异丁烯提纯装置换热网络的能效分析

doi:10.16085/j.issn.1000-6613.2020-0720

摘要/Abstract

摘要：

基于Aspen Plus对抽余C₄提取高纯度异丁烯的工艺流程进行系统灵敏度分析，并以目前我国用户最重视的能源消耗问题与投资成本问题等为改造优化目标，基于Aspen Energy Analyzer对换热网络进行优化分析。对系统灵敏度进行分析得出：在精制塔理论塔板数为36、回流比为5的优化条件下，精制后异丁烯的质量纯度可达到99.95%，回收率可达到99.6% 。本文从夹点理论概念设计法着手，对异丁烯提纯装置换热并对其换热网络进行能效分析，结果表明，在反应温度为60℃，D006树脂做催化剂，结合Aspen Energy Analyzer优化后的能耗参数，计算得出工艺流程的热公用工程用量达到1944.17kW，相比原工艺过程的用能节约了12.9％；冷公用工程用量达到3877.78 kW，相比原工艺流程节约了23.4%，大幅度提升节能降耗效果并节省投资，因此本研究可以为能量的更优利用提供理论依据和可行方案。

关键词: 换热网络, Aspen Plus, Aspen Energy Analyzer, 夹点技术

Abstract:

Based on Aspen Plus, a systematic sensitivity analysis of the extraction process of high purity isobutene from extracted C₄ is carried out, and the energy consumption and investment cost, which are the most important problems for Chinese consumers, are taken as the optimization targets, optimization analysis of heat exchanger network based on Aspen Energy Analyzer. The system sensitivity analysis shows that the purity of isobutene can reach 99.95% and the recovery can reach 99.6% under the optimum conditions of theoretical plate number 36 and reflux ratio 5. Based on the conceptual design method of pinch theory, analyzing the heat exchange of isobutene purification unit and its heat exchange network, the result demonstrates, at 60℃, and D006 resin as catalyst, and combines the Energy consumption parameters optimized by Aspen Energy Analyzer, the calculation results show that the energy consumption of the heat utility project reaches 1944.17kW, which saves 12.9% compared with the original process, and that of the cold utility project.

Key words: heat exchanger network, Aspen Plus, Aspen Energy Analyzer, pinch technology

中图分类号:

TQ021.8

邵缨迪, 胡建杭, 刘慧利, 蔡正达. 异丁烯提纯装置换热网络的能效分析[J]. 化工进展, 2020, 39(S2): 57-65.

Yingdi SHAO, Jianhang HU, Huili LIU, Zhengda CAI. Energy efficiency analysis of heat exchange network of isobutylene purification unit[J]. Chemical Industry and Engineering Progress, 2020, 39(S2): 57-65.

图/表 13

图1 抽余C4制取异丁烯工艺流程0101―抽余C4；0102―水；0103―加压水；0104―水与抽余C4混合物；0105―预热后的混合物；0106―反应产物；0107―加热后的反应产物；0108―C3和其他C4；0109―C3；0110―正丁烷和丁烯；0111―叔丁醇和水的混合物；0112―预热后的叔丁醇和水的混合物；0113―反应产物；0114―异丁烯；0115―水；P0101―泵；M0101―混合器；E0101―换热器；R0101―叔丁醇合成反应器；T0101―叔丁醇精制塔；E0102―换热器；T0102―C3分离塔；R0102―叔丁醇脱水反应器；E0103―换热器；T0103―反应精馏塔；E0103―换热器；T0103―反应精馏塔

图2 基于夹点技术的换热网络设计框图

图3 T0101塔板数与塔顶叔丁醇产品质量分数、再沸器的冷负荷、冷凝器的热负荷的关系

图4 理论板数为第36块时T0101回流比与塔顶叔丁醇产品质量分数、再沸器的冷负荷、冷凝器的热负荷的关系

图5 平衡的组合曲线

图6 总物流曲线

图7 总费用随最小换热温差变化

表1 冷热物流数据

物流类型	物流编号	物流描述	初始温度（T₀）/℃	目标温度（T₁）/℃	热容流率（CP）/kW·℃^-1	热负荷（Q）/kW
热物流	H1	叔丁醇和水的混合物	148.6	85.0	5.30	336.39
	H2	C₃	43.8	9.5	0.27	6.33
	H3	C₃,其他C₄	59.3	57.9	1305.60	1898.61
	H4	异丁烯	35.8	35.2	10833.33	2302.78
冷物流	C1	抽余C₄、水	2.4	60.0	8.24	474.44
	C2	抽余C₄与水的反应产物	60	78	8.50	152.92
	C3	正丁烷、丁烯	57.0	57.4	39.33	39.33
	C4	水	145.6	146.1	1944.17	1944.17

图8 优化前的换热网络

图9 自动优化后的换热网络

图10 最终优化的换热网络图

表2 优化前与优化后的费用信息

费用	热公用工程 /$·s^-1	冷公用工程 /$·s^-1	操作费用 /$·s^-1	设备投资 /$	总费用 /$·s^-1
优化前	5.544×10^-3	1.184×10^-3	6.728×10^-3	2.251×10⁵	9.027×10^-3
优化后	4.905×10^-3	9.100×10^-4	5.815×10^-3	2.241×10⁵	8.104×10^-3

表3 优化前与优化后的换热网络信息

换热网络	热公用工程用量 /kJ·h^-1	冷公用工程用量 /kJ·h^-1	总换热面积/m²
优化前	9.399×10⁶	1.979×10⁷	522.3
优化后	8.189×10⁶	1.515×10⁷	518.9

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