# Numerical Study of Single Well Vapor Extraction Process

Authors: Milad Rahnema; Hamed Rahnema; Marcia D. Mcmillan; Ali Reza Edrisi; Hamid Rahnema
Journal: Journal of Petroleum Engineering
 (2016)

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## Abstract

Vapor extraction (Vapex) is an emerging technology to produce heavy oil and bitumen from subsurface formations. Single well (SW) Vapex technique uses the same concept of Vapex process but only with one horizontal well. In this process solvent is injected from the toe of the horizontal well with oil production at the heel section. The main advantage of SW-Vapex process lies in the economic saving and applicability in problematic reservoirs, where drilling of two horizontal wells is impractical. The performance of SW-Vapex seems to be comparable with dual horizontal Vapex process using proper optimization schemes. This study is grouped into two sections: (i) a screening study of early time operating performance of SW-Vapex and (ii) a sensitivity analysis of the effect of the reservoir and well completion parameters. Simulation results show that solvent injection rate can be optimized to improve oil production rate. Higher injection rates may not necessarily lead to increase in production. This study confirms that SW-Vapex process is very ineffective in reservoirs with high oil viscosity (more than 1,500 cp) and thin formations (less than 10 m).


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## Body

## 1. Introduction

Heavy oil and bitumen reserves represent a considerable portion of worldwide energy resources. It is estimated that these reservoirs contain six trillion barrels of STOOIP which is much higher than the total conventional oil reservoirs. Significant consumption of light oil reserves and therefore their dramatic decline encourage more interest in the exploitation of highly viscous oil and bitumen for future energy demands. For the optimum conditions, the primary recovery of these reservoirs would not exceed 10 percent of the STOOIP. Most of these heavy oil and bitumen deposits are located in Canada, Venezuela, China, and Indonesia. Production from these reservoirs is challenging and technically difficult. Recently, vapor extraction process (Vapex) is introduced as an attractive method for such viscous oil reservoirs [1, 2].In a reservoir where oil is very viscous and cannot flow in reservoir condition, adding of vaporized hydrocarbon solvents (HCS) can drastically reduce oil viscosity. This concept is the fundamental of Vapex. In a conventional Vapex approach, the solvent is injected into a horizontal well located directly above a horizontal producer. As the solvent diffuses and dissolves in the bulk of the reservoir, a chamber of solvent vapor grows around the injection well and helps the gravity drainage of diluted oil toward the production well, from where it is pumped out to the surface.Depending on reservoir condition, several other well configurations are also possible. Butler and Jiang [3] conducted a series of experiments to study the effect of different well configurations on the performance of the Vapex in a homogeneous laboratory model. They found that the performance of process with producer and injector located in the same depth with horizontal separation was as well as conventional Vapex well configuration. Proper selection of well configuration is desirable to control the initial displacement and the profile of vapor chamber in the formation. Yazdani and Maini [4–6] carried out an extensive experimental study using 2D laboratory model to investigate the effect of porous media permeability and effective drainage height on the performance of the Vapex process. Later, Rezaei et al. [7] showed that, unlike SAGD process, the oil-wet condition of the formation positively impacts the oil production rate. To improve the economic viability of Vapex process, Torabi et al. [8–10] suggested injecting the noncondensable gases like CO2 with a hydrocarbon solvent. Using numerical simulation they found out that CH4 or CO2 coinjection is a viable option and results in equal or greater recovery factors in most cases.In single well (SW) Vapex a horizontal well is completed such that it plays the role of both injector and producer. The similar well configuration has been studied for SAGD process [11–13]. In this well setting, the performance of horizontal well section plays a major role in the overall success of the process. A significant body of work has been done on injected fluid distribution along the horizontal section [14–17]. For single well Vapex process, vaporized solvent is injected at the toe of the well, while diluted oil is produced at the heel of the well. Since the vapor chamber grows over a majority of the reservoir, it is expected that only early time production for SW-Vapex varies from conventional approach, and the late-time production results are similar. The main advantages of SW-Vapex are cost saving and its applicability in problematic reservoirs where drilling of two horizontal wells is impractical. However, the process requires more comprehensive study to evaluate its feasibility.Vapex process has been extensively studied using laboratory experiments. The main limitation is the low oil production compared to other thermal recovery processes [1, 3, 18, 19]. Viscosity reduction mechanism in Vapex is based on mass diffusion process which is lower than thermal diffusion by orders of magnitudes which cause significant lower oil dilation and consequently lower oil production rate [20]. Also limited oil-solvent contact area causes another issue that makes this process very sensitive to the formation heterogeneities [21–24].One of the alternative methods is to heat up the injected solvent to take advantage of both thermal and mass diffusion for oil viscosity reduction (N-Solv) [25–27]. Recent studies in this area show that N-Solv can significantly improve the low production rate, in some cases, comparable to SAGD process. However, these estimations are all based on laboratory experiments, and no field applications are available to support the proficiency of N-Solv in steam-based recovery method. One of the main challenges of N-Solv is the low heat capacity of injected solvent compared to steam.Recently, solvent-assisted SAGD process showed promising potential for efficient heavy oil recovery. In this process, steam is used as the main heat carrier and the coinjected solvent is the axillary factor in the further reduction of oil viscosity. Nasr et al. [28–30] proposed this method and using experimental tools they showed that, compared to conventional SAGD, this ES-SAGD (expanding solvent steam assisted gravity drainage) can improve oil production rate with lower steam oil ratio (SOR) and lower energy and water requirements. Proper well constraints (i.e., pressure, temperature, and rates), solvent composition, and steam-solvent ratios are among the important factors impacting the outcome of the ES-SAGD [31–37].Application of one single well in the Vapex process has not been addressed in the literature. However, Elliot and Kovscek [38] have carried out a simulation study on the application of single horizontal well in SAGD process in heavy oil reservoirs. They showed that preheating the near wellbore area improves the performance of single well SAGD process by creating an initial steam chamber in surrounding area of the well. Later, Akin and Bagci [39] performed an experimental study to investigate the efficiency of the single well SAGD and optimized the startup procedure of the production. Also, the experimental results were confirmed by a simulation study. They emphasized that the project economics can be highly influenced by the early production response and showed that the principal mechanism in single well SAGD is steam formation and growth.Although the Vapex process is accomplished by mass transfer and the dominant mechanism in SAGD is heat transfer, the central idea of both processes is the growth of an egg-like vapor (steam or hydrocarbon solvent) chamber within the reservoir. Therefore, in this work, the same methodology was used to move toward the simulation of SW-Vapex. In the present study, a simulation model was developed to investigate the feasibility of single well Vapex. The approach includes, first, optimizing the early time performance of the SW-Vapex and, second, performing a sensitivity analysis to study the effect of the reservoir and well completion parameters on the process.


## 2. Simulation Model

### 2.1. Reservoir Model

The reservoir model selected for simulation of SW-Vapex process is a homogeneous, anisotropic, three-dimensional system consisting of 5,568 grid blocks. The grid system is Cartesian with local grid refinement as detailed in Figures1 and 2. The reservoir is 1400 m inX-direction, 80 m inY-direction, and 19.6 m inZ-direction. With the average porosity of 33% and connate water saturation of 15%, the total reservoir hydrocarbon pore volume is 615,754 m3. The absolute permeability is 1,500 md in theX andY directions and 800 md in the vertical direction. Initially, the average reservoir pressure is 1.1 Mpa, the pressure distribution is hydrostatic, and the reservoir temperature is 20°C. The reservoir and fluid properties are listed in Table 1. The values of these properties were selected based on a typical Alberta reservoir.Table 1
Properties of the simulation model.
Property Value Grid type Cartesian Length inX-direction 1400 m Length inY-direction 80 m Length inZ-direction 19.6 m Number of grid cells 5,568 Average porosity 0.33 Horizontal permeability 1500 md Vertical permeability 750 md Number of components 4 Temperature 20°C Connate water saturation 0.15 Initial pressure 1.1 MPa Initial oil viscosity @ 20°C 8770 mPa·s Solvent composition 0.7 C3 + 0.3 C1 Well length 800 m Total hydrocarbon pore volume 615,754 m3Figure 1
X-Z cross section of the simulation model.Figure 2
Y-Z cross section of the simulation model, perpendicular to the horizontal well.The single horizontal well is simulated using discretized wellbore model [40] (released with CMG version 98.01) that accurately represents fluid and heat transfer in the well. The well is divided into two parts whose lengths are equal, and they coincide end to end. It is assumed that a packer will isolate a 160 m distance between two wells. This configuration provides a flexible model to study different well completion and operating procedure. The properties of crude oil used in simulations were obtained from PVT lab tests. To simplify the analysis and reduce simulation run time, the lumping method was considered in developing the fluid model, and the number of components was decreased to four pseudocomponents. The initial oil viscosity at reservoir condition is 8,770 cp and by raising the oil temperature to 120°C the viscosity will reduce to 136 cp as shown in Figure 3. The relative permeability data are given in Figures 4 and 5.Figure 3
Oil viscosity versus temperature.Figure 4
Oil-water relative permeability curve.Figure 5
Gas-oil relative permeability curve.


### 2.2. Solvent Injection Criteria

The criterion that should be considered in selecting the solvent composition is that it should be at or near to its saturation point or in the case of solvent mixture near its dew point. This decisive factor should be met to avoid any liquefaction of the solvent before it dissolves into heavy oil since this may cause higher solvent consumption, which results in higher oil production cost [41–45]. Since the vapor pressure of typical solvents (propane or butane) is very low at the specified reservoir conditions, liquefaction of the solvent in the high-pressure reservoir is inevitable. To overcome this difficulty, the solvent should be mixed with a suitable noncondensable gas such as methane to reach the dew point state under reservoir conditions. Different solvent mixtures were tested to find the best composition which meets the criterion above. Constructed phase envelope in WinProp module (CMG software) for a mixture of methane and propane indicates that a composition consists of 30% methane and 70% propane by mole fraction complying with this request. According to Figure 6, any change in the composition of the proposed mixture causes the injection operation condition to deviate from solvent saturation state and fall either in the two-phase or the super-heated region. If the operation conditions fall within theP-T diagram, the liquid solvent will be injected into the reservoir which as described before is undesirable.Figure 6
Phase diagram of injected solvent system with respect to reservoir temperature and pressure.


## 2.1. Reservoir Model

The reservoir model selected for simulation of SW-Vapex process is a homogeneous, anisotropic, three-dimensional system consisting of 5,568 grid blocks. The grid system is Cartesian with local grid refinement as detailed in Figures1 and 2. The reservoir is 1400 m inX-direction, 80 m inY-direction, and 19.6 m inZ-direction. With the average porosity of 33% and connate water saturation of 15%, the total reservoir hydrocarbon pore volume is 615,754 m3. The absolute permeability is 1,500 md in theX andY directions and 800 md in the vertical direction. Initially, the average reservoir pressure is 1.1 Mpa, the pressure distribution is hydrostatic, and the reservoir temperature is 20°C. The reservoir and fluid properties are listed in Table 1. The values of these properties were selected based on a typical Alberta reservoir.Table 1
Properties of the simulation model.
Property Value Grid type Cartesian Length inX-direction 1400 m Length inY-direction 80 m Length inZ-direction 19.6 m Number of grid cells 5,568 Average porosity 0.33 Horizontal permeability 1500 md Vertical permeability 750 md Number of components 4 Temperature 20°C Connate water saturation 0.15 Initial pressure 1.1 MPa Initial oil viscosity @ 20°C 8770 mPa·s Solvent composition 0.7 C3 + 0.3 C1 Well length 800 m Total hydrocarbon pore volume 615,754 m3Figure 1
X-Z cross section of the simulation model.Figure 2
Y-Z cross section of the simulation model, perpendicular to the horizontal well.The single horizontal well is simulated using discretized wellbore model [40] (released with CMG version 98.01) that accurately represents fluid and heat transfer in the well. The well is divided into two parts whose lengths are equal, and they coincide end to end. It is assumed that a packer will isolate a 160 m distance between two wells. This configuration provides a flexible model to study different well completion and operating procedure. The properties of crude oil used in simulations were obtained from PVT lab tests. To simplify the analysis and reduce simulation run time, the lumping method was considered in developing the fluid model, and the number of components was decreased to four pseudocomponents. The initial oil viscosity at reservoir condition is 8,770 cp and by raising the oil temperature to 120°C the viscosity will reduce to 136 cp as shown in Figure 3. The relative permeability data are given in Figures 4 and 5.Figure 3
Oil viscosity versus temperature.Figure 4
Oil-water relative permeability curve.Figure 5
Gas-oil relative permeability curve.


## 2.2. Solvent Injection Criteria

The criterion that should be considered in selecting the solvent composition is that it should be at or near to its saturation point or in the case of solvent mixture near its dew point. This decisive factor should be met to avoid any liquefaction of the solvent before it dissolves into heavy oil since this may cause higher solvent consumption, which results in higher oil production cost [41–45]. Since the vapor pressure of typical solvents (propane or butane) is very low at the specified reservoir conditions, liquefaction of the solvent in the high-pressure reservoir is inevitable. To overcome this difficulty, the solvent should be mixed with a suitable noncondensable gas such as methane to reach the dew point state under reservoir conditions. Different solvent mixtures were tested to find the best composition which meets the criterion above. Constructed phase envelope in WinProp module (CMG software) for a mixture of methane and propane indicates that a composition consists of 30% methane and 70% propane by mole fraction complying with this request. According to Figure 6, any change in the composition of the proposed mixture causes the injection operation condition to deviate from solvent saturation state and fall either in the two-phase or the super-heated region. If the operation conditions fall within theP-T diagram, the liquid solvent will be injected into the reservoir which as described before is undesirable.Figure 6
Phase diagram of injected solvent system with respect to reservoir temperature and pressure.


## 3. Results

### 3.1. Early Time Performance

Vapor extraction is a slow process which is governed by mass diffusion, and therefore optimization schemes should be implemented to facilitate the process at the early time. Increasing of the gas-oil contact area at the early period of production should be considered to enhance the whole process by accelerating vapor chamber development. Thermal recovery methods especially steam injection can be used as an efficient alternative for this goal. For uniform heating of the near wellbore area and reducing the oil viscosity, the total length of the horizontal well can be used for steaming. In this way, an initial cavity is formed in the reservoir which increases the oil-solvent mass transfer area and therefore enhances oil dilution. To investigate the importance of initial thermal treatment and choose the appropriate heating method, different scenarios were considered with operation conditions summarized in Table2.Table 2
Operation condition of early time scenarios.
Case Injection rate (CWE m3/day) Description Vapex 2000 (m3/day)∗ Vapex from the beginning SAGD 300 SAGD for 180 days, followed by Vapex Cyclic 1x 300 20 days of injection, 70 days of production, followed by Vapex Cyclic 2x 300 20 days of injection, 70 days of production for 2 times, followed by Vapex ∗Hydrocarbon solvent injection rate.The first scenario assumes thorough Vapex process from the beginning which can provide a reference case for comparison of the performance of other preheating strategies. In second case steam was injected at the toe of the horizontal well and simultaneously diluted oil is produced at the heel. The steam injection schedule which took 180 days was then followed by continuous solvent injection. The third and fourth cases include cyclic steam injection with different soak and production periods. In case 2, steam is continuously injected from the toe of the horizontal well. Low injectivity was one of the main issues for this preheating method. To improve the injectivity problem, steam was injected in a cyclic way. In case 3, the process starts with 20 days of steam injection and a soaking period of 40 days, then followed by 70 days of production (no steam injection). In case 4, steaming, soaking, and production sequence is repeated twice then followed by Vapex process. The oil production profiles are illustrated in Figures7 and 8. It can be seen that the cyclic steam injection with two periods of injection and production leads to higher recovery. Cyclic steaming (case 3 and 4) showed higher efficiency for initial preheating strategy compared to other methods.Figure 7
Cumulative oil production for different early time preheating scenarios during the first 180 days. Cyclic steam injection with two periods of injection/production leads to highest oil production (voidage in the reservoir).Figure 8
Oil production rate for different early time preheating scenarios during the first 180 days.It should be mentioned that in case 1, the solvent is injected with operating pressure which is slightly higher than the average reservoir pressure. The gas breakthrough will happen after a while by immediate establishment of a short circuit between injection and production part of the horizontal well. The breakthrough time depends on oil mobility and the distance between well sections. Since the vaporized solvent remains in contact with a small portion of the reservoir, the efficiency of the process drastically reduces, and vapor chamber development is quite slow. Increasing the separation between the well sections does not improve the recovery, but it just delays the gas breakthrough time. In the following cases, it is attempted to maximize the initial contact area between the solvent and fresh heavy oil by creating a proper voidage in the reservoir.Figure9 indicates the effect of early time strategy on the ultimate oil recovery after 15 years. According to this figure, the cyclic steam injection can be considered as an important option for accelerating the process. Figure 10 displays the temperature profile after a cyclic steaming period which has provided uniform heating along the whole length of the horizontal well as well as a proper initial cavity in the reservoir. Figures 11 and 12 show the vertical view of the oil saturation and the viscosity distribution in the reservoir after 2,500 days according to which vapor chamber has been completely developed. As oil is diluted, it drains toward the producer. These figures obviously clarify that, like conventional Vapex process, SW-Vapex relies on vapor chamber development in the reservoir, and the same mechanism is applied.Figure 9
Effect of early time scenarios on the performance of SW-Vapex, after 15 years.Figure 10
Temperature profile after 180 days, cyclic steam injection 2x.Figure 11
Vertical view of viscosity profile after 2,500 days; layer number inI direction: 24.Figure 12
Vertical view of saturation profile after 2500 days; layer number inI direction: 24.


### 3.2. Sensitivity Study

Here, a series of sensitivity studies has been carried out to investigate the effect of operating conditions and reservoir parameters on the performance of SW-Vapex. Solvent injection rate, the presence of a small gas cap, reservoir thickness, and permeability anisotropy were considered for sensitivity study. All cases are started after 180 days of initial cyclic steam injection. The results are compared with the reference case whose properties are listed in Table1. Figures 13 and 14 present the cumulative oil production for all sensitivity cases. The discussion of the results of each study is as follows.Figure 13
Effect of initial gas cap and gas injection rate (Qsolvent=3,500 m3/day and Qsolvent=4,500 m3/day) on the recovery of SW-Vapex after 15 years of production.Figure 14
Effect of permeability anisotropy (Kh/Kv = 1 and Kh/Kv = 8) and crude oil viscosity (μoil = 15000 cp and μoil = 2000 cp) on ultimate oil recovery after 15 years.Solvent Injection Rate. Solvent was injected with an average rate of 2,000 m3/day. To investigate the effect of solvent injection rate, two other models were developed by increasing the gas injection rate to 3,500 and 4,500 m3/day. Figure 13 shows that increasing the solvent injection rate could raise the oil recovery to some extent, and the amount of oil recovery enhancement is not significant after an optimum gas injection rate. This optimum value depends on the preheating method as well as the reservoir and fluid properties. Even the capillary pressure can intensify the effect of gas injection rate by dispersion phenomenon which has been recently addressed in the literature [14, 24, 46–53]. Mass transfer and gravity drainage are the dominant mechanisms in Vapex process which act side by side. As injected solvent diffuses into heavy oil, the viscosity reduces and oil drains toward the production section by gravity acceleration. Therefore, the injection rate should be adjusted in such a way that a balance between these two mechanisms is achieved. This injection rate corresponds to the optimum value at which the solvent to oil ratio hits the minimum. Extra injected solvent passes through the reservoir without participating in oil dilution process.Gas Cap. To investigate the effect of the presence of a small gas cap a simulation model was created by adjusting a gas zone with 3 m height. Although the simulation results reveal the same ultimate recovery in comparison with the reference case, a higher recovery factor can be achieved in earlier time. This suggests that the existence of a small gas cap is favorable for the process. It is believed that, in such a situation, injected solvent can be distributed over a wider oil interface and improves the mass transfer rate between solvent and in situ fluid.Permeability Anisotropy. The original permeability is set to 1,500 and 750 md in horizontal and vertical directions, respectively. To analyze the effect of permeability anisotropy, two additional models were constructed with horizontal to vertical permeability ratio of Kh/Kv = 1 and 8. The value of horizontal permeability was kept constant, and the vertical permeability has been changed. Figure 14 displays that decreasing of the vertical permeability causes difficulty in the vertical propagation of the hydrocarbon solvent and also hinders the oil drainage toward production. Larger permeability anisotropy is an unfavorable reservoir condition and decreases total oil recovery.Viscosity and Reservoir Height. Fluid properties were altered to examine the effect of viscosity. Two alternative viscosities of 2,000 and 15,000 cp at reservoir temperature were chosen. The results show that the application of SW-Vapex in extra viscous oils is a challenging issue. Initial viscosity greater than 15,000 cp delays the drainage process and prevents the proper growth of the solvent chamber. This can be counterbalanced by more solvent consumption which is not economically viable. The same conclusion can be drawn for the effect of the reservoir thickness. Thin reservoirs cast a shadow over the gravity effect. A vapor chamber of considerable height must be developed for efficient oil drainage. Thin reservoirs with a height of 10 m or less are not good candidates for application of SW-Vapex. However, an increase of the height over 25 meters does not offer significant improvement. Figure 15 compares the cumulative oil recovery for three different reservoir thicknesses of 10, 25, and 35 m.Figure 15
Effect of reservoir thicknesses (10, 19.6, 25, and 35 m) on ultimate oil recovery after 15 years.


## 3.1. Early Time Performance

Vapor extraction is a slow process which is governed by mass diffusion, and therefore optimization schemes should be implemented to facilitate the process at the early time. Increasing of the gas-oil contact area at the early period of production should be considered to enhance the whole process by accelerating vapor chamber development. Thermal recovery methods especially steam injection can be used as an efficient alternative for this goal. For uniform heating of the near wellbore area and reducing the oil viscosity, the total length of the horizontal well can be used for steaming. In this way, an initial cavity is formed in the reservoir which increases the oil-solvent mass transfer area and therefore enhances oil dilution. To investigate the importance of initial thermal treatment and choose the appropriate heating method, different scenarios were considered with operation conditions summarized in Table2.Table 2
Operation condition of early time scenarios.
Case Injection rate (CWE m3/day) Description Vapex 2000 (m3/day)∗ Vapex from the beginning SAGD 300 SAGD for 180 days, followed by Vapex Cyclic 1x 300 20 days of injection, 70 days of production, followed by Vapex Cyclic 2x 300 20 days of injection, 70 days of production for 2 times, followed by Vapex ∗Hydrocarbon solvent injection rate.The first scenario assumes thorough Vapex process from the beginning which can provide a reference case for comparison of the performance of other preheating strategies. In second case steam was injected at the toe of the horizontal well and simultaneously diluted oil is produced at the heel. The steam injection schedule which took 180 days was then followed by continuous solvent injection. The third and fourth cases include cyclic steam injection with different soak and production periods. In case 2, steam is continuously injected from the toe of the horizontal well. Low injectivity was one of the main issues for this preheating method. To improve the injectivity problem, steam was injected in a cyclic way. In case 3, the process starts with 20 days of steam injection and a soaking period of 40 days, then followed by 70 days of production (no steam injection). In case 4, steaming, soaking, and production sequence is repeated twice then followed by Vapex process. The oil production profiles are illustrated in Figures7 and 8. It can be seen that the cyclic steam injection with two periods of injection and production leads to higher recovery. Cyclic steaming (case 3 and 4) showed higher efficiency for initial preheating strategy compared to other methods.Figure 7
Cumulative oil production for different early time preheating scenarios during the first 180 days. Cyclic steam injection with two periods of injection/production leads to highest oil production (voidage in the reservoir).Figure 8
Oil production rate for different early time preheating scenarios during the first 180 days.It should be mentioned that in case 1, the solvent is injected with operating pressure which is slightly higher than the average reservoir pressure. The gas breakthrough will happen after a while by immediate establishment of a short circuit between injection and production part of the horizontal well. The breakthrough time depends on oil mobility and the distance between well sections. Since the vaporized solvent remains in contact with a small portion of the reservoir, the efficiency of the process drastically reduces, and vapor chamber development is quite slow. Increasing the separation between the well sections does not improve the recovery, but it just delays the gas breakthrough time. In the following cases, it is attempted to maximize the initial contact area between the solvent and fresh heavy oil by creating a proper voidage in the reservoir.Figure9 indicates the effect of early time strategy on the ultimate oil recovery after 15 years. According to this figure, the cyclic steam injection can be considered as an important option for accelerating the process. Figure 10 displays the temperature profile after a cyclic steaming period which has provided uniform heating along the whole length of the horizontal well as well as a proper initial cavity in the reservoir. Figures 11 and 12 show the vertical view of the oil saturation and the viscosity distribution in the reservoir after 2,500 days according to which vapor chamber has been completely developed. As oil is diluted, it drains toward the producer. These figures obviously clarify that, like conventional Vapex process, SW-Vapex relies on vapor chamber development in the reservoir, and the same mechanism is applied.Figure 9
Effect of early time scenarios on the performance of SW-Vapex, after 15 years.Figure 10
Temperature profile after 180 days, cyclic steam injection 2x.Figure 11
Vertical view of viscosity profile after 2,500 days; layer number inI direction: 24.Figure 12
Vertical view of saturation profile after 2500 days; layer number inI direction: 24.


## 3.2. Sensitivity Study

Here, a series of sensitivity studies has been carried out to investigate the effect of operating conditions and reservoir parameters on the performance of SW-Vapex. Solvent injection rate, the presence of a small gas cap, reservoir thickness, and permeability anisotropy were considered for sensitivity study. All cases are started after 180 days of initial cyclic steam injection. The results are compared with the reference case whose properties are listed in Table1. Figures 13 and 14 present the cumulative oil production for all sensitivity cases. The discussion of the results of each study is as follows.Figure 13
Effect of initial gas cap and gas injection rate (Qsolvent=3,500 m3/day and Qsolvent=4,500 m3/day) on the recovery of SW-Vapex after 15 years of production.Figure 14
Effect of permeability anisotropy (Kh/Kv = 1 and Kh/Kv = 8) and crude oil viscosity (μoil = 15000 cp and μoil = 2000 cp) on ultimate oil recovery after 15 years.Solvent Injection Rate. Solvent was injected with an average rate of 2,000 m3/day. To investigate the effect of solvent injection rate, two other models were developed by increasing the gas injection rate to 3,500 and 4,500 m3/day. Figure 13 shows that increasing the solvent injection rate could raise the oil recovery to some extent, and the amount of oil recovery enhancement is not significant after an optimum gas injection rate. This optimum value depends on the preheating method as well as the reservoir and fluid properties. Even the capillary pressure can intensify the effect of gas injection rate by dispersion phenomenon which has been recently addressed in the literature [14, 24, 46–53]. Mass transfer and gravity drainage are the dominant mechanisms in Vapex process which act side by side. As injected solvent diffuses into heavy oil, the viscosity reduces and oil drains toward the production section by gravity acceleration. Therefore, the injection rate should be adjusted in such a way that a balance between these two mechanisms is achieved. This injection rate corresponds to the optimum value at which the solvent to oil ratio hits the minimum. Extra injected solvent passes through the reservoir without participating in oil dilution process.Gas Cap. To investigate the effect of the presence of a small gas cap a simulation model was created by adjusting a gas zone with 3 m height. Although the simulation results reveal the same ultimate recovery in comparison with the reference case, a higher recovery factor can be achieved in earlier time. This suggests that the existence of a small gas cap is favorable for the process. It is believed that, in such a situation, injected solvent can be distributed over a wider oil interface and improves the mass transfer rate between solvent and in situ fluid.Permeability Anisotropy. The original permeability is set to 1,500 and 750 md in horizontal and vertical directions, respectively. To analyze the effect of permeability anisotropy, two additional models were constructed with horizontal to vertical permeability ratio of Kh/Kv = 1 and 8. The value of horizontal permeability was kept constant, and the vertical permeability has been changed. Figure 14 displays that decreasing of the vertical permeability causes difficulty in the vertical propagation of the hydrocarbon solvent and also hinders the oil drainage toward production. Larger permeability anisotropy is an unfavorable reservoir condition and decreases total oil recovery.Viscosity and Reservoir Height. Fluid properties were altered to examine the effect of viscosity. Two alternative viscosities of 2,000 and 15,000 cp at reservoir temperature were chosen. The results show that the application of SW-Vapex in extra viscous oils is a challenging issue. Initial viscosity greater than 15,000 cp delays the drainage process and prevents the proper growth of the solvent chamber. This can be counterbalanced by more solvent consumption which is not economically viable. The same conclusion can be drawn for the effect of the reservoir thickness. Thin reservoirs cast a shadow over the gravity effect. A vapor chamber of considerable height must be developed for efficient oil drainage. Thin reservoirs with a height of 10 m or less are not good candidates for application of SW-Vapex. However, an increase of the height over 25 meters does not offer significant improvement. Figure 15 compares the cumulative oil recovery for three different reservoir thicknesses of 10, 25, and 35 m.Figure 15
Effect of reservoir thicknesses (10, 19.6, 25, and 35 m) on ultimate oil recovery after 15 years.


## 4. Discussion

Early time study indicated that applying vapor extraction process alone with single well configuration loses its viability due to inherent slow nature of the solvent. In this point, implementation of an optimization scenario can play a crucial role in the improvement of the oil recovery. By comparing the results of different scenarios, it was found that steam cycling was the most efficient method. The objective of early time heat treatment is to heat the reservoir, as much as possible, in a uniform manner to provide an initial cavity in the formation. It is worth mentioning that selection of early time strategy is fully dependent on reservoir property and operating conditions of the Vapex process and may differ from case to case.Heavy oil viscosity has a pronounced effect on the success of SW-Vapex. Due to related difficulties in the mobilization of the crude oil with a viscosity greater than 15,000 cp, these highly viscous reservoirs may need to use other production methods. The same conclusion can be drawn for the height of the reservoir. A minimum height should exist to allow proper development of the vapor chamber in the vertical direction. For a reservoir with height that is less than 4 meters, the ultimate recovery would not exceed 5% of the STOOIP. Since the practical hydrocarbon solvents used in the operation are almost expensive, the solvent requirement and consumption are the key economic factor for the Vapex recovery. An optimum value should be specified to obtain minimum solvent to oil ratio. As expected the vertical permeability value plays the major role in the rate of vertical propagation of the vapor chamber. Since the diluted oil should be drained toward the producer and the solvent substitutes that, the vertical permeability reduction could reduce the oil recovery. Therefore, the presence of the shale layers in the reservoir is expected to make the process more challenging.


## 5. Conclusions

This study aimed at screening of applicability of single well Vapex process through numerical modeling.(1)
A sound analogy for simulation study of single well Vapex process has been developed to simulate both wellbore and reservoir sections.(2)
Preheating treatment is a must for creating initial proper voidage in the reservoir to enhance vapor propagation. Preheating has a significant effect on the total oil recovery in the long run. Cyclic steaming with two periods of soak and production in 180 days was selected as an efficient preheating scenario to heat the near wellbore area uniformly.(3)
Solvent injection rate should be adjusted to achieve maximum oil production rate by consuming minimum solvent. Higher injection rates just shorten the breakthrough time and leave the oil unaffected.(4)
Application of SW-Vapex in reservoirs with a reservoir thickness approximately less than 10 m and initial oil viscosity more than 1,500 cp seems to be not feasible. The presence of a relatively small gas cap aids the solvent diffusion by increasing the contact surface area.



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*Source: 8925190-2016-11-08.xml*