渗透汽化-隔壁塔精馏耦合初步分离费托合成水的过程研究

doi:10.11949/0438-1157.20211774

化工学报 ›› 2022, Vol. 73 ›› Issue (5): 2020-2030.doi: 10.11949/0438-1157.20211774

渗透汽化-隔壁塔精馏耦合初步分离费托合成水的过程研究

刘鑫¹(),潘阳²,刘公平²,方静¹,李春利¹,李浩¹()

^1.河北工业大学化工学院，天津 300130
^2.南京工业大学化工学院，江苏南京 211816

收稿日期:2021-12-16 修回日期:2022-02-17 出版日期:2022-05-05 发布日期:2022-05-24
通讯作者: 李浩 E-mail:ctstliuxin@163.com;ctstlihao@hebut.edu.cn
作者简介:刘鑫（1996—），男，硕士研究生，ctstliuxin@163.com
基金资助:
国家重点研发计划项目(2017YFB0602500);国家自然科学基金项目(21808047)

Study on the process of preliminary separation of Fischer-Tropsch synthetic water by coupling pervaporation and dividing wall column distillation

Xin LIU¹(),Yang PAN²,Gongping LIU²,Jing FANG¹,Chunli LI¹,Hao LI¹()

^1.School of Chemical Engineering, Hebei University of Technology, Tianjin 300130, China
^2.School of Chemical Engineering, Nanjing Tech University, Nanjing 211816, Jiangsu, China

Received:2021-12-16 Revised:2022-02-17 Published:2022-05-05 Online:2022-05-24
Contact: Hao LI E-mail:ctstliuxin@163.com;ctstlihao@hebut.edu.cn

摘要/Abstract

摘要：

费托合成水中含有醇、酮、酸等多种高附加值含氧有机物可提取出来作为高附加值产品，但由于费托合成水处量大，共沸体系复杂，通常需要首先对其进行初步分离。设计了直接两塔精馏、渗透汽化-两塔精馏、直接隔壁塔精馏、渗透汽化-隔壁塔精馏四种可供选择的初步分离工艺。根据渗透汽化实验数据在Aspen Plus中构建渗透汽化过程模型并进行模拟，结合灵敏度分析得到精馏过程的最佳工艺参数和模拟结果，并对四种工艺的能耗和有效能损失进行对比。结果表明，渗透汽化-隔壁塔精馏工艺具有明显的节能优势，其能耗较直接两塔精馏可降低15.85%，有效能损失降低45.74%。经渗透汽化膜预浓缩后，溶液的浓度可进入隔壁塔的适宜分离浓度区间，以充分发挥隔壁塔优势。由于渗透汽化所需能量可由余热等低品位热源提供，在余热充足的煤化工领域中可显著降低有效能损失。对于该过程而言，当渗透汽化膜价格低于438元/m²时，渗透汽化-隔壁塔精馏耦合工艺将会表现出较高的经济性。

关键词: 费托合成水, 分离, 膜, 渗透汽化, 精馏, 隔壁塔

Abstract:

Fischer-Tropsch synthetic water contains a variety of high value-added oxygen-containing organic compounds such as alcohols, ketones, and acids. However, due to the large amount of water and the complex azeotrope system, it is usually necessary to perform preliminary separation first. In this study, four alternative preliminary separation processes, direct two-column distillation, pervaporation-two-column distillation, direct dividing wall column distillation, and pervaporation-dividing wall column distillation, were designed first. According to the pervaporation experimental data, the pervaporation process model was constructed and simulated in Aspen Plus, and the optimal process parameters and simulation results of the distillation process were obtained through sensitivity analysis. The energy consumption and effective energy loss of the four processes were compared. The results show that the pervaporation-dividing wall column distillation process has obvious energy-saving advantages. Compared with direct two-column distillation, the energy consumption could be reduced by 15.85%, and the effective energy loss could be reduced by 45.74%. After pre-concentration by the pervaporation membrane, the concentration of the solution could enter the appropriate separation concentration range of the dividing wall column, so as to give full play to the advantages of the dividing wall column. Since the energy required for pervaporation could be provided by low-grade heat sources such as waste heat, the loss of effective energy could be significantly reduced in the coal chemical industry with sufficient waste heat. For this process, when the price of pervaporation membrane is lower than 438 CNY/m², the coupled process of pervaporation-dividing wall column distillation would show higher economy.

Key words: Fischer-Tropsch synthetic water, separation, membranes, pervaporation, distillation, DWC

中图分类号:

TQ 529

刘鑫, 潘阳, 刘公平, 方静, 李春利, 李浩. 渗透汽化-隔壁塔精馏耦合初步分离费托合成水的过程研究[J]. 化工学报, 2022, 73(5): 2020-2030.

LIU Xin, PAN Yang, LIU Gongping, FANG Jing, LI Chunli, LI Hao. Study on the process of preliminary separation of Fischer-Tropsch synthetic water by coupling pervaporation and dividing wall column distillation[J]. CIESC Journal, 2022, 73(5): 2020-2030.

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物质	进料侧含量/ %(质量)	渗透侧含量/ %(质量)	分离因子
甲醇	0.5082	3.2413	6.56
乙醇	0.8163	6.7861	8.85
丙醇	0.2246	9.9020	18.03
丁醇	0.1130	3.3914	31.04
丙酮	0.1069	3.2600	31.49
乙酸	0.4426	0.4426	1.00

流股	主要组分	分离要求
A	甲醇、丙酮	乙醇含量尽可能少
B	乙醇、正丙醇、正丁醇	甲醇不超过0.20%
C	水	水中几乎不含非酸性含氧有机物

物质	渗透系数Q_i / (g/(m²·h·kPa))	渗透侧总含量/ %(质量)	进料侧含量/ %(质量)	浓缩倍数
甲醇	99.45	2.07	0.5082	4.07
乙醇	142.32	3.65	0.8163	4.47
丙醇	320.89	1.00	0.2246	4.45
丁醇	8240.92	0.50	0.1130	4.42
丙酮	152.69	0.48	0.1069	4.49
乙酸	461.42	0.44	0.4426	0.99

膜组件	膜面积/m²	渗余侧水含量/ %(质量)	渗透侧水含量/%(质量)	C₂₊醇回收率/%
膜组件1	309	98.34	82.52	33.72
膜组件2	372	98.73	85.79	61.55
膜组件3	529	99.10	88.77	81.92
膜组件4	1005	99.50	91.86	99.98

参数	C1	C2	PV
进料量/(kg/h)	1119.0	—	5000.0
操作压力/kPa	101.325	101.325	101.325
理论板数	26	40	—
进料位置	10	28	—
回流比	1.10	13.00	—
塔顶采出流率/(kg/h)	110.0	29.5	—
甲醇质量回收率/%	—	99.00	—
塔釜水含量/%(质量)	99.50	29.98	—
塔底采出流率/(kg/h)	1009.0	80.5	—
渗透汽化能量/kW	—	—	356
再沸器热负荷/kW	155	113	—
冷凝器热负荷/kW	-76	-113	—
有效能损失/kW	82.37	9.19	42.91

渗透汽化-隔壁塔精馏耦合初步分离费托合成水的过程研究

Study on the process of preliminary separation of Fischer-Tropsch synthetic water by coupling pervaporation and dividing wall column distillation

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参数	数值	参数	数值
进料量/(kg/h)	5000.0	液相分配率	0.30
操作压力/kPa	101.325	塔顶采出流率/(kg/h)	31.0
总理论板数	70	侧线采出流率/(kg/h)	84.0
隔板位置	29~58	塔底采出流率/(kg/h)	4885.0
预分馏段理论板数	30	塔顶甲醇质量回收率/%	99.00
侧线采出位置	48	侧采水含量/%(质量)	31.91
进料位置	36	冷凝器热负荷/kW	-385
回流比	43.75	再沸器热负荷/kW	744
汽相分配率	0.70	有效能损失/kW	396.79

工艺	D	DWC	PV-D	PV-DWC
能耗/kW	675	744	624	568
节能率/%	—	-10.22	7.56	15.85
有效能损失/kW	293.85	396.79	134.47	159.45
混醇产品含水量/%	32.44	31.91	20.98	29.88
混醇产品流率(B)/(kg/h)	84.0	84.0	80.5	80.5
塔顶乙醇含量/%	3.05	1.60	2.37	2.10
塔顶产品流率(A)/(kg/h)	31.0	31.0	29.5	29.5
塔釜水含量/%	99.50	99.50	99.50	99.50
塔釜产品流率(C)/(kg/h)	4885.0	4885.0	1009.0	1009.0

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