精馏塔板气液两相流体力学和传质CFD模拟与新塔板的开发
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摘要
本文以双欧拉两相流模型为基础,建立了三维精馏塔板气液两相流场和浓度场的CFD模型。模型中考虑了相含率对湍流状态的影响,使用改进的混合相k?ε湍流模型来描述气液两相湍流流动,其中相间动量和质量传递源相分别采用Krishna和Higbie的计算方法。
为了证明混合相湍流模型的优越性,在直径为1.2m的工业级筛孔塔板上,模拟计算了气液两相流场,将混合相湍流模型和单相湍流模型的计算结果与实验数据进行了对比,发现混合相湍流CFD模型计算结果与实验结果能够更好的吻合。为了进一步考察所建模型的适用性,本文在0.5×0.5m的矩形筛孔塔板上,模拟了包括漏液、正常和雾沫夹带等全范围操作状态下气液两相流场,计算结果和本文的实验数据吻合较好,表明了所建模型不受操作状态的限制,可以模拟全范围操作状态下塔板气液两相流场。另外,本文还对F1浮阀塔板气液两相流场进行了CFD模拟,模型中的平均体积相含率由本文实验进行关联。模拟得到的板上清液层高度与实验结果吻合较好,证明了模型对不同形式塔板的两相流场具有很好的适用性。
利用本文提出的流动与组分传递相耦合的气液两相CFD模型,对直径1.2m工业级筛孔塔板气液两相浓度场进行了模拟计算,研究了塔板上气液两相浓度场、点效率和传质量的分布规律,发现泡沫层和气锥是传质发生的主要区域,传质面积和板上液流状况是影响塔板效率的主要因素。
为了改善传统塔板上液体流动状况,以提高塔板传质效率,本文采用拟单相流CFD模型,模拟改进塔板结构来改善塔板上液体的不均匀流动状态。模拟是在直径为2.44m的筛孔塔板上进行的。模拟计算结果表明,增设斜度系数为16.5%的梯形入口堰,或者10块0.2m长的导流板,就可以基本消除塔板上回流区和滞流区,从而提高塔板的传质效率。
针对传统的筛板不适合大液气比操作的状况,本文在CFD模拟的基础上,提出了一种新型的气液并流塔板,并进行了流体力学性能的初步测量。实验结果表明,在大液气比条件下,该种塔板具有压降小、通量大、雾沫夹带量小等优良的流体力学性能。
A computational fluid dynamics (CFD) model was developed to predict the hydraulics and mass transfer of distillation trays. The gas and liquid phases were simulated in the Eulerian framework as two interpenetrating phases. A turbulence model based on the k ?εequations for the mixture of the two phases was used. This turbulence model was suitable for computations at all phase fraction values and can be reduced to the equivalent single phase model in the extremes when only one or other of the phase was present. Interaction between the two phases occurred via interphase momentum and mass transfer sources were calculated using the Krishna and Higbie correlations respectively.
The CFD model was applied to simulate the flow patterns and hydraulics of a commercial-scale 1.2m diameter sieve tray. To testify the validity of mixture turbulence model, predicted clear liquid heights by using mixture phase and single phase turbulence model were compared with the experimental data from the literatures. The comparison revealed that the mixture turbulence model gave better predictions than single phase turbulence model. To validate of the CFD model for all operating statuses of sieve tray, hydraulics of weeping, normal and entrainment statue of a 0.5×0.5m rectangular tray was simulated. Predicted weeping rate, clear liquid height and entrainment were found to be in good agreement with the experimental data. Valve tray was the other kind of tray applied widely in chemical engineering. In this paper, the CFD model was also used to simulate the hydraulics of an open valve tray. To provide the closure relation for the model, correlation of average gas hold up fraction was built by estimated experimental data of clear liquid heights. Several simulations were carried out for a 0.5×0.5m rectangular open valve tray with varying superficial gas velocity, weir height and liquid weir load. The clear liquid heights determined by these simulations were in good agreement with the experimental data, and the validity of the CFD model for vavle tray was proved.
Based on the hydraulics simulation, mass transfer of a 1.2m diameter sieve tray was predicted. The simulated results including the outlet concentration, the Murphree tray efficiency and the overall column efficiency agreed reasonably with the experimental data. The rules of concentration field of two phases, point efficiencies and transferred mass between two phases on sieve tray were obtained. Results showed that foaming layer and gas wimbles were the major interphase mass transfer zones, and the effective interfacial area and liquid flow field were the main factors influencing interphase mass transfer.
To improve liquid flow field and interphase mass transfer on distillation tray, a CFD quasi-single phase model was used for a diameter 2.44m sieve tray. Improving -tray structure was used to avoid the uneven fluid flow of liquid. The results of simulations showed that adding trapeziform inlet weir or guide plates could reduce retrograde flow effectively. For simulated sieve tray, the 16.5% trapeziform inlet weir, or ten guide plates with the length of 0.2m were the best way to achieve uniform liquid flow on the tray.
Because of the lower of mass transfer, efficiency and processing capacity, sieve tray does not suit the case of large ratio of liquid to gas, such as absorption, high pressure distillation. To overcome these shortcomings of sieve tray, the new gas-liquid co-current flow tray was invented in this paper. Its hydrodynamics was investigated by experiment, including clear liquid height, pressure drop and entrainment. The experimental results showed that clear liquid height, pressure drop and entrainment increased as the increase of liquid or gas flow, and the performance of gas-liquid co-current flow tray was better than sieve tray under the operating condition of large ratio of liquid to gas.
为了证明混合相湍流模型的优越性,在直径为1.2m的工业级筛孔塔板上,模拟计算了气液两相流场,将混合相湍流模型和单相湍流模型的计算结果与实验数据进行了对比,发现混合相湍流CFD模型计算结果与实验结果能够更好的吻合。为了进一步考察所建模型的适用性,本文在0.5×0.5m的矩形筛孔塔板上,模拟了包括漏液、正常和雾沫夹带等全范围操作状态下气液两相流场,计算结果和本文的实验数据吻合较好,表明了所建模型不受操作状态的限制,可以模拟全范围操作状态下塔板气液两相流场。另外,本文还对F1浮阀塔板气液两相流场进行了CFD模拟,模型中的平均体积相含率由本文实验进行关联。模拟得到的板上清液层高度与实验结果吻合较好,证明了模型对不同形式塔板的两相流场具有很好的适用性。
利用本文提出的流动与组分传递相耦合的气液两相CFD模型,对直径1.2m工业级筛孔塔板气液两相浓度场进行了模拟计算,研究了塔板上气液两相浓度场、点效率和传质量的分布规律,发现泡沫层和气锥是传质发生的主要区域,传质面积和板上液流状况是影响塔板效率的主要因素。
为了改善传统塔板上液体流动状况,以提高塔板传质效率,本文采用拟单相流CFD模型,模拟改进塔板结构来改善塔板上液体的不均匀流动状态。模拟是在直径为2.44m的筛孔塔板上进行的。模拟计算结果表明,增设斜度系数为16.5%的梯形入口堰,或者10块0.2m长的导流板,就可以基本消除塔板上回流区和滞流区,从而提高塔板的传质效率。
针对传统的筛板不适合大液气比操作的状况,本文在CFD模拟的基础上,提出了一种新型的气液并流塔板,并进行了流体力学性能的初步测量。实验结果表明,在大液气比条件下,该种塔板具有压降小、通量大、雾沫夹带量小等优良的流体力学性能。
A computational fluid dynamics (CFD) model was developed to predict the hydraulics and mass transfer of distillation trays. The gas and liquid phases were simulated in the Eulerian framework as two interpenetrating phases. A turbulence model based on the k ?εequations for the mixture of the two phases was used. This turbulence model was suitable for computations at all phase fraction values and can be reduced to the equivalent single phase model in the extremes when only one or other of the phase was present. Interaction between the two phases occurred via interphase momentum and mass transfer sources were calculated using the Krishna and Higbie correlations respectively.
The CFD model was applied to simulate the flow patterns and hydraulics of a commercial-scale 1.2m diameter sieve tray. To testify the validity of mixture turbulence model, predicted clear liquid heights by using mixture phase and single phase turbulence model were compared with the experimental data from the literatures. The comparison revealed that the mixture turbulence model gave better predictions than single phase turbulence model. To validate of the CFD model for all operating statuses of sieve tray, hydraulics of weeping, normal and entrainment statue of a 0.5×0.5m rectangular tray was simulated. Predicted weeping rate, clear liquid height and entrainment were found to be in good agreement with the experimental data. Valve tray was the other kind of tray applied widely in chemical engineering. In this paper, the CFD model was also used to simulate the hydraulics of an open valve tray. To provide the closure relation for the model, correlation of average gas hold up fraction was built by estimated experimental data of clear liquid heights. Several simulations were carried out for a 0.5×0.5m rectangular open valve tray with varying superficial gas velocity, weir height and liquid weir load. The clear liquid heights determined by these simulations were in good agreement with the experimental data, and the validity of the CFD model for vavle tray was proved.
Based on the hydraulics simulation, mass transfer of a 1.2m diameter sieve tray was predicted. The simulated results including the outlet concentration, the Murphree tray efficiency and the overall column efficiency agreed reasonably with the experimental data. The rules of concentration field of two phases, point efficiencies and transferred mass between two phases on sieve tray were obtained. Results showed that foaming layer and gas wimbles were the major interphase mass transfer zones, and the effective interfacial area and liquid flow field were the main factors influencing interphase mass transfer.
To improve liquid flow field and interphase mass transfer on distillation tray, a CFD quasi-single phase model was used for a diameter 2.44m sieve tray. Improving -tray structure was used to avoid the uneven fluid flow of liquid. The results of simulations showed that adding trapeziform inlet weir or guide plates could reduce retrograde flow effectively. For simulated sieve tray, the 16.5% trapeziform inlet weir, or ten guide plates with the length of 0.2m were the best way to achieve uniform liquid flow on the tray.
Because of the lower of mass transfer, efficiency and processing capacity, sieve tray does not suit the case of large ratio of liquid to gas, such as absorption, high pressure distillation. To overcome these shortcomings of sieve tray, the new gas-liquid co-current flow tray was invented in this paper. Its hydrodynamics was investigated by experiment, including clear liquid height, pressure drop and entrainment. The experimental results showed that clear liquid height, pressure drop and entrainment increased as the increase of liquid or gas flow, and the performance of gas-liquid co-current flow tray was better than sieve tray under the operating condition of large ratio of liquid to gas.
引文
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