催化裂化柴油不同加氢转化过程对比研究
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摘要
采用镇海催化裂化(MIP)柴油和伊朗减压馏分油(VGO)为原料油,对加氢精制、加氢改质、加氢转化和加氢裂化4种工艺进行对比。结果表明:加氢精制仅能实现柴油的脱硫精制,十六烷值增幅为2~7单位;加氢改质能够大幅提高十六烷值,增幅达到12~20单位;加氢转化可生产辛烷值大于90的汽油调合组分或高芳烃潜含量石脑油,同时生产低硫柴油,十六烷值增幅为8~30单位;加氢裂化可增产轻石脑油、喷气燃料,同时减少柴油产量,视加氢裂化装置反应条件及掺炼比例的不同,可直接生产十六烷值大于51的优质柴油产品。
Zhenhai MIP diesel and Iran VGO were tested as the feedstocks under four processing conditions of hydrofining,hydro-upgrading,hydro-conversion and hydrocracking,and the 4 processes were compared. The results show that the hydrofining can only achieve desulfurization of diesel oil and elevate cetane number by 2 ~ 7 units; The hydro-upgrading can greatly raise the cetane number by 12 ~ 20 units; Hydro-conversion can produce high octane number gasoline blending components whose octane number is over 90 as well as naphtha with high potential aromatics. At the same time,the low-sulfur diesel is produced whose cetane number is increased by 8 ~ 30 units. The hydrocracking process can increase the production of light naphtha and jet fuel,while reducing the production of diesel. The high-quality diesel product whose cetane number is greater than 51 can be directly produced based upon the different reaction conditions and blending ratio of hydrocracking unit.
Zhenhai MIP diesel and Iran VGO were tested as the feedstocks under four processing conditions of hydrofining,hydro-upgrading,hydro-conversion and hydrocracking,and the 4 processes were compared. The results show that the hydrofining can only achieve desulfurization of diesel oil and elevate cetane number by 2 ~ 7 units; The hydro-upgrading can greatly raise the cetane number by 12 ~ 20 units; Hydro-conversion can produce high octane number gasoline blending components whose octane number is over 90 as well as naphtha with high potential aromatics. At the same time,the low-sulfur diesel is produced whose cetane number is increased by 8 ~ 30 units. The hydrocracking process can increase the production of light naphtha and jet fuel,while reducing the production of diesel. The high-quality diesel product whose cetane number is greater than 51 can be directly produced based upon the different reaction conditions and blending ratio of hydrocracking unit.
引文
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[2]毛安国,龚剑洪.催化裂化轻循环油生产轻质芳烃的分子水平研究[J].石油炼制与化工,2014,45(7):1-6.
[3]龚剑洪,毛安国.LCO催化裂化轻循环油加氢-催化裂化组合生产高辛烷值汽油或轻质芳烃(LTAG)技术[J].石油炼制与化工,2016,47(9):1-5.
[4]张寒,王吉云.催化柴油加工路线选择及经济性分析[J].石油与天然气化工,2014,44(4):39-42.
[5]王宏奎,王金亮,何观伟,等.柴油加氢改质技术研究进展[J].工业催化,2013,21(10):16-19.
[6]任亮.LCO加氢转化生产高辛烷值汽油(RLG)技术开发与工业应用[C]//2015年炼油加氢技术交流会论文集,2015:216-220.
[7]黄新露.重芳烃高效转化生产轻芳烃技术[J].化工进展,2013,32(9):2263-2266.
[8]高磊.催化柴油加工路线选择及优化[J].石油炼制与化工,2017,48(7):64-69.
[9]徐光明,于长青.加氢裂化装置掺炼劣质催化裂化柴油技术的应用[J].炼油技术与工程,2011,41(4):1-5.
[10]孔健.加氢裂化装置掺炼催化裂化柴油的探讨[J].石油化工技术与经济,2012,28(5):18-21.