化工畢業(yè)設(shè)計(jì)題目

題目一：苯-氯苯精餾塔工藝設(shè)計(jì)與原料液預(yù)熱器選型設(shè)計(jì)〔一〕設(shè)計(jì)題目*化工廠擬采用一板式塔別離苯－氯苯混合液：生產(chǎn)能力為年產(chǎn)70000噸99%的氯苯產(chǎn)品；進(jìn)精餾塔的料液含氯苯40%〔質(zhì)量分?jǐn)?shù)下同〕其余為苯；塔頂?shù)穆缺胶坎坏酶哂?%；殘液中氯苯含量不得低于99%；料液初始溫度為30℃用流量為20000kg/h、溫度為160 C的中壓熱水加熱至沸點(diǎn)進(jìn)料試根據(jù)工藝要求進(jìn)展：〔1〕板式精餾塔的工藝設(shè)計(jì)；〔2〕標(biāo)準(zhǔn)列管式原料預(yù)熱器的選型設(shè)計(jì)〔二〕操作條件.塔頂壓強(qiáng)4kPa〔表壓〕；.進(jìn)料熱狀況泡點(diǎn)進(jìn)料；.回流比1.8Rmin；.塔釜加熱蒸汽壓力0.5MPa〔表壓〕；.單板壓降不大于0.7kPa;.年工作日300天每天24小時(shí)連續(xù)運(yùn)行〔三〕設(shè)計(jì)容.設(shè)計(jì)方案確實(shí)定及工藝流程的說明；.塔的工藝計(jì)算；.塔和塔板主要工藝構(gòu)造的設(shè)計(jì)計(jì)算；.塔流體力學(xué)性能的設(shè)計(jì)計(jì)算；.塔板負(fù)荷性能圖的繪制；.塔的工藝計(jì)算結(jié)果匯總一覽表；.生產(chǎn)工藝流程圖及精餾塔工藝條件圖的繪制；.對(duì)本設(shè)計(jì)的評(píng)述或?qū)τ嘘P(guān)問題的分析與討論〔四〕根底數(shù)據(jù).組分的飽和蒸汽壓〔mmHg〕溫度〔℃〕8090100110120130131.8苯760102513501760225028402900氯苯148205293400543719760.組分的液相密度〔kg/m3〕溫度〔℃〕8090100110120130苯817805793782770757氯苯1039102810181008997985純組分在任何溫度下的密度可由下式計(jì)算苯 推薦：氯苯 推薦：式中的t為溫度.組分的外表力〔mN/m〕溫度〔℃〕8085110115120131苯21.220.617.316.816.315.3氯苯26.125.722.722.221.620.4雙組分混合液體的外表力可按下式計(jì)算：〔為A、B組分的摩爾分率〕.氯苯的汽化潛熱常壓沸點(diǎn)下的汽化潛熱為35.3×103kJ∕kmol純組分的汽化潛熱與溫度的關(guān)系可用下式表示：〔氯苯的臨界溫度：〕.其他物性數(shù)據(jù)可查化工原理附錄題目二：苯-氯苯精餾塔工藝設(shè)計(jì)與塔頂冷凝器選型設(shè)計(jì)〔一〕設(shè)計(jì)題目*化工廠擬采用一板式塔別離苯－氯苯混合液：生產(chǎn)能力為年產(chǎn)65000噸99%的氯苯產(chǎn)品；進(jìn)精餾塔的料液含氯苯45%〔質(zhì)量分?jǐn)?shù)下同〕其余為苯；塔頂?shù)穆缺胶坎坏酶哂?%；殘液中氯苯含量不得低于99%；塔頂冷凝器用流量為30000kg/h、溫度為30 ℃的冷水冷卻試根據(jù)工藝要求進(jìn)展：〔1〕板式精餾塔的工藝設(shè)計(jì)；〔2〕標(biāo)準(zhǔn)列管式塔頂冷凝器的選型設(shè)計(jì)〔二〕操作條件.塔頂壓強(qiáng)4kPa〔表壓〕；.進(jìn)料熱狀況泡點(diǎn)進(jìn)料；.回流比1.8Rmin；.塔釜加熱蒸汽壓力0.5MPa〔表壓〕；.單板壓降不大于0.7kPa;.年工作日300天每天24小時(shí)連續(xù)運(yùn)行〔三〕設(shè)計(jì)容.設(shè)計(jì)方案確實(shí)定及工藝流程的說明；.塔的工藝計(jì)算；.塔和塔板主要工藝構(gòu)造的設(shè)計(jì)計(jì)算；.塔流體力學(xué)性能的設(shè)計(jì)計(jì)算；.塔板負(fù)荷性能圖的繪制；.塔的工藝計(jì)算結(jié)果匯總一覽表；.生產(chǎn)工藝流程圖及精餾塔工藝條件圖的繪制；.對(duì)本設(shè)計(jì)的評(píng)述或?qū)τ嘘P(guān)問題的分析與討論〔四〕根底數(shù)據(jù)1.組分的飽和蒸汽壓〔mmHg〕溫度〔℃〕8090100110120130131.8苯760102513501760225028402900氯苯1482052934005437197602.組分的液相密度〔kg/m3〕溫度〔℃〕8090100110120130苯817805793782770757氯苯1039102810181008997985純組分在任何溫度下的密度可由下式計(jì)算苯氯苯推薦：推薦：式中的t為溫度℃.組分的外表力〔mN/m〕溫度〔℃〕8085110115120131苯21.220.617.316.816.315.3氯苯26.125.722.722.221.620.4雙組分混合液體的外表力可按下式計(jì)算：〔為A、B組分的摩爾分率〕.氯苯的汽化潛熱常壓沸點(diǎn)下的汽化潛熱為35.3×103kJ∕kmol純組分的汽化潛熱與溫度的關(guān)系可用下式表示：〔氯苯的臨界溫度：〕.其他物性數(shù)據(jù)可查化工原理附錄題目三：苯-氯苯精餾塔工藝設(shè)計(jì)與塔底再沸器選型設(shè)計(jì)〔一〕設(shè)計(jì)題目*化工廠擬采用一板式塔別離苯－氯苯混合液：生產(chǎn)能力為年產(chǎn)65000噸99%的氯苯產(chǎn)品；進(jìn)精餾塔的料液含氯苯35%〔質(zhì)量分?jǐn)?shù)下同〕其余為苯；塔頂?shù)穆缺胶坎坏酶哂?%；殘液中氯苯含量不得低于99%；塔底再沸器用流量為27000kg/h、溫度為150℃的中壓熱水加熱試根據(jù)工藝要求進(jìn)展：〔1〕板式精餾塔的工藝設(shè)計(jì)；〔2〕標(biāo)準(zhǔn)列管式塔底再沸器的選型設(shè)計(jì)〔二〕操作條件.塔頂壓強(qiáng)4kPa〔表壓〕；.進(jìn)料熱狀況泡點(diǎn)進(jìn)料；.回流比1.8Rmin；.塔釜加熱蒸汽壓力0.5MPa〔表壓〕；.單板壓降不大于0.7kPa；.年工作日300天每天24小時(shí)連續(xù)運(yùn)行〔三〕設(shè)計(jì)容.設(shè)計(jì)方案確實(shí)定及工藝流程的說明；.塔的工藝計(jì)算；.塔和塔板主要工藝構(gòu)造的設(shè)計(jì)計(jì)算；.塔流體力學(xué)性能的設(shè)計(jì)計(jì)算；.塔板負(fù)荷性能圖的繪制；.塔的工藝計(jì)算結(jié)果匯總一覽表；.生產(chǎn)工藝流程圖及精餾塔工藝條件圖的繪制；.對(duì)本設(shè)計(jì)的評(píng)述或?qū)τ嘘P(guān)問題的分析與討論〔四〕根底數(shù)據(jù).組分的飽和蒸汽壓〔mmHg〕溫度〔℃〕8090100110120130131.8苯760102513501760225028402900氯苯148205293400543719760.組分的液相密度〔kg/m3〕溫度〔℃〕8090100110120130苯817805793782770757氯苯1039102810181008997985純組分在任何溫度下的密度可由下式計(jì)算苯 推薦：氯苯 推薦：式中的t為溫度℃.組分的外表力〔mN/m〕溫度〔℃〕8085110115120131苯21.220.617.316.816.315.3氯苯26.125.722.722.221.620.4雙組分混合液體的外表力可按下式計(jì)算：〔為A、B組分的摩爾分率〕.氯苯的汽化潛熱常壓沸點(diǎn)下的汽化潛熱為35.3×103kJ∕kmol純組分的汽化潛熱與溫度的關(guān)系可用下式表示：〔氯苯的臨界溫度：〕.其他物性數(shù)據(jù)可查化工原理附錄題目四：苯-乙苯精餾塔工藝設(shè)計(jì)與原料液預(yù)熱器選型設(shè)計(jì)〔一〕設(shè)計(jì)題目*化工廠擬采用一板式塔別離苯－甲苯混合液：生產(chǎn)能力為年產(chǎn)34000噸98%的乙苯產(chǎn)品；進(jìn)精餾塔的料液含乙苯40%〔質(zhì)量分?jǐn)?shù)下同〕其余為苯；塔頂?shù)囊冶胶坎坏酶哂?%；殘液中乙苯含量不得低于98%；料液初始溫度為30℃用流量為11500kg/h、溫度為160 C的中壓熱水加熱至沸點(diǎn)進(jìn)料試根據(jù)工藝要求進(jìn)展：〔1〕板式精餾塔的工藝設(shè)計(jì)；〔2〕標(biāo)準(zhǔn)列管式原料預(yù)熱器的選型設(shè)計(jì)〔二〕操作條件.塔頂壓力 4kPa〔表壓〕.進(jìn)料熱狀態(tài)泡點(diǎn)進(jìn)料.回流比2倍最小回流比.加熱蒸氣壓力0.5MPa〔表壓〕.單板壓降≤0.7kPa〔三〕塔板類型板式塔〔四〕工作日每年工作日為300天每天24小時(shí)連續(xù)運(yùn)行〔五〕主要物性數(shù)據(jù)1、苯、乙苯的物理性質(zhì)工程分子式分子量沸點(diǎn)℃臨界溫度℃臨界壓強(qiáng)Pa苯AC6H678.1180.1288.56833.4乙苯BC8H10106.16136.2348.574307.72、苯、t/℃2040608010012014028.826.2523.7421.2718.8516.4914.1729.327.1425.0122.9220.8518.8116.823、苯、t/℃0204060801001201400.7420.6380.485乙苯在*些溫度下的外表力乙苯在*些溫度下的粘度0.3810.3080.2550.2150.1840.8740.6660.5250.4260.3540.3000.2590.226苯、乙苯的液相密度t/℃20406080100120140877.4857.3836.6815.0792.5768.9744.1867.7849.8931.8913.6795.2776.2756.7不同塔徑的板間距塔徑D/m0.3-0.50.5-0.80.8-1.61.6-2.44.0板間距HT/mm200-300250-350300-450350-600400-600題目五：苯-乙苯精餾塔工藝設(shè)計(jì)與塔頂冷凝器選型設(shè)計(jì)〔一〕設(shè)計(jì)題目*化工廠擬采用一板式塔別離苯－甲苯混合液：生產(chǎn)能力為年產(chǎn)40000噸98%的乙苯產(chǎn)品；進(jìn)精餾塔的料液含乙苯50%〔質(zhì)量分?jǐn)?shù)下同〕其余為苯；塔頂?shù)囊冶胶坎坏酶哂?%；殘液中乙苯含量不得低于98%；塔頂冷凝器用流量為16000kg/h、溫度為30 ℃的冷水冷卻試根據(jù)工藝要求進(jìn)展：〔1〕板式精餾塔的工藝設(shè)計(jì)；〔2〕標(biāo)準(zhǔn)列管式塔頂冷凝器的選型設(shè)計(jì)〔二〕操作條件.塔頂壓力 4kPa〔表壓〕.進(jìn)料熱狀態(tài)泡點(diǎn)進(jìn)料.回流比2倍最小回流比.加熱蒸氣壓力0.5MPa〔表壓〕.單板壓降≤0.7kPa〔三〕塔板類型板式塔〔四〕工作日每年工作日為300天每天24小時(shí)連續(xù)運(yùn)行〔五〕主要物性數(shù)據(jù)苯、乙苯的物理性質(zhì)工程分子式分子量沸點(diǎn)℃臨界溫度℃臨界壓強(qiáng)Pa苯AC6H678.1180.1288.56833.4乙苯BC8H10106.16136.2348.574307.7苯、乙苯在*些溫度下的外表力t/℃2040608010012014028.826.2523.7421.2718.8516.4914.1729.327.1425.0122.9220.8518.8116.82苯、乙苯在*些溫度下的粘度t/℃0204060801001201400.7420.6380.4850.3810.3080.2550.2150.1840.8740.6660.5250.4260.3540.3000.2590.226苯、乙苯的液相密度t/℃20406080100120140877.4857.3836.6815.0792.5768.9744.1867.7849.8931.8913.6795.2776.2756.7不同塔徑的板間距塔徑D/m0.3-0.50.5-0.80.8-1.61.6-2.44.0板間距HT/mm200-300250-350300-450350-600400-600題目六：苯-乙苯精餾塔工藝設(shè)計(jì)與塔底再沸器選型設(shè)計(jì)〔一〕設(shè)計(jì)題目*化工廠擬采用一板式塔別離苯－甲苯混合液：生產(chǎn)能力為年產(chǎn)35000噸98%的乙苯產(chǎn)品；進(jìn)精餾塔的料液含乙苯45%〔質(zhì)量分?jǐn)?shù)下同〕其余為苯；塔頂?shù)囊冶胶坎坏酶哂?%；殘液中乙苯含量不得低于98%；塔底再沸器用流量為14000 kg/h、溫度為150 ℃的中壓熱水加熱試根據(jù)工藝要求進(jìn)展：〔1〕板式精餾塔的工藝設(shè)計(jì)；〔2〕標(biāo)準(zhǔn)列管式塔底再沸器的選型設(shè)計(jì)〔二〕操作條件.塔頂壓力 4kPa〔表壓〕.進(jìn)料熱狀態(tài)泡點(diǎn)進(jìn)料.回流比2倍最小回流比.加熱蒸氣壓力0.5MPa〔表壓〕.單板壓降≤0.7kPa〔三〕塔板類型板式塔〔四〕工作日每年工作日為300天每天24小時(shí)連續(xù)運(yùn)行〔五〕主要物性數(shù)據(jù).苯、乙苯的物理性質(zhì)工程分子式分子量沸點(diǎn)℃臨界溫度℃臨界壓強(qiáng)Pa苯AC6H678.1180.1288.56833.4乙苯BC8H10106.16136.2348.574307.7.苯、乙苯在*些溫度下的外表力t/℃2040608010012014028.826.2523.7421.2718.8516.4914.1729.327.1425.0122.9220.8518.8116.82.苯、乙苯在*些溫度下的粘度t/℃0204060801001201400.7420.6380.4850.3810.3080.2550.2150.1840.8740.6660.5250.4260.3540.3000.2590.226.苯、乙苯的液相密度t/℃20406080100120140877.4857.3836.6815.0792.5768.9744.1867.7849.8931.8913.6795.2776.2756.7.不同塔徑的板間距塔徑D/m0.3-0.50.5-0.80.8-1.61.6-2.44.0板間距HT/mm200-300250-350300-450350-600400-600題目七：乙醇－水精餾塔工藝設(shè)計(jì)與原料液預(yù)熱器選型設(shè)計(jì)〔一〕設(shè)計(jì)題目*化工廠擬采用一板式塔別離乙醇－水混合液：年處理原料能力為1700噸；進(jìn)精餾塔的料液含乙醇45%〔質(zhì)量分?jǐn)?shù)下同〕；塔頂?shù)囊掖己繛?3%；殘液中乙醇含量不得高于5%；料液初始溫度為30℃用流量為1500kg/h、溫度為160 C的中壓熱水加熱至沸點(diǎn)進(jìn)料試根據(jù)工藝要求進(jìn)展：〔1〕板式精餾塔的工藝設(shè)計(jì)；〔2〕標(biāo)準(zhǔn)列管式原料液預(yù)熱器的選型設(shè)計(jì)〔二〕操作條件.塔頂壓力 4kPa〔表壓〕.進(jìn)料熱狀態(tài)泡點(diǎn)進(jìn)料.回流比1.6倍最小回流比.加熱蒸氣壓力0.5MPa〔表壓〕.單板壓降≤0.7kPa〔三〕工作日每年工作日為300天每天24小時(shí)連續(xù)運(yùn)行〔四〕主要物性數(shù)據(jù).乙醇和水的物理性質(zhì)〔表一〕工程分子量沸點(diǎn)（℃）臨界溫度（℃）臨界壓強(qiáng)（Kpa）乙醇46.0778.3240.776.148水18.01100373.9122.05.乙醇和水的粘度〔表二〕溫度(C)2030405060708090100110水的粘度(mpa.s)1.0020.8020.6620.5920.4690.4000.3300.3180.2480.259乙醇的粘度(mpa.s)1.221.000.830.690.380.480.4150.3510.3050.262.乙醇和水的外表力〔表三〕溫度(℃)2030405060708090100110水的外表力（mN）72.771.069.367.766.064.362.760.158.456.8乙醇的外表力（mN）22.321.220.419.818.818.017.116.215.214.4.乙醇和水的密度〔表四〕溫度（C）2030405060708090100110乙醇的密度（kg∕m3）795785777765755746735730716703水的密度(kg∕m3)998.2995.7992.2988.1983.2977.8971.8965.3958.4951.05.常壓下乙醇--水的汽液平衡數(shù)據(jù)〔表五〕沸點(diǎn)t/乙醇分子/%〔液相〕乙醇分子/%〔氣相〕沸點(diǎn)t/乙醇分子/%〔液相〕乙醇分子/%〔氣相〕10099.999.899.799.599.29998.7597.6495.895.591.389.087.986.785.385.284.183.7582.782.382.300.0040.040.050.120.230.310.390.791.611.904.167.217.419.6612.3812.6416.6117.4123.3725.7526.0800.0530.510.771.572.903.725458.7616.3417.0029.9238.9139.6143.7547.0447.4950.8951.6754.4555.7455.808281.581.380.780.680.179.8579.879.779.579.379.278.9578.7578.7478.678.478.2778.278.1578.1527.332.7333.2439.6542.0948.9252.6850.7951.9861.0257.3265.6468.9272.3674.7275.9979.8283.8785.9789.4189.4356.4459.2658.7861.2262.2264.7066.2865.6465.9970.2968.4172.7174.6976.9378.1579.2681.8384.9186.4089.4189.43題目八：乙醇－水精餾塔工藝設(shè)計(jì)與塔頂冷凝器選型設(shè)計(jì)〔一〕設(shè)計(jì)題目*化工廠擬采用一板式塔別離乙醇－水混合液：年處理原料能力為2000噸；進(jìn)精餾塔的料液含乙醇40%〔質(zhì)量分?jǐn)?shù)下同〕；塔頂?shù)囊掖己繛?4%；殘液中乙醇含量不得高于4%；塔頂冷凝器用流量為1600kg/h、溫度為30℃的冷水冷卻試根據(jù)工藝要求進(jìn)展：〔1〕板式精餾塔的工藝設(shè)計(jì)；〔2〕標(biāo)準(zhǔn)列管式塔頂冷凝器的選型設(shè)計(jì)〔二〕操作條件.塔頂壓力 4kPa〔表壓〕.進(jìn)料熱狀態(tài)泡點(diǎn)進(jìn)料.回流比1.6倍最小回流比.加熱蒸氣壓力0.5MPa〔表壓〕.單板壓降≤0.7kPa〔三〕工作日每年工作日為300天每天24小時(shí)連續(xù)運(yùn)行〔四〕主要物性數(shù)據(jù).乙醇和水的物理性質(zhì)〔表一〕工程分子量沸點(diǎn)（℃）臨界溫度（C）臨界壓強(qiáng)（Kpa）乙醇46.0778.3240.776.148水18.01100373.9122.05.乙醇和水的粘度〔表二〕溫度（℃）2030405060708090100110水的粘度（mpa.s）1.0020.8020.6620.5920.4690.4000.3300.3180.2480.259乙醇的粘度(mpa.s)1.221.000.830.690.380.480.4150.3510.3050.262.乙醇和水的外表力〔表三〕溫度(℃)2030405060708090100110水的外表力(mN)72.771.069.367.766.064.362.760.158.456.8乙醇的外表力(mN)22.321.220.419.818.818.017.116.215.214.4.乙醇和水的密度〔表四〕溫度(C)2030405060708090100110乙醇的密度(kg∕m3)795785777765755746735730716703水的密度(kg∕m3)998.2995.7992.2988.1983.2977.8971.8965.3958.4951.0.常壓下乙醇--水的汽液平衡數(shù)據(jù)〔表五〕沸點(diǎn)t/乙醇分子/%〔液相〕乙醇分子/%〔氣相〕沸點(diǎn)t/乙醇分子/%〔液相〕乙醇分子/%〔氣相〕10099.999.899.799.599.29998.7597.6495.895.591.389.087.986.785.385.284.183.7582.782.382.300.0040.040.050.120.230.310.390.791.611.904.167.217.419.6612.3812.6416.6117.4123.3725.7526.0800.0530.510.771.572.903.725458.7616.3417.0029.9238.9139.6143.7547.0447.4950.8951.6754.4555.7455.808281.581.380.780.680.179.8579.879.779.579.379.278.9578.7578.7478.678.478.2778.278.1578.1527.332.7333.2439.6542.0948.9252.6850.7951.9861.0257.3265.6468.9272.3674.7275.9979.8283.8785.9789.4189.4356.4459.2658.7861.2262.2264.7066.2865.6465.9970.2968.4172.7174.6976.9378.1579.2681.8384.9186.4089.4189.43題目九：乙醇－水精餾塔工藝設(shè)計(jì)與塔底再沸器選型設(shè)計(jì)〔一〕設(shè)計(jì)題目*化工廠擬采用一板式塔別離乙醇－水混合液：年處理原料能力為1900噸；進(jìn)精餾塔的料液含乙醇35%〔質(zhì)量分?jǐn)?shù)下同〕；塔頂?shù)囊掖己繛?5%；殘液中乙醇含量不得高于5%；塔底再沸器用流量為

kg/h、溫度為150 ℃的中壓熱水加熱〔二〕操作條件.塔頂壓力 4kPa〔表壓〕.進(jìn)料熱狀態(tài)泡點(diǎn)進(jìn)料.回流比1.6倍最小回流比.加熱蒸氣壓力0.5MPa〔表壓〕.單板壓降≤0.7kPa〔三〕工作日每年工作日為300天每天24小時(shí)連續(xù)運(yùn)行〔四〕主要物性數(shù)據(jù).乙醇和水的物理性質(zhì)〔表一〕工程分子量沸點(diǎn)（℃）臨界溫度（C）臨界壓強(qiáng)（Kpa）乙醇46.0778.3240.776.148水18.01100373.9122.05.乙醇和水的粘度〔表二〕溫度（℃）20304050607080901001400110水的粘度(mpa.s)1.0020.8020.6620.5920.4690.4000.3300.3180.2480.259乙醇的粘度(mpa.s)1.221.000.830.690.380.480.4150.3510.3050.262.乙醇和水的外表力〔表三〕溫度(℃)2030405060708090100110水的外表力(mN)72.771.069.367.766.064.362.760.158.456.8乙醇的外表力(mN)22.321.220.419.818.818.017.116.215.214.4.乙醇和水的密度〔表四〕溫度(C)2030405060708090100110乙醇的密度(kg∕m3)795785777765755746735730716703水的密度(kg∕m3)998.2995.7992.2988.1983.2977.8971.8965.3958.4951.0.常壓下乙醇--水的汽液平衡數(shù)據(jù)〔表五〕沸點(diǎn)t/乙醇分子/%〔液相〕乙醇分子/%〔氣相〕沸點(diǎn)t/乙醇分子/%〔液相〕乙醇分子/%〔氣相〕10099.999.899.799.599.29998.7597.6495.895.591.389.087.986.785.385.284.183.7582.782.382.300.0040.040.05