...) 1.5D bend radius Long horizontal (developed flow) 3.5D bend radius A 1.5D bend radius with a vertical oriented upstream U A 1.5D bend radius with a horizontal upstream U Figure 2. EXPERIMENTAL SET-UP For the developed flow experiments, the gas/liquid mixing occurred via a small Y-joint...

... multiphase flow hydraulic simulator dip section particle reservoir surveillance sand transport model pipeline flow assurance model flow velocity experiment holdup custom flow assurance model critical velocity integration bhr group mpt2019 upstream oil & gas production monitoring...

... gradients in the CO 2 flow loop are in excellent agreement with the experimental data from the large-scale facilities. The results also confirm that the gas-to-liquid density ratio plays an important role, as showed in [4]. The experiments have provided valuable data sets for the verification...

... tank (C) where oil and water separate by gravity. Air is vented towards atmosphere. 4 EXPERIMENTAL RESULTS A series of experiments have been conducted for different rate and pressure combinations to screen for instabilities in the presented model setup. Some of the experiments (1 to 55) have been...

.... An injectable venturi is a venturi tube that has an opening at its throat and a pipe inclined at 45° is inserted into this opening. Thus, gas is injected counter to the flow coming from upstream of the injectable venturi to choke the working fluid passing through the throat of the venturi. Experiments were...

... velocities However, during the low liquid loading liquid accumulation experimental campaign some experiments were also extended to include high superficial gas velocities in order to obtain some pressure drop measurements (ref Figure 5-4). These experiments showed some unexpected three-phase flow effects...

..., yielding water viscosities in the range 14–42 cP. The aim of the experimental campaign was to produce experimental data relevant for modelling two- and three-phase low liquid loading flows at high gas rates. Earlier experiments [4] had revealed that the pressure drop was significantly higher in three-phase...

... at 30°C. When changing the temperature, we also adjusted the pressure such that the gas density was kept the same in all the experiments. Figure 2: Photograph of the experimental setup. Table 1: Fluid properties at 60 bara © BHR Group MPT2019 443 Density (Kg/m3) Nitrogen @ 30°C 69.4 Exxsol D60 @ 30°C...

... experiment production control pressure drop krieger international conference fluid modeling meg continuous phase fluid system viscosity ratio condensate production logging Rheology study: Comparison of a real condensate-MEG system and a model fluid system H Schümann, J Kjølaas and M Wolden...

...; we again see somewhat larger discrepancies, but the overall performance is quite acceptable. In addition to the uncertainty in the viscosity for the glycerol-water mixture, there may be additional experimental uncertainty due to difficulties in ensuring repeatability of the three phase experiments...

... Group 18 MPT 2017 the focus is on the experimental results and especially on the liquid injection experiments. 3 EXPERIMENTAL SETUP The setup consists of an approximately 3.1 m, ID = 20 mm, transparent tube. The downstream boundary condition is a large separator. In this way, the downstream pressure...

... the interface, where the oil and water phase fractions differ from unity. 2.2 Experimental data The two datasets by Elseth [2] and Amundsen [3], respectively, are complementary. Elseth presented experiments limited to horizontal flow, but spanning multiple combinations of mixture velocities and water cuts, see...

... and the experiments is shown in Figure 9. The experimental data were kindly provided by Professor Azzopardi and Dr. Abdulkadir. From the time traces in Figure 8 and Figure 9, we can clearly distinguish the slug flow regime; there is a reasonably good agreement between the CFD and experimental results. The slug flow...

... this flow regime in the current paper. Instead, we focus on the modelling of bubbly flow, churn- slug flow and slug flow. 2 EXPERIMENTAL SETUP AND RESULTS The experiments were carried out at the SINTEF Multiphase Flow Laboratory in Tiller, Norway. The large scale loop facility was used in this experimental...

... maximum injection pressure experiment water flow rate gas lift experimental data A model for liquid-assisted gas-lift unloading R Coutinho, W Williams, P Waltrich Louisiana State University, USA P Mehdizadeh Production Technology Inc., USA S Scott Petroleum ETC, USA ABSTRACT A numerical model...

... Figure 7 Liquid accumulation point as function of liquid loading, pipe diameter and pipe inclination 5.1.3 Three-phase flow effects on the frictional pressure drop at high superficial gas velocities However, during the low liquid loading liquid accumulation experimental campaign some experiments were...

... consequences for the operability of the system. In the available literature, there are relatively few experimental studies of high-rate three- phase flows in low liquid loading conditions. A common trait of all the available studies that have been identified is that the experiments were conducted in near...

... AGAINST LABORATORY EXPERIMENTS The first test of the new Slug Tracking model is to compare the predicted slug frequency with data from laboratory experiments. Figure 4 shows a comparison of predicted and measured frequency from four experimental studies, two from the WASP loop at Imperial College London...

... experiment flow rate pipe production control variation bhr group 2015 production logging reservoir surveillance slug flow slug production monitoring frequency void fraction sensor gas superficial velocity structure velocity liquid superficial velocity phase flow upstream oil & gas...

... Abstract Oil-water pipe flow experiments in a horizontal and slightly inclined test section are presented. The experimental work was performed in a 16 m acrylic test section with ID of 60 mm , using tap water and a medium viscosity oil (61 cP ) as test fluids. The pipe inclination...