A New Production-Splitting Method for the Multi-Well-Monitor System

Zhang, Jiaqi; He, Chang; Yu, Jichen; Teng, Bailu; Luo, Wanjing; Liu, Xinfei

doi:10.3390/en13215677

Open AccessArticle

A New Production-Splitting Method for the Multi-Well-Monitor System

by

Jiaqi Zhang

¹,

Chang He

²,

Jichen Yu

²

,

Bailu Teng

^1,*

,

Wanjing Luo

¹

and

Xinfei Liu

¹

School of Energy Resources, China University of Geosciences (Beijing), Beijing 100083, China

²

Research Institute of Petroleum Exploration and Development, Beijing 100083, China

^*

Author to whom correspondence should be addressed.

Energies 2020, 13(21), 5677; https://doi.org/10.3390/en13215677

Submission received: 28 August 2020 / Revised: 28 October 2020 / Accepted: 28 October 2020 / Published: 30 October 2020

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Abstract

:

In order to reduce the cost of wellheads, the production rate of the gas wells in the Hechuan Gas Field are mostly measured in groups, which raises a stringent barrier for industries to determine the production rate of each single well. The technique for determining the production of a single well from the production of the well-group can be called the production splitting method (PSM). In this work, we proposed a novel PSM for the multi-well-monitor system (MWMS) on the basis of the Beggs and Brill (BB) correlation. This proposed method can account for the multi-phase flow together with the features of the pipelines. Specifically, we discretize the pipeline into small segments and recognize the flow pattern in each segment. The pressure drop along the pipeline is calculated with the Beggs and Brill correlation, and the production of each well is subsequently determined with a trial method. We also applied this proposed method to a field case, and the calculated results show that the results from this work undergo an excellent agreement with the field data.

Keywords:

production splitting method; multi-well-monitor system; multi-phase flow; Beggs and Brill correlation

Graphical Abstract

1. Introduction

In recent years, great progress has been made in gas exploitation in China [1,2]. The gas fields in China have increasingly replaced the single-well-monitor system (SWMS) with the multi-well-monitor system (MWMS) to reduce the wellhead costs. Figure 1 compares the schematic of the SWMS to that of the MWMS. As one can see in Figure 1a, the wells of the SWMS are equipped with a wellhead pressure gauge and wellhead flow meter, such that the wellhead pressure p_wellhead and the production rate q can be measured. However, the wells of the MWMS are only equipped with a wellhead pressure gauge. The production is transported to a gathering station where the total production rate q_t and the outlet pressure p_out are measured. Therefore, in an MWMS, the production rate of each single well is unknown. In practice, the production data of each single well plays an important role for one to estimate the ultimate recovery and optimize the production strategy. Hence, it is crucial for the industries to split the production of the MWMS.

Generally, in the absence of the production data of a single well, several models can be established to calculate the production. For instance, the inflow performance relationship and hydraulic lifting curves [3,4,5,6,7], reservoir response model, or tailored reservoir model [8,9,10], and the temperature–pressure models [11,12] can be used to calculate the production rate of a single well. However, the above models could not consider the constraint of the production of a multi-well-monitor system. Therefore, these models are not a real sense of the splitting method and are inapplicable to split the production of the MWMS. At present, the studies of splitting the production of the MWMS are still far from adequate. Only a few methods are reported in the existing literature. Kappos et al. proposed a production splitting method (PSM) for the surface pipe network system on the basis of a choke equation [13]. However, their method requires the system being equipped with throttles, which hinders its application in real field cases. Hamad et al. and Abdelmoula et al. introduced an empirical PSM with the aid of a second-grade polynomial equation [14,15]. In order to obtain accurate results for splitting the production, one needs to update the coefficients of their empirical equation for each specific reservoir. However, in practice, the production data are frequently not available for one to generate such empirical equations. In addition, one can also split the production of the MWMS with commercial software (PIPESIM). PIPESIM can split the production by assuming that the properties of the fluid are uniform from different wells. However, in practice, the wells of the MWMS can be drilled in different regions or different layers and the properties of the fluids of different wells can be very different, rendering PIPESIM inapplicable. According to the aforementioned argument, one can find that splitting the production of the MWMS is important to predict the recovery and optimize the production. However, the existing methods bear different deficiencies in real applications. It is imperative for us to develop an inclusive method to split the production of the MWMS. In this work, the author proposed a new method to split the production of the MWMS. In comparison to the existing methods, this proposed method does not require the industries installing extra equipment and can consider the different properties of the fluid from different production wells.

2. Methodology

2.1. Physical Model and Assumptions

Figure 2 illustrates a simplified MWMS with two pipelines. In this figure, p represents pressure (psi), L represents the length of the pipeline (ft), the subscript “1” and “2” represent the first and the second pipeline, the subscript “g” and “l” represent the gas phase and liquid phase, respectively. p₁, p₂, and p_out represent the wellhead pressure of well₁, well₂, and the outlet. q_gt and q_lt represent the total gas and liquid flow rate (scf/d, cubic ft/d). As we have introduced in Section 1, the values of L₁, L₂, p₁, p₂, p_out, q_gt, and q_lt are known, and the values of q_g₁, q_l₁, q_g₂, and q_l₂ are the unknowns.

In order to develop the method for splitting the production of the MWMS, we made the following assumptions:

The appearance of a curved section along the pipeline will not induce extra pressure drop;
The temperature along the pipeline is linearly decreased from T_wellhead at the wellhead to T_out at the outlet;
The pipelines have the same properties, and these properties remain unchanged through the calculation.

2.2. Framework of the Proposed Method

In this section, we will take a two-well-monitor-system, as shown in Figure 2, as an example to illustrate the calculating process for splitting the production. This method is developed with a trial algorithm. The detailed introduction of the proposed method is as follows:

Dividing the total gas flow rate into n_g gas flow rates that have the same interval. The minimum gas flow rate is 0 and the maximum gas flow rate is q_gt. In a similar way, dividing the total water flow rate into n_w water flow rates. Arranging these n_g gas flow rates and n_w water flow rates into n_g × n_w flow rate pairs;
Assuming that the gas flow rate of the first pipe is q_g₁ (scf/d) and the water flow rate of the first pipe is q_w₁ (cubic ft/d) (q_g₁ is one of the n_g gas flow rates and q_w₁ is one of the n_w water flow rates). According to the theory of mass balance, the gas flow rate and water flow rate of the second pipe can be calculated with:

$q_{g 2} = q_{g t} - q_{g 1} .$

(1)

$q_{w 2} = q_{w t} - q_{w 1} .$

(2)
Calculating the pressure loss along the two pipes with the gas and water flow rate. The detailed process for calculating the pressure loss along a pipe will be introduced in the next section;
Calculating the pressure loss along the two pipes with all the n_g × n_w pairs of flow rate, such that we can obtain n_g × n_w pressure loss of the two pipes;
Graphing the pressure loss of the two pipes with these flow rate pairs in 3D graphs, as shown in Figure 3. Figure 3a,b shows the pressure loss graphs of the first pipe and the second pipe, respectively. In Figure 3a,b, the x-axis represents the gas flow rate of the first pipe q_g₁, the y-axis represents the water flow rate of the first pipe q_w₁, and the z-axis represents the pressure loss ∆p;
Since the pressure losses of the two pipes are known, we can obtain all the possible values of q_g₁ and q_w₁ that can induce such pressure loss by intersecting the planes of z = ∆p₁ and z = ∆p₂ with the pressure-loss planes shown in Figure 3, as shown in Figure 4. The lines that are induced by the intersection represent all the possible values of q_g₁ and q_w₁;
Figure 5a,b shows the x–y plane view of the possible-value lines of the two pipes, as shown in Figure 4. It should be noted that a reasonable value of q_g₁ and q_w₁ should ensure that the pressure loss of the first pipe equals to ∆p₁ and the pressure loss of the second pipe equals to ∆p₂. For example, (q_gi, q_wi) indicates a point on the intersection line in Figure 5a but not on the intersection line in Figure 5b. This indicates that flow rate pair (q_gi, q_wi) can lead to a pressure loss of ∆p₁ for the first pipe, but it cannot lead to a pressure loss of ∆p₂ for the second pipe. Therefore, this flow rate pair is not reasonable. The reasonable flow rate pairs can be found by intersecting the possible-value line in Figure 5a and the possible-value line in Figure 5b, as shown in Figure 5c;
The intersections in Figure 5c indicate the two reasonable flow rate pairs that can lead to a pressure loss of ∆p₁ for the first pipe and a pressure loss of ∆p₂ for the second pipe. One can figure out the real flow rate pair from these two reasonable flow rate pairs on the basis of the development strategy and reservoir properties. For example, if the first pipe is connected to a reservoir/layer that has a higher initial water saturation than that of the second pipe, the water flow rate of the first pipe can be higher than that of the second pipe. Hence, one can think that the flow rate pair b (x₂, y₂) in Figure 5c is the real flow rate pair of the first pipe. Additionally, the flow rate of the second pipe is q_gt-x₂ and q_wt-y₂.

2.3. Method of Calculating the Pressure Loss along a Pipeline

The multiphase flow in pipelines can illustrate different flow patterns with different flow velocity, which makes it complicated to calculate the pressure loss along the pipeline. One of the most commonly used methods to calculate the pressure change along the pipes accounting for the different flow patterns is the Beggs and Brill (BB) correlation. In the BB correlation, the fluid flow is divided into three patterns, including segregated flow, intermittent flow, and distributed flow [16]:

Segregated flow: the segregated flow is a flow regime in a pipeline where the different phases of fluid are segregated, as shown in Figure 6a. Specifically, the segregated flow includes three sub-patterns, namely stratified flow, wavy flow, and annular flow;

Intermittent flow: if the gas–liquid ratio is sufficiently high, the gas phase will be observed in the form of plugs or slugs, as shown in Figure 6b, and the intermittent flow contains the sub-patterns of plug flow and slug flow;

Distributed flow: the distributed flow contains bubble flow and mist flow, as shown in Figure 6c. The bubble flow happens to the scenarios of a low gas–liquid ratio, and the mist flow happens to the scenarios of a high gas–liquid ratio.

In addition, since the properties of the fluid and the flow pattern are highly dependent on the pressure and temperature, both the properties of the fluid and the flow pattern will be changed along the pipe as the pressure and temperature are changed along the pipe. In practice, all the flow patterns can be observed in the real field cases under different conditions of pressure and temperature. In order to characterize the varied flow pattern and the varied fluid properties, we need to discretize the pipe into small segments. Figure 7 shows the schematic of a discretized pipe. As shown in this figure, the fluid flows into the pipe through the inlet surface and flows out of the pipe through the outlet surface.

Figure 8 shows the detailed process of calculating the pressure loss in a discretized pipe. The flow properties and pressure loss in the pipeline are calculated iteratively:

Making an initial guess of the pressure of the 1st pipe segment. For example, one can use the pressure at the inlet surface as the initial guessed pressure of the 1st segment. Calculating the properties of the fluid with the guessed pressure by use of the equations in Appendix A;
On the basis of the BB correlation, identifying the flow pattern in the 1st pipe segment and calculating the new pressure within the 1st pipe segment. The introduction of the BB correlation can be found in Appendix B;
Using the calculated pressure to update the fluid properties and flow pattern in the 1st pipe segment and calculating the pressure of the 1st pipe segment with the BB correlation;
If the difference between the new calculated pressure and the old calculated pressure is smaller than a certain threshold value, one can think that the new calculated pressure is the real pressure of the 1st pipe segment; otherwise, updating the fluid properties with the new calculated pressure and repeating the calculating. In this work, if the absolute value of the relative difference between the new pressure and the old pressure is smaller than 0.0001, we think the new calculated pressure is the real pressure;
Calculating the pressure of the next pipe segment with a similar method that is introduced in Steps 1 through 4. For the nth segment, one can use the pressure of the (n − 1)th segment as the initial guess.

3. Validation of the Proposed Method

In this section, we applied this proposed method to an MWMS in the Hechuan Gas Field in China. The gas production Wells X1 and X2 are in the same well group, and the production of these two wells are transmitted with two separate pipes. The properties of the pipes and the schematic of the MWMS are shown in Table 1 and Figure 9.

Figure 10 shows the gas production rate of Well X1, X2, and well group of 30 days, as shown in Figure 10a, and the water production rate of X1, X2, and well group of 30 days, as shown in Figure 10b. Figure 11 presents the wellhead pressure of these two wells, as well as the outlet pressure of 30 days. Therefore, we can split the production of these two wells with the proposed method by use of the total gas and water production rate together with the wellhead pressure and outlet pressure. Subsequently, this proposed method can be validated by comparing the calculated results to the real measured data. In order to conduct a more thorough comparison, we also use the commercial software PIPESIM to split the production.

As introduced in Section 2, we calculated all the possible production rates with the trial algorithm and obtained the two reasonable production rate pairs by intersecting the possible-value lines of Well X1 and that of Well X2. Figure 12 shows the possible-value lines of Well X1, X2, and their intersections of the first five days. The reasonable production rate pairs of the other 25 days can be obtained with the same method.

Table 2 summarizes the values of the reservoir parameters of Well X1 and X2. As one can see in Table 2, the porosity, initial gas saturation, and reservoir thickness of the reservoir of Well X2 are all higher than those of Well X1. Therefore, one can infer that the gas production rate of Well X2 can be higher than that of Well X1. With such a constrained condition, the right production rate pair can be identified from the two reasonable production rate pairs. For example, as one can see in Figure 12a, there are two reasonable production rate pairs of Well X1, c (4,880,263.98 scf/d, 56.54 cubic ft/d), and d (9,400,381.81 scf/d, 33.95 cubic ft/d) in the first day. Therefore, the reasonable production rate pairs of Well X2 are (8,016,020.03 scf/d, 26.02 cubic ft/d) and (3,495,902.20 scf/d, 48.61 cubic ft/d). Finally, we chose the first production rate pair c as the real production rate pair of Well X1.

Figure 13 demonstrates the calculated results from this proposed method, the calculated results from PIPESIM, and the real field data. Figure 13a,b shows the gas production and water production of the two wells, respectively. As one can see in Figure 13, that although both the results from the proposed method and those from PIPESIM undergo good agreement with the real field data for splitting the gas production, as shown in Figure 13a, this proposed method exhibits a better performance than PIPESIM for splitting the water production, as shown in Figure 13b.

Figure 14 compares the relative errors re of this proposed method to those of PIPESIM. The relative error is defined as

r e = \frac{| q_{c a l c u l a t e d} - q_{r e a l} |}{q_{r e a l}} \times 100 % .

(3)

The relative errors of the gas and water production rate of the 30 days are shown in Figure 14a,b. As one can see in Figure 14, the relative error induced by the proposed method is less than that induced by PIPESIM. The average relative errors of the gas production rate calculated by the proposed method and PIPESIM are 6.59% and 15.79%, respectively. The average relative errors of the water production rate calculated by the proposed method and PIPESIM are 5.39% and 50.56%, respectively. The results shown in Figure 13 and Figure 14 indicate that this proposed method is reliable for splitting the production of the MWMS.

4. Sensitivity Analysis

In this section, we conducted a study of the effects of different influencing factors on the calculation outputs. These influencing factors include the inner diameter of the pipes, the absolute roughness of the inner wall of the pipes, and the pressure loss along the two pipes. Since only three influencing factors are examined in this work, the computation load is not heavy, and the computation can be completed in a few seconds. In practice, if more influencing factors are required to be investigated and the computation load is heavy, one can use the software framework that is developed by Vu-Bac et al. [17] to conduct the sensitivity analysis. The benchmark values of the properties of the pipes and the pressure are the same as those used in Section 3.

4.1. The Inner Diameter of Pipes

Figure 15 shows the effect of the inner diameter of the second pipe on the results of production splitting. In Figure 15, the inner diameter of the second pipe is varied from 0.195 ft to 0.202 ft. As one can see in Figure 15, as the inner diameter of the second pipe is increased, the gas production of the second pipe is decreased, while the water production of the second pipe is increased. This can be explained as follows. The gas production of the two wells is significantly higher than the water production rate and the pressure loss along the pipes is mainly induced by the gas flow. Compared with the pressure loss that is induced by the gas flow, the pressure loss that is induced by the water flow is very small. Increasing the inner diameter of a pipe while leaving the flow rate unchanged will reduce the difference between the pressure of the inlet surface and that of the outlet surface, whereas increasing the inner diameter of a pipe while leaving the pressure difference unchanged will reduce the gas flow rate. In Figure 15, the pressure difference remains unchanged during the computation; hence, the gas flow rate is decreased while the water flow rate is increased as the inner diameter of the second pipe is increased.

4.2. The Absolute Roughness of Pipes

Figure 16 shows the split gas and water production rates under different absolute roughness of pipes. It can be observed in Figure 16, as the absolute roughness of the pipe is varied from 10⁻⁴ ft to 10 ft, the gas production and the water production of the two wells show negligible change. This indicates that the absolute roughness of the pipe can slightly influence the results of the production splitting.

4.3. The Pressure Loss of Pipes

Figure 17 shows the gas and water production rates of the two wells with a different pressure loss of the second pipe. As we have stated in Section 4.1, the pressure loss is mainly caused by the gas flow, and a larger pressure loss indicates a higher gas flow rate of the pipe. Therefore, in Figure 17 we can find that the gas flow rate is increased, while the water flow rate is decreased as the pressure loss of the second pipe is increased.

5. Conclusion

In this work, the authors proposed a new method to split the production of the MWMS. This method is constructed on the basis of a trial method and the BB correlation. In order to accurately characterize the flow patterns and the fluid properties along the pipeline, we discretized the pipeline into small segments and identified the flow pattern within each small segment. In comparison to the existing methods for splitting the production, this proposed method does not necessitate installing measuring equipment and can consider the different properties of the fluid from different wells. However, this method can induce multiple reasonable solutions, and one needs to recognize the real solution from the multiple solutions based on the field data. This proposed method was validated against field monitored data. The calculated results from this proposed method show excellent agreement with those of the field data, indicating that this proposed method is reliable to split the production of the MWMS. Besides, we also compared the results from this proposed method to those from commercial software PIPESIM, and the results show that this proposed method can yield more accurate results for splitting the production.

Author Contributions

Conceptualization, J.Z. and C.H.; methodology, B.T.; software, X.L. and C.H.; validation, W.L.; formal analysis, B.T.; investigation, J.Y.; resources, W.L.; data curation, J.Z.; writing—original draft preparation, J.Z.; writing—review and editing, B.T.; visualization, J.Z.; supervision, J.Y.; funding acquisition, W.L. All authors have read and agreed to the published version of the manuscript.

Funding

This research was funded by National Natural Science Foundation of China, grant number 51674227.

Acknowledgments

The authors would like to thank National Natural Science Foundation of China for the support and promotion.

Conflicts of Interest

The authors declare no conflict of interest. The funders had no role in the design of the study; in the collection, analyses, or interpretation of data; in the writing of the manuscript, or in the decision to publish the results.

Appendix A

The pseudocritical pressure and temperature can be calculated with the following equations [18]:

p_{p c} = 756.8 - 131.07 γ_{g} - 3.6 γ_{g}^{2},

(A1)

T_{p c} = 169.2 + 349.5 γ_{g} - 74.0 γ_{g}^{2},

(A2)

where p_pc is the pseudocritical pressure of gas (psi), T_pc is the pseudocritical temperature of gas (°R), and γ_g is the specific gravity for gas.

Using the obtained pseudocritical pressure and temperature, the reduced pressure p_r, temperature T_r, and dimensionless density of gas ρ_r can be calculated [18]:

p_{r} = \frac{p}{p_{p c}},

(A3)

T_{r} = \frac{T}{T_{p c}},

(A4)

ρ_{r} = \frac{0.27 p_{r}}{z T_{r}},

(A5)

where T is temperature (°R), p is pressure (psi).

The gas formation volume factor B_g can be calculated using the real gas equation:

B_{g} = \frac{p_{s c} z T}{T_{s c} p},

(A6)

where p_sc is pressure at standard conditions (psi) and T_sc is temperature at standard conditions (°R).

Using the Dranchuk and Abou-Kassem equation [19], which is based on the generalized Starling equation of state to calculate the gas-deviation factor z:

\begin{array}{l} z = 1 + (A_{1} + \frac{A_{2}}{T_{r}} + \frac{A_{3}}{T_{r}^{3}} + \frac{A_{4}}{T_{r}^{4}} + \frac{A_{5}}{T_{r}^{5}}) ρ_{r} + (A_{6} + \frac{A_{7}}{T_{r}} + \frac{A_{8}}{T_{r}^{2}}) ρ_{r}^{2} \\ - A_{9} (\frac{A_{7}}{T_{r}} + \frac{A_{8}}{T_{r}^{2}}) ρ_{r}^{5} + A_{10} (1 + A_{11} ρ_{r}^{2}) (\frac{ρ_{r}^{2}}{T_{r}^{3}}) \exp (- A_{11} ρ_{r}^{2}), \end{array}

(A7)

where the values of constants A₁ through A₁₁ are shown in Table A1.

Table A1. Values of the constants.

Constants	Value
A₁	0.3265
A₂	−1.0700
A₃	−0.5339
A₄	0.01569
A₅	−0.05165
A₆	0.5475
A₇	−0.7361
A₈	0.1844
A₉	0.1056
A₁₀	0.6134
A₁₁	0.7210

Using the following equations [20] to calculate the viscosity of gas μ_g (cp):

μ_{g} = K_{1} \exp (X ρ^{Y}),

(A8)

where

ρ = \frac{p M_{g}}{z R T} = 0.00149406 \frac{p M_{g}}{z T},

(A9)

K_{1} = \frac{(0.00094 + 2 \times 10^{- 6} M_{g}) T^{1.5}}{(209 + 19 M_{g} + T)},

(A10)

X = 3.5 + \frac{986}{T} + 0.01 M_{g},

(A11)

Y = 2.4 - 0.2 X,

(A12)

where ρ is gas density (g/cm³), K₁ is parameter (cp), and M_g is average molecular weight of gas.

Appendix B

The Bernoulli equation characterizes the fluid flows in pipelines by considering the effects of kinetic pressure loss, hydrostatic pressure loss, and frictional pressure loss. Since the kinetic loss is normally much smaller than the hydrostatic loss and friction loss, the kinetic loss can be neglected, and the Bernoulli equation can be simplified as

∆ p_{T} = ∆ p_{H} + ∆ p_{f},

(A13)

where ∆p_T is total pressure loss (psi), ∆p_H is hydrostatic pressure loss (psi), and ∆p_f is friction pressure loss (psi). The parameters used for characterizing the multi-phase flow are given as follows:

q_{l} = q_{w} B_{w},

(A14)

V_{s l} = \frac{q_{l}}{\frac{π}{4} D^{2}},

(A15)

V_{s g} = \frac{q_{g} B_{g}}{\frac{π}{4} D^{2}},

(A16)

V_{m} = V_{s l} + V_{s g},

(A17)

where q_l is the flow rate of liquid-phase (ft³/d), q_w is the flow rate of water (ft³/d), q_g is the flow rate of gas (ft³/d), B_w is the water volume factor, B_g is the gas volume factor, V_sl is the superficial velocity of liquid (ft/d), V_sg is the superficial velocity of gas (ft/d), V_m is the superficial velocity of mixture (ft/d), and D is the diameter of pipe (ft). It is worth noting that the formation volume factor B_w and B_g indicate the ratio of the fluid volume in the pipe to the fluid volume of the standard condition.

Figure A1 shows the schematic of multiphase flow in a pipe. Due to the change of the pressure, the gas phase will be compressed or expanded along the pipeline, leading to a variation of the volume fraction of the gas phase at different cross-sections of the pipelines. Liquid holdup E_l refers to the proportion of the liquid phase’s cross-sectional area A_l (ft²) in the total cross-sectional area A_P (ft²) during the water–gas two-phase flow. E_l can be defined as follows:

E_{l} = \frac{A_{l}}{A_{P}} .

(A18)

If the slippage effect is neglected, no-slip holdup C_l can be obtained:

C_{l} = \frac{q_{l}}{q_{l} + q_{g} B_{g}} .

(A19)

In this work, we used the Beggs and Brill (BB) correlation to calculate the pressure loss along the pipelines. The BB correlation is applicable to the wells with arbitrary inclinations and can account for the change of flow pattern. In the BB correlation, the flow patterns are summarized into three groups of flow, including segregated flow (including stratified, wavy, and annular flow), intermittent flow (including plug and slug flow), and distributed flow (including bubble and mist flow). Before calculating the pressure loss with the BB correlation, the flow pattern is required to be recognized if the values of no-slip holdup C_l and Froude number F_rm are known prior. The Froude number F_rm is defined as [16]

F_{r m} = \frac{V_{m}^{2}}{g D} .

(A20)

The boundaries between these groups of flow patterns appear as curves in a log-log plot in the original publication by Beggs and Brill. Beggs and Brill (1973) fitted the boundary lines in a log-log plot in order to facilitate the process of determining the flow patterns, which can be summarized as follows.

Figure A1. Schematic of multiphase flow in a pipe.

If F_rm < L₁*, the flow pattern falls within the segregated flow, if F_rm > L₁* and F_rm > L₂*, the flow pattern falls within the distributed flow, if L₁* < F_rm < L₂*, the flow pattern falls within the intermittent flow. L₁* and L₂* are given by:

L_{1}^{*} = \exp (- 4.62 - 3.757 X - 0.481 X^{2} - 0.0207 X^{3}),

(A21)

L_{2}^{*} = \exp (1.061 - 4.602 X - 1.609 X^{2} - 0.179 X^{3} + 0.635 \times 10^{- 3} X^{5}),

(A22)

where

X = \ln (C_{l}) .

(A23)

Once the flow pattern is determined, the liquid holdup E_l can be calculated. The liquid holdup E_l in the BB correlation contains two parts, including a liquid holdup of horizontal flow E_l(0) and a correction coefficient that accounts for the inclination angle. The value of the horizontal liquid holdup E_l(0) should not be less than the value of the no-slip holdup C_l. In the case of E_l(0) < C_l, one can set E_l(0) = C_l.

If the flow pattern falls within the segregated flow. In such cases, one can have [16]:

E_{l} (0) = \frac{0.98 C_{l}^{0.4846}}{F_{r m}^{0.0868}} .

(A24)

In addition, if the flow pattern is intermittent flow:

E_{l} (0) = \frac{0.845 C_{l}^{0.5351}}{F_{r m}^{0.0173}} .

(A25)

If the flow pattern is dispersed flow:

E_{l} (0) = \frac{1.065 C_{l}^{0.5824}}{F_{r m}^{0.0609}} .

(A26)

Once the flow pattern is determined and the horizontal liquid holdup E_l(0) is obtained, the real liquid holdup E_l that considers the inclination angle can be calculated with a correction coefficient B(θ):

E_{l} = B (θ) E_{l} (0),

(A27)

where

B (θ) = β [\sin (1.8 θ) - \frac{1}{3} \sin^{3} (1.8 θ)],

(A28)

where β is a function that is dependent on the flow pattern as well as the flow direction of the fluid.

If the flow direction is uphill, for segregated flow, we can have:

β = (1 - C_{l}) \ln [\frac{0.011 N_{L v}^{3.539}}{C_{l}^{3.768} F_{r m}^{1.614}}],

(A29)

for intermittent flow:

β = (1 - C_{l}) \ln [\frac{2.96 C l^{0.305} F_{r m}^{0.0978}}{N_{L v}^{0.4473}}],

(A30)

for distributed flow:

β = 0 .

(A31)

If the flow direction is downhill flow (all flow patterns), we can have:

β = (1 - C_{l}) \ln [\frac{2.96 C l^{0.305} F_{r m}^{0.0978}}{N_{L v}^{0.4473}}],

(A32)

for all flow patterns, where N_Lv is the liquid velocity number, which is defined as

N_{L v} = 1.938 V_{s l} \sqrt[4]{\frac{ρ_{l}}{σ}} .

(A33)

where σ is liquid surface tension and ρ_l is liquid density.

With the aid of Equations (A24) through (A33), the real liquid holdup E_l can be obtained. The density ρ_m (lb/ft³) and the viscosity μ_m (cp) of the mixture in the pipeline can be calculated with:

ρ_{m} = ρ_{l} E_{l} + ρ_{g} E_{g} = ρ_{l} E_{l} + ρ_{g} (1 - E_{l}),

(A34)

μ_{m} = μ_{l} E_{l} + μ_{g} E_{g} = μ_{l} E_{l} + μ_{g} (1 - E_{l}) .

(A35)

The hydrostatic pressure loss ∆p_H (psi) that is caused by the gravity can be calculated with:

∆ p_{H} = \frac{ρ_{m} g}{144 g_{c}} L \cdot \sin θ,

(A36)

where g_c is the gravitational constant, and θ is the inclination angle with respect to the horizontal direction. For example, for the vertical direction θ = 90°, and for horizontal direction θ = 0°.

The pressure loss ∆p_f (psi) that is caused by the friction can be calculated with:

∆ p_{f} = \frac{2 f_{t p} V_{m}^{2} ρ_{N S} L}{144 g_{c} D} .

(A37)

In Equation (A37), f_tp and ρ_NS (lb/ft³) are the two-phase friction coefficient and no-slip density, respectively. f_tp and ρ_NS are defined as follows:

f_{t p} = f_{N S} e^{s},

(A38)

ρ_{N S} = ρ_{l} C_{l} + ρ_{g} C_{g} = ρ_{l} C_{l} + ρ_{g} (1 - C_{l}),

(A39)

where

f_{N S} = {[2 \log (\frac{N_{R e n s}}{4.5223 \log N_{R e n s} - 3.8215})]}^{- 2},

(A40)

N_{R e n s} = \frac{[ρ_{l} C_{l} + ρ_{g} (1 - C_{l})] V_{m} D}{μ_{l} C_{l} + μ_{g} (1 - C_{l})},

(A41)

S = \frac{\ln y}{- 0.0523 + 3.182 {(\ln y)}^{2} + 0.01853 {(\ln y)}^{4}},

(A42)

y = \frac{C_{l}}{E_{l}^{2}} .

(A43)

If the fluid composition in the pipe is known, using Equations (A19) through (A23) can determine the flow pattern of fluid. Subsequently, one can calculate the pressure loss that is induced by gravity and friction with Equations (A24) through (A43).

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Figure 1. The schematics of the (a) single-well-monitor system (SWMS) and (b) multi-well-monitor system (MWMS).

Figure 2. Simplified model of an MWMS with two pipelines.

Figure 3. The pressure loss of the two pipes with different flow rate pairs: (a) the first pipe; (b) the second pipe.

Figure 4. Intersection between the planes of z = ∆p₁ and z = ∆p₂ and the pressure-loss planes: (a) the first pipe; (b) the second pipe.

Figure 5. Obtaining the reasonable flow rate pairs by intersecting the two intersection lines: (a) the x−y plane view of the possible-value lines of the first pipe; (b) the x−y plane view of the possible-value lines of the second pipe; (c) the reasonable flow rate pairs.

Figure 6. Schematics of different flow patterns: (a) segregated flow; (b) intermittent flow; (c) distributed flow.

Figure 7. Schematic of a discretized pipe.

Figure 8. Flow chart of the process for calculating the pressure of a discretized pipe.

Figure 9. Schematic of an MWMS and the pipes.

Figure 10. The (a) daily gas production data and (b) daily water production data of the well group for 30 days.

Figure 11. The outlet pressure and the wellhead pressure of these two wells of the 30 days.

Figure 12. Obtaining the reasonable flow rate pairs of the first 5 days: (a) 1st day; (b) 2nd day; (c) 3rd day; (d) 4th day; (e) 5th day.

Figure 13. Comparison between the results of the proposed method, the results from PIPESIM, and the real field data: (a) comparison of the gas production data; and (b) comparison of the water production data.

Figure 14. The relative errors of this proposed method and those of PIPESIM: (a) relative error of gas production rate; (b) relative error of water production rate.

Figure 15. Calculation results under different inner diameter of pipes: (a) gas production rate; (b) water production rate.

Figure 16. Calculation results under different absolute roughness of pipes: (a) gas production rate; (b) water production rate.

Figure 17. Calculation results under different pressure loss combinations: (a) gas production rate; (b) water production rate.

Table 1. The properties of the pipes and the measured data.

Parameters	Value	Parameters	Value
Pipeline length of X1	32.81 ft	Pipeline length of X2	39.37 ft
Inner diameter of X1	0.2 ft	Inner diameter of X2	0.2 ft
Pipeline gradient of X1	Downhill	Pipeline gradient of X2	Downhill
Absolute roughness of X1	0.00015 ft	Absolute roughness of X2	0.00015 ft

Table 2. Values of reservoir parameters of Well X1 and Well X2.

Parameter Name	Well X1	Well X2
Reservoir thickness h	16.4 ft	22.17 ft
Reservoir porosity ϕ	0.12	0.32
Reservoir gas saturation S_g	0.52	0.57

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Zhang, J.; He, C.; Yu, J.; Teng, B.; Luo, W.; Liu, X. A New Production-Splitting Method for the Multi-Well-Monitor System. Energies 2020, 13, 5677. https://doi.org/10.3390/en13215677

AMA Style

Zhang J, He C, Yu J, Teng B, Luo W, Liu X. A New Production-Splitting Method for the Multi-Well-Monitor System. Energies. 2020; 13(21):5677. https://doi.org/10.3390/en13215677

Chicago/Turabian Style

Zhang, Jiaqi, Chang He, Jichen Yu, Bailu Teng, Wanjing Luo, and Xinfei Liu. 2020. "A New Production-Splitting Method for the Multi-Well-Monitor System" Energies 13, no. 21: 5677. https://doi.org/10.3390/en13215677

APA Style

Zhang, J., He, C., Yu, J., Teng, B., Luo, W., & Liu, X. (2020). A New Production-Splitting Method for the Multi-Well-Monitor System. Energies, 13(21), 5677. https://doi.org/10.3390/en13215677

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A New Production-Splitting Method for the Multi-Well-Monitor System

Abstract

1. Introduction

2. Methodology

2.1. Physical Model and Assumptions

2.2. Framework of the Proposed Method

2.3. Method of Calculating the Pressure Loss along a Pipeline

3. Validation of the Proposed Method

4. Sensitivity Analysis

4.1. The Inner Diameter of Pipes

4.2. The Absolute Roughness of Pipes

4.3. The Pressure Loss of Pipes

5. Conclusion

Author Contributions

Funding

Acknowledgments

Conflicts of Interest

Appendix A

Appendix B

References

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