催化裂化催化剂小型自动加料器

催化剂小型加料器可根据催化裂化装置生产工艺的要求,分批定时和定量地进行加料。它与人工操作相比,不仅能够提高装置操作的稳定性,而且能降低催化剂的损耗。     

延安炼油厂催化裂化自动加料器的改进

催化小型加料器是催化生产中必不可少的一台催化剂加料设备,其运行的平稳直接影响到催化的收率。随着自动控制技术的发展,催化小型加料器也逐步向控制简单运行可靠方向发展。原来老式的加料器其技术落后,程序复杂,故障率高,维护费用居高不下,仪表工的劳动强度也很大。新型的加料器流程简单,维护方便,故障率低,是催化裂化装置催化剂加料的理想选择。     

容积式自动加料器的设计思路

流化催化裂化装置上都安装有小型自动加料器,大致有两种,秤重式小型自动加料器和计时式小型自动加料器;秤重式小型自动加料器计量比较准确,计时式小型自动加料器比较灵活。容积式自动加料器可以同时具备以上两种加料器的优点。     

催化剂小型加料器的设计及使用

阐述了小型人工加料器的设计制作及使用方法,通过装置运行经济效益分析,证明在小型催化裂化装置中,有自动加料器无法比拟的优点 。     

重油催化裂化装置运行实践及改进意见

简要介绍盐城市石油液化气厂利用苏北原油经常压蒸馏，常压重油直接进入同轴式催化裂化反应再生器，在没有设置（内）外取热器的情况下，生产汽油、柴油和液化石油气的运行实践及其改进意见。     

提高重油催化裂化装置经济效益的措施

以装置经济效益最大化为目的，建立了数学分析模型，并结合大港石化公司的实际状况对不同的生产工艺(如干气预提升、终止剂技术、稳定汽油回炼等)、操作条件(如反应温度、催化剂类型等)进行了统计分析，讨论了这些方案对产品分布和经济效益的影响。同时，以大量生产数据为基础，找出了平衡剂上Ni含量和Sb/Ni与催化剂活性的关系，以及平衡剂活性对转化率和各催化产品分布的影响，从而最终确定出装置经济效益最大化数学模型。讨论了当原料油性质、石油产品市场、新鲜催化剂价格变化时，新鲜催化剂补充速率的调整方案。     

重油催化裂化的工艺改进

针对重油催化裂化生产工艺存在生焦率高、能耗高、轻柴油贮存安定性差、含硫污水冲击污水处理场等问题,采用两级高效再生,大剂油比高温短接触时间,高效雾化喷嘴、快速中止反应、轻烃预提升、再生烟气能量回收、含硫污水汽提等国内外先进技术,解决了生产中存在的这些问题。使生焦率下降了1％～2％(绝对值),能耗从6190.2GJ/t降至3380.0GJ/t。指出今后应进一步降焦、降能耗,治理再生烟气中的SO_x和NO_x。     

The fluidized-bed catalytic cracking unit building its future environment

Fluidized-bed catalytic cracking (FCC) has been considered as one of the largest catalytic process in the world. FCC is the name for a complex process unit that cracks long molecules from gas oils and residua into added value shorter fuel compounds; additionally, this process can be used to produce important petrochemical precursors, such as propylenes. Although historically FCC has been used to optimise production of light cycle oils, gasoline and olefins, nowadays is convenient to revisit its mission. In order to integrate FCC process inside current development and environment respect, it is necessary to see it as a very flexible process. This flexibility will require deeper knowledge about environmental impact of process operation and production objectives, transport phenomena and catalytic reactions taking place inside the riser, the main reactor of the FCC converter, and energy balance integrating energy recovered/generated in the regenerator. This work is devoted to briefly review some propositions about the use of FCC converters and how these aspects demand knowledge of riser reactors, change in the methodology to estimate effective reaction rates (consequence of variation of kinetic and transport phenomena, at catalyst scale and along the riser) and catalyst activity, as well as control actions and its effect on the energy balance of the converter; operation and environmental concerns surrounding this process are addressed. Finally, it tries to draw attention on some facts that need to be analysed in order to ensure the sustainable development of this important process in the short future.     

催化裂化工艺及催化剂的技术进展

介绍了国内外催化裂化工艺以及催化剂的技术进展,并对汽油降烯烃和降硫、生产低硫低芳烃柴油、多产低碳烯烃、重油转化催化裂化工艺及催化剂方面的技术现状和最新进展进行了阐述。对催化裂化工艺和催化剂的发展趋势提出了相关的建议。     

Laboratory evaluation of the impact of the addition of resid in FCC

The conversion and product distributions from a mixture of 10% atmospheric tower bottom resid and a DO hydrocarbon cut similar to LCO that represented commercial feedstocks were assessed over two equilibrium commercial FCC catalysts in a laboratory CREC Riser Simulator reactor. The reaction temperature was 550 °C, the catalyst to oil ratio was 5.8 and the reaction times were up to 25 s. The conversion of the mixture as compared to the DO base feed was higher in the case of the most active, conventional catalyst, and remained very similar on the resid catalyst. Since the yields of the main hydrocarbon groups dry gas, LPG, gasoline and coke followed very similar trends when the two pure feedstocks were converted, the corresponding yields from the mixture also obeyed that behaviour, and were the consequence of the conversion reached. The impact of the different catalyst formulations was observed in, for example, the selectively different yields obtained from the conversion of the resid, and in the composition of the gasoline. Independently of the catalyst, the gasoline was more olefinic and less aromatic when the resid was present. It was shown that in order to evaluate properly a given combination of feeds, catalysts and conditions, they must be considered together.     

FCC柴油氧气氧化萃取法脱硫研究

以氧气作氧化剂,甲酸作催化剂,N-甲基吡咯烷酮(NMP)作萃取剂,采用催化氧化反应与溶剂萃取相结合的方法对催化裂化柴油进行了氧化萃取脱硫实验。通过单因素实验考察了催化剂用量、催化氧化温度、时间、氧气压力及萃取剂的用量等对催化裂化柴油硫质量分数的影响。通过实验得出最适宜的脱硫条件为:反应温度80℃,反应时间90 min,充氧压力0.6 MPa,V(催化剂)∶V(柴油)=10%。经催化氧化,柴油硫质量分数可从1 694.2μg/g降到190.8μg/g,脱硫率达到88.7%;在V(萃取剂)∶V(柴油)=1.0和室温条件下,用NMP萃取3次,柴油硫质量分数为37.5μg/g,小于50μg/g,达到欧Ⅳ排放标准的要求。     

Challenges, catalyst technology and catalytic solutions in resid FCC

The concurrent evolution of resid fluid catalytic cracking (RFCC) processes and catalyst technology over the years is discussed. Resid FCC catalysts today are designed making use of the following features: (a) High activity, selectivity and metals resistant zeolites; (b) Highly accessible catalyst architecture for optimal site utilization, bottoms cracking, Conradson carbon residue (CCR) conversion and easy stripping; and (c) Specially designed metal-support interaction systems to reduce the detrimental effects of metal contaminants. The future will require even more robust RFCC catalyst systems. These catalyst systems should be very accessible and effective in cracking large hydrocarbon molecules and should have the capability to handle contaminants such as metal-, sulfur-, and nitrogen-compounds. Conversion of CCR to non-coke components will be crucial in order to reduce the delta coke and hence improve the processability of heavier resids. Processability here is meant not only in terms of coke and heat balance considerations, but also involves avoiding fouling of the unit hardware by unconverted heavy hydrocarbons and coke precursors. Last, but not the least, present and future catalyst technology must be formulated and adapted to the specific commercial process unit needs and constraints, thus leading to the most cost effective solution for the refiner.     

催化裂化装置吸收稳定系统液态烃中C_2含量影响因素分析

分析了影响催化裂化装置吸收稳定系统液态烃中C2含量的因素,如吸收系统操作温度、操作压力、液气比等。结果发现,解吸塔塔底温度和中部温度对液态烃中C2含量影响最大、最直接。控制好吸收塔和解吸塔操作,可使催化裂化装置液态烃中C2体积分数控制在0.02%以内。     

Reaction performance of FCC slurry catalytic cracking

The condensation of heavy hydrocarbon causes the coke formation inside the disengager vessel. Slurry oil is the heaviest component of FCC hydrocarbon products and most likely to be condensed to form coke. Converting slurry to lighter hydrocarbons can alleviate coke formation. The slurry cracking experiments were carried out in a confined fluidized bed reactor. The results showed that the crackability of slurry was lower than that of FCC feedstock, due to the difference of their properties. About 30 wt.% heavy oil remained in the product after the slurry was cracked, but its end point declined and the heavier component decreased. The comparison of slurry cracking results at different reaction temperatures and regenerated catalyst contents indicated that the appropriate operating conditions for slurry conversion were the reaction temperature of 500 °C and the regenerated catalyst content within 25–50 wt.%.     

Relative reactivities of alkanes in multi-component catalytic cracking reactions

An experimental technique is discussed for measuring relative reactivities of alkanes in the catalytic cracking of multi-component hydrocarbon mixtures over a heterogeneous, Y-zeolitebased catalyst at 250–350 °C. With the technique, ca. 0.1 l of an alkane mixture is evaporated and contacted with a catalyst, after which the mixture of reaction products and the unreacted feed enters the chromatographic column and is immediately analyzed. The technique is used to measure relative reactivities of 21 alkanes in a single experiment. The principal results of these experiments are similar to the results of single-component cracking: alkane reactivity rapidly increases with the increase of the carbon number, and methyl-branched alkanes are more reactive than linear alkanes. However, the variations in alkane reactivities as a function of their molecular weight and skeleton structure differ very significantly between single- and multicomponent experiments.     

Kinetic modeling of high-severity fluidized catalytic cracking

This paper presents the results of kinetic modeling of high-severity fluidized catalytic cracking process using a simplified methodology of estimating kinetic parameters. A 4-lump model was used to demonstrate the new approach for modeling the kinetics data that was collected using micro-activity test (MAT) method. MAT experiments were done at 550, 600 and 650 °C. Kinetic parameters for the 4-lump model and the activation energies are presented.