Simulation and retrofit of desulfurization system in refinery

doi:10.11949/0438-1157.20201877

Abstract

Abstract:

With the trend of processing sulfur-containing crude oil, the circulation of desulfurization solvent is increasing in refineries, which raises the energy consumption for solvent regeneration dramatically. In this paper, Aspen HYSYS is used to simulate a group of desulfurization units, and the minimum desulfurization solvent circulation of each unit is obtained. On this basis, two retrofitting methods, cascaded operation and cascaded-parallel operation, are put forward and used to retrofit the desulfurization system. The results show that the desulfurization solvent circulation can be reduced by 8.82% and 10.01% through the two methods, respectively, and have achieved good economic benefits. Finally, the advantages and disadvantages of the two methods are analyzed and discussed, which provides directions and suggestions for the optimization of refinery desulfurization system.

Key words: desulfurization system, simulation, retrofit, economic, systems engineering

摘要：

随着世界原油含硫化，炼厂脱硫溶剂的循环量不断增加，导致溶剂再生部分能耗剧增。使用Aspen HYSYS对一组脱硫单元进行了模拟，得出该脱硫系统最小的脱硫溶剂循环量。在此基础上，提出了串联操作和串并联操作两种改造方法，并分别使用这两种方法对现行的脱硫系统进行了改造。结果表明，两种改造方法可以使贫胺液的循环量分别减少8.82%和10.01%，取得了良好的经济效益。最后，分析和讨论这两种方法的优缺点，为炼厂脱硫系统的优化提供方向和建议。

关键词: 脱硫系统, 模拟, 改造, 经济, 系统工程

CLC Number:

LI Zhendong, YANG Minbo, FENG Xiao, WANG Yufei. Simulation and retrofit of desulfurization system in refinery[J]. CIESC Journal, 2021, 72(3): 1473-1479.

李振东, 杨敏博, 冯霄, 王彧斐. 炼厂脱硫系统的模拟和改造[J]. 化工学报, 2021, 72(3): 1473-1479.

Figures/Tables 7

References 31

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单元	塔顶压力/ kPa	塔底压力/ kPa	塔板数	进料流量/(kmol·h^-1)	脱硫目标/ kPa
U101	2850	2950	10	120.5	0.056
U102	1570	1650	10	2125	0.041
U103	6280	6330	18	3944	0.647
U104	12000	12050	10	5453	15.816
U105	11600	11650	16	7058	48.72

单元	塔顶压力/ kPa	塔底压力/ kPa	塔板数	进料流量/(kmol·h^-1)	脱硫目标/ kPa
U101	2850	2950	10	120.5	0.056
U102	1570	1650	10	2125	0.041
U103	6280	6330	18	3944	0.647
U104	12000	12050	10	5453	15.816
U105	11600	11650	16	7058	48.72

单元	组成/%(mol)
单元	CH₄	C₂H₆	C₃H₈	i-C₄H₁₀	n-C₄H₁₀	H₂S	H₂O	MDEA	H₂	C₆H₁₄	C₅H₁₂
U101	10.64	7.87	5.4	2.26	0.55	0.2	0	0	72.28	0.8	0
U102	6.21	3.12	0	0	0	0.2	0	0	90.47	0	0
U103	10.16	4.28	1.74	0.3	0.37	1.98	0.16	0	80.51	0.2	0.3
U104	6.15	2.89	1.81	0.76	0.19	0.34	0	0	87.3	0.54	0.02
U105	1.99	0.07	0.04	0.02	0.01	2.64	0	0	95.22	0.01	0
贫胺液	0	0	0	0	0	0.07	93.85	6.08	0	0	0

单元	组成/%(mol)
单元	CH₄	C₂H₆	C₃H₈	i-C₄H₁₀	n-C₄H₁₀	H₂S	H₂O	MDEA	H₂	C₆H₁₄	C₅H₁₂
U101	10.64	7.87	5.4	2.26	0.55	0.2	0	0	72.28	0.8	0
U102	6.21	3.12	0	0	0	0.2	0	0	90.47	0	0
U103	10.16	4.28	1.74	0.3	0.37	1.98	0.16	0	80.51	0.2	0.3
U104	6.15	2.89	1.81	0.76	0.19	0.34	0	0	87.3	0.54	0.02
U105	1.99	0.07	0.04	0.02	0.01	2.64	0	0	95.22	0.01	0
贫胺液	0	0	0	0	0	0.07	93.85	6.08	0	0	0

脱硫单元	最小贫胺液/ (kmol·h^-1)	脱后气体硫化氢分压/kPa	脱硫目标/kPa	相对误差/%
U101	14	0.054	0.056	3.6
U102	355	0.039	0.041	4.9
U103	1623	0.634	0.647	2.0
U104	305	15.264	15.816	3.5
U105	2600	48.488	48.720	0.5
总计	4897	—	—	—