Y型分子筛应用于双环芳烃加氢裂化多产轻芳烃过程研究进展

doi:10.16085/j.issn.1000-6613.2019-1673

摘要/Abstract

摘要：

催化柴油富含双环芳烃，可通过加氢裂化过程选择性多产高价值轻质芳烃（BTX）产物，现有研究已对此过程所需的工艺条件和催化剂性质进行了大量考察。工业应用中催化剂的酸性组分以Y型分子筛为主，研究分子筛性质和反应结果的关系成为重点内容。本文主要介绍了双环芳烃多产BTX产物经历加氢饱和、开环、断侧链等主要反应过程，金属组分及其与分子筛的协同作用；总结了Y型分子筛的性质如孔道性质、小晶粒、酸性质、核壳结构等因素对上述反应过程的影响。初步表明分子筛孔性质、酸性质直接影响目标反应选择性，通过对分子筛性质进行调变，可以达到促进反应物有效转化及提高BTX产物收率的目的。

关键词: Y型分子筛, 双环芳烃, 加氢裂化, 高价值轻质芳烃

Abstract:

The bicyclic aromatics are abundant in light cycle oils and can be selectively converted into high-value light aromatics (BTX) through hydrocracking. The existing researches have investigated the process conditions and catalyst properties. Y zeolites are widely used as the acidic component in industrial catalysts, it is very important to study the relationship between the properties of zeolites and reaction results. This article focuses on the advances of those reaction paths on producing of BTX by bicyclic aromatic hydrocarbons undergoing hydrotreating saturation, ring-opening, and side chain breaking, the synergistic effect between metal components and zeolite is also summarized. The effects of the properties of zeolite Y, such as texture properties, small crystal particle, acid properties, and coated structure were summarized. These results preliminary showed that the properties of pore and acidity from Y zeolite are important factors to improve the selectivity of the target reaction. By adjusting the properties of Y zeolite, the objectives of promoting conversion and increasing the yield of BTX products can be achieved.

Key words: zeolite Y, dicyclic aromatics, hydrocracking, high-value light aromatics

中图分类号:

TE624

羡策, 毛以朝, 龙湘云, 杨平, 杨清河. Y型分子筛应用于双环芳烃加氢裂化多产轻芳烃过程研究进展[J]. 化工进展, 2020, 39(S1): 133-140.

Ce XIAN, Yichao MAO, Xiangyun LONG, Ping YANG, Qinghe YANG. Advances on the application of zeolite Y in the producing light aromatic hydrocarbons from dicyclic aromatics hydrocracking[J]. Chemical Industry and Engineering Progress, 2020, 39(S1): 133-140.

图/表 11

图1 苯、对二甲苯的产量与消费量变化

图2 四氢萘加氢裂化反应机理

表2 需控制的过程及催化剂性质调变方向

需控制的过程	控制程度	催化剂性质调变方向
加氢反应过程	控制加氢深度，防止加氢过度饱和	合适的金属组分及配比，与分子筛协同作用良好
开环反应过程	促进双环芳烃开环后进一步断侧链	需要一定量的强酸位点，恰当的孔道性质利于传质
催化剂失活过程	防止大分子物质结焦，造成催化剂孔道堵塞	适当的酸强度与酸量、孔道性质，有助于大分子物质吸脱附及扩散

表1 国Ⅵ柴油质量标准（部分）及典型炼厂LCO烃类组成

项目	国Ⅵ柴油标准	广州石化	石家庄炼化	高桥石化	齐鲁石化
十六烷值	≥51	15～30
链烷烃（质量分数）/%	—	9.6	12.3	17.1	7.0
环烷烃（质量分数）/%	—	8.8	5.2	10.6	3.1
单环芳烃（质量分数）/%	—	28.5	25.8	20.3	29.0
双环芳烃（质量分数）/%	≤7	42.1	44.4	41.9	52.0
三环芳烃（质量分数）/%		11.0	12.6	10.1	8.9

表3 芳烃、环烷烃分子的尺寸（a×b为分子的最小截面尺寸）

分子式	a×b×c/nm	分子式	a×b×c/nm
	0.341 $×$ 0.666 $×$ 0.729		0.391 $×$ 0.726 $×$ 0.899
	0.341 $×$ 0.730 $×$ 0.907		0.380 $×$ 0.666 $×$ 0.818
	0.542 $×$ 0.729 $×$ 0.901		0.390 $×$ 0.666 $×$ 0.919

表3 芳烃、环烷烃分子的尺寸（a×b为分子的最小截面尺寸）

分子式	a×b×c/nm	分子式	a×b×c/nm
	0.341 $×$ 0.666 $×$ 0.729		0.391 $×$ 0.726 $×$ 0.899
	0.341 $×$ 0.730 $×$ 0.907		0.380 $×$ 0.666 $×$ 0.818
	0.542 $×$ 0.729 $×$ 0.901		0.390 $×$ 0.666 $×$ 0.919

表4 介孔体积对开环产物收率的影响[41]

催化剂类型	孔体积/cm³·g^-1		四氢萘转化率/%	产物分布（质量分数）/%
催化剂类型	微孔	介孔	四氢萘转化率/%	气体产物	单环产物	十氢萘
NiMo/HY(TO)	0.21	0.125	49.4	2.3	26.2	3.5
NiMo/HY(CE)	0.20	0.054	44.9	2.2	25.1	3.8

表5 不同硅铝比的小晶粒Y分子筛孔结构及加氢裂化性能[49]

Si/Al	孔结构		加氢裂化性能
Si/Al	总的比表面积/m²·g^-1	总的孔体积/cm³·g^-1	转化率/%	轻馏分选择性/%	石化产品原料收率（质量分数）/%
工业剂	571.7	0.33	73.2	70.6	75.2
4.7	681.3	0.44	85.5	68.8	70.5
4.9	711.6	0.44	81.2	71.5	71.8
5.2	701.2	0.42	80.1	75.9	80.2
5.4	599.9	0.32	79.2	70.4	80.3
6.2	595.8	0.41	74.8	71.1	80.2

图3 不同硅铝比的小晶粒Y分子筛酸量及酸性中心分布[49]

表6 反应前后催化剂酸量[51]

催化剂类型	反应前酸量/ $μ m o l N H 3 ? g c a l - 1$				反应后酸量/ $μ m o l N H 3 ? g c a l - 1$
催化剂类型	总酸量	弱酸量	中强酸量	强酸量	总酸量	弱酸量	中强酸量	强酸量
Pt/Y12	498	154	326	18	386	242	143	1
Pd/Y12	600	182	305	113	279	170	107	2
Pt-Pd/Y12	550	90	385	75	357	204	151	2
Pt/Y5	678	255	259	164	551	294	240	17
Pd/Y5	803	251	334	218	557	317	243	17
Pt-Pd/Y5	686	311	252	123	605	336	249	20

表6 反应前后催化剂酸量[51]

催化剂类型	反应前酸量/ $μ m o l N H 3 ? g c a l - 1$				反应后酸量/ $μ m o l N H 3 ? g c a l - 1$
催化剂类型	总酸量	弱酸量	中强酸量	强酸量	总酸量	弱酸量	中强酸量	强酸量
Pt/Y12	498	154	326	18	386	242	143	1
Pd/Y12	600	182	305	113	279	170	107	2
Pt-Pd/Y12	550	90	385	75	357	204	151	2
Pt/Y5	678	255	259	164	551	294	240	17
Pd/Y5	803	251	334	218	557	317	243	17
Pt-Pd/Y5	686	311	252	123	605	336	249	20

表7 酸量对产物分布影响[53]

催化剂类型	酸量 / $μ m o l N H 3 ? g c a l - 1$	四氢萘转化率（摩尔分数）/%	产物收率（摩尔分数）/%
催化剂类型	酸量 / $μ m o l N H 3 ? g c a l - 1$	四氢萘转化率（摩尔分数）/%	芳烃产物	加氢产物	开环产物	裂化产物
NiMo/Alu	471	18.8	1.6	17.2	0.9	0.5
NiMo/SiAl	554	27.8	7.1	20.7	7.7	1.9
NiMo/AluZ	695	53.3	20.1	33.3	30.5	17.7

表7 酸量对产物分布影响[53]

催化剂类型	酸量 / $μ m o l N H 3 ? g c a l - 1$	四氢萘转化率（摩尔分数）/%	产物收率（摩尔分数）/%
催化剂类型	酸量 / $μ m o l N H 3 ? g c a l - 1$	四氢萘转化率（摩尔分数）/%	芳烃产物	加氢产物	开环产物	裂化产物
NiMo/Alu	471	18.8	1.6	17.2	0.9	0.5
NiMo/SiAl	554	27.8	7.1	20.7	7.7	1.9
NiMo/AluZ	695	53.3	20.1	33.3	30.5	17.7

表8 核壳结构分子筛对产物分布的影响[58,59]

催化剂类型	催化剂制作方法	产物分布（质量分数）/%
催化剂类型	催化剂制作方法	苯	甲苯	乙苯	对二甲苯	其他烷基苯
NMAZ	Al₂O₃与USY分子筛物理混合	6.89	2.03	14.33	14.89	35.00
NMACZ	Al₂O₃包裹在USY分子筛表面	7.81	2.63	17.26	16.90	35.32

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