带控制点工艺流程图

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1、说明F:流量’kg/h温度，°CP:压力，MPa(g)O：热流S»106kcal/h逬料硕热器E-101TI7E-101塔顶冷凝器E-102塔底产品冷却器E-105厂-60E4110V-101F=14110L—®:原料罐V-101YQ二0・23P-101A/B逬料泵P-101塔顶产品冷却器厂二86E404厂二14789E405"0.15T-101V-102CW1V-103£>102卩二81.F=7394CW厂二81.6F二14789"1.6F二6716F=7394E-1047M0U88.4⑧F=67I6卜®U17囲P=0.8

2、MPa7=154=33?=95F=14110厂二154F二6716E403P-102A/B釜液泵再沸器精溜塔P-102E-10JT:101P-103A/B回流罐回流泵P403V4022-0.13P-104A/B塔顶产品罐产品泵~V:103P-101苯、乙苯分离带控制点工艺流程图P-105A/B塔底产品雄产品泵V-104P-105分离系统物流表物流号VVVVVVVVVV温度/弋6060.229581.5154.282.040154.588.4540压力/MPa(绝)0.150.40.40.110.140.450.40.350.

3、350.3摩尔流量/kmol/h154.63154.63154.6394.99259.638、94.99294.99259.63859.63859.638质量流M/kg/h4109.9714109.9714109.977393.9226716.057393.9227393.9226716.056716.056716.05组成(摩尔分数)苯0.5982620.5982620.5982620.9738631.43E-070.9738630.9738631.43E-071.43E-071.43E-07甲苯0.006020.0060

4、20.006020.0097734.20E-050.0097730.0097734.2E-Q54.2E-054.2E-05乙苯0.3091260.3091260.3091260.0064660.7912060.0064660.0064660.7912060.7912060.791206二乙苯0.009069.06E-030.009061.30E-100.0234911.30E-101.30E-100.0234910.0234910.023491三乙苯0.0627816.28E-O20.0627812.57E-120.1627

5、82.57E-122.57E-120.162780.162780.16278多乙苯0.003113.11E-O30.003111.81E-240.0080641.81E-241.81E-240.0080640.0080640.0080M焦油0.005565.56E-030.005568.08E-340.0144168.08E-348.08E-340.0144160.0144160.014416水0.006080.()06086.08E-030.0098978.94E-080.0098970.0098978.94E-088.9

6、4E-088.94E-08比热容/[j/(kg-K)J1871.0351871.7281997.4321887.1032250.8231887.7711747.0882250.9822025.1511761.181密度/(kg/m3)827.165827.155793.684809.971728.155809.904853.675728.263786.362829.19粘度/(mPa-8)3.9194373.9194373.9194372.0538671.8655692.0538672.0538671.8655691.865

7、5691.865569