課程設(shè)計(jì)--苯-甲苯混合液篩板（浮閥）精餾塔設(shè)計(jì)-文庫(kù)吧
2024-12-29 19:15 本頁(yè)面
【正文】 3.192)983.01(11.78983.0kmolMD=180。+180。=)/(kg3.192)024.01(11.78024.0kmolMW=180。+180。=⑶ 物料衡算 )/( 2433055.8430000000hkmolF=180。180。=總物料衡算 D + W = 苯物料衡算 WDF02.098.0 += 聯(lián)立解得D = Kmol/h W = Kmol/h式中 F原料液流量 D塔頂產(chǎn)品量 W塔底產(chǎn)品量4 塔板數(shù)的計(jì)算根據(jù)苯甲苯的汽液平衡數(shù)據(jù)作yx圖及txy圖，參見(jiàn)下圖。因泡點(diǎn)進(jìn)料，在圖中對(duì)角線自點(diǎn)e（,）作垂線即為q線，該線與平衡線的交點(diǎn)坐標(biāo)為yq= ,xq= ,此即最小回流比時(shí)操作線與平衡線的交點(diǎn)坐標(biāo)。依最小回流比計(jì)算式： Rmin = ( xD yq ) / ( yq xq ) 代入數(shù)據(jù)得：Rmin= , R = 2Rmin= 5 全塔效率ET根據(jù)塔頂、塔底液相組成查上圖txy，℃，該溫度下進(jìn)料液相平均黏度為：μm = +（）μB = mPa˙s故 ET = – = = 52％6 實(shí)際塔板數(shù)精餾段：N1 =4/ ≈8層提餾段：N2 =7/ ≈14層7 精餾塔的氣、液相負(fù)荷 L = RD = = kmol/hV = (R+1)D = = kmol/hL’ = RD + qF = kmol/hV’ = (R+1)D – (1q)F = kmol/h(8) 精餾操作方程： 提溜段方程： 、 精餾段工藝條件及有關(guān)物性的計(jì)算⑴ 操作壓力的計(jì)算塔頂操作壓力：PD = + 4 = kpa 每層塔板壓降：ΔP = kpa 進(jìn)料板的壓力：PF = + 8 = kpa 精餾段平均操作壓力：Pm =（ + ）/ 2 = kpa ⑵ 操作溫度的計(jì)算安托因方程： lg P0 = A – B / (t + C) ABC苯甲苯 對(duì)苯甲苯可看作理想物系，并查設(shè)計(jì)手冊(cè)得：α = x1 = y1 / (y1 –(1 –y1)) y1 = xD x1 = t = B/（A lgP0） C PD0 = PDy1 / x1 = kpa tD = / ( – ) – = ℃同樣,根據(jù) yn+1 = + xn = yn / (yn +α(1 yn)) 解得：y1 = xD = x1 = y2 = x2 = y3 = x3 = y4 = x4 = y5 = x5 = y6 = x6 = PF0 = / = kpa tF = / ( – ) – = ℃ 精餾段平均溫度：tm = ( + ) / 2 = ℃ ⑶ 平均相對(duì)分子質(zhì)量計(jì)算 塔頂 xD = y1 = x1 = , 則 進(jìn)料板 yF = xF = , 則 )/(35.7813.92)774.01(11.78774.0m,kmolkgMFV=180。+180。= )/(07.8513.92)504.01(11.78504.0m,kmolkgMFL=180。+180。= 則，精餾段平均相對(duì)分子質(zhì)量 MVFm = ( + ) / 2 = kg/kmol MLFm = ( + ) / 2 = kg/kmol ⑷ 平均密度計(jì)算① 液相密度液相平均密度依下式計(jì)算，即 1/ρLm = αA /ρLA + αB /ρLB （α 為質(zhì)量分?jǐn)?shù)）塔頂液相平均密度的計(jì)算 1/ρLMD = + ：ρLMD = kg/m3 進(jìn)料板 xF = αA = () / ( + ) = 1/ρLMF = + (1 – )/ ρLMF = kg/m3 ② 氣相密度ρVM = pMm,1/RT = (( + ))= kg/m3 ⑸ 液體表面張力 σm = ∑xiσi σmD = + = mN/m σmF = + = mN/m 則，精餾段平均表面張力為： σm（1） = （ + ）/2 = ⑹ 液體黏度 μLm = ∑xiμi μLD = + = μLF = + = 則，精餾段平均液相黏度為： μLm = （ + ）/2 = 塔和塔板主要工藝尺寸計(jì)算
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