工廠為符合製程或產品規格改變需針對蒸餾塔操作進行調整，然而操作人員主觀的判斷造成能源不必要的浪費，若能以操作導引系統建立客觀的操作依據，將能增加人員對於蒸餾塔的掌握，減少人為因素的不當操作。本研究之目標是在Excel-VBA平台上建立含板效率之蒸餾塔平衡模式，蒸餾塔板效率經由F.R.I的回歸效率模型取得，在不含複雜的質傳速率模型下，此模式可以反應出塔內因效能變化造成的影響。本研究已針對甲醇水溶液之蒸餾系統獨立撰寫，包括熱力學、氣液相物性、蒸餾塔數學模式，並利用Aspen Plus蒸餾塔平衡與速率模式進行模式的驗證，獲得非常接近的結果，未來將應用於現場操作之導引。

The operating conditions of distillation column has to be adjusted in order to meet the change of the process or product specifications. However, unnecessary energy waste may occur due to subjective judgments of operators. If operating guidelines based on accurate models can be established, the mastery of operators for the distillation column can be improved. This study is to build an equilibrium model of distillation columns with tray efficiency in the Excel-VBA platform for achieving that goal. Tray efficiencies of the column are obtained using the correlations from F.R.I. This approach allows the estimation of efficiencies without using complex rate-based models. The column model developed includes the MESH equations, thermodynamic phase equilibrium equations and physical property correlations. The model for a methanol-water distillation column has been established and verified using both equilibrium and rate-based models from Aspen Plus with very good agreement. This model will be implemented for guiding the on-site operation in the future.

中文摘要	I
英文摘要	II
目錄	IV
圖目錄	VII
表目錄	IX
第一章	實習簡介	1
1.1實習機構簡介	1
1.2實習內容概述	2
1.3實習心得與自我期許	5
第二章	緒論	6
2.1前言	6
2.2.1蒸餾塔計算方法	9
2.2.2構件質傳效率模型-規整填充物	11
2.3動機與目的	14
2.4產品及市場概況	14
2.5可行性及利基分析	15
2.6論文架構	15
第三章	蒸餾塔平衡模式建立	16
3.1蒸餾塔數學模式	17
3.2 熱力學模式	19
3.2.1相平衡常數計算	20
3.2.2熱焓計算	21
3.3 設計自由度分析	23
3.4蒸餾塔求解方法-內外演算法	25
3.4.1各迭代變量定義與MESH方程改寫	26
3.4.2蒸餾塔平衡模式之求解步驟	32
3.4.3布羅伊登法(Broyden method)	37
3.5操作介面建立	39
3.6蒸餾塔平衡模式驗證	44
3.6.1基本個案建立	44
3.6.2產品預測結果	45
3.6.3操作預測結果	46
3.6.4 蒸餾塔模式預測	48
第四章	規整填充塔效率模型建立	50
4.1 F.R.I構建質傳效率模型	50
4.1.1 理論板相當高度(HETP)	50
4.1.2莫非板效率(Murphree efficiency)	60
4.1.3 壓降	62
4.2物性計算	66
4.2.1密度計算(莫耳體積)	66
4.2.2黏度計算	67
4.2.3擴散係數計算	70
4.2.4表面張力計算	73
4.3填料的輸入介面	74
4.4 含效率模型之蒸餾塔內外演算法求解步驟	75
4.5 蒸餾塔效率模型驗證	81
4.5.1基本個案建立	81
4.5.2分段數對HETP影響	82
4.5.3 模式驗證結果	83
第五章	結論與未來展望	88
參考文獻	89

圖目錄
圖1. 1工業技術研究院光復院區大樓及實驗設施	1
圖1. 2旋風蒸發器與實驗藥品	3
圖1. 3 DWC蒸餾塔系統	4
圖1. 4 DWC蒸餾塔與附屬設備	4
圖1. 5批次蒸餾設備	5
圖2. 1化工業各能耗比例(工研院提供)	6
圖2. 2板式塔與填充塔內部構造簡圖	7
圖2. 3程式運行模式	14
圖3. 1蒸餾塔系統示意圖	16
圖3. 2蒸餾塔內外演算法之求解步驟	32
圖3. 3蒸餾塔條件設定介面	39
圖3. 4蒸餾塔猜值設定介面	41
圖3. 5模擬結果介面	41
圖3. 6各物流性質模擬結果介面	42
圖3. 7 OPC連接介面	43
圖3. 8甲醇水溶液蒸餾塔-產品預測	44
圖3. 9甲醇水溶液蒸餾塔-操作預測	45
圖3. 10蒸餾塔塔內溫度與組成分布-產品預測	46
圖3. 11蒸餾塔內部分溫度與組成分布-操作預測	47
圖3. 12進料組成變化之塔內分佈(a)溫度(b)液相組成(c)氣相組成	48
圖3. 13進料溫度變化之塔內分佈(a)溫度(b)液相組成(c)氣相組成	48
圖4. 1 系統圖與組成關係圖	53
圖4. 2填充高度與液相分佈關係示意圖	55
圖4. 3塔內返混效應示意圖	56
圖4. 4 由操作性能圖確定泛溢點	57
圖4. 5塔內駝峰效應示意圖	60
圖4. 6 塔內每段之填料高度	61
圖4. 7 各流速下之塔內示意圖	64
圖4. 8 填料資訊設定	74
圖4. 9各段填充床設定	74
圖4. 10含效率模型之蒸餾塔Inside-out方法之求解步驟	75
圖4. 11 BX填料蒸餾塔	81
圖4. 12各分段數之HETPavg	83
圖4. 13塔內氣液相負荷值	84
圖4. 14氣液相擴散係數	84
圖4. 15各板HETP數值	85
圖4. 16各板HTUL與HTUV數值	86
圖4. 17各板壓降	86
圖4. 18塔內分佈(a)溫度(b)液相組成(c)氣相組成	87


 
表目錄
表1. 1實習期間參與工作	2
表2. 1各類型蒸餾塔的適用情況	8
表2. 2各規整填充物的參數計算模型	12
表3. 1平衡常數中各參數數值	21
表3. 2熱焓中各參數數值	23
表3. 3獨立方程式與變數數目	25
表3. 4可選用條件與單位	40
表3. 5塔頂物流模擬結果	45
表3. 6塔底物流模擬結果	45
表3. 7冷凝器操作條件	46
表3. 8再沸器操作條件	46
表3. 9進料組成變化之冷凝器與再沸器操作條件	49
表3. 10進料溫度變化之冷凝器與再沸器操作條件	49
表4. 1 密度參數	67
表4. 2 黏度參數	69
表4. 3液相擴散係數參數	71
表4. 4氣相擴散係數參數	72
表4. 5 表面張力參數	73
表4. 6 BX填料資訊	82

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