Frictional Pressure Losses for Annular Flow of Drilling Mud and Mud-Gas Mixtures

1985 ◽  
Vol 107 (1) ◽  
pp. 142-151 ◽  
Author(s):  
J. P. Langlinais ◽  
A. T. Bourgoyne ◽  
W. R. Holden
Keyword(s):  
Experimental Data ◽  
Single Phase ◽  
Two Phase Flow ◽  
Hydraulic Diameter ◽  
Phase Flow ◽  
Drilling Mud ◽  
Two Phase ◽  
Bingham Plastic ◽  
Pressure Losses ◽  
Annular Geometry

The calculation of single-phase and two-phase flowing pressure gradients in a well annulus is generally based on an extension of empirical correlations developed for Newtonian fluids in circular pipes. Various techniques for extending pipe flow correlations to an annular geometry have been presented in the literature which involve the representation of the annular well geometry with an equivalent circular diameter and the representation of non-Newtonian fluid behavior with an apparent Newtonian viscosity. Unfortunately, little experimental data have been available which would allow a comparison of the relative accuracy of the various proposed techniques. In this study, experimental pressure gradient data have been taken in two 6000-ft wells. Frictional pressure losses for single-phase flow (mud only) in two annuli were compared to values predicted by the Bingham plastic and power law models. These calculations utilized the equivalent diameters defined by the Crittendon criteria, the hydraulic diameter, and the slot approximation. Also, total pressure difference for two-phase flow was measured for one annular geometry. This data was compared to that predicted by the Poettmann and Carpenter, Hagedorn and Brown, Orkiszewski, and Beggs and Brill correlations. Comparison of experimental data with the various prediction techniques was favorable, each having advantage in certain situations. For the data investigated, the Crittendon criteria using a Bingham plastic model gave the best results. The two-phase flow data was best predicted by the Hagedorn and Brown correlation utilizing an equivalent hydraulic diameter.

Frictional Pressure Losses for Single-Phase and Two-Phase Flow of Drilling Muds

1983 ◽  
Vol 105 (3) ◽  
pp. 372-378 ◽  
Author(s):  
F. A. Elfaghi ◽  
J. P. Langlinais ◽  
A. T. Bourgoyne ◽  
W. R. Holden
Keyword(s):  
Single Phase ◽  
Two Phase Flow ◽  
Phase Flow ◽  
Drilling Mud ◽  
Two Phase ◽  
Rheological Models ◽  
Bingham Plastic ◽  
Well Control ◽  
Pressure Losses ◽  
Drilling Muds

The vertical flow of mud and gas-mud mixtures in long pipes is of interest in the design and operation of subsea well control equipment where long choke lines are required. Heretofore, the question of two-phase flow of non-Newtonian drilling muds has not been investigated experimentally in full-scale well systems. Frictional-pressure losses were measured in a 2 3/8-in., 3000-ft long, vertical tubing when flowing drilling mud alone, and flowing mud-gas mixtures. The single-phase data was compared to values predicted by both the Bingham plastic and power law rheological models, which are commonly used to describe non-Newtonian fluids. The multiphase pressure loss data were used to evaluate various published correlation techniques.

Two-Phase Flow in Liquid Filled Vessels During the Depressurization by Periodic Venting

2003 ◽  
Author(s):  
Dieter Mewes ◽  
Dirk Schmitz
Keyword(s):  
Single Phase ◽  
Two Phase Flow ◽  
Bubbly Flow ◽  
Exothermic Reaction ◽  
Liquid Mixtures ◽  
Phase Flow ◽  
Two Phase ◽  
Pressure Losses ◽  
Short Period ◽  
Liquid Flows

Pressurized chemical reactors or storage vessels are often partly filled with liquid mixtures of reacting components. In case of an unexpected and uncontrolled exothermic reaction the temperature might increase. By this the pressure follows and would exceed a critical maximum value if there would be no mechanism to decrease the pressure and the temperature in a very short period of time. A sudden venting by the opening of a safety valve or a rupture disc causes a rapid vaporization of the reacting liquid mixture. A two-phase flow will pass the ventline. Since two-phase gas-liquid flows cause high pressure losses and give rise to limited mass flows leaving the reactor, single-phase gas flows are preferred. This is emphasized by a periodic venting mechanism of the pressurized vessel. Each time the two-phase flow from the bubbling-up liquid inside the vessel reaches a certain cross-section close the entrance of the ventline. The outlet-valve is closed. Inside the vessel the increasing pressure stops the two-phase flow and only single phase flow is leaving the vessel. The two-phase bubbly flow inside the vessel is detected by a tomographic measurement device during the venting process. Experimental results for local and time dependant phase void fractions as well as pressures are compared with those obtained by numerical calculations of the instationary bubble swarm behavior inside the vessel.

Use of a Bubble Tracking Method for Prediction of Downhole Natural Separation Efficiency

2005 ◽  
Vol 127 (4) ◽  
pp. 479-486
Author(s):  
Bin Liu ◽  
Mauricio Prado
Keyword(s):  
Experimental Data ◽  
Flow Field ◽  
Single Phase ◽  
Two Phase Flow ◽  
Separation Efficiency ◽  
Phase Flow ◽  
Two Phase ◽  
Tracking Method ◽  
Wide Range ◽  
Natural Separation

For any pumping artificial lift system in the petroleum industry, the free gas significantly affects the performance of the pump and the system above the pump. A model, though not a complete two-phase flow model, has been developed for the effective prediction of separation efficiency across a wide range of production conditions. The model presented is divided into two main parts, the single-phase flow-field solution and the bubble-tracking method. The first part of the model solves the single-phase liquid flow field using the computational fluid dynamics approach. Then, a simple bubble-tracking method was applied to estimate the down-hole natural separation efficiency for two-phase flow. A comparison between the results of the model and the experimental data was conducted. It shows a very good agreement with the experimental data for lower gas void fractions (bubble flow regime).

Correlations Between Pressure Drop and Two-Phase Flow Regimes in Microchannel Networks

2009 ◽  
Author(s):  
Christian Weinmu¨ller ◽  
Dimos Poulikakos
Keyword(s):  
Experimental Data ◽  
Pressure Drop ◽  
Flow Regime ◽  
Single Phase ◽  
Two Phase Flow ◽  
Flow Regimes ◽  
Phase Flow ◽  
Two Phase ◽  
Research Activities ◽  
Wide Range

Microfluidics has experienced a significant increase in research activities in recent years with a wide range of applications emerging, such as micro heat exchangers, energy conversion devices, microreactors, lab-on-chip devices and micro total chemical analysis systems (μTAS). Efforts to enhance or extend the performance of single phase microfluidic devices are met by two-phase flow systems [1, 2]. Essential for the design and control of microfluidic systems is the understanding of the fluid/hydrodynamic behavior, especially pressure drop correlations. These are well established for single phase flow, however, analytical correlations for two-phase flow only reflect experimentally obtained values within an accuracy of ± 50% [3, 4]. The present study illustrates the effect of two-phase flow regimes on the pressure drop. Experimental measurement data is put into relation of calculated values based on established correlations of Lockhart-Martinelli with Chisholm modifications for macroscopic flows [5, 6] and Mishima-Hibiki modifications for microscale flows [7]. Further, the experimental pressure drop data is superimposed onto two-phase flow maps to identify apparent correlations of pressure drop abnormalities and flow regimes. The experiments were conducted in a square microchannel with a width of 200 μm. Optical access is guaranteed by an anodically bonded glass plate on a MEMS fabricated silicon chip. Superficial velocities range from 0.01 m/s to 1 m/s for the gas flow and from 0.0001 m/s to 1 m/s for the liquid flow with water as liquid feed and CO2 as gas. The analysis of the flow regimes was performed by imaging the distinct flow regimes by laser induced fluorescence microscopy, employing Rhodamine B as the photosensitive dye. The pressure drop was synchronically recorded with a 200 mbar, 2.5 bar and 25 bar differential pressure transmitter and the data was exported via a LabView based software environment, see Figure 1. Figure 2 illustrates the experimentally obtained pressure drop in comparison to the calculated values based on the Lockhard-Martinelli correlation with the Chisholm modification and the Mishima-Hibiki modification. For both cases the predications underestimate the two-phase pressure drop by more than 50%. Nevertheless, the regression of the experimental data has an offset of linear nature. Two-phase flow is assigned to flow regime maps of bubbly, wedging, slug or annular flow defined by superficial gas and liquid velocities. In Figure 3 the pressure drop is plotted as a surface over the corresponding flow regime map. Transition lines indicate a change of flow regimes enclosing an area of an anticline in the pressure data. In the direct comparison between the calculated and the measured values, the two surfaces show a distinct deviation. Especially, the anticline of the experimental data is not explained by the analytical correlations. Figure 4 depicts the findings of Figure 3 at a constant superficial velocity of 0.0232 m/s. The dominant influence of the flow regimes on the pressure drop becomes apparent, especially in the wedging flow regime. The evident deviation of two-phase flow correlations for the pressure drop is based on omitting the influence of the flow regimes. In conclusion, the study reveals a strong divergence of pressure drop measurements in microscale two-phase flow from established correlations of Lockhart-Martinelli and recognized modifications. In reference to [8, 9], an analytical model incorporating the flow regimes and, hence, predicting the precise pressure drop would be of great benefit for hydrodynamic considerations in microfluidics.

Modeling Downhole Natural Separation Using a Bubble Tracking Method

2004 ◽  
Author(s):  
Bin Liu ◽  
Mauricio Prado
Keyword(s):  
Experimental Data ◽  
Flow Field ◽  
Single Phase ◽  
Two Phase Flow ◽  
Separation Efficiency ◽  
Phase Flow ◽  
Two Phase ◽  
Tracking Method ◽  
Wide Range ◽  
Natural Separation

For any pumping artificial lift system in petroleum industry, the free gas significantly affects the performance of the pump and the system above the pump. A model, though not a complete two-phase flow model, has been developed for the effective prediction of separation efficiency across a wide range of production conditions. The model presented is divided into two main parts, the single-phase flow field solution and the bubble tracking method. The first part of the model solves the single-phase liquid flow field using the CFD approach. Then, a simple bubble-tracking method was applied to estimate the down-hole natural separation efficiency for two-phase flow. A comparison between the results of the model and the experimental data was conducted. It shows a very good agreement with the experimental data for lower gas void fractions (bubble flow regime).

Analysis of Friction Factor of Two-Phase Flow in Helically Coiled Tubes

2021 ◽  
Author(s):  
Baihui Jiang ◽  
Zhiwei Zhou ◽  
Yu Ji
Keyword(s):  
Experimental Data ◽  
Pressure Drop ◽  
Friction Factor ◽  
Single Phase ◽  
Two Phase Flow ◽  
Phase Flow ◽  
Steam Generators ◽  
Two Phase ◽  
Frictional Pressure Drop ◽  
Applicable Range

Abstract With compact structure and enhanced heat transfer capacity, helical-coiled once through steam generators (HTSGs) are widely used in the small modular reactors (SMRs). Nevertheless, the inside centrifugal forces make the flow more complicated, and increase the frictional pressure drop, which is closely related to the dual test of alternating thermal stress and flow instability. Therefore, the analysis of the friction factor in helically coiled tubes is significant to the efficient and safe operation of HTSGs. While the friction factor of single-phase flow in helically coiled tubes was fully studied and extensive correlations have been validated by a large amount of experimental data, the friction factor of two-phase flow still lacks feasible prediction due to its much more complexity. The existed correlations of two-phase flow in helically coiled tubes are mostly based on specified experimental parameters, so the applicable range is limited. Few scholars have tried to extend these correlations to broader applicability, but the trivial applicable range is unsuitable for program development or engineering design, which needs an accurate prediction of friction factor in a wider range. In this paper, existing frictional pressure drop correlations are investigated. The accuracy of single-phase frictional pressure drop correlations is verified through the comparison of calculation results. Since the known experimental data cannot cover a wide range of parameters, two assumptions are proposed, and the rationality is verified through the existing experimental data and calculation analysis. Based on the two assumptions and calculation, a set of calculation correlations for frictional pressure drop of two-phase flow in helically coiled tubes are proposed. The accuracy of this calculation model is validated by experimental data. The scope of application of this model is: D / d = 15–100, P = 0.12–6.3MPa, G = 200–1500kg / m2s, which is sufficient to support the design and operation of steam generators and the development of the simulation programs.

Single-Phase and Two-Phase Flow Pressure Drop in a Long Double Helicoidally-Coiled Tube

2021 ◽  
Author(s):  
Veera Manek ◽  
Tao Fang ◽  
S. Mostafa Ghiaasiaan ◽  
Jeff Patelczyk
Keyword(s):  
Experimental Data ◽  
Pressure Drop ◽  
Single Phase ◽  
Two Phase Flow ◽  
Reynolds Numbers ◽  
Phase Flow ◽  
Single Phase Flow ◽  
Two Phase ◽  
Friction Factors ◽  
Flow Experiments

Abstract Single-phase and two-phase frictional pressure drop in horizontally-oriented double helically coiled tubes confined in a cylindrical shell is experimentally studied using an instrumented test loop that represents a prototypical liquified natural gas (LNG) fuel delivery system for internal combustion (IC) engines. Adiabatic experimental data addressing liquid (water) and gas (nitrogen) single-phase flows, as well as two-phase flows (air-water) in the helicoidally coiled tubes are presented. The range of Reynolds numbers for single-phase flow experiments is 2600 to 4800. In two-phase flow experiments the liquid-only and gas-only Reynolds numbers varied in 1030 to 6600 and 1700 to 17700 ranges, respectively. In laminar single-phase flow regime the measured friction factors are in relatively good agreement with well-established correlations. In the turbulent flow regime the measured friction factors are moderately higher than the prediction of well-established published correlations. Two-phase flow frictional pressure drops are compared with some relevant correlations, with poor agreement. The generated experimental data are empirically correlated based on the two-phase flow multiplier concept.

scholarly journals Experimental data for the slug two-phase flow characteristics in horizontal pipeline

Data in Brief ◽  
2018 ◽  
Vol 16 ◽  
pp. 527-530 ◽  
Author(s):  
Abdalellah O. Mohmmed ◽  
Mohammad S. Nasif ◽  
Hussain H. Al-Kayiem
Keyword(s):  
Experimental Data ◽  
Two Phase Flow ◽  
Flow Characteristics ◽  
Phase Flow ◽  
Two Phase

Pressure losses of two-phase flow in a variable-diameter tube

2012 ◽  
Vol 47 (11-12) ◽  
pp. 717-724
Author(s):  
V. N. Novozhilov ◽  
D. A. Baranov
Keyword(s):  
Two Phase Flow ◽  
Phase Flow ◽  
Two Phase ◽  
Pressure Losses ◽  
Variable Diameter
Sign in / Sign up

Export Citation Format

Share Document