Desolidification structure and optimization of specially-shaped hydrocyclone three-phase separation device for industrial waste oil

doi:10.11949/0438-1157.20220963

Abstract

Abstract:

Dehydration and desolidification of industrial waste oil is an important part of waste oil resource process. In order to efficiently remove water and solid particle impurities in waste oil emulsion, a specially-shaped hydrocyclone three-phase separation device that can realize efficient separation of oil-water-solid phase was proposed. The device structure and its parameters play a key factor in the oil-water-solid three-phase separation efficiency. Therefore, a numerical model of the specially-shaped hydrocyclone three-phase separation device was established by coupling the multiphase flow governing equations, the population balance equation and the solid particle tracking equation under the condition of sparse particles, ignoring the influence of particle on the conservation of mass and momentum. The influence of the desolidification section structure of the separation device on the desolidification and dehydration efficiency was investigated, and the desolidification section structural parameters of the separation device were further optimized. Numerical and experimental results showed that the desolidification section structure variation of the device significantly affected the desolidification performance of the specially-shaped hydrocyclone three-phase separation device, but the effect on the dehydration rate is not obvious. When the diameters of the optimal bottom flow pipe, solid removal pipe and side flow pipe are 6, 15 and 6 mm respectively, the solid particle recovery rate and oil removal rate of the side flow outlet of the device reach the highest at the same time, which can reach more than 87%. It provides theoretical and technical support for the design and development of high-performance industrial waste oil recycling devices.

Key words: multiphase flow, separation, computational fluid dynamics, numerical analysis

摘要：

工业废油脱水去固处理是其资源化工艺的重要环节，为高效地去除废油乳化液中的水和固体颗粒杂质，提出一种能够实现油-水-固相高效分离的异构旋流三相分离装置。装置结构及其参数是影响油-水-固三相分离效率的关键因素。于是，通过耦合多相流控制方程、群体平衡和稀疏颗粒条件下的颗粒追踪方程，忽略颗粒对整体质量守恒和动量守恒的影响，建立了异构旋流三相分离数值模型，通过模型考察了分离装置去固段结构对去固脱水效率的影响，并进一步优化了分离装置去固段的结构参数。计算与实验结果表明：装置去固段结构的变化会显著影响异构旋流三相分离装置的去固性能，对脱水率的影响不明显；最佳底流管、去固管和侧流管直径分别为6、15和6 mm时，装置侧流口的固体颗粒回收率和脱油率同时达到最高，可达87%以上，为设计研制高性能工业废油资源化装置提供理论和技术支撑。

关键词: 多相流, 分离, 计算流体力学, 数值分析

CLC Number:

TG 96

Haifeng GONG, Xin LUO, Ye PENG, Bao YU, Yang YANG, Haohua ZHANG. Desolidification structure and optimization of specially-shaped hydrocyclone three-phase separation device for industrial waste oil[J]. CIESC Journal, 2022, 73(11): 5025-5038.

龚海峰, 罗鑫, 彭烨, 余保, 杨阳, 张浩华. 工业废油异构旋流三相分离装置去固结构及优化[J]. 化工学报, 2022, 73(11): 5025-5038.

Figures/Tables 17

Fig.1 Geometric structure of specially-shaped hydrocyclone three-phase separation device

Table 1 Structural parameters of specially-shaped hydrocyclone three-phase separation device

D_o/mm	D_i/mm	L_o/mm	D_s/mm	D/mm	D_h/mm	D_u/mm	D_w/mm	L₀/mm	L₁/mm	δ/mm	L₃/mm	L₄/mm
18.0	12.0	45.0	70.0	26.0	4.0~8.0	3.0~9.0	11.0~19.0	124.7	305.5	25.0	100.0	50.0

Fig.2 Calculation grid of specially-shaped hydrocyclone three-phase separation device

Fig.3 Radial distribution curves of axial and tangential velocities for different mesh numbers

Fig.4 Separation efficiency of different sideflow out split ratios

Fig.5 Oil-water-solid three-phase separation experimental device and process

Table 2 Physical parameters

ρ_o/(kg/m³)	ρ_w/(kg/m³)	ρ_p/(kg/m³)	μ_o/(mPa·s)	μ_w/(mPa·s)	d_p/μm
863	998.3	2650	16.807	1.003	50

Fig.6 Comparison of numerical results and experimental results of specially-shaped hydrocyclone three-phase separation device

Fig.7 Tangential velocity distributions of different underflow pipe diameters: (a) Tangential velocity distribution contour of different underflow pipe diameters at y=0 section; Tangential velocity distributions of different underflow pipe diameters on different sections: (b) z=100.0 mm; (c) z=200.0 mm

Fig.8 Solid particle distribution of different underflow pipe diameters: (a) The trajectory of the solid particle of different underflow pipe diameters; (b) Solid particle escape rate of different underflow pipe diameters; (c) Solid particle recovery rate of different underflow pipe diameters

Fig.9 Separation efficiency of different underflow pipe diameters

Fig.10 Tangential velocity distributions of different desolidification pipe diameters: (a) Tangential velocity distribution contour of different desolidification pipe diameters at y=0 section; Tangential velocity distributions of different underflow pipe diameters on different sections: (b) z=100.0 mm, (c) z=200.0 mm

Fig.11 Solid particle distribution of different desolidification pipe diameters: (a) The trajectory of the solid particle of different desolidification pipe diameters; (b) Solid particle escape rate of different desolidification pipe diameters; (c) Solid particle recovery rate of different desolidification pipe diameters

Fig.12 Separation efficiency of different desolidification pipe diameters

Fig.13 Tangential velocity distributions of different sideflow pipe diameters: (a) Tangential velocity distribution contour of different sideflow pipe diameters at y=0 section; Tangential velocity distributions of different sideflow pipe diameters on different sections: (b) z=100.0 mm, (c) z=200.0 mm

Fig.14 Solid particle distribution of different sideflow pipe diameters: (a) The trajectory of the solid particle of different sideflow pipe diameters; (b) Solid particle escape rate of different sideflow pipe diameters; (c) Solid particle recovery rate of different sideflow pipe diameters

Fig.15 Separation efficiency of different sideflow pipe diameters

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