胺液吸收-分步解吸脱硫工艺的设计与评价

doi:10.16085/j.issn.1000-6613.2023-0460

摘要/Abstract

摘要：

脱硫工艺作为炼厂必不可少的一部分，随着H₂S下游加工技术的日益丰富，逐渐由杂质驱动型向资源驱动型转变，提高酸性气（解吸塔顶气）中H₂S纯度，继而提高产品附加值，成为盈利的重要方向。基于此提出胺液吸收-分步解吸脱硫工艺，以此得到部分高纯度酸性气。采用速率级精馏方法进行模拟，通过系统工程方法论对工艺进行研究，提出逐级设计和塔压、进料温度作为主副调控手段的设计策略，并建立了基于设备购买曲线的经济评价框架进行工艺对比分析。结果表明，新工艺相比于传统工艺，年固定投资费用和年操作费用分别提高了30.86%和40.82%，但由于产品附加值的提高，利润提高了65.45%。随着解吸塔数量的增多，能耗上涨幅度会越来越大，经济效益反而下降。

关键词: 吸收, 速率级精馏, 模拟, 系统工程, 经济评价

Abstract:

As an essential part of refinery, sweetening process has gradually changed from impurity driven to resource driven with the enrichment of H₂S processing technology. Through improving the purity of H₂S in acid gas, the added value of products can be increased, which becomes an important direction to increase profit. Based on this, a sweetening process with amine solution absorption and multiple desorption was proposed to obtain part of high purity acid gas. The rate based distillation method was used to simulate the process, and the process was studied by system engineering methodology. A design strategy of hierarchical design and desorber pressure and feed temperature as main and secondary adjustment means was proposed. An economic evaluation framework based on equipment purchase curve was established for comparative analysis of process. The results showed that compared with the traditional process, the annual fixed investment cost and annual operating cost increased by 30.86% and 40.82%, respectively. The profit increased by 65.45% due to the increase of the added value of the product. In addition, with the increase of the number of desorbers, energy consumption will increase more and more, and the economic benefits will decrease.

Key words: absorption, rate based distillation, simulation, systems engineering, economic evaluation

中图分类号:

TQ113

张凤岐, 崔成东, 鲍学伟, 朱炜玄, 董宏光. 胺液吸收-分步解吸脱硫工艺的设计与评价[J]. 化工进展, 2023, 42(S1): 518-528.

ZHANG Fengqi, CUI Chengdong, BAO Xuewei, ZHU Weixuan, DONG Hongguang. Design and evaluation of sweetening process with amine solution absorption and multiple desorption[J]. Chemical Industry and Engineering Progress, 2023, 42(S1): 518-528.

图/表 21

参考文献 31

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参数	数值
流量/kmol·h^-1	500
温度/℃	40
压力/kPa	7010
组分（摩尔分数）/%
二氧化碳	4.48
硫化氢	5.38
甲烷	63.35
氮气	0.11
乙烷	13.9
丙烷	6.03
正丁烷	5.39
异丁烷	1.36

参数	数值
流量/kmol·h^-1	500
温度/℃	40
压力/kPa	7010
组分（摩尔分数）/%
二氧化碳	4.48
硫化氢	5.38
甲烷	63.35
氮气	0.11
乙烷	13.9
丙烷	6.03
正丁烷	5.39
异丁烷	1.36

操作/设备参数	参数值
塔内径/m	0.7
塔板类型	浮阀
塔板间距/m	0.6
塔板数	9
溶液进料温度/℃	40
溶液组成（MDEA质量分数）/%	35
塔压/kPa	7000

操作/设备参数	参数值
塔内径/m	0.7
塔板类型	浮阀
塔板间距/m	0.6
塔板数	9
溶液进料温度/℃	40
溶液组成（MDEA质量分数）/%	35
塔压/kPa	7000

因素	水平1	水平2	水平3	水平4	水平5
A因素（进料温度）/℃	60	70	80	90	100
B因素（塔压）/kPa	650	700	750	800	850