LF—30Ⅳ型氯乙烯聚合釜传热性能评价

采用热量衡算法测定了国产LF30—Ⅳ型氯乙烯聚合釜的传热性能,结果表明：夹套和内冷管传热系数均随冷却水流量的增加而增加,当夹套冷却水和内冷管冷却水流量分别在100～255m3／h和51～129m3／h时,冷模传热系数分别在2788～3252kJ／m2·℃·h和5534～6629kJ／m2·℃·h之间;在相近冷却水流量时,LF30-Ⅳ型聚合釜的传热系数高出LF30－Ⅱ型聚合釜10％以上,由Wison图解法计算了夹套和内冷管的α1和α2。     

间歇釜热交换过程的分析与计算

分析了间歇釜热交换过程中物料与（热）载体温度随传热量及时间的变化规律。推导出间歇釜热交换的需时间及传热面积的计算公式，附有计算举例。     

改进聚合工艺提高聚合釜生产能力

介绍了为提高LF—30IV型聚合釜生产能力而采取的工艺和技术改进措施及取得的效果。     

聚合釜传热对聚合反应的影响

本文旨在通过对１２ｍ＾３聚合釜传热的计算,论证聚合釜的传热状况,寻求聚合反应操作的方法和操作条件,以解决聚丙烯生产中的传热问题,促进降丙烯的稳定生产。     

提高30m~3聚合釜生产能力

介绍了提高聚合釜生产能力的措施,改变聚合水油比,由原来的1.77降低到1.70,增加投料系数0.16;采用新助剂和密闭投料等新工艺,缩短聚合反应周期2.7h。使30m3聚合釜生产能力从5kt/a提高到6.5kt/a。     

提高PVC装置夏季生产能力的措施

分析了聚合循环水温度对聚合生产的影响，提出了优化引发剂配方，采用复合引发剂，做好聚合釜的涂釜工作避免粘釜和使用低温盐水等措施。通过改进，提高了聚合釜的传热能力，使聚合装置生产能力得到提高。     

高密度聚乙烯装置聚合釜生产能力评估

研究了高密度聚乙烯（ＨＤＰＥ）装置聚合釜生产能力的影响因素,通过自行编制的计算机程序对聚合系统进行了模拟,研究了在现有生产条件下,聚合釜的最大生产能力,并指出了提高生产能力的途径。     

12m3聚合釜的改造

本文分析了二分之一工段12m^3聚合釜挂胶严重,清釜周期短的原因,阐述了该釜进行改造的必要性。     

PVC聚合釜防粘釜技术

论述了PVC聚合釜防粘釜技术的机理及选择防粘釜剂的技术要点。重点介绍了自主开发的PVC聚合釜防粘釜喷涂设备及其操作要点。     

丙烯聚合釜密封和传热的设计

介绍了丙烯聚合时反应热量的计算与传热结构的设计,以及一种能可靠运行1年以上的中压填料密封的设计。     

“饥饿”反应器中苯乙烯聚合动力学

本文对“饥饿”反应器中ＡＩＢＮ引发苯乙烯聚合行为进行了详细的研究，建立了相应的聚合动力学模型，在模型中，考虑了由于初级自由基与单体反应生成单体自由基时所消耗的单体量，并将链终止速率常数与聚合物的累积数均链长进行校正。利用实验数据对模型参数进行了回归。     

预聚反应器液位对生产能力的影响

分析预聚反应器的生产情况,讨论预聚反应器对生产和产品质量的影响,提出通过提出预矛反应器物料液位来提高装置生产能力的可行性。     

聚合釜远程监控系统的开发

对聚合釜设备的远程监控系统的开发背景、技术基础、远程监控的实现以及应用过程进行了阐述,同时分析了聚合釜远程监控系统的应用效果和作用。     

乙烯淤浆聚合反应器的模型与模拟

建立了乙烯淤浆聚合反应器的多相全混流模型,描述了包括乙烯共聚合反应动力学、气液和液固传质、反应器传热在内的物理化学过程。通过模拟计算分析了聚合过程的控制步骤,得到了反应器生产能力与有关操作变量之间的关系,对某工业反应器的模拟结果表明计算值与生产数据具有很好的一致性。     

Study of Ethylene Polymerization Under Single Liquid Phase and Vapor‐Liquid Phase Conditions in a Continuous‐Flow Tubular Reactor

The feasibility of using continuous‐flow tubular reactors (CFTR) as an efficient research tool for polymerization reactions is investigated. This is a continuation of the extensive effort that had been made at Dow in recent years to set up and employ an electro‐thermal microreactor (an ohmically‐heated CFTR), which resulted in several internal and external publications and a US Patent. The main focus of this work is to investigate the effect of operating conditions and flow composition, mainly the number of existing phases, on the molecular weight of the polymer. A series of polymerization experiments were performed in single‐phase (liquid) and two‐phase (vapor‐liquid) flow regimes. In single‐phase polymerization, the ethylene concentration falls continuously along the length of the reactor. This will have a significant effect on the kinetics of polymerization, particularly the molecular weight of the produced polymer. A key advantage of operating in the two‐phase region is that an almost constant ethylene concentration is maintained along the length of the reactor. In effect, the vapor phase serves as a reservoir that replenishes the ethylene consumed in the liquid phase by polymerization. The molecular weight data show that this assumption is valid provided that the rate of mass transfer is significantly higher than the rate of the polymerization reaction.     

Reactor Modeling of Gas‐Phase Polymerization of Ethylene

A model is developed for evaluating the performance of industrial‐scale gas‐phase polyethylene production reactors. This model is able to predict the properties of the produced polymer for both linear low‐density and high‐density polyethylene grades. A pseudo‐homogeneous state was assumed in the fluidized bed reactor based on negligible heat and mass transfer resistances between the bubble and emulsion phases. The nonideal flow pattern in the fluidized bed reactor was described by the tanks‐in‐series model based on the information obtained in the literature. The kinetic model used in this work allows to predict the properties of the produced polymer. The presented model was compared with the actual data in terms of melt index and density and it was shown that there is a good agreement between the actual and calculated properties of the polymer. New correlations were developed to predict the melt index and density of polyethylene based on the operating conditions of the reactor and composition of the reactants in feed.     

丁苯橡胶聚合反应釜的制造技术

对丁苯橡胶装置聚合反应釜的制造难点进行了分析。对反应釜壳体的成形方法、复合钢板的焊接、封头与壳体的连接、冷却管组的成形与管束的分布形式等进行了深入的研究,解决了反应釜内件的组装难题,并对反应釜体内部进行了抛光。总结了聚合反应釜的制造经验,提高了产品质量和经济效益,可以为同类设备的制造提供参考。     

A Laboratory Reactor for Gas‐Phase Olefin Polymerization

A new reactor system for gas‐phase ethylene/α‐olefin polymerization is described. Good gas‐phase temperature control at high polymerization rates was achieved with the 2‐L semi‐batch reactor. Ethylene/1‐hexene and ethylene polymerization results showing the effects of operating conditions on temperature profiles are presented. Good gas‐phase temperature control is required to obtain reliable activity profiles. A gas‐sampling and analysis system, which allows relatively rapid (< 3 min) and accurate determination of ethylene/1‐hexene contents in the gas‐phase of the reactor, is also described. Rapid and reliable hydrogen contents were also measured with this relatively inexpensive system.     

杜邦干法腈纶提高反应速率的研究

通过提高抚顺石油化工公司腈纶化工厂干法腈纶生产中聚合釜反应速率,考察了运行参数的变化,进行了实验分析,聚合釜反应速率由原来的95 t/d提高到110 t/d,聚合釜运行周期20天,在腈纶生产力求效益最大化和装置最优化方面进行了探讨。     

下喷式环流反应器液相流动特性研究

液相停留时间分布分析用于下喷式环流反应器导流筒顶部区域、底部区域、环隙流体流动特性研究。分别将轴向扩散模型应用到各个区域,实验结果表明轴向扩散模型能较好的预测反应器内流体的停留时间分布。采用最小二乘法拟合实验响应曲线,得到模型方程参数。结果表明各个部分的Pe值均随液体喷射速度的增大而减小。导流筒顶部区域的Pe值变化范围为:25.4~6.6;导流筒底部区域的Pe值变化范围为:45.4~11.6;环隙的Pe值变化范围为:60.0~39.2。结果表明导流筒顶部区域返混最大,环隙区域接近于平推流。反应器混和时间随液体喷射速度的增大而减小,变化范围为:88.3~12.5 s。