pcd盤來(lái)自移動(dòng)紐曼結(jié)題報(bào)告

低溫甲醇洗裝置流程模擬與開發(fā)研究報(bào)告人：李燕指導(dǎo)教師：孫津生2006.11.1結(jié)題報(bào)告報(bào)告提綱工藝介紹模擬結(jié)果工藝改進(jìn)主要結(jié)論論文提綱低溫甲醇洗凈化法

低溫甲醇洗法是一個(gè)物理吸收和解吸的過(guò)程，采用的吸收介質(zhì)是甲醇。甲醇是一種極性溶劑，對(duì)CO2、H2S、COS等酸性氣體有較強(qiáng)的溶解能力，而H2、CO、CH4等氣體在其中的溶解度甚微。利用甲醇的這種選擇性吸收的特性，在高壓、低溫條件下，甲醇對(duì)CO2、H2S、COS進(jìn)行選擇性吸收，使煤氣得到凈化；低壓、高溫有利于解吸。根據(jù)這種特性，甲醇中溶解氣在解壓、升溫時(shí)又很容易從溶劑中解吸出來(lái)，從而使甲醇得以再生循環(huán)使用。低溫甲醇洗凈化法適用于以煤、重油、瀝青等重質(zhì)烴類為原料的合成氨、羥基合成氣、甲醇合成氣、城市煤氣等氣體凈化。工藝特點(diǎn)優(yōu)點(diǎn)能吸收各種雜質(zhì)有良好的選擇性凈化度高再生好能低溶劑損失小粘度小吸收劑價(jià)廉易得流程操作經(jīng)濟(jì)性強(qiáng)吸收能力強(qiáng)，溶劑循環(huán)量小溶劑的熱穩(wěn)定性和化學(xué)穩(wěn)定性好甲醇與水可以任何比例互溶缺點(diǎn)甲醇毒性強(qiáng)設(shè)備材質(zhì)要求高保冷要求高吸收劑回收要求高甲醇洗塔的模擬甲醇洗塔的模擬熱力學(xué)方程的選擇

甲醇洗塔主要組分有CH3OH、CO2

、H2S、N2、CO、CH4

、H2O、Ar、H2

、COS等10個(gè)，分屬極性物質(zhì)、超臨界組分和締合性組分等，在低溫(－50℃——－60℃)、高壓（35atm左右）下非理想性很強(qiáng)。對(duì)于H2S吸收段和CO2

吸收段采用PRWS、RKSWS、PSRKSR-POLAR進(jìn)行模擬，得到RKSWS與實(shí)際直較接近；對(duì)于V11，由于體系高度非理想液體，選擇NRTL進(jìn)行模擬計(jì)算。甲醇洗塔的模擬熱力學(xué)方程的比較PRWSRKSWSPSRKSR-POLARCH4O6.7E-55.8E-41.76E-51.78E-5CO24.6E-50.11.1E-31.41E-3H20.7230.670.690.677N23.7E-34E-34E-34.1E-3H2S1.5E-87.8E-91.68E-81.7E-8H2O1.01E-82.1E-83.52E-93.1E-9Ar1.23E-31.67E-31.4E-31.4E-3CH44.32E-41.1E-31.1E-31.1E-3CO0.2720.310.3020.315COS4.8E-173.4E-145.5E-172.2E-16TotalFlowkmol/hr4826.6455507.1025261.4825498.649TemperatureK233.042223.506222.1684221.5242以107為衡量標(biāo)準(zhǔn)對(duì)各方程模擬計(jì)算結(jié)構(gòu)進(jìn)行比較甲醇洗塔的模擬二元交互作用參數(shù)的修改

為了使模擬所得結(jié)果與實(shí)際情況相符，對(duì)BinaryInteraction里的RKSWSK-1進(jìn)行修改，Binaryparameters設(shè)定如圖：甲醇洗塔的模擬模擬結(jié)果與工藝包數(shù)據(jù)的比較CH4OCO2H2N2H2SH2OAr103S5.82E-40.330.452.77E-36.05E-83.39E-99.97E-4T5.44E-40.320.462.84E-34.55E-83.58E-91.01E-3107S1.33E-40.0150.674.03E-35.84E-91.66E-81.44E-3T1.63E-40.020.663.98E-36.21E-91.12E-81.43E-3112S0.85860.1343.5E-32.79E-51.69E-71.25E-36.63E-5T0.87330.1222.5E-33.19E-51.92E-71.27E-31.05E-5114S0.83110.1631.98E-34.35E-51.67E-71.21E-31.37E-5T0.83730.1581.69E-33.62E-51.85E-61.21E-31.15E-5116S0.80330.1911.84E-34.08E-51.83E-71.17E-31.28E-5T0.80330.1911.84E-34.04E-41.82E-71.17E-31.27E-5118S0.7870.2072.02E-34.44E-51.43E-31.15E-32.89E-6T0.7870.2061.89E-34.42E-51.43E-31.15E-31.36E-5注：S為模擬計(jì)算值，T為工藝數(shù)據(jù)包值；數(shù)值皆為摩爾百分比。甲醇洗塔的模擬CH4COCOSTotalFlowkmol/hrTemperatureKPressureatm103S8.05E-40.2136.7E-178257.936253.4635.2T8.19E-40.2161E-158047252.435.2107S1.12E-30.3014E-175537.642226.80134.5T1.11E-30.3044.8E-165626.422232.5534.5112S4.47E-52.96E-31E-1511557.84249.057535.0T2.45E-51.9E-31E-1511370252.50235.0114S2.89E-52.47E-31.1E-1511940.5249.525235.1T2.66E-52.1E-31.4E-1511860249.267735.1116S2.8E-52.3E-31.7E-1512366.73250.58135.2T2.8E-52.3E-31.6E-1512358252.115835.2118S2.42E-52.97E-43E-155665.801250.72235.6T3.0E-52.46E-33E-155674.107251.2635.6模擬結(jié)果與工藝包數(shù)據(jù)的比較(續(xù))CO2再生塔的模擬CO2再生塔的模擬模擬結(jié)果與工藝包數(shù)據(jù)的比較CH4OCO2H2N2H2SH2OAr202S2.8E-30.9621.94E-54.12E-27.82E-57E-93E-12T2.66E-30.9631.82E-53.31E-27.09E-58.12E-91.2E-12203S6.42E-40.9782.69E-38.16E-34.05E-69.1E-105.67E-5T9.3E-40.9792.69E-37.29E-32.92E-66.9E-105.68E-5213S0.85490.1447.8E-73.15E-61.89E-71.24E-33.83E-7T0.85590.1435.5E-74.01E-63.1E-71.25E-34.48E-8214S0.83870.1592.15E-91.65E-51.07E-31.22E-32.9E-10T0.83870.1595.86E-95.40E-51.08E-31.22E-34.9E-10311S0.9168.1E-22.9E-92.67E-58E-41.2E-31E-15T0.91957.8E-23.05E-92.67E-58.03E-41.34E-31E-15注：S為模擬計(jì)算值，T為工藝數(shù)據(jù)包值；數(shù)值皆為摩爾百分比。CO2再生塔的模擬CH4COCOSTotalFlowkmol/hrTemperatureKPressureatm202S1.14E-34.4E-75E-1580.40246.92313.42T1.17E-34.48E-73E-1581.41247.33.42203S4.32E-49.7E-32.8E-15325.3825230.62562.94T4.37E-49.7E-34.8E-15325.439229.08912.94213S1.71E-66.74E-61.8E-152105229.12.94T1.55E-68.21E-61.4E-152105229.12.94214S6.61E-62.0E-91.7E-157470.027232.40643.42T6.39E-69.94E-81.6E-1574702303.42311S2.8E-52.3E-31.7E-1511366.73250.5813.42T3.08E-63E-101E-1510790247.33.42模擬結(jié)果與工藝包數(shù)據(jù)的比較(續(xù))CO2再生塔的模擬H2S濃縮塔的模擬H2S濃縮塔的模擬模擬結(jié)果與工藝包數(shù)據(jù)的比較CH4OCO2H2N2H2SH2OAr301ST4.5E-20.8484.47E-37.83E-38.66E-22.36E-56.8E-11302S2.68E-30.7121.18E-30.2784.93E-44.33E-91.8E-11T2.77E-30.7161.21E-30.2783.61E-44.14E-91.8E-11TailgasS1.5E-40.8157.96E-40.1824.59E-62.7E-108E-8T7.6E-40.8187.87E-40.1793.67E-61.1E-107.9E-8312S0.9118.7E-21.9E-72.1E-47.86E-41.33E-31.1E-14T0.9128.5E-21.4E-72.7E-47.98E-41.33E-39.5E-15315S0.9895.3E-34E-194.85E-53.76E-31.44E-33.4E-18T0.98696.7E-31E-194.57E-44.54E-31.44E-33.4E-18318ST0.11865.3E-22.79E-67.3E-102.42E-70.4988.8E-10H2S濃縮塔的模擬CH4COCOSTotalFlowkmol/hrTemperatureKPressureatm301ST7.61E-31.81E-51E-15434.8302S2.03E-34.78E-61.3E-151622.77240.71332.1T2.08E-34.9E-65.5E-151603240.32.1TailgasS1.37E-31.78E-52.8E-152446.045221.39201.7T1.32E-31.77E-57.6E-152471.023216.38931.7312S2.17E-54.6E-91.8E-1510900.96221.19731.9T1.18E-53.6E-97.2E-1610875.214216.27051.9315S1.9E-145.8E-191.6E-1510078.43237.14172.3T2.1E-143.9E-191.4E-1510072.15232.68142.3318ST8.89E-82.35E-41E-1545.25328.5模擬結(jié)果與工藝包數(shù)據(jù)的比較(續(xù))甲醇再生塔的模擬二元交互作用參數(shù)的修改甲醇再生塔的模擬經(jīng)模擬計(jì)算選擇，NRTL較符合工藝包數(shù)據(jù)，對(duì)其二元交互作用參數(shù)的修改如下：H2S濃縮塔的模擬CH4OCO2H2N2H2SH2OAr402S0.1410.5009E-73.3E-20.3258E-62.9E-10H2SS5.5E-40.6081.1E-64.1E-20.34974.3E-33.6E-10模擬結(jié)果CH4COCOSTotalFlowkmol/hrTemperatureKPressureatm402S3.5E-87.6E-51.3E-15138.887320.00333.2H2SS4.4E-89.5E-5044.7122402.8甲醇再生塔的模擬甲醇再生塔的模擬甲醇水塔的模擬模擬結(jié)果與工藝包數(shù)據(jù)的比較CH4OCO2H2N2H2SH2OAr401S0.9722.7E-21.17E-63E-112.6E-71.1E-33.7E-10T0.9722.7E-21.17E-63.1E-112.6E-71.2E-33.7E-10511S0.99855.2E-91.4E-141E-151.9E-71.44E-31E-15T0.99855.1E-91.4E-141E-151.9E-71.46E-31E-15512S0.4061.7E-26.2E-101.6E-151.2E-70.57641E-15T0.4061.7E-26.1E-101.7E-151.2E-70.57641E-15513S4.2E-71E-209.8E-284.6E-331.4E-2019.4E-32T3.3E-73.7E-245.6E-231.2E-567E-2514.3E-42甲醇水塔的模擬CH4COCOSTotalFlowkmol/hrTemperatureKPressureatm401S4.6E-89.9E-51.4E-15107.682374.21663.7T4.6E-89.9E-51E-15107.7374.23.7511S1E-151E-151E-1573.3332.93.7T1E-151E-151E-1573.3332.96.9512S3.2E-81E-151E-1527.59245.24T3.2E-81E-151E-1527.59245.24513S6E-334.9E-264.7E-2838.458416.30823.9T6.8E-331E-243.9E-5338.456416.33753.9模擬結(jié)果與工藝包數(shù)據(jù)的比較(續(xù))甲醇水塔的模擬甲醇水塔的模擬熱力學(xué)方程的選擇匯總熱力學(xué)方程所適用的塔修改后的RKSWSC110、C120、C130、C140SR-POLARC200RK-ASPENC310PSRKC320修改后的NRTLC400PRWSC500NRTL部分換熱器熱力學(xué)方程的選擇匯總應(yīng)達(dá)標(biāo)準(zhǔn)計(jì)算結(jié)果甲醇洗塔中凈化氣CO2≤3％總硫＜0.1ppm(mol)CO2＝1.5%總硫＝0.038ppmCO2再生塔中產(chǎn)品CO2H2+CO+CH4O+CH4＜1.1%H2S+COS≤5mg/m3H2+CO+CH4O+CH4＝0.869％H2S+COS=1.2mg/m3H2S濃縮塔中尾氣H2S+COS≤5mg/m3H2S+COS=1.6mg/m3甲醇再生塔中產(chǎn)品H2SH2S≥25％H2S=34.97%甲醇水塔中廢水CH3OH≤0.5％(wt)CH3OH=0.074%(wt)工藝改進(jìn)

由于甲醇具有很強(qiáng)的毒性，所以這套裝置對(duì)密封性的要求很高，這樣就會(huì)提高成本，而且對(duì)人體健康很不利。設(shè)想由另一種無(wú)毒或毒性較弱的物質(zhì)替代甲醇進(jìn)行凈化處理。分析甲醇的分子結(jié)構(gòu)及物性，選擇與其相似物質(zhì)乙醇、乙二醇、異丙醇、正丁醇進(jìn)行比較和試計(jì)算，認(rèn)為乙醇可以滿足要求。工藝改進(jìn)物質(zhì)比較甲醇乙醇乙二醇異丙醇正丁醇相對(duì)分子量34.04246.06962.06960.09674.123常壓結(jié)晶點(diǎn)K175.5159.1260.2184.7183.9標(biāo)準(zhǔn)沸點(diǎn)K337.7351.4470.5355.4390.9臨界溫度K512.6513.9645508.3563.1臨界壓力bar80.961.47747.644.2臨界體積cm3/mole118.0167.1-220275臨界壓縮系數(shù)pcVc/(RTc)0.2240.24-0.2480.259Pitzer偏心系數(shù)0.5560.644-0.6650.593偶極矩debyes1.71.7-1.71.8工藝改進(jìn)試計(jì)算

甲醇乙醇乙二醇異丙醇正丁醇

0.00053950.000258312.72E-080.0001851.48E-05CO20.27928260.251092540.353453190.2187180.210309H20.48712730.506782610.437027080.529510.535213N20.00300620.003120580.002702020.0032470.003284H2S5.27E-084.84E-084.80E-074.46E-084.07E-08H2O2.34E-073.70E-073.49E-084.30E-073.53E-07AR0.00105930.001093160.00096020.0011290.001142CH40.00086030.000879950.000786770.0008950.000908CO0.22812450.23677240.205070180.2463160.249128COS5.16E-163.87E-161.36E-152.99E-162.84E-16Fkmol/hr7678.54667372.090958566.906717039