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双语推荐：间歇精馏

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在常规的间歇萃取精馏实验装置中,研究了以蒸馏水为萃取剂间歇萃取精馏分离甲醇-丙酮共沸物的过程。考察了萃取剂、全回流时间、共沸物组成、溶剂与混合物的体积比、加盐、加碱等因素对萃取精馏分离甲醇-丙酮共沸体系的影响,从而得出最佳的萃取条件。
The methanol-acetone azeotrope was separated by batch extractive distillation with distilled water as extracting agent. The effect of factors of extractant, total reflux time, azeotrope composition, volume ratio of sol-vent and compound, saline and alkaline on batch extractive distillation azeotrope system was investigated. The best extraction conditions were obtained.

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用常规的间歇萃取精馏实验装置，研究了以单乙醇胺（MEA）为萃取剂间歇萃取精馏分离甲醇—丙酮恒沸物的过程。考察了萃取剂、全回流时间、共沸物组成、溶剂与混合物的体积比、回流比等因素对萃取精馏分离甲醇—丙酮共沸体系的影响，从而得出最优的萃取条件。
s:Batch extractive distillation process of methanol-acetone binary azeotrope in the conventional batch extractive distillation experimental device with MEA as extracting agent was studied. Effect of extractant, total reflux time, azeotrope composition,volume ratio of solvent and mixture,reflux ratio and other factors on the extractive distillation separation of methanol - acetone azeotropic system was investigated, and the best extraction conditions were determined.

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利用ChemCAD流程模拟软件,在1 atm下,对苯-氯苯-邻二氯苯三元体系间歇精馏回收苯和氯苯的过程进行模拟计算,并进行了实验验证。模拟结果表明：全塔理论级数为10,间歇精馏过程采用变回流比,分三步进行,回流比分别为：15：1、5：1和15：1,热力学性质采用PR模型计算,精馏时间约4.4 h,得到纯度为100%的苯,回收率为5.11%,纯度为99.99%氯苯,回收率为34.68%。模拟了间歇精馏塔各步操作的温度分布,塔顶最低温度为80.2℃,塔底最高温度为152.5℃,模拟值与实验值吻合良好。
Batch rectification process for preparation of benzene and chlorobenzene from benzene-chlorobenzene-o-dichlorobenzene ternary system was simulated by ChemCAD simulation software at 1atm. Simulation resuts were compared with experimental data. The simulation results showed that the whole tower theory series for 10, the banch rectification model was chosen for simulation and operated by three steps, re-flux ratio respectively was: 15:1,5:1,15:1. PR model was used to calculate the thermodynamic properties of the material srstem and the rectification period about 4.4 h. The purity of benzene was 100%, the solvent re-covery rate was 5.11% and the purity of chlorobenzene was 99.99%, the solvent recovery rate 34.68%. Each step operation temperature distribution of the batch rectification column wered simulated, the minimum tem-perature of tower top was 80.2℃, the highest temperature of bottom 152.5℃. Simulation results and experim ental data agree satisfactorily.

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甲醇三塔精馏过程中,常压塔经常出现负压的现象,公司采用在常压塔回流槽内充入惰性气体N2的方法。此方法虽然有效解决了常压塔负压的现象,但同时也对甲醇精馏效率、工艺操作带来负面的影响,间歇向常压塔回流槽冲入氮气,不仅破坏了精馏过程中汽-液两相间质与热的平衡,同时对精馏操作也造成了很大的不便。
The process for methanol distillation with three towers ,the atmospheric rectification tower often appears the phenomenon of negative pressure,the company adopts the method of filling an inert gas in the reflux tank . Although this method solves the problem effectively,but has a negative impact in distillation efficiency and process operation. Filling nitrogen into the reflux tank of atmospheric tower intermittently,not only destroying the balance of gas - liquid two phase in heat and mass,but also causing great inconvenience to distillation operation.

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在常规的间歇萃取精馏实验装置中,研究了以N,N-二甲基酰胺(DMF)和二甲亚砜(DMSO)作萃取剂;在间歇萃取精馏塔中分离乙醇-乙酸乙酯体系的过程。对全回流时间、不同萃取剂、恒沸物组成、溶剂和混合物的体积比、加盐及加碱等因素考察,分析萃取精馏分离乙醇-乙酸乙酯共沸体系的影响,从而得出最佳的萃取条件。
In the conventional batch extractive distillation experimental device, the batch extractive distillation process of ethanol- ethyl acetate system by using N,N-dimethy formamide and dimethy sulphoxide as extracting agents was studied. Effects of total reflux time, extractant, azeotrope composition, volume ratio of solvent to mixture ,adding salt, adding alkali and other factors on the extractive distillation separation of ethanol- ethyl acetate system were investigated, then the best extractive distillation conditions were obtained .

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采用共沸精馏技术处理合成氨工艺流程中脱碳工段产生的含大量正丙醇混醇废液。本文采用共沸精馏的方法,选用合理可行的共沸剂,在间歇精馏塔内进行正丙醇-水共沸物系的分离实验,优化了该共沸精馏技术处理工业混醇废液的最佳操作条件。结果表明:采用共沸精馏方法,以环己烷为共沸剂,可使原料液中20%～40%的正丙醇含量提纯至质量分数≥95%,塔顶回收的共沸剂质量分数≥97%。该工艺流程较大地减小了设备投资和能耗。实验表明采用共沸精馏技术用于正丙醇-水共沸物系的分离具有可靠性和实用性。
Azeotropic distillation technology was used to treat industrial mixed-alcohol wastewater coming from ammonia synthesis. Using this technology and taking a feasible azeotropic agent,the distillation experiment of 1-propanol-water azeotrope system was conducted in batch distillation column. The operating condition of treating industrial mixed alcohol waste water was optimized. The results indicated that using this technology and taking cyclohexane as azeotropic agent,1-propanol in raw material could be purified from 20%~40% to ≥95%,and cycloihexane entrainer at the tower top could be purified to ≥97%. This technology greatly reduced equipment investment and energy consumption. The experimental results showed that using azeotropic distillation for separation of 1-propanol - water azeotrope system could be reliable and practicable.

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利用UNIFAC基团贡献法对常用萃取剂进行了筛选,选取邻二甲苯作为该二元共沸物的萃取剂,并通过汽液平衡实验对其分离效果进行了验证;进行甲醇-甲苯分离的间歇萃取精馏实验考察所选萃取剂的效果。结果表明：邻二甲苯能够有效提高甲醇-甲苯的相对挥发度。间歇萃取精馏塔塔板数为30,溶剂比为1,恒回流比（R=3）操作下塔顶得到摩尔分数为99.688%的甲醇产品。
1,2-dimethylbenzene was chosen as solvent through UNIFAC group contribution method and its effect was verified by vapor-liquid equilibrium experiment.The effectiveness of the selected solvent was investigated by batch extractive distillation experiment.The results show that 1,2-dimethylbenzene can increase the relative volatility significantly.The batch extractive distillation was carried out in a packed column of 30 theoretical plates.With the constant reflux ratio of 3 and the solvent mole ratio of 1:1,the product mole fraction of methanol reaches 99.688％.

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采用间歇减压精馏法实现了2-甲基吡啶和2-羟乙基吡啶这一热敏性混合物的分离,并考察了投料组成与操作压力对减压精馏过程的影响。结果表明,高真空条件降低了塔釜温度从而避免了物料在塔釜中受热变性,对于热敏物料2-羟乙基吡啶,减压精馏过程中压力应控制在4325 Pa以下,此时塔釜产品2-羟乙基吡啶的质量分数均能大于97%,同时收率能保持在86%以上。在压力为1325 Pa时,不同投料组成下塔顶产品2-甲基吡啶的质量分数和塔釜产品2-羟乙基吡啶的质量分数均高于98%,两者的收率也均在85%以上,能够很好地满足工业生产要求。
2-Picoline and heat-sensitive material 2-ethanolpyridine were separated by batch vacuum distillation. The effects of feed composition and operating pressure on vacuum distillation process were also investigated. The results showed that high vacuum in the column lowering the bottom temperature ensured the feed in the reboiler against the thermal degeneration. The optimal pressure was below 4325 Pa for 2-ethanolpyridine in vacuum distillation process. The mass fraction of 2-ethanolpyridine in the reboiler could be more than 97% and the yield of 2-ethanolpyridine could be over 86% under this condition. When the pressure was 1325 Pa the mass fraction of 2-picoline in the distillate and 2-ethanolpyridine in the reboiler were both up to 98%, with yields above 85%, meeting the requirements of industrial production well.

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研究了以溴代异戊烯水解工艺和精馏分离工艺为基础来制备3-甲基-2-丁烯-1-醇的新工艺。通过优化溶剂种类得到当水解溶剂为偶极类溶剂乙腈时，得到产物的选择性最高。并通过进一步优化实验操作条件，得到当溶剂加入量为 v(乙腈)：v(溴代异戊烯)=1∶1，水解温度为70℃，碱用量为 n(NaOH)∶n(溴代异戊烯)=1.2∶1和反应时间为25min时，水解部分3-甲基-2-丁烯-1-醇的转化率最高可达63.35%。水解后的料液通过间歇精馏得到纯的3-甲基-2-丁烯-1-醇，最终的3-甲基-2-丁烯-1-醇总收率达到57.4%。
A new technology for the preparation of 3-methyl-2-butene-1-ol was investigated based on the hydrolysis of brominated isoamylene and distillation separation technology. By choosing a dipolar solvent,acetonitrile,for the hydrolysis the products showed the highest selectivity. And through further the optimization of experimental operating conditions,hydrolysis yield of 3-methyl-2-butene-1-ol reached 63.35%under the condition of the solvent amount v(acetonitrile)∶v(bromo-3-ene)=1∶1, hydrolysis temperature 70℃,base amount n(NaOH)∶n(bromo-3-ene)=1.2∶1 and reaction time 25 minutes. The pure 3-methyl-2-butene-1-ol was made of the feed liquid after hydrolysis by batch distillation operation,and the final total yield of 3-methyl-2-butene-1-ol reached 54%.

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针对提取天然烟碱传统工艺中粗烟碱精制过程烟碱损失量大及烟碱产品纯度不够高的问题,采用真空间歇精馏方法对烟碱粗产品进行了精制,并确定了适宜的操作条件。该过程包含如下两阶段：溶剂回收阶段,塔顶压力50～100 kPa,回流比2～4,溶剂收率为88.7%;烟碱精制阶段,塔顶压力不超过0.5 kPa,回流比3～5,烟碱质量分数和收率分别到达99.5%和74.0%以上。此方法操作稳定可靠,便于控制,易于实现工业化。
Because of big loss and low purity of product in traditional refining process for extraction of natural nicotine,an innovative method for purification of nicotine by vacuum batch distillation was studied.And the suitable operating conditions were obtained.The distillation process included two stages as follows:In solvent recovery stage,the appropriate pressure was 50-100 kPa and reflux ratio was 2-4,respectively,and the recovery of chloroform was 88.7％.While in nicotine refining stage,the suitable operating pressure was not more than 0.5 kPa,the reflux ratio was 3-5.And the purity (mass fraction)and yield of nicotine was more than 99.5％ and 74.0％,respectively.The method to refine nicotine is steady,convenient for control and easy to be realized in industrialization.

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