催化液态烃产品硫含量超标原因分析与控制

某炼厂3.5Mt·a^-1重油催化裂化装置液态烃的硫含量控制指标为≤20mg·m^-3。原油的重质化和劣质化,导致液态烃脱硫系统高负荷运行,抗波动能力弱,液态烃产品的硫含量持续超标。本文从催化原料的性质、催化剂活性、吸收油气比、解吸气量、碱液浓度等方面,分析了催化液态烃产品的硫含量超标的原因,通过优化系统的主要控制参数,确保了液态烃的硫含量低于10mg·m^-3,满足工业和民用液态烃的标准要求。     

CA-2000 FCC催化剂在ARGG装置上的应用

详细介绍了CA-2000流化催化裂化(FCC)催化剂在扬州石油化工厂采用中国石化石油化工科学研究院开发的ARGG技术的FCC装置上的应用情况。工业应用结果表明,CA-2000催化剂具有较强的重油转化能力,产品选择性好焦炭产率低,液态烃收率高,抗重金属污染能力较强,可以满足原油性能变差、重油掺炼比提高后工厂的实际生产要求。     

第三代降烯烃催化剂GOR-Ⅲ的开发和工业应用

针对进一步增强催化剂的降烯烃能力、汽油辛烷值不降或少降、提高重油裂化能力和改善产品的市场需求,开发了第三代降烯烃催化剂GORⅢ并进行了工业应用。工业应用结果表明,采用新型基质材料ASP、改性活性组分制备的GORⅢ催化剂降烯烃能力强,同时能在一定程度上提高稳定汽油的辛烷值,且汽油的诱导期延长,催化汽油性质有所改善。GORⅢ催化剂具有活性高、重油裂化能力强,产品选择性好,轻质油收率高等优点。     

降低油浆和焦炭的裂化催化剂RSC-2006的工业应用

催化裂化催化剂RSC-2006采用焦炭选择性较好的大孔富硅基质以降低焦炭收率;添加活性基质组分以增强催化剂的重油裂化能力,同时调节基质的表面酸性,在保证重油预裂化能力的同时改善焦炭选择性;对分子筛进行物化处理,清理和疏通分子筛的孔道,改善分子筛对劣质重油催化裂化的可接近性;引入抗金属污染组分,提高催化剂的抗金属污染能力。工业应用结果表明,催化剂具有优异的重油转化能力和优良的焦炭选择性。与对比催化剂相比,油浆和焦炭收率降低,大幅增加高价值产品收率,液化气+汽油+柴油收率提高。     

LHO-1重油裂解催化裂化催化剂的工业应用

兰州石化公司开发的重油转化和抗重金属能力强的LHO-1催化剂,在锦西石化分公司重油催化裂化装置上进行工业应用.标定结果表明:LHO-1催化剂有高的重油转化能力和较好的抗重金属污染性能力以及优良的降低汽油烯烃含量的特点.     

提高汽油辛烷值催化剂DOCP(jl)配方设计及工业应用

本文介绍了为吉林油田炼油厂2^＃催化裂化装置专门设计的DOCP(jl)提高汽油辛烷值催化剂的配方设计思路及性能特点,并且对其工业应用情况进行了总结。该催化剂产品选择性好,重油裂化性能强,抗金属污染能力强,热和水热稳定性好,能满足该装置直接生产90号汽油的要求。     

AIC-950重油催化裂化催化剂的工业应用

介绍了重油催化裂化催化剂AIC-950在山东东明石化集团有限公司Ⅳ套催化裂化装置上工业应用的情况。结果表明,当AIC-950催化剂达到系统藏量的60%后,与对比剂相比,干气收率下降1.40百分点,同时,油浆收率下降0.11百分点,总液体收率上升1.40百分点,轻质油收率上升1.51百分点。由此可见,采用AIC-950催化剂时产品选择性好、轻质油收率高、总液体收率高、重油转化能力强。     

充分发挥催化裂化深度加工的骨干作用

我国催化裂化总能力已达到1亿吨/年，大部分是重油催化裂化，是我国炼油工业第一位的深度加工装置。当前，由于原料质量变劣，面临装置结焦倾向严重、产品质量差、产品结构不合理以及能耗高等严重挑战。为此需要采取优化操作，降低结焦；采用清洁燃料技术，提高产品质量；调整产品结构；降低能耗和开发重油新催化剂等措施，使催化裂化充分发挥深度加工的骨干作用。     

LHO-1和CDC型重油裂解降烯烃催化剂的性能评价

利用XTL-5型提升管中试装置，对LHO-1和CDC型重油裂解降烯烃催化剂的裂化性能进行了评价。结果表明, 与参比催化剂相比，LHO-1和CDC型重油裂解降烯烃催化剂具有较强的重油转化、降烯烃和芳构化能力。     

ORBIT-3300Z催化剂的工业应用

介绍了ORBIT-3300Z催化剂在湛江东兴炼油厂催化裂化装置上的试验及结果。结果表明,ORBIT-3300Z催化剂具有重油转化能力强,产品选择性好,抗金属能力显著等特点,完全能满足生产要求。     

LCC-2多产液态烃催化剂的工业应用

介绍了LCC-2催化剂在广西东油沥青有限公司催化裂化装置上的应用情况。工业标定结果表明,该催化剂在高含重金属镍的催化原料条件下,提高液态烃收率4.32%,催化裂化转化率达77%,选择性能较好,干气、油浆和焦炭收率分别为3.96%、2.21%和8.87%,但催化剂抗重金属性和耐磨性能不够理想,有待进一步改进。     

Secondary Cracking of C4 Hydrocarbons from Heavy Oil Catalytic Pyrolysis

For C4 hydrocarbons from heavy oil catalytic pyrolysis, the cracking behaviours on catalyst CEP‐1 and quartz sand were investigated in a confined fluidized bed reactor. C4 hydrocarbons show a good cracking ability on CEP‐1, and butene is easier to convert than butane. Only at high reaction temperatures can butane present a good cracking ability. On catalyst CEP‐1, C4 hydrocarbons can undergo not only cracking reactions, but also such reactions as hydrogen transfer, polymerization and aromatization. The conversion of C4 hydrocarbons thermal pyrolysis is high, indicating that free radical reactions play an important part in the secondary cracking of C4 hydrocarbons. The product yields of C4 hydrocarbons pyrolysis on quartz sand are usually lower than those on catalyst CEP‐1. For both catalytic pyrolysis and thermal pyrolysis of C4 hydrocarbons, the selectivity of propene is higher than that of ethene.     

Thermal and catalytic upgrading of a biomass‐derived oil in a dual reaction system

The thermal and catalytic upgrsding of bio‐oil to liquid fuels was studied at atmospheric pressure in a dual reactor system over HZSM‐5, silica‐alumina and a mixed catalyst containing HZSM‐5 and silica‐alumina. This bio‐oil was produced by the rapid thermal processing of the maple wood. In this work, the intent was to improve the catalyst life. Therefore, the first reactor containing no catalyst facilitated thermal cracking of blo‐oil whereas the second reactor containing the desired catalyst upgraded the thermally cracked products. The effects of process variables such as reaction temperature (350°C to 410°C), space velocity (1.8 to 7.2 h^?1) and catalyst type on the amounts and quality of organic liquid product (OLP) were investigated, In the case of HZSM‐5 catalyst, the yield of OLP was maximum at 27.2 wt% whereas the selectivity for aromatic hydrocarbons was maximum at 83 wt%. The selectivities towards aromatics and aliphatic hydrocarbons were highest for mixed and silica‐alumina catalysts, respectively. In all catalyst cases, maximum OLP was produced at an optimum reaction temperature of 370°C in both reactors, and at higher space velocity. The gaseous product consisted of CO and CO₂, and C₁‐C₆ hydrocarbons, which amounted to about 20 to 30 wt% of bio‐oil. The catalysts were deactivated due to coking and were regenerated to achieve their original activity.     

RE-Ⅱ助剂对CRMI-2催化剂催化裂化性能的影响

目前炼油工业实现重油轻质化的主要措施仍然是重油催化裂化工艺，借助催化裂化工艺可将低附加值重质油品转化为高附加值轻质油品。我国成品油市场中75%以上的汽油调和组分来自于催化裂化工艺。借助优化操作条件，改善进料喷嘴的雾化效果，提高汽提效率，虽能部分提高催化裂化反应产物中的轻油收率，但受自身工艺条件的限制，很难满足进一步提高轻油收率的要求。在FFB小型固定流化床反应装置上考察添加RE-Ⅱ助剂对CRMI-2催化剂催化裂化性能的影响，采用XRD、NH3-TPD和BET等对反应后CRMI-2催化剂的结构、酸性和比表面积进行表征。结果表明，与空白样品相比，添加质量分数0.6%RE-Ⅱ助剂的CRMI-2催化剂，催化裂化反应产物的总液收和轻油收率分别为88.99%和71.64%，与CRMI-2催化剂相比,提高了2.04个百分点和2.43个百分点，焦炭收率为3.70%，降低了0.48个百分点。     

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.%.     

LHO-1降烯烃催化剂的工业应用

榆林炼油厂12万t/a催化裂化装置加工的原料为长庆石蜡基原油,混合原料性质较好,表现为重金属含量一般,残碳低,密度不高,易裂化及轻质油收率高等。为提高装置总液收率和进一步降低汽油组分中的烯烃含量,催化裂化装置开始试用LHO-1催化剂。工业实验表明,LHO-1的综合性能优于LBO-16催化剂。使用LHO-1降烯烃催化剂以来,H/C降低了22.9%,抗重金属污染性能较好,水热稳定性较好,流动性能较好,催化剂单耗由0.85 kg/t油降到0.82 kg/t油,油浆产率降低了1.2%,产品收率提高了1.1%,催化汽油烯烃含量较使用LBO-16催化剂降低约5%,变化不明显。     

Performance studies of various cracking catalysts in the conversion of canola oil to fuels and chemicals in a fluidized-bed reactor

Studies were conducted at atmospheric pressure at temperatures in the range of 400–500°C and fluidizing gas velocities in the range of 0.37–0.58 m/min (at standard temperature and pressure) to evaluate the performance of various cracking catalysts for canola oil conversion in a fluidized-bed reactor. Results show that canola oil conversions were high (in the range of 78–98 wt%) and increased with an increase in both temperature and catalyst acid site density and with a decrease in fluidizing gas velocity. The product distribution mostly consisted of hydrocarbon gases in the C₁–C₅ range, a mixture of aromatic and aliphatic hydrocarbons in the organic liquid product (OLP) and coke. The yields of C₄ hydrocarbons, aromatic hydrocarbons and C₂–C₄ olefins increased with both temperature and catalyst acid site density but decreased with an increase in fluidizing gas velocity. In contrast, the yields of aliphatic and C₅ hydrocarbons followed trends completely opposite to those of C₂–C₄ olefins and aromatic hydrocarbons. A comparison of performance of the catalysts in a fluidized-bed reactor with earlier work in a fixed-bed reactor showed that selectivities for formation of both C₅ and iso-C₄ hydrocarbons in a fluidized-bed reactor were extremely high (maximum of 68.7 and 18 wt% of the gas product) as compared to maximum selectivities of 18 and 16 wt% of the gas product, respectively, in the fixed-bed reactor. Also, selectivity for formation of gas products was higher for runs with the fluidized-bed reactor than for those with the fixed-bed reactor, whereas the selectivity for OLP was higher with the fixed-bed reactor. Furthermore, both temperature and catalyst determined whether the fractions of aromatic hydrocarbons in the OLP were higher in the fluidized-bed or fixed-bed reactor.     

催化裂化再生剂铁含量分析及应对措施

针对某炼化企业重油催化裂化装置平衡剂铁含量偏高的问题,分析了在重油催化裂化过程中,随着原油重质化与酸质化的不断增加,重金属铁不仅对活性的影响,更会产生重油转化率降低、目的产品收率降低等方面的问题。通过对该催化裂化装置催化剂铁中毒现象进行分析,原料油性质、平衡催化剂等方面进行对比,研究催化裂化平衡剂铁含量高应对策略。     

两段提升管重油催化裂化(Ⅰ型)新工艺的初步研究

针对目前催化裂化提升管反应器后半段催化剂性能严重下降以及产品分布不太合理的状况,提出了采用两段提升管催化裂化新工艺技术取代常规的单段提升管催化裂化工艺技术.该工艺的突出特征是催化剂接力、分段反应、大剂油比和短反应时间. 在对新工艺进行理论分析的基础上,以大庆蜡油掺兑65%渣油为原料,采用ZC-7300催化剂,在小型提升管催化裂化装置上进行了一系列实验,考察两段提升管催化裂化（Ⅰ型）新工艺的可行性和先进性. 实验结果表明：与常规单段工艺相比,在相近转化率下,两段柴油产率提高6～8个百分点,轻油产率提高1～2个百分点;汽油烯烃含量减少,辛烷值提高,产品质量提高. 新工艺在提高柴油收率及改善产品分布和产品质量方面具有明显优势.