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. 2020 Dec 23;6(12):e05778.
doi: 10.1016/j.heliyon.2020.e05778. eCollection 2020 Dec.

Techno-economic analysis of aniline production via amination of phenol

Sergio Bugosen  1 , Ivan D Mantilla  2 , Francisco Tarazona-Vasquez  1
Affiliations

Techno-economic analysis of aniline production via amination of phenol

Sergio Bugosen et al. Heliyon. .

Abstract

The purpose of this research is to demonstrate through a techno-economic assessment that aniline can be industrially produced using a profitable and inherently safer process than the ones currently employed. The aniline production process was designed using process simulation software. From this, the mass and energy balances were determined, the equipment sizing was performed and the net present value (NPV) was calculated to be USD 93.5 million. Additionally, a heat integration analysis was carried out in order to improve process profitability, obtaining a new NPV of USD 97.5 million. The economic sensitivity analysis showed that the process could withstand fixed capital investment changes of up to +89%, weighted average cost of capital changes between 16-24% and a decrease in cyclohexylamine demand of up to 44%. The conceptual design is still profitable when aniline price is varied in a range of 1224-1840 $/t and phenol cost in a range of 815-1178 $/t.

Keywords: Chemical engineering; Computer-aided engineering; Economic evaluation; Energy analysis; Industrial chemistry; Phenol to aniline; Process design; Process modeling; Process safety; Safety engineering.

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Conflict of interest statement

The authors declare no conflict of interest.

Figures

Figure 1
Figure 1
Aniline production block flow diagram.
Figure 2
Figure 2
PFD – Flow sheet 100 – Reaction system.
Figure 3
Figure 3
PFD – Flow sheet 100 – Separation units.
Figure 4
Figure 4
PFD – Flow sheet 200 – hydrogen and ammonia recovery units.
Figure 5
Figure 5
PFD – Flow sheet 300 – phenol removal units.
Figure 6
Figure 6
PFD – Flow sheet 400 – MIBK, aniline and dicyclohexylamine separation units.
Figure 7
Figure 7
Hot spot value with different mitigation strategies in the first reactor (R-101).
Figure 8
Figure 8
Process NPV corresponding to the first, second and third integration.
Figure 9
Figure 9
PFD corresponding to the third integration.
Figure 10
Figure 10
HPS and cooling water energy requirement for the baseline and integrated processes.
Figure 11
Figure 11
NPV variation in the selected FCI range.
Figure 12
Figure 12
NPV variation in the selected phenol unit cost range.
Figure 13
Figure 13
NPV variation in the selected aniline selling price range.
Figure 14
Figure 14
NPV variation when the byproduct demand decreases.
Figure 15
Figure 15
NPV variation in the selected WACC range.
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