内容发布更新时间 : 2024/12/29 0:09:30星期一 下面是文章的全部内容请认真阅读。

年处理1.2万吨乙醇-水连续筛板精馏塔设计

摘 要

乙醇-水是工业上最常见的溶剂，也是非常重要的化工原料之一，是无色、无毒、无致癌性、污染性和腐蚀性小的液体混合物。但是由于乙醇-水体系有共沸现象，普通的精馏对于得到高纯度的乙醇。因此，研究和改进乙醇-水体系的精馏设备是非常必要的。本设计基于精馏的原理，查阅乙醇-水体系的相关物性参数，对精馏装置进行设计.而这一设计过程中的主要内容有:物料衡算，热量衡算，塔体工艺设计，塔板工艺设计，塔附属设备设计以及部分机械设计。

本次设计筛板塔是化工生产中主要的气液传质设备。此设计针对二元物系的精馏问题进行分析、选取、计算、核算、绘图等，是较完整的精馏设计过程，该设计方法被工程技术人员广泛应用。精馏设计包括设计方案的选取，精馏装置设计和核算的结果中，塔高15.38m，塔径0.8m，塔板数24块，精馏段10块，提馏段14块，进料的塔板数是第5块，最小回流比是3.1，板间距0.35m堰高精馏段0.0415m, 提馏段0.04m,堰长0.42m，相对挥发度精馏段2.26，提馏段2.27，人孔直径0.5m。工艺参数的选定泡点进料，泡点回流。设备的结构设计和工艺尺寸的设计计算，辅助设备的选型，工艺流程图，主要设备的工艺条件图等内容。通过对精馏塔的运算，可以得出精馏塔的各种设计如塔的工艺流程、生产操作条件及物性参数是合理的，各种接管尺寸是合理的，以保证精馏过程的顺利进行并使效率可能的提高。经过流体力学验算，满足设计要求。

本设计的多数接管管径取大，为了能使塔有一定操作弹性，允许气体液体流量增大，所以采取大于工艺尺寸所需的管径。

关键词：乙醇-水；精馏塔设计；筛板塔；工艺要求

Annual Processing Capacity of the Design of 12000 Tons of Ethanol - Eater

Continuous Sieve Plate Distillation Tower

Abstract: Ethanol - water industry is the most common solvent, is also an important chemical raw materials, is a colorless, non-toxic, no carcinogenicity, pollution and corrosion of liquid mixtures. Due to its excellent physical and chemical properties, widely used in the national economy in many sectors, in recent years, due to rising fuel prices, ethanol fuel are increasingly replacing traditional fuel trend. But as a result of ethanol - water system with azeotropic phenomenon, ordinary distillation to obtain high purity ethanol. Therefore, to study and improve the ethanol-water distillation equipment is very necessary. Based on the design of rectification principle, consult the ethanol - water system of the relevant physical parameters, the rectification device design. This design process, the main contents are: material balance, heat balance, the tower body column plate process design, process design, tower equipment design as well as some mechanical design.

The design of sieve plate tower in the chemical production is mainly of gas-liquid mass transfer equipment. The design for the two yuan of property of the distillation problem analysis, selection, calculation, calculation, drawing, is a complete distillation design process, the design method has been widely used in engineering and technical personnel. Distillation design including design plan selection, distillation device design and calculation results, tower 15.38m, tower diameter 0.8m, plate number 24, rectification section 10, a stripping section 14, feeding the plate number is fifth, small reflux ratio is3.1，plate spacing 0.35m weir high rectifying section 0.0415m, stripping section 0.04m, weir long 0.42m, relative volatility and distillation section 2.26, a stripping section 2.27, manhole diameter 0.5m. Process parameter selection of bubble point feeding, bubble point return. Equipment structure design and process dimensions of the design calculation, equipment selection, process flow, main equipment conditions of content. Through the distillation tower operation, can draw the distillation tower design such as the tower process flow, operation conditions and physical property parameters is reasonable, all kinds of pipe size is reasonable, to ensure the rectification process smoothly and make efficiency may be improved. After the fluid mechanics calculation, to meet the design requirements.

The design of most pipe diameter and big, in order to make the tower has certain elasticity of operation, allowing the flow of gas and liquid increases, so take more than size desired diameter.

Keywords: ethanol - water; distillation tower design; distillation tower design of sieve plate

tower; technical requirements

目 录

1.引言 ······································································································· 1 1.1精馏操作在化工生产中的应用 ···································································· 1 1.2精馏的原理 ···························································································· 2 1.3操作条件的选择 ······················································································ 2 1.3.1操作压强 ····························································································· 2 1.3.2进料状况 ····························································································· 2 1.3.3加热和冷凝 ·························································································· 2 1.3.4热能利用 ····························································································· 2 2设计方案及计算 ························································································ 3 2.1进料方式 ······························································································· 3 2.2流程说明 ······························································································· 3 2.3设计方案 ······························································································· 4 2.4精馏塔的物料衡算 ··················································································· 4 2.5原料液及塔顶、塔底产品的摩尔分率 ··························································· 4 2.6原料及塔顶、塔底产品的平均摩尔质量 ························································ 5 2.7物料衡算 ······························································································· 5 2.8塔温的确定 ···························································································· 5 2.9塔顶与塔底的平均温度下的挥发度 ······························································ 6 2.10操作线的确定 ······················································································· 9 3塔板数的确定 ··························································································· 9 3.1理论塔板数的确定 ··················································································· 9 3.2进料板 ································································································ 10 3.3全塔效率 ····························································································· 10 3.4实际塔板数 ·························································································· 11 4精馏塔的工艺条件及有关物性数据的计算 ····················································· 11 4.1操作压强 ····························································································· 11 4.2温度 ··································································································· 12