灵活多效催化裂化工艺集总动力学模型

针对灵活多效催化裂化(FDFCC)工艺,以工业装置数据为基础建立了重油提升管催化裂化10集总和汽油提升管催化裂化7集总动力学模型,求取了10集总模型的43个动力学参数和7集总模型的18个动力学参数.结果表明,所获得的模型动力学参数是可靠的,所建立的模型能够较好地预测FDFCC装置的产品产率,并对汽油组成和丙烯产率具有良好的预测性.     

渣油加氢脱金属动力学模型研究

依据茂名渣油加氢工业装置(S-RHT)的大量实测数据,通过合理的模型假定,采用常规的动力学模型研究方法,建立了渣油加氢脱金属动力学模型和催化剂失活函数表达式.经过工业装置实测数据的验证,拟合结果良好.该方法为进一步研究全面的渣油精制动力学打下了基础.     

工业渣油催化裂化过程六集总组合反应器模型

工业渣油催化裂化反应主要发生在提升管段和出口的沉降器段的复杂流体动力学区域。通过对工业现场装置流程和过程数据的分析,将发生裂化反应的整个反应器中提升管部分作为活塞流反应器(PFR)和沉降器部分作为全混流反应器(CSTR)的串联组合反应器,并按照渣油催化裂化反应特点建立了简化的6集总组分的串行和并行动力学反应网络模型。所建立的稳态催化裂化反应产率预测模型在数学上表现为提升管部分的微分方程组和沉降器部分的代数方程组。模型设置7个装置因数来校正模型的计算产率与实测产率之间的偏差,并采用工业现场数据回归装置因数。通过对工业装置数据的计算比较,得到的模型产率预测精度很好地满足在线软测量计算要求。     

催化裂化提升管反应器建模研究

根据提升管反应器的动态机理,考虑反应对压力的影响,结合物料平衡、能量平衡方程,建立了馏分油5集总催化裂化反应动力学模型。使用Nelder-Mead最优化法进行了参数的拟合,并用MATLAB对模型进行了仿真。通过对工业装置数据的计算比较表明,该模型能较好的预测催化裂化产品产率,可用于实际催化裂化过程。     

工业催化裂化过程在线工艺计算技术开发与应用

针对MIP工艺的原料（减渣／油浆层、蜡油／回炼油层、柴油层）和产物（汽油、液化气＋干气、焦炭）六个集总组分渣油催化裂化动力学模型,并根据某工业催化裂化提升管反应器流场特性应用序列理想平推流反应器与理想全混流反应器模型的混合反应器模型,建立了工业渣油催化裂化装置反应再生过程工艺计算模型。结合采用由化验值校正和模型参数交替校正的双重校正策略,在某工业连续催化裂化装置上进行在线工艺计算应用,以在线预测过程的裂化产物收率与产物分布。在进料和反应操作条件较大的变化范围内,在线预测趋势和预测精度均令人满意,符合工业过程先进控制的工艺计算精度需求。     

渣油加氢脱硫反应动力学物理模型的建立

催化加氢以其轻质油品收率高和产品质量好等优点,成为石油加工行业发展较快的技术之一。石油馏分HDS反应动力学一直受到研究者的广泛关注。提出了以集总方法研究渣油HDS反应动力学的科学合理性。运用集总的方法,根据硫化物HDS反应机理,结合渣油中的硫化物检测分析水平和计算工作量等因素,提出了以渣油四组分中的硫化物分析为基础的HDS动力学模型,不仅可以预测渣油加氢过程中的硫化物转化率,还可预测加氢生成油中的类型硫化物存在情况,具有较好的应用前景。     

渣油催化裂化反应再生系统过程优化

本文采用十三集总动力学模型对大庆油田化工总厂60万吨／年渣油催化裂化装置进行了模拟计算,考查了不同掺渣比,反应温度,雾化蒸汽量和急冷油量对产品分布的影响,确定了较优的工艺条件。研究结果表明,该模型具有良好的模拟精度,能很好地预测不同条件下的产品分布,对生产具有一定指导意义。     

催化裂化模拟优化软件的工业应用

以催化裂化集总动力学模型为基础,开发了催化裂化模拟优化软件(FCCSW)。该软件可预测催化裂化主要产品分布、产品性质和最佳操作条件。FCCSW软件在工业催化裂化装置上得到了良好的验证和应用,以最小化柴油收率为优化目标,根据软件推荐的操作条件进行调整后,汽油收率提高1.46个百分点,液化气收率提高0.86个百分点,柴油收率降低2.91个百分点,降低装置柴汽比效果明显。     

渣油加氢脱残炭的动力学模型研究

根据渣油残炭的构成来源和加氢脱残炭的反应历程．提出了渣油加氢脱残炭的三集总一级反应动力学模型．并建立一集总和二集总加氢脱残炭反应动力学模型与之进行了比较。结果表明．三集总一级加氢脱残炭反应动力学模型的预测精度优于一集总和二集总的反应动力学模型。     

S-Zorb反应器的机理建模与基于改进鲸群算法的参数估计

汽油吸附脱硫(S-Zorb)装置是我国催化裂化汽油的主要脱硫装置之一。针对S-Zorb工业模型缺乏,实验室模型无法预测产品油辛烷值等问题,作者提出了一种基于过程机理的反应器建模方法。该方法将催化裂化汽油划分为5个集总,在集总基础上构建了反应动力学模型、辛烷值关联模型等。另外,针对传统群优化算法参数估计耗时长的缺点,提出了一种改进的鲸群算法,并成功应用于S-Zorb模型。通过与工业数据对比验证结果表明,所提模型能够有效地预测脱硫率、辛烷值等关键指标,从而为后续的优化生产提供基础。     

Z-18抗焦活化剂在苏丹炼厂重催装置上的应用

介绍了Z–18催化分子筛抗焦活化剂在苏丹喀土穆炼油有限公司重油催化裂化装置（简称KRC）上的工业应用。应用结果表明,该剂在以通过调节催化裂化剂酸性中心为主的机理下使催化剂反应活性得以有效维持,从而减小了催化剂表面结焦,改善了产品分布及产品质量。     

Effect of Feedstocks on High‐Severity Fluid Catalytic Cracking

A novel fluid catalytic cracking (FCC) process, that utilizes a downer reactor, has been developed to enhance the yield of light olefins under high‐severity reaction conditions. The effect of heavier feedstock on this high‐severity fluid catalytic cracking (HS‐FCC) process has been investigated using a small‐scale HS‐FCC pilot plant (0.1 b/d). Hydrotreated and virgin vacuum gas oils (VGO), hydrotreated and virgin atmospheric residues (AR) were used as test‐feeds in a previous study. The yield of desired products, such as gasoline and light olefins, produced from virgin VGO cracking was 79 wt.‐%, which is much higher than that obtained from a conventional FCC process. In the case of hydrotreated VGO, the yield of desired products decreased to 76%, however. On the other hand, AR feeds exhibited a performance similar to VGO with a slight increase in coke formation. In this study microactivity test (MAT) results are reported in which the activity and selectivity of the Y‐zeolite based catalyst is evaluated. Kinetic modeling was also done based on a four‐lump reaction model.     

Kinetic modelling of 1, 3, 5-triisopropylbenzene catalytic cracking using a CREC Riser Simulator emulating FCC operation: The C/O ratio effect

The present study establishes the suitability of a kinetic model for the catalytic cracking of 1, 3, 5-triisopropylbenze (TIPB) using the data obtained in the Chemical Reactor Engineering Centre (CREC) Riser Simulator. The postulated kinetic model accounts for both the TIPB and the various major products formed experimentally, such as: 1, 3-diisopropylbenzene, isopropylbenzene, benzene, propylene, and coke. It is proven that the proposed kinetics is suitable to describe the chemical concentration changes in a CREC Riser Simulator at various reaction times, partial pressures, temperatures, and C/O (catalyst/feedstock) ratios. It is demonstrated that the proposed kinetics simulates well the experimental data from the CREC Riser Simulator, including an experimentally observed C/O optimum ratio. It is anticipated that this type of kinetic model, accounting for intrinsic kinetics, coke deactivation, and diffusional phenomena, could have significant value in establishing the influence of catalyst solid fluxes, at set hydrocarbon feed fluxes, in both industrial riser and downer fluid catalytic cracking (FCC) units.     

FCA-100A重油裂解助剂在催化装置的工业试验

介绍中油大连石化公司140万吨/年重油催化裂化装置试用上海纳克公司生产的FCA-100A重油裂解剂情况,通过近2个月的工业应用情况的日常数据统计分析和工艺标定得出FCA-100A助剂在原料基本不变的情况下可提高催化液收0.79个百分点(助剂比例达到19.49%),烧焦、油浆产率降低1.22个百分点;催化剂单耗下降0.1kg/t以上。     

Lumped Kinetic Modeling Method for Fluid Catalytic Cracking

A new fluid catalytic cracking (FCC) lumped kinetic modeling method was put forward to improve the prediction accuracy of the FCC kinetic model. This model divided the feedstock into three lumps and the products into six lumps. The parameters of the kinetic model were obtained by combining the fourth-order Runge-Kutta integral method and the two-swarm cooperative particle swarm optimization algorithm. Compared with dividing the feedstock according to the group composition and the distillation range, the average relative error between the experimental data and the calculated values proves the higher fitting accuracy of the new lumped method. The kinetic model established by the method exhibits better adaptability to different feedstock and fewer requirements for feedstock analysis data.     

Towards modelling production of clean fuels: sour gas formation in catalytic cracking

Although one important by‐product of fluidised‐bed catalytic cracking of hydrocarbons is the sour gas (mainly hydrogen sulfide), there are no kinetic models to predict its generation. Moreover, if feedstock sulfur is not directed to sour gas, it will be present in gasoline, cycle oils and coke. These products are used as fuels, which could emit sulfur oxides during their combustion. In order to be able to model production of clean fuels, a kinetic scheme that considers sour gas as unmatched product was developed; meanwhile, the sulfur distribution in cracking products is predicted. Model parameters are validated using industrial operating data. This kinetic scheme is employed to model steady state operation of an industrial catalytic cracking riser and to find operating conditions that diminish the sulfur content in fuels. Copyright © 2004 Society of Chemical Industry     

Numerical Simulation on Gas-Solid Two-Phase Turbulent Flow in FCC Riser Reactors(Ⅰ) Turbulent Gas-Solid Flow-Reaction Model

Gas-solid two-phase turbulent flows,mass transfer,heat transfer and catalytic cracking reactions areknown to exert interrelated influences in commercial fluid catalytic cracking(FCC)riser reactors.In the presentpaper,a three-dimensional turbulent gas-solid two-phase flow-reaction model for FCC riser reactors was devel-oped.The model took into account the gas-solid two-phase turbulent flows,inter-phase heat transfer,masstransfer,catalytic cracking reactions and their interrelated influence.The k-V-k_P two-phase turbulence modelwas employed and modified for the two-phase turbulent flow patterns with relatively high particle concentration.Boundary conditions for the flow-reaction model were given.Related numerical algorithm was formed and a nu-merical code was drawn up.Numerical modeling for commercial FCC riser reactors could be carried out with thepresented model.     

Catalytic conversion of postconsumer PE/PP waste into hydrocarbons using the FCC process with an equilibrium FCC commercial catalyst

A mixture of postconsumer polyolefin waste (PE/PP) was pyrolyzed over cracking catalysts using a fluidizing reaction system similar to the fluid catalytic cracking (FCC) process operating isothermally at ambient pressure. Experiments carried out with various catalysts gave good yields of valuable hydrocarbons with differing selectivity in the final products dependent on reaction conditions. Greater product selectivity was observed with a commercial FCC equilibrium catalyst (Ecat‐F1) with more than 50 wt % olefins products in the C₃‐C₆ range. A kinetic model based on a lumping reaction scheme for the observed products and catalyst coking deactivations has been investigated. The model gave a good representation of experiment results. Moreover, this model provides the benefits of lumping product selectivity, in each reaction step, in relation to the performance of the FCC equilibrium catalyst used, the effect of reaction temperature, and the particle size selected. © 2009 Wiley Periodicals, Inc. J Appl Polym Sci, 2009