精餾塔的操作與塔效率的測(cè)定-實(shí)驗(yàn)報(bào)告

精餾塔的操作與塔效率的測(cè)定原始數(shù)據(jù)進(jìn)料溫度：16.8℃塔頂原料塔釜序號(hào)折光率摩爾分率折光率摩爾分率折光率摩爾分率11.36130.9698251.38920.3017971.39130.23262821.36120.971381.38930.2985631.39460.11859131.36130.9698251.38940.2953241.39480.11146941.36110.9729291.3890.3082471.39490.10792、圖解法求理論塔板數(shù)(塔頂組成)(原料液組成)(塔釜組成)回流比：R=22/16=1.375比熱汽化潛熱r1=40.476KJ/molr2=45.9006KJ/mol泡點(diǎn)查得為T(mén)=98.0℃℃（用溫度計(jì)在原料儲(chǔ)罐中測(cè)出）從圖示所得:NT=6塔板效率:T/℃117.60115.00112.50110.00107.50105.00100.00x乙0.00000.03450.06850.10550.14500.18800.2840y乙0.00000.12500.22850.32700.41600.49600.6345T/℃95.0090.0087.5085.0082.5080.0078.30x乙0.39900.53650.61600.70300.79950.90801.0000y乙0.74950.84300.88300.91690.95080.97981.0000圖1泡點(diǎn)溫度圖解法xxf=0.3144T=98.0x乙→圖2圖解法求理論塔板數(shù)繪圖步驟:將講義上給出的相平衡數(shù)據(jù)（T~x~y數(shù)據(jù)中的x~y）標(biāo)繪到x~y坐標(biāo)上，得相平衡曲線；作一條對(duì)角線；從xd、xf、xw作垂直線至對(duì)角線上，交于點(diǎn)a、d、b；在Y軸上標(biāo)出截距為的點(diǎn)，連接此點(diǎn)和a點(diǎn)，得精餾段操作線；過(guò)d點(diǎn)作斜率為K的一條直線交精餾段操作線與c點(diǎn)；連接bc得提餾段操作線；從a點(diǎn)開(kāi)始，在精餾段操作線、提餾段操作線與相平衡曲線之間來(lái)回作階梯，即得理論板數(shù)。aadbc相平衡曲線精餾段操作線提餾段操作線進(jìn)料輔助線↑xw↑xf↑xdT/℃117.60115.00112.50110.00107.50105.00100.00x乙0.00000.03450.06850.10550.14500.18800.2840y乙0.00000.12500.22850.32700.41600.49600.6345T/℃95.0090.0087.5085.0082.5080.0078.30x乙0.39900.53650.61600.70300.79950.90801.0000y乙0.74950.84300.88300.91690.95080.97981.0000

圖1泡點(diǎn)溫度圖解法xfxf=0.