化学工程
化學工程
화학공정
CHEMICAL ENGINEERING
2014年
5期
1-5
,共5页
辛燕平%赵明%夏铭%许春建
辛燕平%趙明%夏銘%許春建
신연평%조명%하명%허춘건
吡啶%水%热集成%变压精馏%模拟%优化
吡啶%水%熱集成%變壓精餾%模擬%優化
필정%수%열집성%변압정류%모의%우화
pyridine%water%heat-integrated%pressure swing distillation%simulation%optimization
基于吡啶-水体系的共沸组成对压力变化敏感，提出了热集成变压精馏的新工艺。新工艺采用冷凝器-再沸器式热集成，利用高压塔塔顶蒸汽加热低压塔再沸器，以节省能耗和操作费用。选择NRTL活度方程为物性计算模型，使用Aspen Plus软件对该工艺流程进行严格稳态模拟。为了获得经济最优的工艺条件，提出了局部经济优化和全局经济优化相结合的优化方案，并建立了优化迭代流程。优化结果显示：当低压塔和高压塔的操作压力分别为16 kPa和1200 kPa，总理论板数分别为12和14，新鲜原料和循环物流分别从低压塔第9块板和从第6块板进料，高压塔的物流进料位置为第8块板，高压塔质量回流比为0．59时，年度总费用（TAC）最小。与常规的变压精馏工艺相比，热集成变压精馏工艺更加节能经济，可以节约能耗43．52％，节省年度总费用40．70％。
基于吡啶-水體繫的共沸組成對壓力變化敏感，提齣瞭熱集成變壓精餾的新工藝。新工藝採用冷凝器-再沸器式熱集成，利用高壓塔塔頂蒸汽加熱低壓塔再沸器，以節省能耗和操作費用。選擇NRTL活度方程為物性計算模型，使用Aspen Plus軟件對該工藝流程進行嚴格穩態模擬。為瞭穫得經濟最優的工藝條件，提齣瞭跼部經濟優化和全跼經濟優化相結閤的優化方案，併建立瞭優化迭代流程。優化結果顯示：噹低壓塔和高壓塔的操作壓力分彆為16 kPa和1200 kPa，總理論闆數分彆為12和14，新鮮原料和循環物流分彆從低壓塔第9塊闆和從第6塊闆進料，高壓塔的物流進料位置為第8塊闆，高壓塔質量迴流比為0．59時，年度總費用（TAC）最小。與常規的變壓精餾工藝相比，熱集成變壓精餾工藝更加節能經濟，可以節約能耗43．52％，節省年度總費用40．70％。
기우필정-수체계적공비조성대압력변화민감，제출료열집성변압정류적신공예。신공예채용냉응기-재비기식열집성，이용고압탑탑정증기가열저압탑재비기，이절성능모화조작비용。선택NRTL활도방정위물성계산모형，사용Aspen Plus연건대해공예류정진행엄격은태모의。위료획득경제최우적공예조건，제출료국부경제우화화전국경제우화상결합적우화방안，병건립료우화질대류정。우화결과현시：당저압탑화고압탑적조작압력분별위16 kPa화1200 kPa，총이론판수분별위12화14，신선원료화순배물류분별종저압탑제9괴판화종제6괴판진료，고압탑적물류진료위치위제8괴판，고압탑질량회류비위0．59시，년도총비용（TAC）최소。여상규적변압정류공예상비，열집성변압정류공예경가절능경제，가이절약능모43．52％，절성년도총비용40．70％。
A new method for pyridine-water separation was presented by using heat-integrated pressure swing distillation since the azeotropic compositions change significantly with pressure.Condenser-reboiler type heat integration was used between the condenser in high pressure distillation column and the reboiler in low pressure distillation column to save energy and operating costs.NRTL activity model was chosen as the property package in the simulation.Rigorous steady state simulations were implemented by means of commercial software Aspen Plus. To obtain the optimized configurations for this process,an optimization scheme combining partial economical optimization with global economical optimization was proposed.Sequential iterative optimization procedure was presented to facilitate the optimization.The optimal operating pressures for the two columns are 16 kPa and 1 200 kPa,respectively.The optimal total numbers of stages for low pressure distillation column and high pressure distillation column are 12 and 14,respectively.The fresh feed stream and recycle stream are fed into low pressure distillation column from stages 9 and 6.The feed location of high pressure distillation column is stage 8.The optimal mass reflux ratio of high pressure distillation column is 0.59.Compared with the corresponding traditional pressure swing distillation scheme,heat-integrated pressure swing distillation scheme is more energy-saving and economical,with energy decreased by 43.52% and total annual cost (TAC)decreased by 40.70%.
