Dynamic control of heat pump assisted extractive distillation process for separation of ethyl acetate/isopropanol/water mixture

Shan, Baoming; Niu, Chengqun; Meng, Dapeng; Zhao, Qing; Huo, Bingjie; Ma, Yixin; Wang, Yinglong; Zhang, Fangkun; Zhu, Zhaoyou

doi:10.1002/jctb.6764

Cited by 11 publications

(3 citation statements)

References 27 publications

(22 reference statements)

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“…Separation of high-purity isopropanol from aqueous solution is challenging due to an azeotrope (Table 1). Following recommendations from the literature, [39][40][41][42][43][44] extractive distillation with ethylene glycol was chosen for final isopropanol dehydration. Nonetheless, since the bottom product from column C2 contains only about 31.1 wt% of isopropanol, preconcentration is needed prior to dehydration by extractive distillation.…”

Section: Isopropanol Purificationmentioning

confidence: 99%

Advanced purification of isopropanol and acetone from syngas fermentation

Janković,

Straathof,

Kiss

2023

J of Chemical Tech & Biotech

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BACKGROUNDIsopropanol and acetone production by syngas fermentation is a promising alternative to conventional fossil carbon‐dependent production. However, this alternative technology has not yet been scaled up to an industrial level owing to the relatively low product concentrations (about 5 wt% in total). This original research aims to develop cost‐effective and energy‐efficient processes for the recovery of isopropanol and acetone from highly dilute fermentation broth (>94 wt% water) for large‐scale production (about 100 ktIPA+AC y−1).RESULTSVacuum distillation and pass‐through distillation enhanced with heat pumps or multi‐effect distillation were efficiently coupled with regular atmospheric distillation and extractive distillation in several innovative intensified downstream processes. Over 99.2% of isopropanol and 100% of acetone were recovered as high‐purity end‐products (>99.8 wt%). Advanced heat pumping (mechanical vapor recompression) and heat integration techniques were implemented to decrease total annual costs (0.109–0.137 USD kgIPA+AC−1), reduce energy requirements (1.348–2.043 kWth h kgIPA+AC−1) and lower CO2 emissions (0.067–0.191 kgCO2 kgIPA+AC−1), resulting in highly competitive recovery processes.CONCLUSIONThe proposed three novel isopropanol and acetone recovery processes from dilute broth significantly contribute to the expansion of sustainable industrial fermentation. Furthermore, this original research is the first one to develop novel pass‐through distillation technology for the complex isopropanol–acetone–water system. All the designed processes are highly economically competitive and environmentally viable. In addition to recovering efficiently both isopropanol and acetone, the designed downstream processes offer the possibility to enhance the fermentation process by recycling all the present microorganisms and reducing fresh‐water requirements. © 2023 The Authors. Journal of Chemical Technology and Biotechnology published by John Wiley & Sons Ltd on behalf of Society of Chemical Industry (SCI).

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Section: Isopropanol Purificationmentioning

confidence: 99%

Advanced purification of isopropanol and acetone from syngas fermentation

Janković,

Straathof,

Kiss

2023

J of Chemical Tech & Biotech

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“…For dynamic control, the suitable temperature stages should be determined first to avoid using a complex control scheme 32 . The slope criterion is a simple and effective method for selecting the sensitive stages of the PSD processes.…”

Section: Dynamic Process Controlmentioning

confidence: 99%

“…Determination of temperature-sensitive stage For dynamic control, the suitable temperature stages should be determined first to avoid using a complex control scheme. 32 The slope criterion is a simple and effective method for selecting the sensitive stages of the PSD processes. Figure 5 shows the slope of the temperature distribution for PSD-A2 and PSD-B2.…”

Section: Dynamic Process Controlmentioning

confidence: 99%

Economic optimization and dynamic control of pressure‐swing distillation for separating the ternary azeotrope of butanone/n‐heptane/isopropanol

Sun

Zhang

et al. 2022

J of Chemical Tech & Biotech

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BACKGROUND Economic optimization and dynamic control of the separation process for recovering the ternary mixture of butanone (MEK)/n‐heptane/isopropanol (IPA) from industrial wastewater is a significant topic. In this work, the optimal pressure‐swing distillation (PSD) sequence, heat integration and dynamic control for separating MEK/n‐heptane/IPA were investigated systematically. The optimal separation sequence was determined by combining the minimum total annual cost (TAC) with the residual curves map (RCM). Pressure‐swing distillation with non‐heat integration, partial heat integration or full heat integration was compared in terms of TAC. Dynamic control schemes were designed for optimal processes of two separation sequences with and without heat integration. RESULTS The results demonstrate that the TAC of optimal PSD with non‐heat integration process can be reduced by 31.11%, whereas the TAC of optimal partial heat integration and full heat integration schemes can be reduced by 39.73% and 40.96%, respectively. The dynamic performance of all control schemes that can resist ±20% feed flow disturbances and composition disturbances are compared with the integral of squared error. CONCLUSION It is demonstrated that PSD with full integration process (FHIPSD) for separating MEK/n‐heptane/IPA has optimal economic performance, whereas PSD with non‐heat integration process (NTIPSD) has the optimal dynamic performance and robust stability. This work provides a significant reference for industrial separation of MEK/n‐heptane/IPA. © 2022 Society of Chemical Industry (SCI).

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