FCC重循环油选择性加氢改质-催化裂化多产高附加值产品

doi:10.16085/j.issn.1000-6613.2022-0343

摘要/Abstract

摘要：

面对国内柴油产量过剩，汽油需求低迷新形势，降低柴汽比以及增产化工原料产品成为炼厂优选转型路线。催化裂化重循环油中含有大量多环芳烃，难以催化加工利用，成为炼厂转型升级的结构性难题。本研究从分子结构出发，提出先将重循环油进行选择性加氢，使重循环油中难以转化的多环芳烃转化为可裂化结构，然后再进行催化裂化，并根据市场需求，灵活调节装置以多产轻质油或化工原料等高附加值产品。研究表明，重循环油选择性加氢后，催化裂化转化率最高可提升至60.14%（质量分数）；与加氢前相比，汽油和柴油收率分别增加了19.16%（质量分数）和6.50%（质量分数）；汽油辛烷值最高可达95.6，此时汽油中总芳烃含量为56.8%（质量分数），其中三苯含量为21.3%（质量分数），约占总芳烃含量的37%；同时重油和焦炭产率大幅降低。

关键词: 石油, 重循环油, 反应, 催化裂化, 加氢

Abstract:

With the excess domestic diesel output and low gasoline demand, reducing the diesel-to-gasoline ratio and increasing the production of chemical products have become the preferred transformation route for refineries. In this work, based on the molecular structure, HCO was selectively hydrogenated to convert PAHs to crackable components, which were then cracked in an FCC unit. According to market demand, flexible adjustment between light oil and chemical feeds could be made. After selective hydrogenation of HCO, FCC conversion rate is up to 60.14%(mass ratio), and the yield of gasoline and diesel increased 19.16%(mass ratio) and 6.50%(mass ratio) from HCO, respectively. The total aromatics in gasoline is 56.8%(mass ratio), of which triphenyl is 21.3%(mass ratio), about 37% of the total aromatics. Moreover, the yields of heavy oil and coke decrease significantly.

Key words: petroleum, heavy cycle oil, reaction, fluid catalytic cracking, hydrogenation

中图分类号:

TE624

方东, 何怡, 崔笑晨. FCC重循环油选择性加氢改质-催化裂化多产高附加值产品[J]. 化工进展, 2022, 41(12): 6358-6363.

FANG Dong, HE Yi, CUI Xiaochen. FCC heavy cycle oil selective hydrogenation-catalytic cracking to produce more high value products[J]. Chemical Industry and Engineering Progress, 2022, 41(12): 6358-6363.

图/表 14

参考文献 12

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项目	值
密度（20℃）/g·cm^-3	0.9798
平均分子量	269.7
C元素质量分数/%	89.03
H元素质量分数/%	9.83
S元素质量分数/%	0.62
N元素质量分数/%	0.52
H/C（原子比）	1.32
平均分子式	C_20.11H_27.13
馏程/℃
IBP（初馏点）/10%/30%	190/322/366
50%/70%/90%	393/410/441
FBP（终馏点）	558

项目	值
密度（20℃）/g·cm^-3	0.9798
平均分子量	269.7
C元素质量分数/%	89.03
H元素质量分数/%	9.83
S元素质量分数/%	0.62
N元素质量分数/%	0.52
H/C（原子比）	1.32
平均分子式	C_20.11H_27.13
馏程/℃
IBP（初馏点）/10%/30%	190/322/366
50%/70%/90%	393/410/441
FBP（终馏点）	558

项目	值
加氢催化剂
比表面积/m²·g^-1	145
孔体积/cm³·g^-1	0.40
平均孔径/nm	10.92
NiO质量分数/%	4.0~5.0
MoO₃质量分数/%	16.0~20.0
WO₃质量分数/%	0.2~0.4
FCC催化剂
比表面积/m²·g^-1	141
孔体积/cm³·g^-1	0.30
堆密度/g·cm^-3	0.84
0~40μm粒径分布（质量分数）/%	7.30
40~80μm粒径分布（质量分数）/%	53.80
＞80μm粒径分布（质量分数）/%	38.90
Al₂O₃质量分数/%	45.0~50.0
Re₂O₃质量分数/%	1.5~2.5
比表面积/m²·g^-1	141
孔体积/cm³·g^-1	0.30
微反活性	68

项目	值
加氢催化剂
比表面积/m²·g^-1	145
孔体积/cm³·g^-1	0.40
平均孔径/nm	10.92
NiO质量分数/%	4.0~5.0
MoO₃质量分数/%	16.0~20.0
WO₃质量分数/%	0.2~0.4
FCC催化剂
比表面积/m²·g^-1	141
孔体积/cm³·g^-1	0.30
堆密度/g·cm^-3	0.84
0~40μm粒径分布（质量分数）/%	7.30
40~80μm粒径分布（质量分数）/%	53.80
＞80μm粒径分布（质量分数）/%	38.90
Al₂O₃质量分数/%	45.0~50.0
Re₂O₃质量分数/%	1.5~2.5
比表面积/m²·g^-1	141
孔体积/cm³·g^-1	0.30
微反活性	68

条件	干气	液化气	汽油	柴油	重油	焦炭	转化率
A	2.02	7.98	15.94	20.83	43.25	9.98	35.92
B	2.10	8.65	18.11	21.47	38.83	10.84	39.70
C	3.94	9.53	16.70	20.18	37.20	12.45	42.62