FCC原料预处理催化剂FF-14的性能和应用

介绍了催化裂化原料加氢预处理催化剂FF-14的反应性能及工业应用.FF-14催化剂具有较好的加氢脱硫性能及原料适应性.工业应用结果表明,FF-14加氢催化剂脱硫活性高.     

FH-98加氢催化剂在石油三厂120万 t/a 中压加氢装置的应用

抚顺石化公司石油三厂120万 t/a 柴油中压加氢装置于2002年7月建成投产,并开车一次成功.2010年装置换用 FH-98加氢精制催化剂,工业应用表明,FH-98催化剂具有优异的加氢性能和高的加氢脱硫活性,加氢处理焦化汽油、柴油混合油,生产清洁柴油和合格的乙烯裂解原料.     

高空速重整原料预加氢技术的开发及工业应用

为适应催化重整装置扩能改造及连续重整预加氢技术发展的需要，开发了高空速重整原料预加氢技术，介绍了抚顺石油化工研究院开发的高空速重整原料预加氢催化剂的反应性能及其工业应用情况。     

FH-DS柴油深度加氢脱硫催化剂的工业应用

为扩大福建炼油化工有限公司柴油加氢装置的处理量,并能生产出含硫质量分数低于300μg.g-1的低硫柴油,以满足公司新标准车用柴油的出厂要求,柴油加氢装置选用了抚顺石油化工研究院研制开发的FH-DS柴油深度加氢脱硫催化剂。工业应用结果表明:FH-DS催化剂具有在较高空速条件下仍保持活性高、选择性好的特点;具有良好的深度加氢脱硫活性和原料适应性。采用FH-DS催化剂达到了装置扩能的目的,装置处理能力由60万t/a提高至80万t/a;同时还生产出了硫质量分数低于300μg.g-1的低硫柴油,满足了公司车用柴油的出厂要求。     

ＦＺＣ系列常压渣油加氢处理催化剂的开发及工业应用

为提高我国的渣油加氢处理技术，抚顺石油化工研究院（ＦＲＩＰＰ）开发了ＦＺＣ系列常压渣油加氢处理配套催化剂，可用于含硫常压渣油加氢处理。工业应用结果表明，催化剂活性高、稳定性好，装置运行平稳，产品质量好，满足了用户生产使用的要求。     

SHP-01型裂解汽油加氢催化剂的工业应用

介绍了SHP-01型催化剂在中原石化裂解汽油加氢装置上的工业应用情况,对催化剂投用、工业试验标定及再生过程进行了技术分析,SHP-01催化剂具有良好的原料适应性和较长的使用寿命,综合性能优于曾使用过的同类催化剂.     

惠州石化VRDS装置渣油深度脱金属的工业应用

论述了CLG公司固定床渣油加氢处理技术在中海油惠州石化有限公司400万t/aVRDS装置的工业应用。该装置原料设计镍+钒含量102 wppm,经深度加氢脱金属,加氢重油产品镍+钒含量可以达到10 wppm以下。该装置第一周期运行结果表明,深度加氢脱金属同时能够实现装置长周期运行。     

丁醛气相加氢催化剂的工业应用试验

介绍了丁醛气相加氢催化剂在工厂应用中的加氢流程、装填、升温还原等情况。工业考核及工业运转数据表明,丁醛气相加氢催化剂在工业应用上是成功的,其性能达到了国际同类催化剂的先进水平,能够满足工厂生产要求。     

焦化干气加氢催化剂在制氢装置的长期稳定运行

介绍了JT-1G型加氢转化催化剂在锦州石化分公司的工业应用。生产运行表明，该催化剂具有很强的有机硫加氢转化活性，完全满足在制氢装置生产过程中对制氢原料的净化要求。     

新型蜡油加氢处理催化剂的性能评价与工业应用

KL-18催化剂是新型高活性蜡油加氢处理催化剂,以脱沥青油为原料,按照工业装置运行工艺条件,对KL-18催化剂进行加氢处理小试性能评价,结果表明：当反应温度为375～390℃时,硫、氮含量均小于10μg·mL-1;重润馏分（>460℃）收率从68.92%逐渐降低到45.74%;生成油重润黏度指数由81逐渐提高到103;芳烃含量由2.0%逐渐降低到1.3%;说明该催化剂具有良好的加氢精制活性、芳烃深度饱和及提高黏度指数的能力。对其工业生产应用情况进行跟踪,生成油质量达到了后续加氢异构段的进料要求,满足催化剂工业应用的要求。     

Hydroprocessing of straight run diesel mixed with light cycle oil from fluid catalytic cracking,using sulfide NiMo catalyst on zeolite-containing supports

It is proposed that the sulfide NiMo system supported on alumina-SAPO-31 composite (NiMo/Al₂O₃-SAP catalyst) be used to obtain high-quality diesel fuel from a mixture of straight run diesel (SRGO) and light cycle oil (LCO) produced by fluid catalytic cracking (FCC). It is shown that the use of this catalyst ensures the synthesis of diesel fuel of higher quality upon hydroprocessing a feedstock with 30 wt % LCO, compared to the traditional sulfide NiMo/Al₂O₃ or CoMo/Al₂O₃ catalysts. It is found that the content of aliphatic hydrocarbons is raised in the products of hydrotreatment, compared to the initial feedstock. This confirms the ability of NiMo/Al₂O₃-SAP catalyst to facilitate the reaction of ring opening. Using the proposed catalyst should improve the quality of diesel fuels obtained via the hydroprocessing of LCO-containing feedstock.     

重芳烃高效转化生产轻芳烃技术

催化裂化柴油中富集了60%～80%的芳烃,导致催化裂化柴油密度大、十六烷值低,难以通过常规加氢改质技术来生产清洁柴油。本文主要介绍了中国石化抚顺石油化工研究院开发的一种利用富含芳烃的催化裂化柴油来生产轻芳烃的高效加氢转化FD2G新技术。该技术通过对加氢催化剂和工艺技术的组合优化实现了对催化裂化柴油的选择性加氢,可以将催化裂化柴油中富含的重质芳烃高效地转化为轻芳烃等高附加值的产品,为高芳烃含量的催化裂化柴油改质提供了一条经济、有效的加工途径。研究结果表明,应用催化柴油加氢转化FD2G技术加工高芳烃含量的催化柴油,可以生产30％～50％的优质催化重整原料,该馏分中C6～C9芳烃含量超过50%,BTX含量可以达到32%,同时改质柴油质量与原料相比改善幅度较大。     

催化裂化油浆的加工工艺及进展

随着原油变重和炼厂掺炼渣油比例的增加，使重油催化裂化装置加工难度增加，并影响了其产品质量及分布。为了提高重油催化裂化装置的加工能力和轻油收率，外甩油浆是改善催化裂化操作的有效手段。油浆作为劣质的重油，催化裂化加工困难。目前油浆用于调和燃料油，但经济效益低。油浆中有相当数量的具有较好裂化性能的烃类，是催化裂化的理想原料，同时富含的稠环芳烃是生产针状焦、增塑剂等高附加值化工产品的原料。本文阐述了催化裂化油浆净化、加氢处理、溶剂脱沥青、溶剂精制、延迟焦化等工艺技术及其发展。     

催化裂化汽油临氢异构化/芳构化改质过程的反应特性

采用工业Ni-Mo/Al₂O₃-HZSM-5催化剂在小型固定床加氢微反装置上对催化裂化（FCC）汽油临氢改质过程的反应特性进行了研究,通过考察反应温度、压力、空速和氢油体积比对改质后的FCC汽油烃类组成的影响,分析了汽油中不同烃类的转化性能。结果表明,氢油比对产物组成影响不大,高温、低压、低空速有利于增加芳烃的选择性,低温、高压、高空速则有利于增加异构烷烃的选择性;临氢改质后,FCC汽油的烯烃含量明显降低,芳烃和异构烷烃含量增加,因而产品汽油的辛烷值基本保持不变;全馏分、轻馏分和重馏分FCC汽油临氢改质实验结果表明,烯烃含量较高的轻馏分具有更高的转化活性;在FCC汽油临氢改质过程中,同碳数的端烯烃反应活性高于内烯烃,直链烯烃的反应活性高于支链烯烃。     

国内重油催化裂化催化剂工业应用现状

介绍了国内典型重油催化裂化催化剂工业应用现状。分别阐述高掺渣比催化剂、抗重金属型催化剂、增产低碳烯烃催化剂和加工M-100专用CORH、CMO催化剂的使用情况,并对各催化剂的性能进行了综合比较,指出不同催化剂所适用原料的特性,最后提出了新型重油催化裂化催化剂的发展趋势。     

Effect of multistage hydroprocessing on aromatic and nitrogen compositions of shale oil

Geokinetics crude shale oil, a distillate and processing intermediates sampled during four-stage catalytic hydroprocessing of the distillate were analysed for total nitrogen, basic nitrogen and olefinic and aromatic contents. Successive hydroprocessing stages yielded products containing 80, 46, 16 and 2% of the nitrogen content in the feedstock. Total nitrogen, basic nitrogen and aromatic contents were also reduced. Apparent relative reactivities of aromatic hydrocarbons and nitrogen-containing compounds are in agreement with reactivities observed in model compound studies. Hydrodenitrogenation of nitrogen-containing compounds occurred concurrently with hydrogenation of non-nitrogen-containing aromatic hydrocarbons. Hydroprocessing conditions necessary for essentially complete removal of nitrogen yielded a refined oil with low aromatic content.     

Fundamental Studies of Transition Metal Sulfide Hydrodesulfurization Catalysts

Hydroprocessing catalysts based upon the transition metal sulfides have been widely used for over 60 years and catalysts such as Co/Mo/Al₂O₃ remain the industry “workhorses” in hydroprocessing of petroleum-based feedstocks [1]. Such applications include sulfur removal (hydrodesulfurization), nitrogen removal (hydrogenitrogenation), and product quality improvement (hydrotreating, hydroconversion). Original interest (prior to World War II) in these catalysts centered on their activityin the hydrogenation of coal liquids which contain considerable amounts of sulfur, thus maintaining the transition metal in the sulfided state. It was quickly discovered that Co, Ni, Mo, and W sulfides and their mixtures were the most active and least expensive of the transition metal sulfides [2]. Later (post-World War II) their major uses shifted to hydroprocessing of sulfur- and nitrogen-containing petroleum-based feedstocks with Co- and Ni-promoted Mo and W catalysts usually supported on Al₂O₃. However, as petroleum feedstock supplies dwindle, we are required to process larger quantities of “dirtier” feeds containing larger amounts of sulfur, nitrogen, and metals. In order to meet these requirements in the future, a new generation of transition metal sulfidebased catalysts will be needed which have higher activities, greater selectivity to desired products, and greater resistance to poisons.     

Nitrogen compound distributions in hydrotreated shale oil products from commercial-scale refining

The distributions of nitrogen compounds in crude and hydrotreated shale oil products have been determined. About 11600 m³ (73000 bbl) of Paraho retorted shale oil were hydrotreated by The Standard Oil Company of Ohio at their Toledo refinery. A hydrotreated whole product, a jet fuel, a diesel fuel, and a residuum were produced and individually separated into compound-type fractions by adsorption chromatography. The nitrogen compound types in these fractions were characterized by i.r. spectroscopy, differential potentiometric titration, and high-resolution m.s. The distributions of nitrogen compound types and nitrogen base types in the hydrotreated products are compared with those in the Paraho retorted shale oil feedstock used in the hydroprocessing. The nitrogen compound types that were readily hydrodenitrogenated during commercial-scale refining are similar to nitrogen compound types removed during one-pass, bench-scale hydroprocessing.     

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.     

Fundamental Studies of Transition Metal Sulfide Hydrodesulfurization Catalysts

Hydroprocessing catalysts based upon the transition metal sulfides have been widely used for over 60 years and catalysts such as Co/Mo/Al₂O₃ remain the industry “workhorses” in hydroprocessing of petroleum-based feedstocks [1]. Such applications include sulfur removal (hydrodesulfurization), nitrogen removal (hydrogenitrogenation), and product quality improvement (hydrotreating, hydroconversion). Original interest (prior to World War II) in these catalysts centered on their activityin the hydrogenation of coal liquids which contain considerable amounts of sulfur, thus maintaining the transition metal in the sulfided state. It was quickly discovered that Co, Ni, Mo, and W sulfides and their mixtures were the most active and least expensive of the transition metal sulfides [2]. Later (post-World War II) their major uses shifted to hydroprocessing of sulfur- and nitrogen-containing petroleum-based feedstocks with Co- and Ni-promoted Mo and W catalysts usually supported on Al₂O₃. However, as petroleum feedstock supplies dwindle, we are required to process larger quantities of “dirtier” feeds containing larger amounts of sulfur, nitrogen, and metals. In order to meet these requirements in the future, a new generation of transition metal sulfidebased catalysts will be needed which have higher activities, greater selectivity to desired products, and greater resistance to poisons.