催化柴油加氢改质异构降凝装置试生产标准质量分析

在催化柴油加氢改质异构降凝装置正式投入使用之前,都需要进行装置的试生产质量标准分析。因此,基于这种认识,本文以FH-98和FC-20为装置的加氢精制催化剂和异构降凝催化剂,对20万t/a催化柴油加氢装置进行了试生产质量标准分析,从而为关注这一话题的人们提供参考。     

萘气相催化氧化制备1,4-萘醌的放大试验研究

对萘气相催化氧化制备1,4-萘醌反应装置进行放大,采用该装置测试催化剂的性能,结果表明增大催化剂颗粒和改变催化剂表面酸碱性可使催化剂对1,4-萘醌选择性提高15%左右,改变催化剂构型,制备瓷环催化剂,可有效改善催化剂性能,降低放大效应。     

PH-98型催化剂用于大庆焦化柴油和重油催化轻柴油混合油加氢精制的研究

为解决大庆焦化柴油和重油催化轻柴油产品的安定性和对加氢装置扩能的需要,进行了FH-98型催化剂用于大庆焦化柴油和重油催化轻柴油混合油加氢精制工艺的研究。研究结果表明,FH-98型催化剂对大庆焦化和重油催化混合柴油进行加氢精制,可以生产出0^#一等品柴油,能满足加氢装置扩能的需要。     

流化裂化催化剂市场面临重大变化

流化裂化催化剂市场最近经历了重大变化,更加剧烈的变化有可能即将发生。催化裂解装置是现代炼油厂的重要组成部分,催化裂解装置使用的流化裂化催化剂是含非晶相和晶相物的硅铝酸盐。流化裂化催化剂的消费量大大高于大多数催化剂的消费量。一台催化裂解装置装有200吨催化剂,为了保持催化剂的活性,根     

化学镀法制备单钯汽车尾气净化催化剂

首次采用化学镀法制备出单钯汽车尾气催化剂,通过XRD和TEM等分析技术对催化剂的结构和表面形貌进行了表征,在模拟汽车尾气净化催化装置上初步研究了其催化效果,并与传统浸渍法所制备的催化剂进行性能对比。结果表明,化学镀法可以实现纳米钯微晶颗粒在助剂涂层上的均匀负载,并且省去了传统制备方法中的高温还原活化步骤,催化剂的催化性能也优于传统浸渍法所得催化剂的催化性能。     

催化汽油加氢装置催化剂HR-845、HR-806再生后的性能分析

中国石油大港石化公司采用法国Axens公司的Pmne—G＋工艺，对催化汽油进行选择性加氢和深度脱硫。装置运行一个周期后，对催化剂HR～845、HR-806进行了再生处理，再生剂在装置上的应用结果表明：再生后催化剂的活性恢复良好，催化汽油脱硫效果显著，混合汽油产品辛烷值损失小，硫含量满足公司调油需求。     

CDOS型催化裂化催化剂在格尔木炼油厂的应用

阐述格尔木炼油厂催化裂化装置针对本厂催化汽油辛烷值偏低、产品分布不合理等几个问题,通过对几种催化剂型号的试用,对其产品分布以及催化汽油辛烷值等综合收益进行对比后,改良催化剂选型,提高催化汽油辛烷值,并获得更好的产品分布,增大了企业效益。     

精准加料设备及顺酐生产系统

涉及催化氧化生产的技术领域,包括助催化剂计量装置、氮气供应装置、鼓泡装置和混合装置;实现了助催化剂对固定床氧化反应器中催化剂的均匀、精准加料,保证了氧化反应的收率、转化率,确保催化剂的寿命。     

流化催化精馏过程汽液传质系数的测定

提出了在三相流态化板式塔中进行催化精馏的设想，将球形强酸性离子交换树脂催化剂置于单板装置的筛板上，进行了甲缩醛合成流化催化精馏试验，测定了汽液传质系数，考察了催化剂浓度、操作汽、液速度对传质系数的影响     

煤制油催化剂段降低含盐废水量的装置改进研究

本文主要介绍神华煤直接液化制备高效催化剂工艺现状,对催化剂制备过程产生的含盐废水(催化剂废水)来源进行了分析,研究通过催化剂制备工段的操作优化及装置改进,降低催化工段废水产生量。结果表明,在该改进装置条件下催化剂制备工段产生的含盐废水量每小时降低14.5 t。     

合成间同立构PS用单中心催化剂的研究进展

综述了茂金属催化剂和非茂钛催化剂合成间同立构聚苯乙烯的研究进展,其中,茂金属催化剂主要包括茂钛催化剂、单茂钛催化剂、茚钛催化剂、双核金属催化剂及负载型催化剂等。今后的研究重点是负载型茂金属催化剂和非茂钛催化剂,单中心催化剂将对合成间同立构聚苯乙烯的工业化发展发挥重要的作用。     

Study of Deactivation of Pd(OH)2/C Catalyst in Reductive Debenzylation of Hexabenzylhexaazaisowurtzitane

The conversion of hexabenzylhexaazaisowurtzitane (HBIW) to 2,6,8,12‐tetraacetyl‐4,10‐dibenzyl‐2,4,6,8,10,12‐hexaazaisowurtzitane (TADB) is the major challenge in the production of hexanitrohexaazaisowurtzitane (HNIW) which only proceeds over supported palladium catalyst in a reductive debenzylation reaction. The catalyst is quickly deactivated during the debenzylation reaction. In this study, the change in Pd content in the catalyst during the reaction was measured. It was demonstrated that a portion of the palladium particles in the catalyst was leached during the reaction. The H₂ chemisorption isotherm on the catalyst at 303 K showed that the volume of chemisorbed H₂ on spent catalyst was significantly less than that on fresh catalyst. The N₂ physisorption isotherm on the catalyst at 77 K revealed that the surface area of spent catalyst was less than that of fresh catalyst. Moreover, the FESEM‐EDS and TEM images and also wide‐angle XRD patterns demonstrated that the mean sizes of palladium crystallites and particles in spent catalyst were larger than those in the fresh catalyst. These results demonstrated that the leaching of palladium particles and the aggregation of palladium particles in catalyst play active roles in the deactivation of catalyst in the debenzylation of HBIW.     

催化剂装填分率对催化蒸馏干气制乙苯过程的影响

在改性的β沸石催化剂上研究了催化剂与金属填料混合装填条件下,催化剂装填分率对催化蒸馏干气制乙苯过程的影响。通过冷模试验考察了催化剂装填分率对催化剂床层流体力学性能的影响,并在小型的催化蒸馏干气制乙苯装置上考察了催化剂装填分率对反应结果的影响。试验结果表明,催化剂装填体积分率直接影响催化剂床层的流体力学和反应性能。就催化蒸馏干气制乙苯过程而言,适宜的催化剂装填体积分率为10％～30%。     

丁辛醇合成催化剂制备及工业侧线研究

丁辛醇是合成精细化工产品的重要原料,低压羰基合成为目前主要的工业生产工艺,其核心催化剂为三苯基膦乙酰丙酮羰基铑（ROPAC）。介绍了ROPAC催化剂制备过程及工业侧线实验结果,并通过工业放大生产实验,解决了ROPAC催化剂制备过程中的问题,二步合成单程总收率可达98%以上,ROPAC催化剂中氯离子质量分数小于0.005%。依托于天津渤化永利化工有限公司的450 kt/a丁辛醇装置,成功进行了ROPAC催化剂国产化替代工业侧线试验,自制催化剂与进口参比催化剂在100%负荷下各运行520 h,自制ROPAC催化剂与进口催化剂醛耗丙烯、产物正异比和母液中聚合物含量等指标一致,产品醛各项指标合格,催化剂整体性能与进口催化剂基本一致。     

裂化装置催化剂跑损分析

针对裂化催化剂使用中磨损和热崩导致细粉增多、易跑损和剂耗高的现状,分析催化剂颗粒单体强度、黏结强度、球形度、表面粗糙度、原料油性能及操作条件对磨损和热崩的影响,探讨影响催化剂使用寿命因素的作用机理,提出减少跑损的相应措施。     

聚烯烃催化剂载体材料研究进展

综述了近年来聚烯烃茂金属催化剂载体的研究进展,包括新型载体的研制、结构特点及以此载体负载茂金属对聚合产物性能的影响。人工合成的具有空心结构SiO2团粒载体,可望作为一种新型催化剂载体,不仅可以应用于传统催化剂的Ziegler-Natta催化剂、茂金属催化剂,还可以应用于后茂金属催化剂以及非茂金属催化剂等聚烯烃催化剂,替代国外进口载体,实现硅胶作为聚烯烃催化剂载体的国产化。     

CIM-6单元镍油脂氢化催化剂的研制

在用H2 冷等离子体处理常规Cu -Ni二元油脂加氢催化剂 ,发现一种新的、有用的催化剂表面结构和研制开发成功CIMCu -Ni二元油脂加氢催化剂及其相关技术的基础上 ,研制成了CIM - 6单元镍油脂加氢催化剂。实验结果表明 :1 CIM - 6催化剂用于豆油加氢制食用氢化油 ,其活性 (以催化剂的时空转化率计 )是SP - 7催化剂 (美国EngelhardCo.)的 4 5倍 ;用于菜油加氢制食用氢化油 ,其活性是SP - 7的 7 3倍。 2 CIM - 6的抗硫能力 (n(S) =3× 10 - 6 )是SP - 7的1 6倍。 3 CIM - 6的选择性比SP - 7略好     

全球催化剂市场工业化进展及前景展望

介绍了全球催化剂在环境保护催化剂市场,炼油催化剂市场及加氢催化剂市场3个方面的工业化进展及动向。并对全球炼油催化剂市场的发展前景进行了分析,认为全球化的整合及创新技术将成为催化剂市场的主要发展趋势。     

Operability of an Industrial Methanol Synthesis Reactor with Mixtures of Fresh and Partially Deactivated Catalyst

Disposal of spent catalyst is a common practice in industrial methanol synthesis. However, the spent catalyst has, generally, a good level of activity and can be used if mixed with fresh catalyst. In this work the operation of an industrial methanol synthesis reactor with mixtures of fresh and partially deactivated catalyst was investigated using a one‐dimensional transient model. Analysis of the deactivation behavior of low‐pressure methanol synthesis catalyst shows there is an extremely sharp rate of deactivation in a small part of the catalyst life‐time, which is followed by a relatively slow rate of deactivation in the remaining catalyst cycle‐time. Different configurations were studied for catalyst recycling, and two limiting cases are discussed in detail in this paper, namely layered and homogeneous (mixed) bed models. In the first one, the catalyst was segregated into two alternate layers of fresh and partially deactivated catalyst, while in the second homogeneity of the catalyst bed was simulated by segregating a large number of alternate layers of fresh and partially deactivated catalyst. It was observed in both cases that when catalyst recycling is used, the process does not depart significantly from the standard operating conditions, and also that the mixed bed had less influence on the reactor performance than layered one.     

Hydrogenation of cottonseed oil with reused catalyst

Cottonseed oil was hydrogenated using both new (Rufert catalyst flakes) and reused (up to five uses) catalysts at 130–169C, at a pressure of 45 psig, and with high degrees of agitation. The activity of the catalyst increased initially with use, especially at 130C, but with continued use the activity decreased. The selectivity of the hydrogenation decreased with reuse of the catalyst, especially at lower temp. Isomerization decreased slightly as the catalyst was used only at higher temps. The induction period found with fresh catalyst at 130C was eliminated in runs with second- and third-use catalyst. A small induction period was noted with fifth-use catalyst. Treatment of once-use catalyst with air severely reduced the catalyst activity. Steam- and vacuum-treatment of the catalyst resulted in a slightly less active catalyst than a hydrogen-treated catalyst. None of these treatments significantly affected selectivity or isomerization. Results of this investigation can be explained in large part by the concn of hydrogen absorbed on the catalyst surface.