摘要
本文首先对直接接触传热过程、直接接触冷凝过程和降膜冷凝理论及研究进展进行了总结和介绍。对规整填料内气—液两相流动过程和传热传质行为的研究进展进行了综述，并简介了连续热力学方法及其研究进展。
针对的原油减压塔换热段波纹板规整填料的体积传热系数缺乏理论预测模型的现状，本文分别建立了三个数学模型并结合了实验研究。本文第二部分建立了减压下气液两相烃类混合物在倾斜通道内直接接触传热传质过程的二维CFD模型。模型中提出了一种新的基于VOF方法的传热传质源项，源项采用“松弛因子×距离热力学平衡的推动力”的形式，在气—液相界面上构建了一个动态的气液两相接近热力学平衡的“内边界条件”。模型中的烃类混合物采用5个虚拟组分来描述。本文还对该模型进行了气液进口边界条件的参数学习。本文第三部分在第二部分所建模型的基础上，建立了基于连续热力学方法的气液直接接触传热传质过程的二维CFD模型。基于连续热力学的汽液平衡关系、传递方程等已有理论，本文提出基于连续热力学方法的气液传热传质源项形式。本文还对该模型进行了气液进口边界条件的参数学习，模拟结果同第二章类似。
本文第四部分别对常、减压下水-水蒸气系统和柴油系统在规整填料内的直接接触冷凝过程进行了实验研究。实验发现在常、减压下，两种系统中气相冷凝速率均为在填料段下端第一盘填料内最高，在减压操作下，这种趋势更为明显。当汽液温差及喷淋密度均较大时，会发生剧烈的雾化现象从而使填料的局部体积传热系数下降。实验得到的填料局部体积传热系数均比工业减压塔中填料的全局体积传热系数高一个数量级。
本文第五部分在第三部分所建模型的基础上，建立了整盘及多盘波纹板规整填料内气液直接接触传热传质过程的数学模型，并根据第四部分中柴油系统的实验数据，对该模型进行了初步实验验证。模拟结果与实验结果吻合较好。本文还根据原油减压塔的现场数据，对减压塔顶循段进行了模拟计算。模拟结果显示，气相中烃类混合物的冷凝过程主要发生在填料下方的四盘填料内，并且每盘填料的体积传热系数从填料下端向上依次降低。沿气体流动方向，气相中烃类混合物平均分子量下降，组分变轻。沿液膜流动方向，液膜组成先变轻后变重。从总体上看，润湿面积和不凝气含量是影响气相中烃类混合物冷凝速率的两个重要因素。
In the first part of this dissertation, a brief review of DCH (Direct contact heattransfer), DCC (Direct contact condensation) and falling film condensation, includingtheir related theory and the development was introduced. Published works on theresearch of vapor-liquid two phase flow, heat and mass transfer in structured packingwere also reviewed. In addition, development of CTM (Continuous ThermodynamicsMethod) was introduced.
In view of the lack of prediction model for the volume heat transfer coefficientin the corrugate plate structured packing of the heat transfer area in a crude oilvacuum distillation tower, three theory models were developed and relatedexperiment researches were carried out. In the second part of this dissertation, a2-DCFD model of direct contact heat and mass transfer of a multicomponent two-phaseflow in an inclined channel at sub-atmospheric pressure was developed, in which anovel source form for heat and mass transfer based on VOF method was presented.While the form of “relaxation parameter×distance to the state of thermodynamicequilibrium” was selected, a “inner boundary condition” close to the state ofthermodynamic equilibrium was formed. Five pseudo-components were used fordescribing the hydrocarbon mixtures. Parameters of gas and liquid inlet boundaryconditions were studied. Based on the model developed in the second part, a2-D CFDmodel of direct contact heat and mass transfer of a two-phase flow coupled with CTMwas developed. According to the existing theory of vapor-liquid equilibrium andtransport equations for CTM, a novel source form base on CTM for heat and masstransfer at gas-liquid interface was presented. Parameters of gas and liquid inletboundary conditions were also studied, and the results were similar to that in thesecond part.
In the fourth part of this dissertation, direct contact condensation process ofwater-steam and diesel-diesel vapor mixtures in structured packing under atmosphericand vacuum pressure was investigated experimentally. The result showed thatcondensation rate in the first layer was the highest under atmospheric andsub-atmospheric, this trend was more obviously under vacuum condition. When bothtemperature difference and liquid sprayed density were large, serious mistphenomenon occurred which made a lower local volume heat transfer coefficient inthe structured packing. The local volume heat transfer coefficients from the experimental result were an order higher than the total volume heat transfercoefficient in industrial vacuum tower.
Base on the model in the third section, in the fifth part of this dissertation, amulti-scale model of heat and mass transfer in a structured packing layer or sectionwas developed. Preliminary experimental verification for the model was carried outaccording to the experimental result of diesel-diesel vapor in the fourth section. Thesimulation result of the model was in good agreement with the experimental result. Asimulation focus on the top cycle in the vacuum tower was carried out according tothe industrial data. The result showed that most condensation process of the gashydrocarbon mixtures occurred in the lower four structured packing layers and thevolume heat transfer coefficient of every packing layer decreased in an upwarddirection. Along the direction of gas flow, the molecular weight of the gashydrocarbon mixtures decreased with a lighter composition. Along the direction ofliquid film flow, the film composition was lighter first and then turned heavier. Ingeneral, the area of wet and the mass fraction of non-condensable gas were twoimportant factors which influenced the condensation rate of hydrocarbon mixtures inthe gas phase.
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