Sage Journals: Discover world-class research

Abstract

Based on the mechanistic model of the two-phase swirling annular flow behavior, a calculation method for the effective distance of vortex tool is obtained by taking Kelvin–Helmholtz instability into account. The rationality of the proposed method is validated by comparing the predicted liquid film thickness and pressure under non-swirling flow with the commonly used correlations. Then, the influences of gas–liquid ratio, helix angle, and hub diameter of vortex tool on the liquid film thickness, pressure drop, and effective distance have been analyzed. Results show that the presence of the vortex tool causes the decrease in the liquid film thickness and increase in the pressure drop. The liquid film thickness increases gradually as the helix angle and the hub diameter increase, and the larger helix angle results in smaller pressure drop. The effective distance increases with an increase in the gas–liquid ratio and decreases with an increase in helix angle and hub diameter. A sudden decrease occurs when the helix angle exceeds 60°. The gas–liquid ratio and helix angle are more dominant factors than the hub diameter on the liquid film thickness, pressure drop, and effective distance.

Keywords

Vortex tool effective distance two-phase swirling annular flow liquid film thickness helix angle

Introduction

Swirl flows have a variety of applications in the oil and gas industry, such as in casing turbulators,¹ rotary gas separators,² and vortex tools,³ due to good separating properties and conveyance performance. The vortex tool is a newly developed downhole equipment to unload liquid and restore continuous production of low-rate gas wells. At present, the commonly used vortex tool consists of a fishing head, a corkscrew deflector, a draft tube, and the setting device, as shown in Figure 1. It has no moving parts and does not need additional energy source. Field tests and laboratory experiments^3,4,5 revealed that the vortex tool was able to lower the critical gas velocity, reduce the tubing pressure loss, and improve the liquid-carrying capacity of gas wells.

Figure 1.

Structural diagram of the vortex tool.

When the fluid flows through the annular channel between the corkscrew deflector and the tubing, the flow pattern is transformed from straight flow to swirling flow due to the centrifugal force, and the swirling flow will propagate over a long distance. However, due to the wall friction in the downstream of the vortex tool, the swirling flow will gradually decay and revert back to the upstream straight flow. The work by Kreith and Sonju⁶ showed that a turbulent swirl decays to about 10%–20% of its initial intensity in a distance of about 50 pipe diameters. And recently, Liu and Bai⁷ have conducted experimental investigations to study the decay of the gas–liquid two-phase swirling flow. The results showed that the gas–liquid two-phase swirling flow decays quickly and the swirl intensity reduces to 1% of the initial swirl intensity at about 30 pipe diameters. Obviously, the decay of swirling flow is inevitable. Therefore, numerous researchers have studied the decay rate of the swirling flow. To summarize, the decay of the swirling flow is best fitted by an exponential law,⁸ and the decay rate is mainly affected by the pipe roughness,⁹ the Reynolds number,¹⁰ the geometry of the swirler, and the initial swirl intensity.¹¹

So, it is an alternative method to increase the effective swirl distance by optimizing the geometrical configuration of vortex tool to reduce the swirl intensity decay rate. In addition, a more effective way is to install multiple vortex tools along the tubing to maintain the continuity of the swirling flow. Table 1 shows the stages and installation depth of vortex tools in partial gas wells in China.

Table 1.

Statistics of vortex tool stages and installation depth.

Well no.	Gas field	Stages of vortex tool	Vortex tool installation depth (m)
			First stage	Second stage	Third stage
B1-91	Hubuzhai Gas Field¹²	3	3270	2500	1600
S14-11-38	Sulige Gas Field¹³	2	3350	1775
S6-16-25	Sulige Gas Field¹⁴	2	3200	1600
C45	Cainan Oilfield	2	2320	1315
S-5	Yakela-Dalaoba Gas Field¹⁵	3	4500	3000	1500

As shown, the given five test wells are equipped with multiple stages of vortex tools. In wells S14-11-38, S6-16-25, C45, and S-5, the vortex tools are almost equally spaced, and the distance between adjacent vortex tools in well B1-9 increases upward along the tubing. The minimum spacing is 770 m and the maximum spacing is 1775 m, which are much greater than the swirl distance obtained from the swirl intensity decay theory. Obviously, the spacings given in Table 1 are not the true swirl distances of the vortex tools. Therefore, it is of great significance to investigate the effective swirl distance of vortex tool theoretically. Unfortunately, works addressing these problems directly are rare in the literature.

Chen et al.¹⁶ studied the decay law of swirl flow induced by vortex tools numerically and defined the effective swirl distance as the length from the export of the tool to the point where swirl intensity equaled zero. The numerical results indicated that the effective distance of vortex tool is in the range of 10–100 m, and the inlet velocity and gas–liquid ratio (GLR) are the main influencing factors. In the early 1990s, Wells and Smith¹ investigated the effects of flow rate, viscosity, density, and turbulator blade geometry on the effective distance of the swirl flow produced by casing turbulators numerically and experimentally. In his work, the effective swirl distance was defined as the axial distance along the casing annulus where the flow angle remained greater than 3° from on-axis. Results showed that the effective swirl distance increased with an increase in turbulator blade angle and flow rate. Shu and Luo¹⁷ obtained the attenuation regularity of swirl flow induced by casing turbulators through experimental simulation and established a calculation formula for the installation space of turbulators on the basis of force balance analysis.

In addition, several investigators have studied the effective distance of vortex generator. The work by Eibeck and Eaton¹⁸ revealed that in a rectangular straight channel, the continuous distance of the longitudinal vortex can be approximately 100 times as long as the height of the vortex generator. Through numerical simulation, Wang et al.¹⁹ suggested that in a narrow rectangular straight channel, the reference value of the longitudinal spacing of the vortex generator is 30–45 times the thickness of the channel gap. Zhang et al.²⁰ studied the effect of curvature and Reynolds number on the effective distance of vortex generator numerically and found that the effective distance of the vortex generator increased with a decrease in curvature and an increase of Reynolds number. It can reach 79 times the height of the vortex generator with the curvature of 0.05, attack angle of 10°, and Reynolds number of 5370.

In order to study the effective swirl distance, the effective swirl time can be studied first. Hoffmann and Stein²¹ studied the liquid film residence time in the gas–liquid cyclone theoretically. Assuming that all of the liquid was gathered at the wall of the cyclone to form the liquid film under the impact of the centrifugal force, he derived a theoretical liquid film residence time calculation model based on the force balance on the gas and liquid phase in the axial direction. To verify the accuracy of the Hoffmann model, Yang et al.²² performed a cold model experiment to investigate the average liquid film residence time in a gas–liquid cyclone using a holdup method. The experimental results showed that the liquid residence time obviously decreased with an increase in inlet liquid holdup and decreased less with an increase in inlet gas velocity. And the predicted residence times by Hoffmann model were in good agreement overall with the measured values. However, the predicted residence times were higher than the measured values within the liquid film Reynolds number smaller than 1200.

The main objective of this study is to establish a prediction model of the swirling annular flow behavior induced by the vortex tool based on the force balance of liquid film, and then derive a calculation method for the effective distance of interfacial disturbance wave, in which the Kelvin–Helmholtz (KH) instability was taken into account. Moreover, the influences of GLR, helix angle, and hub diameter of vortex tool on the liquid film thickness, pressure drop, and effective distance are investigated.

Theoretical analysis of the swirling annular flow

After the downhole fluids flow through the vortex tool, the heavier liquid will gather toward the pipe wall to form a liquid film under the impact of the centrifugal force, while the lighter gas is centered to form a gas core. Therefore, the gas–liquid two-phase flow pattern is transformed to the swirling annular flow. In this study, to simplify the analysis, the gas–liquid two-phase swirling annular flow is decomposed into an axial annular flow and a tangential circular motion. By analyzing the axial force characteristics of annular flow, a mechanism model is established.

Force balance analysis

Assuming that all of the liquid in the pipe flows along the wall in the form of a uniformly thin film, as shown in Figure 2, the force balance on the liquid phase is²³

- τ_{w} \frac{S_{w}}{A_{f}} + τ_{i} \frac{S_{i}}{A_{f}} + {(\frac{dp}{dz})}_{f} - ρ_{l} g = 0

(1)

and that on the gas phase is

- τ_{i} \frac{S_{i}}{A_{c}} + {(\frac{dp}{dz})}_{c} - ρ_{g} g = 0

(2)

Figure 2.

Schematic of force balance in the axial annular flow.

Suppose that ε is the gas void fraction, the perimeter and cross-sectional area of liquid film and gas core can be expressed as

S_{w} = π D

(3)

A_{f} = \frac{π D^{2}}{4} (1 - ε)

(4)

S_{i} = π ε^{0.5} D

(5)

A_{c} = \frac{π D^{2}}{4} ε

(6)

When the liquid film is in equilibrium with the air core, we can get the following new correlation with equations (1)–(6) by eliminating the pressure gradient

- \frac{4 τ_{w}}{D (1 - ε)} + \frac{4 τ_{i}}{D ε^{0.5} (1 - ε)} - (ρ_{l} - ρ_{g}) g = 0

(7)

According to the annular theory by Wallis,²⁴ the axial shear force between the liquid film and the pipe wall can be written as

τ_{w} = \frac{1}{2} f_{sw} ρ_{l} v_{l}^{2} = \frac{1}{2} f_{sw} ρ_{l} \frac{v_{sl}^{2}}{{(1 - ε)}^{2}}

(8)

Similarly, the axial shear force between the liquid film and the gas core can be expressed as

τ_{i} = \frac{1}{2} f_{si} ρ_{g} {(v_{g} - v_{l})}^{2} = \frac{1}{2} f_{si} ρ_{g} {(\frac{v_{sg}}{ε} - \frac{v_{sl}}{1 - ε})}^{2}

(9)

where f_sw and f_si are the wall friction factor and interfacial friction factor in the swirling field, respectively. However, no prior study has been performed to evaluate the friction factor of swirling flow induced by the vortex tools. Considering the similarity between the twisted tape and the guide vane of vortex tool, the friction factor calculation method developed from the twisted tape is introduced here. Gambill et al.²⁵ believed that the twisted tape increased the frictional surface area of the fluid, resulting in the swirl flow friction coefficient being greater than that of the straight pipe axial flow. The following correlation was established

\frac{f_{s}}{f} = \frac{{(4 y^{2} + π^{2})}^{3 / 2}}{8 y^{3}}

(10)

where f_s and f are the friction factor in the pipe with and without twisted tape, and y is the twist ratio defined as the ratio between the tape turn length of 180° along its axis and the tube diameter

y = \frac{L_{p}}{2 D}

(11)

Lopina and Bergles²⁶ also performed an experimental study of the friction factor inside tubes with twisted tape and found that the Gambill correlation was not suitable for the smooth tube systems. Thus, a correlation for smooth tube was given

\frac{f_{s}}{f} = 2.75 y^{- 0.406}

(12)

According to equation (12), it can be concluded that the predicted swirling flow friction factors are less than those of the non-swirl axial flow if the twist ratio is above a certain lever. Therefore, Jensen et al.²⁷ recommended that the Gambill correlation was used for the twist ratio greater than 11.25, and Lopina–Bergles correlation was used for the twist ratio less than 11.25. In this study, Jensen’s recommendation is applied. For the vortex tool, the following relationship exists between the helix angle, pitch, and pitch diameter of the guide vane

\tan θ = \frac{L_{p}}{π d_{p}}

(13)

where the helix angle θ is defined as the angle of guide vane with respect to the horizontal direction. The pitch diameter can be written as

d_{p} = \frac{1}{2} (D + d_{v})

(14)

Substituting equations (13) and (14) into equation (11), the twist ratio of vortex tool can be obtained

y_{v} = \frac{π \tan θ (D + d_{v})}{4 D}

(15)

According to equations (10) and (12), in order to calculate the friction factor for the pipe with vortex tool, the friction factor for empty pipe is needed. Here, the correlation of Ouyang et al.²⁸ is used to calculate the wall friction factor f_w, given as

f_{w} = \frac{1.629}{{Re}_{f}^{0.516}} {(\frac{v_{sg}}{v_{sl}})}^{0.0926}

(16)

where Re_f is the liquid film Reynolds number. The following expression based on Wallis²⁴ is used for evaluating the interfacial friction factor f_i

f_{i} = \frac{0.079}{{Re}_{g}^{0.25}} (1 + 300 \frac{δ}{D})

(17)

For thin films in the pipe, equation (17) can be approximated to

f_{i} = \frac{0.079}{{Re}_{g}^{0.25}} [1 + 75 (1 - ε)]

(18)

By combining equations (7)–(18), we can get an implicit expression of the gas void fraction. After iteratively solving the gas void fraction, the liquid film thickness, gas and liquid velocity, and pressure drop can be obtained.

Effective swirl distance of vortex tool

In this section, the KH instability theory is applied to analyze the development of liquid film in the gas–liquid two-phase swirling flow field in the downstream of the vortex tool. According to Chandrasekhar,²⁹ when two fluids flow relatively along the interface, the KH instability occurs due to the existence of a velocity shear layer between two fluids. Therefore, there must be KH instability between the gas–liquid interfaces for the annular flow. In Berna et al.’s³⁰ study, the liquid film in annular flow is considered to be composed of two parts: a thick, fast-moving disturbance wave and a thin, slow-moving base film, as shown in Figure 3.

Figure 3.

Schematic of the disturbance wave.

Just as the harmonic amplitude evolves with respect to the distance to the excited base,³¹ the disturbance wave at the fluid interface grows linearly and weakly nonlinearly and eventually develops into a turbulent mixture with the development of the annular flow. According to the instability theory, the disturbance amplitude in the linear phase increases exponentially. So, the disturbance amplitude can be expressed as

a = a_{0} e^{κ t}

(19)

where a₀ is the disturbance wave amplitude at the initial time and κ is the perturbation linear growth rate. According to Chandrasekhar²⁹ and Wang et al.,³² the perturbation linear growth rate in the classical KH instability is

κ = w_{n} | v_{l} - v_{g} | \frac{\sqrt{ρ_{l} ρ_{g}}}{ρ_{l} + ρ_{g}}

(20)

In equation (20), the disturbance wave number w_n can be calculated by the following equation

w_{n} = \frac{2 π}{λ} = \frac{2 π}{u / fr}

(21)

where λ represents the disturbance wavelength, u represents the disturbance wave velocity, and fr represents the disturbance wave frequency. With respect to the disturbance wave velocity and frequency, several researchers have proposed the corresponding correlations. In this study, the Kumar et al.³³ model is used to calculate the disturbance wave velocity. Assuming that the interfacial friction factors based on the gas velocity and liquid velocity are equaled, Kumar presented the wave velocity by the following expression

u = \frac{ψ \cdot v_{sg} + v_{sl}}{1 + ψ}

(22)

where ψ can be obtained from the following empirical correlation

ψ = 5.5 \sqrt{\frac{ρ_{g}}{ρ_{l}}} {(\frac{{Re}_{l}}{{Re}_{g}})}^{0.25}

(23)

And the Sekoguchi³⁴ model is applied to estimate the wave frequency, given by

fr = f_{1} (Eo) \cdot f_{2} ({Re}_{l}, F r_{g}) \cdot \frac{v_{sg}}{D}

(24)

where Eo is the Bond number and Fr_g is the Froude number, defined, respectively, as follows

Eo = \frac{g D^{2} (ρ_{l} - ρ_{g})}{σ}

(25)

F_{rg} = \frac{v_{sg}}{\sqrt{gD}}

(26)

Through regression analysis of the experimental data, Sekoguchi³⁴ obtained the empirical expressions for f₁ and f₂, which can be written as

f_{1} (Eo) = E o^{- 0.5} [0.5 \ln (Eo) - 0.47]

(27)

f_{2} ({Re}_{l}, F r_{g}) = 0.0076 \ln (\frac{{Re}_{l}^{2.5}}{F r_{g}}) - 0.051

(28)

Obviously, the perturbation linear growth rate κ can be obtained by combining equations (20)–(28) once the gas and liquid velocity are solved from the previous section. According to equation (19), in order to get the duration time of disturbance wave, the wave amplitude must be determined first. As mentioned before, the swirling flow eventually reverts back to the upstream straight flow as the swirl intensity decays. The liquid film on the pipe wall will be dispersed in the gas phase as droplets again with the development of disturbance wave. Sawant et al.,³⁵ Berna et al.³⁰ and Pan et al.³⁶ think that the disturbance wave is a necessary condition for the entrainment of droplets from the wavy interfaces. Therefore, it can be considered that the final disturbance amplitude is equal to the inner diameter of the pipe (a≈D) when the swirling flow transformed to the straight flow. The initial disturbance amplitude (a₀) can be calculated by the Han model³⁷

a_{0} = 4000 D {Re}_{g}^{- 1.12}

(29)

After the duration time of the disturbance wave is obtained, the effective distance of the disturbance wave (effective swirl distance) can be approximately estimated by the following formula

L_{e} = v_{sm} \cdot t_{s}

(30)

where v_sm is the average velocity of the gas–liquid mixture and t_s is the duration time of the disturbance wave. The average velocity of the gas–liquid mixture can be written as

v_{sm} = v_{sg} ε + v_{sl} (1 - ε)

(31)

Results and discussions

Liquid film thickness

In order to verify the reliability of the newly proposed method in this article, a comparison with the commonly used liquid film thickness correlations has been made. The typical conditions for comparison are taken from a real gas well (well C45) and the parameters needed are shown in Table 2. The gas deviation factor and viscosity are estimated by Dranchuk–Purvis–Robinson³⁸ method and Lee–Gonzalez–Eakin³⁹ method, respectively. It should be noted that the existing correlations proposed by Tatterson et al.,⁴⁰ Fukano and Furukawa,⁴¹ Okawa et al.,⁴² Berna et al.,³⁰ and Pan et al.³⁶ are all established based on the non-swirling two-phase gas–liquid flow. Therefore, for the sake of consistency, the wall friction factor and interfacial friction factor under non-swirling flow are used when using the new proposed method to calculate the liquid film thickness.

Table 2.

Basic parameters of well C45.

Parameters	Value
Bottom hole pressure, P (MPa)	7.13
Bottom hole temperature, T (°C)	76.3
Gas production rate, q_g (10⁴ m³/d)	1.24
Water production rate, q_l (m³/d)	1.05
Gas gravity, γ_g	0.583
Water density, ρ_l (kg/m³)	1050
Tubing inside diameter, D (m)	0.062

Figure 4 displays the liquid film thickness predicted by various models under different gas rates. As shown, the predicted liquid film thickness decreases with an increase in gas rate (gas superficial velocity) at a given water rate (water superficial velocity). Moreover, compared with the proposed method in this article, the predicted values of other empirical models under high pressure (7.13 MPa) change marginally with the gas superficial velocity. In addition, the predicted values by the new method are close to the Pan’s correlation when the gas superficial velocity is greater than 1.2 m/s. In Figure 4(b), the predicted liquid film thicknesses by the new method are in good agreement with Berna’s correlation under low pressure (0.2 MPa). From the above analysis, it can be concluded that there is no order of magnitude difference in the liquid film thickness predicted by the new method and the commonly used correlations, which explains to some extent the rationality of the new method in the calculation of liquid film thickness.

Figure 4.

Comparison of liquid film thickness predicted by different correlations: (a) P = 7.13 MPa, v_sl = 0.004 m/s and(b) P = 0.2 MPa, v_sl = 0.01 m/s.

To further investigate the difference in liquid film thickness under swirling and non-swirling flow, the film thicknesses in the downstream of vortex tools with different helix angles and hub diameters are compared with those without vortex tool, as shown in Figure 5. It is obvious that the liquid film thickness decreased after the installation of vortex tool. This demonstrates that the liquid-carrying capacity of gas is enhanced in the swirling flow field. The increase in the drag force of the air core on the liquid film leads to more liquid phase being dispersed in the air core in the form of droplets. Moreover, the reduction of the liquid film thickness is greater at lower gas flow rates. So a more pronounced effect can be achieved to use the vortex tool at a low gas flow rate.

Figure 5.

Effects of the structure parameters of vortex tool on the liquid film thickness: (a) helix angle and (b) hub diameter.

The results in Figure 5 also show that the larger the helix angle and the hub diameter, the larger the liquid film thickness. The liquid film thickness increases more with an increasing helix angle than with an increasing hub diameter, which means the helix angles have a more dominant effect on the liquid film thickness than hub diameters. The results in respect to liquid film thickness are in good agreement with the experimental results of Takeshima et al.⁴³ and numerical results of Park and Chang.⁴⁴ The investigations on gas–liquid two-phase flow characteristics in a helical wire inserted tube by Takeshima and Park demonstrated that the average liquid film thickness increased as the pitch length and the inserted wire diameter increased. Therefore, priority should be given to the helix angle when designing vortex tools. And the liquid-carrying capacity of the vortex tool can be improved by reducing the helix angle.

Pressure drop

The proposed model can also be applied to predict the pressure distribution under annular flow conditions. Figure 6 shows the comparison of wellbore pressure distribution of well C45 predicted by the new model and six commonly used empirical correlations.^45–50 The calculation results are obtained without vortex tool. The depth of well C45 is 2400 m. As can be seen, the pressure values predicted by the proposed method are between the Mukherjee and Brill model and the Hagedorn and Brown model and have better consistency with the Hagedorn and Brown model. According to the study by Zhou et al.,⁵¹ the Hagedorn and Brown model has higher accuracy when calculating wellbore pressure. Therefore, the proposed model is reliable in the calculation of pressure drop.

Figure 6.

Comparison of pressure distribution predicted by available correlations.

In addition to the gas–liquid two-phase axial flow, the pressure drop in swirling flow can also be calculated. Figure 7 illustrates results that the helix angle affects the pressure drop in swirling flow induced by the vortex tool. The pressure drop at five helix angles were obtained with the gas superficial velocity varying from 0.9 to 1.5 m/s at a constant water superficial velocity of 0.004 m/s, respectively. It shows that the presence of the vortex tool results in an increase in the pressure drop and the pressure drop in the downstream of vortex tool increases with an increase in the gas superficial velocity and decreases with an increase in the helix angle. The pressure drop decreases by 27%–37% with the helix angle increasing from 30° to 70°. That is because the vortex tool with a larger helix angle has a longer pitch and the long pitch can reduce resistance along the way. The effect of helix angle on the pressure drop is in good agreement with the study by Takeshima et al.⁴³ and Park and Chang.⁴⁴

Figure 7.

Effects of the helix angle on the pressure drop.

Effective distance of vortex tool and influencing parameters analysis

Similar to the swirl intensity, the effective distance of the vortex tool is related not only to its geometrical configuration but also to the gas and liquid velocities. In this section, the influences of the GLR, helix angle, and hub diameter on the effective distance are analyzed.

Influence of the GLR on the effective distance

The effective distances of vortex tool at 4 different liquid rates and 11 different GLRs have been calculated by the established model, respectively, where the helix angle is 45° and the hub diameter is 42 mm. The GLR ranges from 0.50 × 10⁴ m³/m³ to 1.50 × 10⁴ m³/m³. Figure 8 shows the effective distance varies with the GLR when the liquid rate is 1, 2, 3, and 5 m³/d. As illustrated in Figure 8, the effective distance increases with an increase in GLR at a constant liquid rate, and the increment gradually decreases. However, when the liquid rate reaches a certain level, such as 5 m³/d, the GLR has little effect on the effective distance of the vortex tool. It can also be seen that the effective distance increases with an increase in the liquid rate at a constant GLR, and the effect of the liquid rate on the effective distance decreases with an increase in GLR. Referring to the studies by Kreith and Sonju,⁶ Najafi et al.,⁸ and Rocha et al.,¹⁰ the swirl intensity decay rate decreases with an increase in Reynolds number. Therefore, the swirl flow can propagate over a longer distance at higher Reynolds number, which is in agreement with the results of this study. The effective distance of the vortex tool is 2.97–10.36 m (about 48–167 pipe diameters) under the given study conditions, which has a same magnitude as the research of Kreith and Sonju⁶ and Liu and Bai.⁷ The study by Kreith showed that the turbulent swirl decayed to about 10%–20% of its initial intensity in a distance of about 50 pipe diameters, while Liu found that the swirl intensity reduced to 1% of the initial swirl intensity at about 30 pipe diameters. Likewise, the results of Shu and Luo¹⁷ indicated that the effective distance of the casing turbulator was generally not more than 10 m.

Figure 8.

Effects of the gas–liquid ratio on the effective distance of vortex tool.

Influence of the helix angle and hub diameter on the effective distance

Figure 9 depicts the effective distance of the swirling flow in the downstream of vortex tools with different helix angles at three given GLRs. As illustrated, for a certain GLR, an increase in the helix angle leads to a decrease in the effective distance. The effect of the helix angle on the effective distance is less significant under large GLRs. When the GLR is 1.2 × 10⁴ m³/m³, the effective distance decreases from 9.6 to 8.8 m with the helix angle increasing from 30° to 75°, and the reduction of the effective distance is only 0.8 m.

Figure 9.

Effects of the helix angle on the effective distance of vortex tool.

Furthermore, the reduction of the effective distance with the increasing helix angle is not a constant. There is a sudden decrease as the helix angle exceeds 60°. Therefore, it is recommended that the helix angle be controlled within 60° when designing the vortex tool.

Figure 10 shows the variation of effective distance with the hub diameter under different GLRs. It can be seen that for a given GLR, the effective distance decreases approximately linearly with increasing hub diameter. But the reduction is very small. Obviously, the effect of the hub diameter on the effective distance is less significant than the helix angle.

Figure 10.

Effects of the hub diameter on the effective distance of vortex tool.

Conclusion

A mechanistic model is established for the prediction of the swirling annular two-phase flow behavior in the downstream of the vortex tool, which is helpful to understand and recognize the difference of the dynamic characteristics of swirling and non-swirling flow. Comparing the liquid film thickness and pressure calculated by the proposed model under non-swirling flow with the commonly used correlations, the rationality of the new model is validated. Combined with the development of the interfacial disturbance wave and taking the KH instability into account, a calculation method for the effective distance of vortex tool is first derived. Once the effective distance of the first-stage vortex tool is determined, the installation position of the next-stage tool can be obtained, which lays the foundation for the determination of the optimal installation position of each vortex tool and the optimal total number of vortex tools. Taking well C45 as an example, the influences of helix angle and hub diameter of vortex tool on the liquid film thickness, pressure drop, and effective distance are investigated.

The presence of the vortex tool results in a decrease in the liquid film thickness and an increase in the pressure drop. But the liquid film thickness increases gradually as the helix angle and the hub diameter increase, and the pressure drop decreases as the helix angle increases. The effect of the helix angle on the liquid film thickness is more significant than the hub diameter, which has good agreement with the experimental results of Takeshima et al. and numerical results of Park et al.

The effective distance increases with an increase in the GLR. Within the scope of the study, the effective distance of the vortex tool is 2.97–10.36 m, approximately 48–167 pipe diameters, which is similar to the analysis results of the swirl intensity decay. However, an increase in the helix angle and hub diameter leads to a decrease in the effective distance. A sudden decrease occurs when the helix angle exceeds 60°.

The GLR and helix angle are more dominant factors than the hub diameter on the liquid film thickness, pressure drop, and effective distance. Therefore, priority should be given to the helix angle when designing vortex tools and the helix angle should not exceed 60°.

Footnotes

Appendix 1 Acknowledgements

The authors would like to appreciate the editors and reviewers for their helpful suggestions.

Handling Editor: Dumitru Baleanu

Declaration of conflicting interests

The author(s) declared no potential conflicts of interest with respect to the research, authorship, and/or publication of this article.

Funding

The author(s) disclosed receipt of the following financial support for the research, authorship, and/or publication of this article: This work was supported by the National Natural Science Foundation of China (grant no. 61572084) and the 13th Five-Year National Major Projects (grant no. 2016ZX05056004002).

ORCID iD

Zhao Zhang

References

Wells

Smith

Analysis of cementing turbulators. SPE Drill Eng1991; 6: 9–15.

Derakhshan

Riahi

Bashiri

Efficiency improvement of a rotary gas separator by parametric study and gas/liquid-flow analysis. SPE Prod Oper2017; 33: 320–335.

Simpson

Vortex flow technology finding new applications. Rocky Mt Oil J2003; 83: 40–45.

Yang

et al . A new technology of vortex dewatering gas recovery in gas wells and its application. Nat Gas Ind2012; 32: 63–66.

Ali

Scott

Fehn

Investigation of new tool to unload liquids from stripper-gas wells. SPE Prod Facil2005; 20: 306–316.

Kreith

Sonju

The decay of a turbulent swirl in a pipe. J Fluid Mech1965; 22: 257–271.

Liu

Bai

Swirl decay in the gas–liquid two-phase swirling flow inside a circular straight pipe. Exp Therm Fluid Sci2015; 68: 871–895.

Najafi

Mousavian

Amini

Numerical investigations on swirl intensity decay rate for turbulent swirling flow in a fixed pipe. Int J Mech Sci2011; 53: 801–811.

Murakami

Kito

Katayama

et al . An experimental study of swirling flow in pipes. Bull JSME1976; 19: 118–126.

10.

Rocha

Bannwart

Ganzarolli

Numerical and experimental study of an axially induced swirling pipe flow. Int J Heat Fluid Fl2015; 53: 81–90.

11.

Ahmadvand

Najafi

Shahidinejad

An experimental study and CFD analysis towards heat transfer and fluid flow characteristics of decaying swirl pipe flow generated by axial vanes. Meccanica2010; 45: 111–129.

12.

Ren

Zhang

et al . Pilot test of vortex-based water drainage gas recovery technology in Hubuzhai Gas Field. Petrol Eng Constr2016; 4: 58–61.

13.

Yang

Wei

Xiao

et al . Exploration and study of underground vortex tool drainage and gas production in Sulige gas field. Drill Prod Technol2013; 36: 125–127.

14.

Zhang

Jin

Wang

et al . Drainage gas recovery by downhole eddy current used for Sulige Gasfield. Nat Gas Technol Econ2012; 6: 45–48.

15.

Zhou

et al . Dynamic analysis of a liquid droplet and optimization of helical angle for vortex drainage gas recovery. Nat Gas Ind B2016; 3: 339–345.

16.

Chen

Yao

Han

et al . Effective length of vortex tools for liquid discharge in gas wells. Fault-Block Oil Gas Field2016; 23: 5375–5340.

17.

Shu

Luo

Design method for the space of spiral centralizers in Bingham plastic fluid. Acta Petrol Sin2017; 38: 461–467.

18.

Eibeck

Eaton

Heat transfer effects of a longitudinal vortex embedded in a turbulent boundary layer. J Heat Transf1987; 109: 16–24.

19.

Wang

Huang

Chen

et al . Numerical optimization of spacing between LVGs in narrow rectangular channel. J Eng Therm2009; 30: 135–137.

20.

Zhang

Fluid flow in rectangular helical channels with vortex generator. CIESC J2014; 65: 3838–3845.

21.

Hoffmann

Stein

Gas cyclones and swirl tubes: principles, design, and operation. 2nd ed.Berlin: Springer, pp. 318–326, 2007.

22.

Yang

Zhao

Wang

et al . Mean residence time of liquid phase in gas-liquid cyclone. CIESC J2015; 66: 4373–4379.

23.

Vieira

Parsi

Torres

et al . Experimental characterization of vertical gas–liquid pipe flow for annular and liquid loading conditions using dual wire-mesh sensor. Exp Therm Fluid Sci2015; 64: 81–93.

24.

Wallis

One dimensional two-phase flow. New York: McGraw-Hill, 1969.

25.

Gambill

Bundy

Wansbrough

Heat transfer, burnout, and pressure drop for water in swirl flow through tubes with internal twisted tapes (Report). Oak Ridge, TN: Oak Ridge National Laboratory, 1960.

26.

Lopina

Bergles

Heat transfer and pressure drop in tape-generated swirl flow of single-phase water. J Heat Transf1969; 91: 434–441.

27.

Jensen

Pourdashti

Bensler

Two-phase pressure drop with twisted-tape swirl generators. Int J Multiphas Flow1985; 11: 201–211.

28.

Ouyang

L-B

Aziz

. Development of new wall friction factor and interfacial friction factor correlations for gas-liquid stratified flow in wells and pipes. In: Proceedings of the western regional meeting, Anchorage, AL, 22–24 May 1996. Richardson, TX: Society of Petroleum Engineers.

29.

Chandrasekhar

Hydrodynamics and hydromagnetic stability. London: Oxford University, 1961.

30.

Berna

Escrivá

Muñoz-Cobo

et al . Review of droplet entrainment in annular flow: interfacial waves and onset of entrainment. Prog Nucl Energ2014; 74: 14–43.

31.

Marin

Baleanu

On vibrations in thermoelasticity without energy dissipation for micropolar bodies. Bound Value Probl2016; 2016: 111.

32.

Wang

Xue

et al . Destabilizing effect of density gradient on the Kelvin–Helmholtz instability. Phys Plasmas2009; 16: 112104.

33.

Kumar

Gottmann

Sridhar

Film thickness and wave velocity measurements in a vertical duct. J Fluids Eng2002; 124: 634–642.

34.

Sekoguchi

Takashi

Osamu

An investigation of the flow characteristics in the disturbance wave region of annular flow: 2nd report, on correlation of principal flow parameters. Transactions of the Japan Society of Mechanical Engineers B 1985; 51: 1798–1806.

35.

Sawant

Ishii

Hazuku

et al . Properties of disturbance waves in vertical annular two-phase flow. Nucl Eng Des2008; 238: 3528–3541.

36.

Pan

et al . Experimental study and modeling of disturbance wave height of vertical annular flow. Int J Heat Mass Tran2015; 89: 165–175.

37.

Han

Zhu

Gabriel

A study on the effect of gas flow rate on the wave characteristics in two-phase gas–liquid annular flow. Nucl Eng Des2006; 236: 2580–2588.

38.

Dranchuk

Purvis

Robinson

. Computer calculation of natural gas compressibility factors using the Standing and Katz correlation. In: Proceedings of the annual technical meeting, Edmonton, AB, Canada, 8–12 May 1973. Calgary, AB, Canada: Petroleum Society of Canada.

39.

Lee

Gonzalez

Eakin

The viscosity of natural gases. J Petrol Technol1966; 18: 997–1000.

40.

Tatterson

Dallman

Hanratty

Drop sizes in annular gas-liquid flows. AIChE J1977; 23: 68–76.

41.

Fukano

Furukawa

Prediction of the effects of liquid viscosity on interfacial shear stress and frictional pressure drop in vertical upward gas–liquid annular flow. Int J Multiphas Flow1998; 24: 587–603.

42.

Okawa

Kitahara

Yoshida

et al . New entrainment rate correlation in annular two-phase flow applicable to wide range of flow condition. Int J Heat Mass Tran2002; 45: 87–98.

43.

Takeshima

Fujii

Takenaka

et al . The flow characteristics of an upward gas-liquid two-phase flow in a vertical tube with a wire coil: part 1. Experimental results of flow pattern, void fraction, and pressure drop. Nihon Kikai Gakkai Ronbunshu B Hen2002; 31: 639–651.

44.

Park

Chang

Swirl flow analysis in a helical wire inserted tube using CFD code. Nucl Eng Des2010; 240: 3405–3412.

45.

Aziz

Govier

Pressure drop in wells producing oil and gas. J Can Petrol Technol1972; 11: 38–48.

46.

Hagedorn

Brown

Experimental study of pressure gradients occurring during continuous two-phase flow in small-diameter vertical conduits. J Petrol Technol1965; 17: 475–484.

47.

Duns

Jr Ros

. Vertical flow of gas and liquid mixtures in wells. In: Proceedings of the 6th world petroleum congress, Frankfurt am Main, 19–26 June 1963. London: World Petroleum Council.

48.

Mukherjee

Brill

Pressure drop correlations for inclined two-phase flow. J Energ Resour Tech1985; 107: 549–554.

49.

Beggs

Brill

A study of two-phase flow in inclined pipes. J Petrol Technol1973; 25: 607–617.

50.

Orkiszewski

Predicting two-phase pressure drops in vertical pipe. J Petrol Technol1967; 19: 829–838.

51.

Zhou

et al . Optimization of methods for liquid loading prediction in deep condensate gas wells. J Petrol Sci Eng2016; 146: 71–80.

Dynamics and effective distance of gas–liquid two-phase swirling flow induced by vortex tools

Abstract

Keywords

Introduction

Theoretical analysis of the swirling annular flow

Force balance analysis

Effective swirl distance of vortex tool

Results and discussions

Liquid film thickness

Pressure drop

Effective distance of vortex tool and influencing parameters analysis

Influence of the GLR on the effective distance

Influence of the helix angle and hub diameter on the effective distance

Conclusion

Footnotes

Appendix 1

Acknowledgements

Declaration of conflicting interests

Funding

ORCID iD

References