柴油加氢裂化转化的切割方案

以直馏柴油和催化裂化柴油为原料,选用柴油加氢精制催化剂与柴油缓和加氢裂化催化剂的复合催化体系,采用固定床双反应器串联、一次通过工艺进行加氢裂化转化实验。结果表明:在直馏柴油加氢裂化多产乙烯裂解原料过程中,若能将重石脑油馏分中低于90 ℃的轻组分,以及柴油馏分中高于250 ℃馏分段分离出来,可有效提高乙烯裂解原料的品质。在催化裂化柴油加氢裂化生产高辛烷值汽油和高十六烷值柴油过程中,与大于220 ℃馏分相比,200～220 ℃馏分的密度和链烷烃质量分数较低,收率约为前者的16.4%;200～220 ℃馏分单环芳烃质量分数较高,可以作为回炼组分用以提高汽油中芳烃质量分数。     

膜分离技术在加氢裂化装置低分气提浓制氢气中的应用

为提浓回收利用低分气中的氢气,中国石油长庆石化公司在加氢裂化装置上设置了Prism膜分离单元。标定结果表明,自2010年建成投产以来,Prism膜分离单元已连续稳定运行了4 a多;膜系统的实际处理能力为4 600~5 500 m3/h,比设计指标低1 500~2 400 m3/h;虽然产品氢(渗透气)中H2的体积分数只有约92%(比设计指标低约6个百分点),但完全能满足加氢裂化装置的用氢要求;氢回收率大于设计指标要求的88%。     

不同催化体系下渣油悬浮床加氢的结焦状况

 在高压反应釜中，采用不同分散型催化剂体系，以克拉玛依常压渣油为原料进行加氢裂化反应，测定反应体相产物>360℃馏分的甲苯不溶物含量和颗粒大小，并对其进行SARA四组分分离，考察了反应器结焦状况与反应产物性质之间的关系。结果表明，反应产物体相>360℃馏分的甲苯不溶物含量、沥青质含量与反应器内部结焦量有直接关系，甲苯不溶物和沥青质含量越高，反应器内部结焦趋势越明显。反应器内部的结焦状况受甲苯不溶物粒度大小的影响相对较小。     

Mathematical modelling of a hydrocracking reactor for triglyceride conversion to biofuel: model establishment and validation

In the study, a 2D, non‐isothermal, heterogeneous model of a triglyceride hydrocracking reactor is investigated. The internal heat and mass transfer within the phases in the reactor were considered using the film theory. The conservation equations for energy and mass were solved simultaneously using appropriate numerical techniques whose reliability was assessed by comparison of the results with previously reported experimental data. The modelling was performed with consideration of two proposed hydrocracking kinetic models. The model predictions showed reasonable correlation with published experimental data and conversion rates. The calculations indicated that at feed temperature of 380 °C, liquid hourly space velocity of 8 h^?1 and hydrogen : feed ratio of 1500:1, the total triglyceride conversion was 82.54% for four major classes of hydrocarbons (light, middle, heavy and oligomerised). In addition, the concentration distribution and temperature profile along the reactor were investigated. The product concentrations along the reactor show that higher rates of production at the beginning of the reactor were achieved because of high concentration of triglyceride due to the exothermic hydrocracking reactions and counter‐current flow modes of triglyceride and hydrogen; a jump of 90 °C was shown at the beginning of the reactor temperature profile. Copyright © 2014 John Wiley & Sons, Ltd.     

30年来大庆加氢裂化装置的发展——纪念我国第一套加氢裂化联合装置建成投产30周年

回顾了我国第一套大型加氢裂化联合装置建成投产的过程以及30年来的发展.对在大庆石化总厂加氢裂化装置上进行的劣质油中压加氢改质和蜡油中压加氢处理的工业试验及其应用作了阐述.     

先进控制技术在加氢裂化装置的应用

介绍了HoneywellHi Spec公司的鲁棒多变量预估控制技术在齐鲁石油化工公司胜利炼油厂加氢裂化装置的应用情况。通过现场阶跃测试获取装置的动态数学模型 ,结合分馏工艺计算软件包、支路平衡控制、非线性液位控制和质量点数据校正等辅助手段 ,消除装置的“瓶颈” ,从而保证装置的平稳安全运行 ,获得良好的经济效益。     

基于超临界流体萃取的悬浮床加氢尾油的分离与评价

 用超临界流体萃取分馏(SFEF)装置将克拉玛依渣油悬浮床加氢尾油（KMHR）分离为8个窄馏分和萃余残渣。测定并计算了馏出油的残炭及杂质脱除率，考察了窄馏分SARA族组成、残炭、密度、硫、氮、金属及平均结构参数等的递变规律，预测了窄馏分的裂化性能，并用XRD表征了甲苯不溶物的存在形态。结果表明，超临界流体萃取可以脱除尾油中全部沥青质及甲苯不溶物，质量分数99.5％以上的金属和70.4％以上的残炭富集到萃余残渣中。馏出油符合催化裂化或加氢裂化进料要求并具有优良的裂化性能。     

用正交配置法模拟加氢裂化反应器

结合物料平衡、能量平衡和加氢裂化反应动力学方程,按照加氢裂化反应的特点,建立了加氢裂化反应器6集总动态机理模型。反应动力学采用原料油、柴油、航空煤油、重石脑油、轻石脑油、气体6集总模型。对总动态机理模型提出了正交配置法和龙格-库塔法相结合的求解方法。新的求解方法计算量小、精度高,并且能求得微分数学模型的近似解析解。应用6集总动态机理模型对加氢裂化反应器进行了模拟,考察了模型的预测精度。模拟结果表明,该模型能较好地模拟和预测加氢裂化产品的收率分布和反应器的温度分布,具有较高的预测精度,模型可靠。     

柴油润滑性的影响因素考察

以加氢裂化柴油为空白原料，考察了不同芳烃、硫化物、氮化物和含氧化合物及其混合物对柴油润滑性的影响。结果表明，微量的环烷酸和含氮化合物能有效地改善柴油润滑性，而单环、双环芳烃和硫化物对柴油润滑性的改善效果不明显；不同的化合物混合对柴油润滑性的影响不同。     

Performance Evaluation Studies of First- and Second-Stage Hydrocracking Catalysts Using Kuwait Vacuum Gas Oil Feedstocks

In a two-stage hydrocracking process, two types of catalyst are used to remove undesirable contaminants (such as S, N, hydrogenation of aromatic compounds, etc.) and convert the heavy feedstock to lighter products. In the present work, individual set of experiments were conducted to obtain information regarding activity and selectivity with emphasis on the evaluation of kinetic parameters of first- and second-stage commercial catalysts used in hydrocracking process. The performance tests were conducted in a down-flow fixed-bed hydrocracking pilot plant using a single reactor. The hydrotreating type A catalyst and hydrocracking type B catalyst were used individually with typical Kuwaiti refinery feedstocks, namely, hydrotreated vacuum gas oil (HVGO) and unconverted residual oil (UCRO), respectively. The order of reaction in this study shows first-order kinetics for HDS and HDN over CAT-A, and first-order hydrocracking conversion over CAT-B. For CAT-A the activation energies were found for HDS and HDN reactions at 22 and 27.3 kcal/gmole, while for CAT-B activation energies were 27.4 kcal/gmole.