本研究旨在探討於成本固定下，逆流式Frazier型平板熱擴散塔組中四項設計條件(傾斜角、板間距、塔數及長寬比)對分離效率之影響。結果發現四項設計條件中，無兩項或兩項以上的最佳設計條件同時存在。至於每一單獨項的最佳設計條件計算公式，以及其對應的最大分離度的計算公式，可順利推導而出，而以其他三項設計條件為參數。文中並列舉兩個範例，利用其結果來比較四項最佳設計條件下的分離效率。結果發現：對分離苯-正庚烷混合物而言，組立一逆流式Frazier型平板熱擴散塔組的最佳方法為，採取最佳的板間距，並令傾斜角、長寬比及塔數在不違反常態之下盡量加大;對分離水同位素混合物而言，應該採取最佳的傾斜角，並令板間距、長寬比及塔數在不違反常態之下盡量加大。

The effect of four design conditions ( angle of inclination, plate spacing, column number and plate aspect ratio) on thermal diffusion performances in the countercurrent-flow Frazier scheme at fixed expense have been investigated. The equations for predicting each optimal design condition for the corresponding maximum separation have been derived with other three design conditions as parameters. However, there are no two optimal design conditions existing simultaneously for the best performance. The limitations of practical applications were also delineated. Two numerical examples were presented for illustration, and the performances obtained at each optimal design condition were compared. It was found that for separation of benzene-n-heptane system, the best way to construct a countercurrent-flow Frazier scheme is designed at the optimal plate spacing with larger inclination angle, larger plate aspect ratio and larger number of columns. For separation of water-isotope mixture, the best way to construct a countercurrent-flow Frazier scheme is designed at the optimal inclination angle with larger plate spacing, larger plate aspect ratio and larger number of columns.

中文摘要                                                  I
英文摘要                                                 II
目錄                                                    III
 圖目錄                                                VI
 表目錄                                              VII
第一章 緒論	1
1-1 熱擴散沿革	1
1-2 熱擴散的應用	7
1-3 重水的用途	8
1-4 研究動機與目的	21
第二章 分離理論分析	23
2-1 熱擴散塔之現象	23
2-2 等塔高Frazier裝置中的分離度公式	25
2-2-1 一般二成份系統	28
2-2-2 水同位素中回收重水系統	30
2-3傾斜式等塔高Frazier裝置的最佳設計之分離度公式	31
2-3-1傾斜式熱擴散塔之最佳傾斜角度 及其最大分離度	33
2-3-2傾斜式熱擴散塔之最佳板間距 及其最大分離度	33
2-3-3傾斜式熱擴散塔之最佳長寬比 及其最大分離度	34
2-3-4傾斜式熱擴散塔之最佳塔數 及其最大分離度	34
第三章 傾斜式等塔高Frazier裝置之最佳設計	35
3-1 前言	35
3-2一般二成份系統	37

3-2-1計算範例	37
3-2-2 傾斜式等塔高Frazier熱擴散塔之最佳傾斜角度(θ*)及  其分離度	38
3-2-3 傾斜式等塔高Frazier熱擴散塔之最佳板間距(2ω*)及其分離度	44
3-2-4 傾斜式等塔高Frazier熱擴散塔之最佳長寬比(ξ*)及其分離度	52
3-2-5 傾斜式等塔高Frazier熱擴散塔之最佳塔數(N*)及其分離度	57
3-3水同位素中回收重水系統	63
3-3-1計算範例	63
3-3-2傾斜式等塔高Frazier熱擴散塔之最佳傾斜角度(θ*)其分離度	64
3-3-3傾斜式等塔高Frazier熱擴散塔之最佳板間距(2ω*)及其分離度	70
3-3-4傾斜式等塔高Frazier熱擴散塔之最佳長寬比(ξ*)及其分離度	78
3-3-5傾斜式等塔高Frazier熱擴散塔之最佳塔數(N*)及其分離度	83
第四章 結論	89
符號說明	93
參考文獻	98






















圖目錄
圖1-1 Ludwing之實驗裝置示意圖	1
圖1-2 Dufour效應，因濃度梯度產生瞬時溫度梯度示意圖	2
圖1-3 Soret效應，因溫度梯度產生濃度梯度示意圖	3
圖1-4水平平板式熱擴散塔裝置示意圖	4
圖1-5熱重力式熱擴散塔裝置示意圖	5
圖1-6續流效應(Cascading Effect)示意圖	6
圖1-7核分裂與核融合反應	14
圖2-1熱重力式熱擴散塔裝置圖	                          24
圖2-2 Frazier裝置圖	25
圖2-3傾斜式等塔高Frazier之裝置圖	32
圖4-1一般二成份系統中最佳條件下之流速v.s.改良率	  91
圖4-2水同位素中回收重水系統中最佳條件下之流速v.s.改良率	92












表目錄
表1-1普通水與重水的比較[44]	10
表1-2氘、氚及氦3之同位素所形成的核融合反應	17
表3-1 分離苯與正庚烷在最佳傾斜角度下的極限流速值(σ, (g/min)): (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	  39
表3-2 分離苯與正庚烷在最佳傾斜角度下的塔寬(B, cm):           (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	40
表3-3 分離苯與正庚烷在最佳傾斜角度下的塔寬高(h, cm):        (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	41
表3-4 分離苯與正庚烷之最佳傾斜角度(θ*): (a) (2ω)=0.09cm ;    (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	42
表3-5 分離苯與正庚烷在最佳傾斜角度下的分離度 :            (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm    43
表3-6 分離苯與正庚烷在最佳傾斜角度、長寬比及塔數下的溫度差(ΔT): (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	45
表 3-7 分離苯與正庚烷在最佳板間距下的溫度差(ΔT): (a) θ=75° ; (b) θ=80° ; (c) θ=85°	46
表3-8 分離苯與正庚烷在最佳板間距下的塔寬(B, cm): (a) θ=75° ;  (b) θ=80° ; (c) θ=85°	47
表3-9 分離苯與正庚烷在最佳板間距下的塔高(h, cm): (a) θ=75° ;  (b) θ=80° ; (c) θ=85°	48
表 3-10分離苯與正庚烷之最佳板間距(2ω*): (a) θ=75° ;        (b) θ=80 ; (c) θ=85°	49
表3-11 分離苯與正庚烷在ξ=10的最佳板間距下之分離度 :      (a) θ=75° ; (b) θ=80° ; (c) θ=85°	50
表3-12 分離苯與正庚烷在ξ=20的最佳板間距下之分離度 :      (a) θ=75° ; (b) θ=80° ; (c) θ=85°	51
表3-13 分離苯與正庚烷在最佳長寬比下的塔寬(B, cm):           (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	53
表3-14 分離苯與正庚烷在最佳長寬比下的塔高(h, cm):           (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	54
表3-15 分離苯與正庚烷之最佳長寬比(ξ*): (a) (2ω)=0.09cm ;     (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	55
表3-16 分離苯與正庚烷在最佳長寬比下的分離度 :             (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	56
表3-17 分離苯與正庚烷在最佳塔數下的塔寬(B, cm):             (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm    58
表3-18 分離苯與正庚烷在最佳塔數下的塔高(h, cm):             (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	59
表3-19 分離苯與正庚烷之最佳塔數(N*): (a) (2ω)=0.09cm ;        (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	60
表3-20 分離苯與正庚烷在ξ=10的最佳塔數下之分離度 :        (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	61
表3-21 分離苯與正庚烷在ξ=20的最佳塔數下之分離度 :        (a) (2ω)=0.09cm ; (b) (2ω)=0.095cm ; (c) (2ω)=0.1cm	62
表3-22 回收重水系統在最佳傾斜角度下的極限流速值(σ, (g/hr)):   (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	65
表3-23 回收重水系統在最佳傾斜角度下的塔寬(B, cm):           (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	66
表3-24 回收重水系統在最佳傾斜角度下的塔寬高(h, cm):         (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	67
表3-25 回收重水系統之最佳傾斜角度(θ*): (a) (2ω)=0.0406cm ;   (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	68
表3-26 回收重水系統在最佳傾斜角度下的分離度 :             (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	69
表3-27 回收重水系統在最佳傾斜角度、長寬比及塔數下的溫度差 (ΔT): (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ;           (c) (2ω)=0.0606cm	71
表3-28 回收重水系統在最佳板間距下的溫度差(ΔT): (a) θ=75° ; (b) θ=80° ; (c) θ=85°	72
表3-29 回收重水系統在最佳板間距下的塔寬(B, cm): (a) θ=75° ;  (b) θ=80° ; (c) θ=85°	73
表3-30 回收重水系統在最佳板間距下的塔高(h, cm): (a) θ=75° ;  (b) θ=80° ; (c) θ=85°	74
表3-31 回收重水系統之最佳板間距(2ω*): (a) θ=75° ; (b) θ=80° ; (c) θ=85°	75
表3-32 回收重水系統在ξ=10的最佳板間距下之分離度 :        (a) θ=75° ; (b) θ=80° ; (c) θ=85°	76
表3-33 回收重水系統在ξ=20的最佳板間距下之分離度 :        (a) θ=75° ; (b) θ=80° ; (c) θ=85°	77
表3-34回收重水系統在最佳長寬比下的塔寬(B, cm):             (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	79
表3-35回收重水系統在最佳長寬比下的塔高(h, cm):              (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	80
表3-36回收重水系統之最佳長寬比(ξ*):(a) (2ω)=0.0406cm ;      (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	81
表3-37回收重水系統在最佳長寬比下的分離度 :(a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	82
表3-38回收重水系統在最佳塔數下的塔寬(B, cm):               (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	84
表3-39回收重水系統在最佳塔數下的塔高(h, cm):                (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	85
表3-40 回收重水系統之最佳塔數(N*):(a) (2ω)=0.0406cm ;        (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	86
表3-41回收重水系統在ξ=10的最佳塔數下之分離度 :           (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	87
表3-42回收重水系統在ξ=20的最佳塔數下之分離度 :           (a) (2ω)=0.0406cm ; (b) (2ω)=0.0506cm ; (c) (2ω)=0.0606cm	  	88

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