浆态床渣油加氢裂化催化剂反应性能影响因素及其评价
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摘要
在500 mL高压釜装置上,采用高分散型钼系ZHS均相加氢裂化催化剂,考察了其加入量、反应温度、反应压力、反应时间等因素对渣油加氢裂化反应转化率和生焦率的影响,并利用自主设计的50 mL配置旋流反应器的浆态床小型加氢装置进行了催化剂的小试评价。结果表明:在反应温度为440℃,初始氢压为7.0 MPa,反应时间为60 min的评价条件下,随着催化剂加入量的增加,反应生焦率明显下降,转化率呈增大趋势;随着反应温度的升高,转化率和生焦率均逐渐明显增加;反应压力对提高转化率和抑制生焦均具有正向影响;随着反应时间的延长,转化率和生焦率均呈增加趋势;小试装置累计运行300 h,转化率超过90%,总生焦量小于0.8%(质量分数),反应器未发生明显结焦现象。
The ZHS homogeneous hydrocracking catalyst with highly dispersed molybdenum system was used and the effects of catalyst dosage, reaction temperature, reaction pressure and reaction time, et al, were investigated on the conversion and coking rate of residue hydrocracking reaction in a 500 mL high-pressure autoclave unit and the small-scale test of the catalyst was carried out in a slurry bed of hydrogenation unit in a 50 mL self-designed swirl reactor.The results showed that under the evaluation conditions of reaction temperature 440 ℃, initial hydrogen pressure 7.0 MPa and reaction time 60 min, with the incrseasing of catalyst amount, the coke yield decreased obviously, the conversion rate showed an evident uptrend; with the rising of reaction temperature, the conversion and the coke yield increased gradually; the reaction pressure had the positive influence for increasing the conversion and resisting the coke; with the extension of reaction time, the conversion and the coking yield had an increased trend; the small-scale device had been running for 300 h, the conversion was more than 90%, the total coke amount was less than 0.8%(mass fraction), and the coking did not occur evidently in the reactor.
The ZHS homogeneous hydrocracking catalyst with highly dispersed molybdenum system was used and the effects of catalyst dosage, reaction temperature, reaction pressure and reaction time, et al, were investigated on the conversion and coking rate of residue hydrocracking reaction in a 500 mL high-pressure autoclave unit and the small-scale test of the catalyst was carried out in a slurry bed of hydrogenation unit in a 50 mL self-designed swirl reactor.The results showed that under the evaluation conditions of reaction temperature 440 ℃, initial hydrogen pressure 7.0 MPa and reaction time 60 min, with the incrseasing of catalyst amount, the coke yield decreased obviously, the conversion rate showed an evident uptrend; with the rising of reaction temperature, the conversion and the coke yield increased gradually; the reaction pressure had the positive influence for increasing the conversion and resisting the coke; with the extension of reaction time, the conversion and the coking yield had an increased trend; the small-scale device had been running for 300 h, the conversion was more than 90%, the total coke amount was less than 0.8%(mass fraction), and the coking did not occur evidently in the reactor.
引文
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[8]李传,陈磊,邓文安.委内瑞拉常压渣油悬浮床加氢裂化尾油循环反应实验研究[J].石油学报(石油加工), 2016, 32(3):569-577.
[9]邓文安,王磊,李传,等.马瑞常压渣油悬浮床加氢裂化反应生焦过程[J].石油学报(石油加工),2017,33(2):291-302.
[10]宋官龙,赵德智,吴青,等.反应条件对渣油悬浮床加氢裂化反应的影响[J].石油化工高等学校学报,2017,30(5):17-21.
[11]李传,石斌,李慎伟,等.克拉玛依常压渣油浆态床加氢裂化反应胶体性质[J].石油化工高等学校学报,2006,19(1):34-39.
[2]吴青,吴晶晶.沸腾床加氢及其未转化油改质重视研究与技术经济性分析[J].炼油技术与工程. 2016,46(11): 1-5.
[3]Motghi M. Slurry phase hydrocracking-possible solution to refining margins[J].Hydrocarbon Processing, 2011,90(2):37-43.
[4]刘东,邓文安,周家顺,等.水溶性分散型加氢催化剂催化作用的研究[J].燃料化学学报,2004,32(4):461-465.
[5]程之光.重油加氢技术[M].北京:中国石化出版社,1994:316-325.
[6]黎元生.渣油浆态床加氢技术现状[J].炼油,1996(4):15-22.
[7]王建明,江林.减压渣油浆态床加氢裂化技术—当代炼油工业的前言技术[J].中外能源,2010,15(6):63-76.
[8]李传,陈磊,邓文安.委内瑞拉常压渣油悬浮床加氢裂化尾油循环反应实验研究[J].石油学报(石油加工), 2016, 32(3):569-577.
[9]邓文安,王磊,李传,等.马瑞常压渣油悬浮床加氢裂化反应生焦过程[J].石油学报(石油加工),2017,33(2):291-302.
[10]宋官龙,赵德智,吴青,等.反应条件对渣油悬浮床加氢裂化反应的影响[J].石油化工高等学校学报,2017,30(5):17-21.
[11]李传,石斌,李慎伟,等.克拉玛依常压渣油浆态床加氢裂化反应胶体性质[J].石油化工高等学校学报,2006,19(1):34-39.