＿＿＿＿＿35
圖3-3-4	朗吉庫塔法求解聯立方程組之計算示意圖＿＿＿＿＿39
圖3-3-5	郎吉庫塔之布幅於實際螺旋通道型模組之示意圖＿＿39
圖3-3-6	朗吉庫塔法求解聯立方程組之計算示意圖＿＿＿＿＿40
圖3-3-7	修正後朗吉庫塔法求解聯立方程組之計算示意圖＿＿41
圖3-3-8	螺旋通道型系統之計算簡單示意圖＿＿＿＿＿＿＿＿42
圖3-3-9	螺旋通道型系統計算方式(1)＿＿＿＿＿＿＿＿＿＿＿42
圖3-3-10	螺旋通道型系統計算方式(2)＿＿＿＿＿＿＿＿＿＿＿43
圖3-3-11	螺旋通道型系統計算方式(3)＿＿＿＿＿＿＿＿＿＿＿43
圖3-3-12	不同操作流態之溫度分布示意圖	＿＿＿＿＿＿＿＿＿44
圖3-3-13	熱對流係數運算流程圖＿＿＿＿＿＿＿＿＿＿＿＿＿47
圖3-3-14	順流套管型薄膜蒸餾系統運算流程圖＿＿＿＿＿＿＿48
圖3-3-15	逆流套管型薄膜蒸餾系統運算流程圖＿＿＿＿＿＿＿49
圖3-3-16	順流螺旋通道型薄膜蒸餾系統運算流程圖＿＿＿＿＿50
圖3-3-17	逆流螺旋通道型薄膜蒸餾系統運算流程圖＿＿＿＿＿51
圖4-1-1	順流螺旋通道型直接接觸式薄膜蒸餾系統簡圖＿＿＿58
圖4-1-2	逆流螺旋通道型直接接觸式薄膜蒸餾系統簡圖＿＿＿58
圖4-1-3	直接接觸式薄膜蒸餾實驗設備圖	＿＿＿＿＿＿＿＿＿59
圖4-1-4	溢流桶實際圖＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿61
圖4-2-1	直接接觸式薄膜蒸餾模組示意圖	＿＿＿＿＿＿＿＿＿62
圖4-2-2	內側壓克力管實際圖＿＿＿＿＿＿＿＿＿＿＿＿＿＿62
圖4-2-3	中央之壓克力管實際圖＿＿＿＿＿＿＿＿＿＿＿＿＿63
圖4-2-4	螺旋型檔板實際圖＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿64
圖4-2-5	固定螺旋檔板後之薄膜管＿＿＿＿＿＿＿＿＿＿＿＿65
圖4-2-6	直接接觸式模組實際圖＿＿＿＿＿＿＿＿＿＿＿＿＿65
圖5-1-1	通道流體速度與通道截面積關係圖＿＿＿＿＿＿＿＿70
圖5-1-2	納賽數理論值與實驗值比較圖＿＿＿＿＿＿＿＿＿＿71
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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿75
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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿76
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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿77
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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿78
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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿81
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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿82
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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿83
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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿84
圖5-3-1	順流操作下且熱側流體為純水時，裝載寬度2cm之螺旋型檔板，不同操作參數對於透膜通量之關係圖＿＿＿＿＿＿＿＿＿88
圖5-3-2	順流操作下且熱側流體為鹽水時，裝載寬度2cm之螺旋型檔板，不同操作參數對於透膜通量之關係圖＿＿＿＿＿＿＿＿＿89
圖5-3-3	逆流操作下且熱側流體為純水時，裝載寬度2cm之螺旋型檔板，不同操作參數對於透膜通量之關係圖＿＿＿＿＿＿＿＿＿90
圖5-3-4	逆流操作下且熱側流體為鹽水時，裝載寬度2cm之螺旋型檔板，不同操作參數對於透膜通量之關係圖＿＿＿＿＿＿＿＿＿91
圖5-3-5	順流操作下且熱側流體為純水時，裝載寬度3cm之螺旋型檔板，不同操作參數對於透膜通量之關係圖＿＿＿＿＿＿＿＿＿92
圖5-3-6	順流操作下且熱側流體為鹽水時，裝載寬度3cm之螺旋型檔板，不同操作參數對於透膜通量之關係圖＿＿＿＿＿＿＿＿＿93
圖5-3-7	逆流操作下且熱側流體為純水時，裝載寬度3cm之螺旋型檔板，不同操作參數對於透膜通量之關係圖＿＿＿＿＿＿＿＿＿94
圖5-3-8	逆流操作下且熱側流體為鹽水時，裝載寬度3cm之螺旋型檔板，不同操作參數對於透膜通量之關係圖＿＿＿＿＿＿＿＿＿95
圖5-3-9	順流操作下且熱側流體為鹽水時，不同螺旋型檔板之寬度與操作參數對於透膜通量之關係圖＿＿＿＿＿＿＿＿＿＿＿＿＿96
圖5-3-10	逆流操作下且熱側流體為鹽水時，不同螺旋型檔板之寬度與操作參數對於透膜通量之關係圖＿＿＿＿＿＿＿＿＿＿＿＿＿97
圖5-3-11	順流狀態下且熱側流體為鹽水時，套管型系統與螺旋通道型系統於主流區域與薄膜表面溫度分佈之影響＿＿＿＿＿＿＿＿102
圖5-3-12	逆流狀態下且熱側流體為鹽水時，套管型系統與螺旋通道型系統於主流區域與薄膜表面溫度分佈之影響＿＿＿＿＿＿＿＿103
圖5-3-13	順流狀態下且熱側流體為鹽水時，不同螺旋型檔板之寬度與操作參數於溫度極化係數之影響＿＿＿＿＿＿＿＿＿＿＿＿＿104
圖5-3-14	逆流狀態下且熱側流體為鹽水時，不同螺旋型檔板之寬度與操作參數於溫度極化係數之影響＿＿＿＿＿＿＿＿＿＿＿＿＿105
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損耗提升程度比較圖	＿＿＿＿＿＿＿＿＿＿＿＿＿＿113
圖5-4-2	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較圖	＿＿＿＿＿＿＿＿＿＿＿＿＿＿114
		
表目錄
表1-1-1	全球水資源的蘊含量與分布情形＿＿＿＿＿＿＿＿＿2
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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿54
表3-5-2	疏水性薄膜(聚四氟乙烯+聚丙烯複合膜)相關參數＿＿54
表3-5-3	流體相關參數＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿55
表3-5-4	流體相關參數式＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿56
表4-2-1	PTFE/PP複合膜之薄膜性質＿＿＿＿＿＿＿＿＿＿＿＿64
表5-1-1	納賽數經驗公式所需實驗數據之操作變因表＿＿＿＿67
表5-2-1	順流操作下套管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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿79
表5-2-2	順流操作下套管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＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿80
表5-2-3	不同操作流向於平均溫度極化係數之影響比較表＿＿85
表5-3-1	順流純水操作下螺旋通道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	＿＿＿＿＿＿＿＿＿＿＿＿＿＿98
表5-3-2	順流鹽水操作下螺旋通道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＿＿＿＿＿＿＿＿＿＿＿＿＿＿99
表5-3-3	逆流純水操作下螺旋通道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	＿＿＿＿＿＿＿＿＿＿＿＿＿＿100
表5-3-4	逆流鹽水操作下螺旋通道型直接接觸式薄膜蒸餾系統，實驗值與理論值相對誤差比較表＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿101
表5-3-5	不同操作流向與模組於平均溫度極化係數之影響比較表＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿＿106
表5-4-1	順流純水操作下套管型與螺旋通道型直接接觸式薄膜蒸餾模組系統同螺旋檔板寬度之理論透膜通量增益比例表＿＿＿＿＿110
表5-4-2	逆流純水操作下套管型與螺旋通道型直接接觸式薄膜蒸餾模組，不同螺旋檔板寬度之理論透膜通量增益比例表＿＿＿＿＿110
表5-4-3	順流鹽水操作下套管型與螺旋通道型直接接觸式薄膜蒸餾模組，不同螺旋檔板寬度之理論透膜通量增益比例表＿＿＿＿＿111
表5-4-4	逆流鹽水操作下套管型與螺旋通道型直接接觸式薄膜蒸餾模組，不同螺旋檔板寬度之理論透膜通量增益比例表＿＿＿＿＿111
表5-4-5	不同螺旋檔板寬度之水力損耗提升程度比較表＿＿＿112
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	＿＿＿＿＿＿＿＿＿＿＿＿＿＿115
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	＿＿＿＿＿＿＿＿＿＿＿＿＿＿115

參考文獻
1.	Pidwireny M., “Fundanmentals of Physical Geography.” The Hydrologic Cycle, 2nd Edition (2006).
2.	樓基中編著，水資源與環境保育SOS環保救地球，台北市，五南圖書出版股份有限公司，初版，2010。
3.	Kalogirou SA., “Seawater desalination using renewable energy sources,” Prog. Energy Combust. Sci., 31, 242-281 (2005).
4.	Thomson M., Miranda M.S., and Infield D., “A small-scale seawater reverse-osmosis system with excellent energy efficiency over a wide operating range,” Desalination, 153, 229–236 (2002).
5.	Cath T.Y., Adams V.D. and Childress E., “Experimental study of desalination using direct contact membrane distillation: a new approach to flux enhancement,” J. Membr. Sci., 228, 5–16 (2004).
6.	Meindersma G.W., Guijt C.M. and de Haan A.B., “Desalination and water recycling by air gap membrane distillation,” Desalination, 187, 291–301 (2006).
7.	El-Bourawi M.S., Ding Z., Ma R. and Khayet M.A., “A framework for better understanding membrane distillation separation process,” J. Membr. Sci., 285, 4–29 (2006).
8.	Ho-Ming Yeh, “The improvement in separation of concentric tube thermal diffusion columns,” Geogia Institute of Technology, (1969).
9.	Banat F., Jwaied N., Rommel M., Koschikowski J. and Wieghaus M., “Desalination by a "compact SMADES" autonomous solarpowered membrane distillation unit,” Desalination, 217, 29–37 (2007).

10.	Rommel M., Koschikowski J. and Wieghaus M., “Solar driven desalination systems based on membrane distillation,” NATO Security through Science Series C: Environmental Security, 247–257 (2007).
11.	Calabro V., Drioli E. and Matera F., “Membrane distillation in the textile wastewater treatment,” Desalination, 83, 209–224 (1991).
12.	Cartinella J.L., Cath T.Y., Flynn M.T., Miller G.C., Hunter K.W. and Childress A.E., “Removal of natural steroid hormones from wastewater using membrane contactor processes,” Environ. Sci. Technol., 40, 7381–7386 (2006).
13.	Calabro V., Jiao B.L. and Drioli E., “Theoretical and experimental study on membrane distillation in the concentration of orange juice,” Ind. Eng. Chem. Res., 33, 1803–1808 (1994).
14.	Onsekizoglu P., Bahceci K.S. and Acar J., “The use of factorial design for modeling membrane distillation,” J. Membr. Sci., 349, 225–230 (2010).
15.	Tomaszewska M., Gryta M. and Morawski A.W., “Study on the concentration of acids by membrane distillation,” J. Membr. Sci., 102, 113–122 (1995).
16.	Tomaszewska M., Gryta M., and Morawski A.W., “Mass transfer of HCl and H2O across the hydrophobic membrane during membrane distillation,” J. Membr. Sci., 166, 149–157 (2000).
17.	Sakai K., Muroi T., Ozawa K., Takesawa S., Tamura M. and Nakane T., “Extraction of solute-free water from blood by membrane distillation,” Trans. Am. Soc. Artif. Intern. Organs , 32, 397-400 (1986).
18.	Lawson  K.W. and Lloyd D.R., “Membrane distillation.” J. Membr. Sci., 124, 1-25 (1997).
19.	Tomaszewska M., Gryta M., Morawski A.W. and Grzechulska J., “Membrane distillation of NaCl solution containing natural organic matter,” J. Membr. Sci., 181, 279–287 (2001)
20.	Khayet M., Mengual J.I., and Matsuura T., “Porous hydrophobic/hydrophilic composite membranes: Application in desalination using direct contact membrane distillation,” J. Membr. Sci., 252, 101–113 (2005).
21.	Banat F.A., Abu Al-Rub F.A., Jumah R. and Al-Shannag M., “Modeling of desalination using tubular direct contact membrane distillation modules,” Sep. sci. technol., 34, 2191-2206 (1999).
22.	Bodell B.R., “Silicone rubber vapor diffusion in saline water distillation,” United States Patent Application Serial No. 285,32 (1963).
23.	Weyl P.K. Recovery of demineralized water form saline waters, United States Patent 3,340,186 (1967).
24.	Findley M.E., “Vaporization through porous membranes,” Ind. Eng. Chem. Process Des. Dev., 6, 226-230 (1967).
25.	Drioli E. and Wu Y., “Membrane distillation : An experimental study,” Desalination, 53, 339-346 (1985).
26.	Schofield R.W., Fane A.G. and Fell C.J.D.. “Heat and mass transfer in membrane distillation,” J. Membr. Sci., 33, 299–313 (1987).
27.	Schofield R.W., Fane A.G., Fell C.J., and Macoun R., “Factors affecting flux in membrane distillation,” Desalination, 77, 279–294 (1990).
28.	Phattaranawik J. and Jiraratananon R., “Direct contact membrane distillation：effect of mass transfer on heat transfer,” J. Membr. Sci., 188, 137-143 (2001).
29.	Phattaranawik J., Jiraratananon R., Fane A.G. and Halim C., ”Mass flux enhancement using spacer filled channels in direct contact membrane distillation,” J. Membr. Sci., 187, 193-201 (2001).
30.	Phattaranawik J., Jiraratananon R. and Fane A.G., “Effects of net-type spacers on heat and mass transfer in direct contact membrane distillation and comparison with ultrafiltration studies,” J. Membr. Sci., 217, 193-206 (2003).
31.	Kakac S., Shah R.K. and Bergles A.E.,“Low Reynolds Number Flow Heat Exchangers,” Hemisphere, Washington, DC, 1983.
32.	Gryta M, Tomaszewska M, Morawski AW. “Membrane distillation with laminar flow,” Sep. Purif. Technol., 11, 93–101 (1997).
33.	Martínez-Díez L, Vázquez-González MI. “Effects of polarization on mass transport through hydrophobic porous membranes,” Ind. Eng. Chem. Res., 37, 4128-4135 (1998).
34.	Phattaranawik J, Jiraratananon R, Fane AG. “Heat transport and membrane distillation coefficients in direct contact membrane distillation,” J. Membr. Sci., 212, 177-193 (2003).
35.	Khayet M, Godino MP, Mengual JI. “Theoretical and experimental studies on desalination using the sweeping gas membrane distillation method,” Desalination, 157, 297-305 (2003).
36.	Bui VA, Vu LTT, Nguyen MH. “Modelling the simultaneous heat and mass transfer of direct contact membrane distillation in hollow fibre modules,” J. Membr. Sci., 353, 85-93 (2010).
37.	Lawson KW, Lloyd DR. “Membrane distillation. II. Direct contact MD,” J. Membr. Sci., 120, 123-133 (1996).
38.	Srisurichan S, Jiraratananon R, Fane AG. “Mass transfer mechanisms and transport resistances in direct contact membrane distillation process,” J. Membr. Sci., 277, 186-194 (2006).
39.	Gryta M, Tomaszewska M. “Heat transport in the membrane distillation process.,” J. Membr. Sci., 144, 211-222 (1998).
40.	Fernández-Pineda C, Izquierdo-Gil MA, García-Payo MC. “Gas permeation and direct contact membrane distillation experiments and their analysis using different models,” J. Membr. Sci., 198, 33-49 (2002).
41.	Zhongwei D, Liying L, Runyu M. “Study on the effect of flow maldistribution on the performance of the hollow fiber modules used in membrane distillation,” J. Membr. Sci., 215, 11-23 (2003).
42.	Chen T.C., Ho C.D., Yeh H.M. “Theoretical modeling and experimental analysis of direct contact membrane distillation,” J. Mem. Sci., 330, 279-287 (2009).
43.	Schofield R.W., Fane A.G., Fell C.J.D. “Gas and vapour transport through microporous membranes. II. Membrane distillation,” J. Membr. Sci., 53, 173-185 (1990).
44.	Da Costa A.R., Fane A.G., Fell C.J.D, Franken A.C.M. “Optimal channel spacer design for ultrafiltration,” J. Membr. Sci., 62, 275-291 (1991).
45.	Da Costa A.R., Fane A.G., Wiley D.E. “Spacer characterization and pressure drop modeling in spacer-filled channels for ultrafiltration,” J. Membr. Sci., 87, 79-98 (1994).
46.	Washall T. A. and Mellpolder. “Improving the separation efficiency of liquid thermal diffusion columns,” Ind. Eng. Chem. Process Des., 1(1) 26-28 (1962).
47.	Howell J.A., Field R.W. and Wu D., “Yeast cell microfiltration: flux enhancement in baffled and pulsatill flow system,.” J. Membr. Sci., 80, 59-65, (1993). 
48.	Gupta B.B., Howell J.A., Wu D. and Field R.W., “A helical baffle for cross-flow microfiltration.” J. Membr. Sci., 99, 31-42 (1995).
49.	Yeh H. M., Dong J. F., Hsieh M. J. and Yang C. C., “Prediction of permeate flux for ultrafiltration in wire-rod tubular-membrane modules.” J. Membr. Sci., 209, 19-26 (2002).
50.	Poskas. P., Simonis. V. and Ragaisis. V., “Heat transfer in helical channals with two-side heating in gas flow.” International Journal of heat and mass transfer, 54, 847-853 (2011).
51.	 Garcı́a-Payoa M.C., Rivierb C.A., Marisonb I.W. and Stockar U. von. “Separation of binary mixtures by thermostatic sweeping gas membrane distillation: II. Experimental results with aqueous formic acid solutions.” J. Membr. Sci., 198, 197-210 (2002).
52.	Lawson K.W., Lloyd D.R. “Membrane distillation,” J. Membr. Sci., 124, 1-25 (1997).
53.	Phattaranawik J, Jiraratananon R and Fane A.G., “Effect of pore size distribution and air flux on mass transport in direct contact membrane distillation,” J. Membr. Sci., 215, 75-85 (2003)
54.	.Ding Z.W., Ma R.Y. and Fane A.G., “A new model for mass transfer in direct contact membrane distillation. ” Desalination, 151, 217 (2003).
55.	Banat F.A. and Simandl J., “Desalination by membrane distillation : a parametric study.” Sci. Techol., 33, 201-226 (1998).
56.	Iversen S.B., Bhatia V.K., Dam-Jphasen K., Jonsson G. “Characterization of microporous membranes for use in membrane contactors.” J. Membr. Sci., 130, 205-217 (1997).
57.	Fuller E.N., Schettler P.D. and Giddings J.C., “New method for prediction of binary gas-phase diffusion coefficients.” Industrial and Engineering Chemistry, 58, 18-27 (1966).
58.	Sarti G.C., Gostoli C., Matulli S. “Low energy desalination processes using hydrophobic membranes,” Desalmation, 56, 277-286 (1985).
59.	Phattaranawik J, Jiraratananon R, Fane A.G., Halim C. “Mass flux enhancement using spacer filled channels in direct contact membrane distillation,” J. Membr. Sci., 187, 193-201 (2001).
60.	Phattaranawik J, Jiraratananon R, Fane A.G. “Effects of net-type spacers on heat and mass transfer in direct contact membrane distillation and comparison with ultrafiltration studies,” J. Membr. Sci., 217, 193-206 (2003).
61.	Schwinge J., Wiley D.E., Fane A.G., Guenther R. “Characterization of a zigzag spacer for ultrafiltration,” J. Membr. Sci., 172, 19-31 (2000).
62.	Poskas P. and Vytautsa S., “ Heat transfer in initial part of thermal stabilization of helical channels in air flow,” Heat Transfer Resarch, 43(5), 443-460 (2012).
63.	Welty JR, Wick CE, Wilson RE. Fundamentals of Momentum, Heat, and Mass Transfer, third ed. John Wiley & Sons, New York, 1984.
64.	Satish G. Kandlikar, Derek Schmitt. “Characterization of surface roughness effects on pressure drop in single-phase flow in minichannels,” PHYSICS OF FLUIDS, 17, 100606 (2005).
65.	Bird R.B., Stewart W.E., Lightfoot E.N. Transport Phenomena, second ed., John Wiley & Sons, New York, 2007.
66.	Ozbek H., Phillips S.L. “Thermal conductivity of aqueous sodium chloride solutions from 20 to 330°C,” J. Chem. Eng. Data, 25, 263-267 (1980).
67.	Incropera FP, DeWitt DP. Fundamentals of Heat and Mass Transfer. fourth ed., New York: John Wiley & Sons Inc., 1996.
68.	Chenlo F., Moreira R., Pereira G., Ampudia A. “Viscosities of aqueous solutions of sucrose and sodium chloride of interest in osmotic dehydration processes,” J. Food Eng., 54, 347-352 (2002).
69.	Magalhães M.C.F., Königsberger E., May P.M., Hefter G. “Heat capacities of concentrated aqueous solutions of sodium sulfate, sodium carbonate, and sodium hydroxide at 25 °C,” J. Chem. Eng. Data, 47, 590-598 (2002).