380万t/a连续重整装置混合重石脑油原料的模拟优化及应用

利用广东辛孚科技有限公司开发的SP-Reform流程模拟软件，在浙江石油化工有限公司380万t/a连续重整装置上建立了全流程反应机理模型，并结合其3种重石脑油原料馏程差异的生产实际，进行了模型的模拟优化。结果表明:建模后的优化模拟结果与装置实际工况基本相吻合，特别是关键目标产品C≥6重整生成油性质相关指标与实际工况的相近，说明所建模型可靠，可用于该装置的工艺流程优化及生产指导；在保持柴油加氢裂化重石脑油与蜡油加氢裂化重石脑油的重整进料掺混比为1∶1情况下，焦化石脑油加氢重石脑油的掺混质量分数不宜超过57%，以确保C≥6重整生成油的溴指数合格；当市场上苯产品畅销且创效较好时，应控制该装置的精制重石脑油混合原料初馏点不高于86 ℃，以多产苯；否则，应将其控制不低于90 ℃，以多产轻石脑油去乙烯装置，助力生产其他高附加值产品；为了尽可能保留产物中C9~10 芳烃有效组分含量，同时减少C≥11重芳烃含量，宜控制其精制重石脑油混合原料终馏点不高于 172 ℃较好，以确保该装置经济效益最大化。

Simulation optimization and application of mixed heavy naphtha feedstockin 3.8 Mt/a continuous catalytic reforming unit

Using the SP-Reform process simulation software developed by Guangdong Syspetro Technology Co Ltd，the whole process reaction mechanism model was established for 3.8 Mt/a continuous catalytic reforming unit of Zhejiang Petroleum & chemical Co Ltd，and the simulation and optimization of 3 different distillation heavy naphtha feedstocks were conducted by the mechanism model. The results showed that the optimized simulation results after modeling were basically consistent with the actual working conditions of this unit，especially for the key target product properties of the generated C≥ 6 reforming oil were similar to the actual working conditions，indicating that the mechanism model was reliable and could be used for the process optimization and operation guidance of this unit. It was recommended that，while maintaining the reforming feed blending ratio of diesel cracked heavy naphtha to wax cracked heavy naphtha at 1∶1，the blending mass fraction of heavy naphtha from coking naphtha hydrogenation should not exceed 57%，so as to ensure that the bromine index of C≥6 reforming oil product was qualified. When benzene products were sold well at high price in the market，the initial distillation point of the hydrotreating heavy naphtha should be controlled to not exceed 86 ℃ in order to produce more benzene. Otherwise，it should be controlled at no less than 90 ℃ to increase the production of light naphtha for the ethylene unit to assist in producing more other high value-added products instead. In order to preserve the effective component content of C9~10 aromatics in the products as much as possible，meanwhile reducing the content of C≥11 heavy aromatics，it was better to control the final distillation point of hydrotreating heavy naphtha mixture raw material to not greater than 172 ℃，so as to ensure maximum economic benefits of this unit.