异丙醇 (IPA) 路线丙酮工厂主要装置的设计与模拟

Elias Ojong Ojong, Victor Ita Etim, G. Aquah, R. I. Uzono
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摘要

我们设计了一套 225[公吨/年]异丙醇(IPA)丙酮装置。设计考虑了质量和能量平衡的基本原则,确定了丙酮装置各单元的尺寸,特别是吉布斯反应器、分离器、吸收器和蒸馏塔。工厂设计的精妙之处在于考虑材料和能量守恒原理的相互作用,并明确工厂主要单元操作的尺寸。丙酮装置的设计使用了 HYSYS 仿真软件,并根据流体的特性手动确定了装置的尺寸。由异丙醇和水(起催化剂作用)反应生成丙酮和氢气的四种成分是 2-丙醇、丙酮、氢气和水。这些成分如何加热、反应、冷却、分离、吸收,以及从异丙醇/水的混合物中蒸馏出丙酮的平衡,通过工厂关键单元操作的材料和能量值草图,以逻辑的方式展现出来。对装置进行了机械设计,以确定柱子的厚度。此外,还对丙酮进行了成本加经济分析。结果表明,装置的选型结果如下:手动反应器的直径和高度分别为 5.4[立方米]、1.56[米]和 2.34[米],分离器的直径和高度分别为 1.78[米]和 2.34[米]。吸收塔直径为 0.085[m],高度为 1.1[m],蒸馏塔设计值为 0.202[m],高度为 10.8[m],堰长为 0.154[m]。整个装置的总成本(包括公用事业成本)为 779.2 万美元;等效年运营成本为 440.8 万美元;反应器、分离器、吸收器和稀释塔的厚度分别为 2.42[毫米]、11.71[毫米]、1.99[毫米]和 3.36[毫米]。用 HYSYS 仿真结果对手工设计进行了验证,结果表明设计模型是可靠的,可以用于设计,因为各单元规格的偏差值很小,在 0.04 - 0.4 之间。设计结果表明,建议采用 IPA 路线生产丙酮,HYSYS 模拟是丙酮装置整个设计的一部分。
本文章由计算机程序翻译,如有差异,请以英文原文为准。
Design and Simulation of the Major Units of Acetone Plant from Isopropyl Alcohol (IPA) Route
A design of 225[metric tons per year] of an acetone plant from isopropanol alcohol (IPA) was developed. The design considers the fundamental principles of mass and energy balance to size the units of the acetone plant, particularly the Gibbs reactor, separator, absorber, and distillation columns. The beauty of plant design is to account for the material and energy conservation principles interactions and specify the dimensions of the main unit operations of the plant. The HYSYS simulation software was used to design the acetone plant, and the properties of the fluid were used to manually size the plant. The four components resulting from the reaction of IPA and water (acting as a catalyst) to obtain acetone and hydrogen are 2-propanol, acetone, hydrogen, and water. The balance of how these components is heated, reacted, cooled, separated, absorbed, and distilled of acetone from a mixture of IPA/water is shown logically with sketches for the material and energy values of the key unit operations of the plant. The mechanical design of the units was performed to determine the thickness of the columns. In addition, a cost-plus-economic analysis of acetone was carried out. The results indicate that, the sizing of the units gave the following results viz: manually, the reactor with sized 5.4 [m3], 1.56[m] and 2.34[m] as the diameter and height respectively, the separator was sized to 1.78[m] diameter and 2.67[m] height with 6.631[m3] volume, the absorber column gave 0.085[m] diameter, 1.1[m] height, and the distillation column design values are 0.202[m] column diameter, 10.8[m] height and the weir length of 0.154[m]. The overall cost, including the cost of utilities for the entire plant, was [$]7.792million; the equivalent annual operating cost was [$]4.408million; and the thicknesses of the reactor, separator, absorber, and dilation columns are respectively 2.42[mm], 11.71[mm], 1.99[mm] and 3.36[mm]. Validation of the manual design was carried out with HYSYS simulation results, which indicated that the design models were reliable and could be adopted for the design because the deviation values on the specifications of the units are small ranges from 0.04 – 0.4. The result of the design showed that acetone production from the IPA route was recommended and that the HYSYS simulation formed part of the entire design of the acetone plant.
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