Effects of High Oil Viscosity on Drift Velocity for Horizontal and Upward Inclined Pipes
- Authors
- Bahadir Gokcal (University of Tulsa) | Abdel Salam Al-Sarkhi (University of Tulsa) | Cem Sarica (University of Tulsa)
- DOI
- https://doi.org/10.2118/115342-PA
- Document ID
- SPE-115342-PA
- Publisher
- Society of Petroleum Engineers
- Source
- SPE Projects, Facilities & Construction
- Volume
- 4
- Issue
- 02
- Publication Date
- June 2009
- Document Type
- Journal Paper
- Pages
- 32 - 40
- Language
- English
- ISSN
- 1942-2431
- Copyright
- 2009. Society of Petroleum Engineers
- Disciplines
- 4.1.9 Tanks and storage systems, 4.1.5 Processing Equipment, 4.2 Pipelines, Flowlines and Risers, 5.3.2 Multiphase Flow, 4.3 Flow Assurance, 4.6 Natural Gas, 5.1.8 Seismic Modelling
- Downloads
- 1 in the last 30 days
- 558 since 2007
- Show more detail
- View rights & permissions
| SPE Member Price: | USD 12.00 |
| SPE Non-Member Price: | USD 35.00 |
Summary
The translational velocity, velocity of slug units, is one of the key closure relationships in two-phase flow mechanistic modeling. It is described as the summation of the maximum mixture velocity in the slug body and the drift velocity. The existing equation for the drift velocity is developed by using potential flow theory. Surface tension and viscosity are neglected. However, the drift velocity is expected to be affected with high oil viscosity. In this study, the effects of high oil viscosity on drift velocity for horizontal and upward inclined pipes are experimentally observed. The experiments are performed on a flow loop with a test section 50.8 mm ID for inclination angles of 0° to 90°. Water and viscous oil are used as test fluids. Liquid viscosities vary from 0.001 to 1.237 Pa•s. A new drift velocity model is proposed for high oil viscosity for horizontal and upward inclined pipes. The experimental results are used to evaluate the performances of proposed model for drift velocity. The calculated drift velocities are compared very well with the experimental results. The proposed model could be easily implemented into translational velocity equation. It should improve the existing two-phase flow models in the development and maintenance of heavy oil fields.
Introduction
High-viscosity oils are produced from many oil fields around the world. Oil production systems are currently flowing oils with viscosities as high as 10 Pa•s. Current multiphase flow models are largely based on experimental data with low viscosity liquids. Commonly used laboratory liquids have viscosities less than 0.020 Pa·s. Multiphase flows are expected to exhibit significantly different behavior for higher viscosity oils.
Gokcal et al. (2008b) observed slug flow to be the dominant flow pattern for the high-viscosity oil and gas flows. The knowledge of the slug flow characteristics is crucial to design pipelines and process equipments. In order to improve the accuracy of slug characteristics for high-viscosity oils, new models for slug flow are needed such as translational velocity.
Translational velocity is composed of a superposition of the bubble velocity in stagnant liquid (i.e. the drift velocity, vd, and the maximum velocity in the slug body). The research efforts have been focused on the drift velocity in horizontal and upward inclined pipes.
| File Size | 497 KB | Number of Pages | 9 |
References
Alves, I.N., Shoham, O., and Taitel, Y. 1993. Drift velocity ofelongated bubbles in inclined pipes. Chem. Eng. Sci. 48(17): 3063-3070. doi:10.1016/0009-2509(93)80172-M.
Bendiksen, K.H. 1984. An experimentalinvestigation of the motion of long bubbles in inclined tubes. Int. J.Multiphase Flow 10 (4): 467-483.doi:10.1016/0301-9322(84)90057-0.
Benjamin, T.B. 1968. Gravity currents and relatedphenomena. J. Fluid. Mech. 31 (2): 209-248.doi:10.1017/S0022112068000133.
Bhaga, D. and Weber, M.E. 1981. Bubbles in viscous liquids:shapes, wakes, and velocities. J. Fluid Mech. 105:61-85. doi:10.1017/S002211208100311X.
Bonnecaze, R.H., Eriskine, W. Jr., and Greskovich, E.J. 1971. Holdup and pressure drop fortwo-phase slug flow in inclined pipelines. AIChe Journal17 (5): 1109-1113. doi:10.1002/aic.690170516.
Carew, P.S, Thomas, N.H., and Johnson, A.B. 1995. A physically basedcorrelation for the effects of power law rheology and inclination on slugbubble rise velocity. Int. J. Multiphase Flow 21 (6):1091-1106. doi:10.1016/0301-9322(95)00047-2.
Davies, R.M. and Taylor, G.I. 1950. The Mechanics of Large BubblesRising through Extended Liquids and through Liquids in Tubes. Proc. R.Soc. Lond. A 200 (1062): 375-390.doi:10.1098/rspa.1950.0023.
Dukler, A.E. and Hubbard, M.G. 1975. A Model for Gas-Liquid Slug Flowin Horizontal and Near-Horizontal Tubes. Ind. Eng. Chem. Fundamen.14 (4): 337-347. doi:10.1021/i160056a011.
Dumitrescu, D.T. 1943. Strömung an einer Luftblaseim senkrechten Rohr. ZAMM—Zeitschrift für Angewandte Mathematik undMechanik 23 (3): 139-149. doi:10.1002/zamm.19430230303.
Gokcal, B, Al-Sarkhi, A.S., and Sarica, C. 2008a. Effects of High OilViscosity on Drift Velocity for Horizontal Pipes. Presented at the 6th NorthAmerican Conference on Multiphase Technology, Banff, Canada, 4-6 June.
Gokcal, B., Wang, Q., Zhang, H.-Q., and Sarica, C. 2008b. Effects of High Oil Viscosity onOil/Gas Flow Behavior in Horizontal Pipes. SPE Proj Fac & Const3 (2): 1-11. SPE-102727-PA. doi: 10.2118/102727-PA.
Hasan, A.R. and Kabir, C.S. 1986. Predicting Multiphase Flow Behaviorin a Deviated Well. SPE Prod Eng 3 (4): 474-482.SPE-15449-PA. doi: 10.2118/15449-PA.
Joseph, D.D. 2003. Rise velocity of a sphericalcap bubble. J. Fluid Mech. 488: 213-223.doi:10.1017/S0022112003004968.
Nicholson, M.K., Aziz K., and Gregory G.A. 1978. Intermittent Two-Phase Flowin Horizontal Pipes: Predictive Models. Can. J. Chem. Eng.56: 653-663.
Nicklin, D.J., Wilkes, J.O., and Davidson, J.F. 1962. Two-Phase Film Flow inVertical Tubes. Trans. Inst. Chem. Eng. 40: 61-68.
Shosho, C.E. and Ryan, M.E. 2001. An experimental study ofthe motion of long bubbles in inclined pipes. Chem. Eng. Sci.56 (6): 2191-2204. doi:10.1016/S0009-2509(00)00504-2.
Wallis, G.B. 1969. One Dimensional Two-Phase Flow. New York:McGraw-Hill.
Weber, M.E. 1981. Drift in intermittent two-phase flow in horizontal pipes.Can. J. Chem. Eng. 59: 398-399.
Weber, M.E., Alarie, A., and Ryan, M.E. 1986. Velocities of extendedbubbles in inclined tubes. Chem. Eng. Sci. 41 (9):2235-2240. doi:10.1016/0009-2509(86)85073-4.
Zukoski, E.E. 1966. Influence of viscosity,surface tension, and inclination angle on motion of long bubbles in closedtubes. J. Fluid Mech. 25 (4): 821-837.doi:10.1017/S0022112066000442.
