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炼厂延迟焦化装置的产品焦化蜡油(CGO),因碱性氮和芳烃含量较高,可裂化性较差,一般要先进加氢处理装置经加氢后再进催化裂化装置加工,这样可提高催化裂化装置加工CGO的经济性。在某炼厂蜡油加氢装置停运期间,焦化装置正常开工,两个月CGO产量达到36000t,因储罐容量有限,只能采用催化裂化装置直接掺炼未经加氢的CGO,为此探索了催化裂化装置直接加工CGO的新工艺路线,经中试和工业运行初期工艺数据的摸索,确定了工业运行的方案。工业运行方案如下:一是采用抗碱氮催化剂RSC-2006(JM),其初始活性比原催化剂RSC-2006高1%～3%,反再平衡催化剂微反活性由65%～66%提高到68%～69%,大幅度提高了抗碱氮能力。二是调整工艺操作条件,提高剂油比和反应温度。通过提升管底部注入重整拔头油提高剂油比(注入量为13.15m3/h);原料反应温度从524℃提高到528℃。其综合结果为:催化剂循环量提高了224t/h,剂油比增加了2.07,重质油总反应时间增加了1.11s,反再催化剂总藏量增加了4.79t,提升管底部和中部温度提高4～6℃,油剂接触机会增加25%以上,原料反应的裂化反应热增加了75.69kJ/kg。经工业运行证明,催化裂化装置直接加工未加氢CGO的工业试验是成功的。但由于该方案导致催化液体收率明显下降,相比之下,CGO经加氢处理后再进催化裂化装置经济效益更好,所以蜡油加氢装置仍有必要开工运行。催化裂化装置直接掺炼未加氢CGO的工艺方案只有在蜡油加氢装置停运期间,焦化装置正常开工的情况下,为解决CGO出路时采用的权宜之计。
Coking wax oil (CGO), a product of delayed coking units in refineries, is poorly cracked due to high levels of basic nitrogen and aromatics. Generally, advanced hydrotreating units are processed by hydrogenation and then into a catalytic cracking unit, so that Improve the economy of processing CGO in catalytic cracking unit. During the shutdown of the refinery waxy hydrogenation unit, the coking unit started normally. The CGO output reached 36000t in two months. Due to the limited capacity of the storage tank, only the CGO without hydrogenation can be directly blended by the catalytic cracking unit. The new process route of direct processing of CGO in catalytic cracking unit was explored. After the pilot process and the process data in the initial stage of industrial operation, the program of industrial operation was confirmed. The industrial operation scheme is as follows: First, the use of anti-alkali nitrogen catalyst RSC-2006 (JM), the initial activity of 1% to 3% higher than the original catalyst RSC-2006, anti-rebalancing catalyst micro-activity increased from 65% to 66% 68% ~ 69%, a substantial increase in anti-alkaline nitrogen capacity. Second, adjust the process operating conditions, increase the ratio of oil and the reaction temperature. Through the bottom of the riser, the ratio of oil to oil in the reforming draw-up oil was increased to 13.15m3 / h. The reaction temperature of the feedstock increased from 524 ℃ to 528 ℃. The overall results are as follows: the catalyst circulation increased by 224t / h, the ratio of oil to solvent increased by 2.07, the total reaction time of heavy oil increased by 1.11s, the total amount of counter-catalyst increased by 4.79t, and the temperature at the bottom and middle of the riser increased 4 ~ 6 ℃, the chance of oil contact increased by more than 25%, the cracking reaction heat of feedstock reaction increased by 75.69kJ / kg. Industrial operation proved that direct commercial catalytic cracking unit without hydrogenation CGO industrial test was successful. However, due to the solution leads to a marked decline in the yield of catalytic liquid, compared with CGO hydroprocessed into the catalytic cracking unit is more economical, so it is still necessary to start the operation of the wax hydrotreating unit. Direct coffering of FCC unit without hydrogenation of CGO process program Only in the waxy oil hydrogenation unit outage, coking unit under normal circumstances, in order to solve the CGO outlet used expedient.