{'fraction_non_alphanumeric': 0.028453816711200983, 'fraction_numerical': 0.017091548109097035, 'mean_word_length': 4.586605701990317, 'pattern_counts': {'":': 0, '<': 0, '<?xml version=': 0, '>': 1, 'https://': 0, 'lorem ipsum': 0, 'www.': 0, 'xml': 0}, 'pii_count': 0, 'substrings_counts': 0, 'word_list_counts': {'cursed_substrings.json': 0, 'profanity_word_list.json': 0, 'sexual_word_list.json': 0, 'zh_pornsignals.json': 0}}
Brine/CO2 Interfacial Properties and Effects on CO2 Storage in Deep Saline Aquifers

Résumé — Propriétés interfaciales saumure/CO 2 et effets sur le stockage du CO 2 dans des aquifères salins profonds — Il est admis depuis longtemps que les propriétés interfaciales (tension interfaciale, mouillabilité, capillarité et transfert de masse) régissent la distribution et le comportement des fluides au sein des milieux poreux. Par conséquent, les propriétés interfaciales entre le milieu poreux constituant le réservoir, le CO 2 , la saumure et/ou le gaz du réservoir jouent un rôle important sur l’efficacité de n’importe quelle opération de stockage de CO 2 . Dans le cas des aquifères salins profonds, il existe un manque de données certain en ce qui concerne les propriétés interfaciales saumure-CO 2 en conditions de stockage. Plus spécifiquement, des données expérimentales de tension interfaciale saumure-CO Abstract — Brine/CO 2 Interfacial Properties and Effects on CO 2 Storage in Deep Saline Aquifers — It has been long recognized that interfacial interactions (interfacial tension, wettability, capillarity and interfacial mass transfer) govern fluid distribution and behaviour in porous media. Therefore the interfacial interactions between CO 2 , brine and reservoir oil and/or gas have an important influence on the effectiveness of any CO 2 storage operation. There is a lack of experimental data related to interfacial properties for all the geological storage options (oil & gas reservoirs, coalbeds, deep saline aquifers). In the case of deep saline aquifers, there is a gap in data and


INTRODUCTION
Large-scale subsurface storage of anthropogenic carbon dioxide is considered as a potential technology for greatly stabilizing greenhouse gas concentration in the atmosphere [1]. At least three options exist for geological storage of CO 2 [2]: oil and gas reservoirs, deep saline aquifers and unmineable coal beds. Because of its expertise and knowledge of many geological sites considered as prospects for CO 2 storage, the oil industry is usually uniquely positioned to sequester CO 2 , no matter the source. Successful CO 2 sequestration in deep saline aquifers and different types of hydrocarbon reservoirs is largely governed by the fluid-fluid and fluid-rock interfacial interactions. These interactions are represented by the Laplace equation (see Eq. 1), where the key parameters to take into account are the interfacial tension and the wettability. Therefore, the quality of the data related to these properties is particularly important in CO 2 storage modeling. On the one hand these properties highly influence the flow process, and on the other hand they control the capillary-sealing efficiency: (1) where P c is the capillary pressure, γ b,CO 2 is the brine-CO 2 interfacial tension, R is the largest connected pore throat and θ is the contact angle, which is related to reservoir wettability. This paper deals with γ b,CO 2 and wettability at CO 2 storage conditions. For interfacial tension, experimental data of pure water-CO 2 system at reservoir conditions, γ w,CO 2 have been reported by several authors since 1957 [3][4][5][6]. Nevertheless, there are some concerns with the use of these data [6], related to the thermodynamic equilibrium, the image analysis of experimental values of brine-CO 2 Interfaciale Tension (IFT) at pressure, temperature and salt concentration conditions representative of those of a CO 2 storage operation. A correlation is derived from experimental data published in a companion paper [Chalbaud C.,  method which was used, and the non consideration of the dissolved CO 2 effect on the water phase density [7]. At the same time, efforts to estimate γ w,CO 2 from molecular dynamics computer simulations [8,9] or theoretical models [10][11][12] have not lead to satisfactory results. To our knowledge, there is no complete set of experimental data concerning the brine-CO 2 system (at high pressures, high temperatures and different salt concentrations), which could be used to estimate γ b,CO 2 under representative storage conditions. To our knowledge, as far as wettability is concerned, the only significant contributions to gather data and knowledge, have been focused on capillary seal efficiency of the caprock. Chiquet et al. [12] , measured contact angle between CO 2 and brine, on both mica and quartz surfaces. According to the authors, there is change in the contact angle while increasing the pressure; this indicates a passage from a strongly waterwet media to an intermediate-wet media. Chiquet [13,14] explanations are based on the DLVO theory (disjoining pressure). Chiquet points out a strong change in electrostatic forces while increasing the pressure. This change is a consequence of pH reduction, due to the dissolution of CO 2 in the aqueous phase. Such wettability alteration is detrimental to CO 2 geological storage because it induces lower breakthrough pressures across the caprock (see Eq. 2). To our knowledge, no other analogous work can be found in the literature which study fluid flows and phase distributions in silica or carbonate rocks for different wettability scenarios. (2) where P th c is the threshold capillary pressure in the caprock saturated with brine, and R the largest connected pore throat in the caprock.

APPROACH
Three different scales are investigated in this paper: the interface, the pore scale (Poiseuille) and the rock scale (Darcy). For the Interfaciale Tension (IFT), the Axi-symmetric Drop Shape Analysis technique (ADSA) was used, in the case of a rising drop. These measurements have been performed for pressures ranging from 45 to 255 bars, temperatures from 27 to 100°C and NaCl concentrations (salinity) from 5000 to 150 000 ppm. A correlation was then developed on the basis of the Parachor model, the salt effect and a regression fit of more than one hundred IFT experimental values. For the wettability, glass micromodels have been used to study qualitatively the fluid distribution in the case of different wettabilities and thermodynamic conditions. Next, in order to obtain quantitative data, CO 2 and N 2 core flooding tests were performed in a carbonate core sample. During these tests local saturation measurements have been carried out and the heterogeneous approach [17] was used for the numerical interpretation. P c curves for different wettability scenarios have been estimated.

Experimental Section
For a given salt concentration and a given temperature, an average of ten γ b,CO 2 values were measured. Thermodynamic conditions ranged from 45 bars up to 255 bars; three temperatures 27, 71 and 100°C, and four salinities (5000; 50 000; 100 000 and 150 000 ppm) were investigated. The density values of brine solutions were calculated from Søreide and Whitson [16] and Rowe and Chou [17]. This calculation takes into account the effect of dissolved CO 2 and NaCl. The CO 2 density was considered as equal to that of pure CO 2 according to King et al. [18].

Experimental Equipment
The experimental set-up presented in Figure 1 is designed to work under representative reservoir conditions (up to 260 bars and 120°C). It allows measurements of interfacial tension for two phase systems using the rising (or pendant) drop method.
This device consists of three items: the high pressure visualization cell, the fluid circuit and feeding system, and the imaging system. A CO 2 cap is maintained at the ceiling of the visualization cell in order to improve the thermodynamic equilibrium. For the same reason, fluids are pre saturated under the same conditions as the measurements. This means that, in the CO 2 cell CO 2 is equilibrated with brine and in the brine cell brine is in contact with CO 2 ). The term "pre saturate" is used instead of "saturate" because experiments showed that using this method does not lead to a perfect stabilization and to a complete saturation of both phases [6]. The imaging system consists of a linear arrangement of a light source, a glass diffuser, the rising drop and the digital camera.  Drop-shape techniques have been widely used and are among the most accurate methods. The Axi-Symmetric Drop Shape Analysis (ADSA) was selected for this study. ADSA acquires images of a drop and extracts the experimental profile of this drop, using edge detection techniques. Details of the ADSA methodology can be found elsewhere [19].

Experimental Procedure
CO 2 drops are generated at the tip of a glass capillary tube (1.5 mm o.d) in the visualization cell, which has been previously filled with the brine solution. A CO 2 cap is placed at the ceiling of this cell to maintain a good CO 2 saturation of the brine solution within the cell. The capillary tube is also used as an internal metric standard to determine the exact drop size. A range of pressures between 45 and 255 bars was investigated along each isotherm, using a compression process. For each pressure step, the IFT was obtained taking the average of at least 5 measured values.
As the equilibrium of the system is of primary importance to the accuracy of the measurements, once the drop is generated and enlarged at the tip of the capillary, it was maintained in the cell during several minutes. Measurements were taken over time during this period as shown in Figure 2. The equilibrium IFT is a static value that was reached almost 8-15 min after the drop was generated, depending on the thermodynamic conditions. The period during which IFT decreases corresponds to the dissolution of CO 2 in brine and vice versa. If CO 2 is not pre saturated before the drop formation and if the CO 2 ceiling is not present in the visualization cell, static IFT values would be more difficult to achieve. The evolution of the IFT presented in Figure 2 is the consequence of using the saturated aqueous phase density values  (equilibrium not reached), instead of the instantaneous ones. As densities cannot be measured in the viewing cell, the only possible approach was effectively to consider this saturated aqueous phase density for all the points and to wait until a constant value of IFT was reached.

Brine/CO 2 IFT vs Pressure and Temperature
All results are presented in terms of NaCl molal concentration, in order to allow comparison of the linear relationship between the increase in the IFT and the molal concentration of salt observed by previous authors mentioned in the introduction. The maximum standard deviation of the presented experimental data is close to 3.5%. A complete description of these results will be found in Chalbaud et al. [20] γ b, CO 2 isotherms were obtained at 27, 71 and 100°C. Figure 3a shows isotherms at 27°C. The evolution of γ b,CO 2 with pressure and temperature is similar to the one reported by other authors for γ w, CO 2 , under similar conditions [3][4][5][6]: at low pressures γ b,CO 2 decreases with pressure; this decrease is more pronounced at low temperature. At high pressures a plateau value of γ b,CO 2 is reached for all NaCl concentrations investigated. At 27°C this plateau is reached at 80 bars, while at 71°C, it is reached at 150 bars. At 100°C it is not possible to claim that a plateau has been reached. It is interesting to note that the pressure at which this plateau is reached does not depend on the NaCl concentration neither at 27°C nor at 71°C. Nevertheless, the value of γ b,CO 2 at the plateau does depend on the salt concentration. At these temperatures the γ b,CO 2 value is the same once the plateau has been reached. It is of approximately 26 mN/m for 5000 ppm of NaCl. At highest temperatures (100°C), the minimal γ b,CO 2 is also close to 26 mN/m for 5000 ppm. We call this value γ Wplateau , where the W subscript refers to a very low salinity brine or to pure water. For a similar range of temperatures and pressures, several authors [3,6] have already reported the presence of a plateau in the IFT of pure water-CO 2 . Figure 3a presents the IFT of pure water-CO 2 and those of brine-CO 2 at different salt concentrations at 27°C. It can be seen from this figure that the difference between the measured IFT values for pure water and the lowest salinity brine (5000 or 0.085 m) is negligible. The results at 0.085 m NaCl can be considered as analogous to those of pure water. For such a low NaCl concentration a negligible effect of salt has already been reported for pressures up to 60 bars [21]. temperatures this incompressibility is reached for a lower pressure. A similar evolution of CO 2 solubility in water and brine with pressure has been reported [22][23][24] (additional CO 2 solubility in brine from an increment in pressure strongly decreases at higher pressures). This clearly shows that there is an important reduction of phase and solubility effects on the interfacial tension that could explain the existence of plateau in the γ b,CO 2 above a given pressure. This value therefore depends only on the temperature. These results point out a possible extrapolation of γ b,CO 2 for higher pressures, and establish a value of 26 mN/m (γ Wplateau ) for pure water or very low salinities (and other values according only on the salt concentration).
The applicability of this suggestion at temperatures near or above 100°C would need additional γ b,CO 2 experimental values for pressures above 300 bars.

γ γ b,CO 2 vs Salt Concentration
Similarly to previous works [21,25], a linear relationship between the increase of brine-CO 2 interfacial tension and molal salt concentration was found. This increase becomes more important at higher temperatures, as shown in Figure 4a. Once the plateau is reached the influence of temperature on the IFT becomes negligible. Therefore it is possible to establish an IFT increase independent of the temperature once the  Average increase of the IFT as a function of the NaCl molality for different temperatures, a) before reaching a plateau and b) after the IFT plateau.
plateau is achieved (Fig. 4b). Before reaching the plateau at 27°C this linear relationship is as follows: where δγ represents the increases of the IFT and m represents the molal concentration of salt. At T = 71°C and T = 100°C the slopes δγ/m of the linear relation before reaching the plateau are higher (see Fig. 4). After reaching the plateau we found a unique slope value (independent of the temperature) of 1.43. According to Argaud [25] IFT increase is given by a slope δγ/m of 1.63 for a water-air system at ambient conditions. In the case of NaCl, this relation is almost constant over a large range of molalities. Similar relationships exist for other chlorides at ambient conditions [25]. For KCl, MgCl 2 and CaCl 2 this increase is not linear at high values of molalities (>1.0m). Nevertheless, in most of the cases the concentration of these salts in reservoir brines is in the range of molalities inside which linear relations has been reported. There is no available data to evaluate the interfacial tension increase for a system which contains different salts, for example to know whether this increase would be additive or not. Massoudi and King [21] have found γ b,CO 2 values at 25°C for the brine-CO 2 system that indicated a linear relationship between the γ b,CO 2 and the molal concentration of NaCl (up to 5m) for pressures up to 60 bars. The δγ/m slope was near to 1.58 instead of 1.49 as presented in Equation (3). They also found a very slight (negligible according to the authors) decrease of this coefficient with pressure.
The evolution of the interfacial tension increase with molal concentration of NaCl in water is analogous to that reported by Massoudi and King [20] and those summarized by Argaud [25]. At 27°C, and after reaching the plateau, the value of the coefficient obtained for the linear relationship is very close to those reported by the above authors. These results do not support a proportional relation of the IFT increase with the Kelvin temperature suggested by Aveyard and Saleem [26], and Johansson and Eriksson [27]. In fact the difference in the IFT increase we observed between 71°C and 100°C is within the standard deviation of our results.

Possible Implications on CO 2 Storage
The available data existing in literature, which could be used by reservoir engineers to estimate IFT of water-CO 2 systems, do not take into account the effect of CO 2 dissolution on the aqueous phase density. At high pressure and low temperature, this effect becomes more important, because the density difference between the brine and the CO 2 is minimal. For example: at 27°C and 240 bars, the density difference is 14% lower if the dissolution of the CO 2 into the brine phase is not taken into account. Recently, Chiquet et al. [28] showed that under a pressure of 450 bars, this difference can be up to 70%. Due to the fact that density difference enters linearly in the IFT calculation, this could explain why at high pressures (once the plateau has been reached), there is a difference in γ w,CO 2 reported values, between low and high temperatures [6]. This indicates that available γ w,CO 2 data could be underestimated, especially at low temperatures. Chiquet et al. [28] have studied the interfacial tension of brine-CO 2 systems, for very low salinity, for high pressures (up to 450 bars), and a similar range of temperatures. They report a similar IFT plateau for a temperature lower than 100°C. This means that the IFT values reported in this paper for pressures up to 255 bars could be extrapolated up to 450 bars. Concerning the implications of salt effects, we observed that for salt (NaCl) concentrations above 30 000 ppm, the IFT increase is higher than the standard deviation; therefore it should not be neglected.
Additionally, if reported effects of CaCl 2 or MgCl 2 [29], both present in carbonate reservoirs, on surface tension, are extrapolated to high pressure and a wide range of temperatures, the increase of IFT due to their presence in the brine would be near the double of that of NaCl at storage conditions. This means that for pressures over 150 bars and temperatures between 27 and 71°C, the increase would be close to 8 mN/m for CaCl 2 or MgCl 2 , instead of 4 mN/m measured for 150 000 ppm of NaCl. This increase is as high as 30% of the γ w,CO 2 value. Therefore, the estimation of the γ b,CO 2 at storage condition, without taking into account the dissolved CO 2 in the aqueous phase nor the effect of salts, is strongly underestimated.
If γ b,CO 2 is underestimated, the capillary pressure threshold (P th c ) calculated from Equation (2), which determines the CO 2 breakthrough in the cap rock and the height of CO 2 column stored, is also underestimated; this leads to an underestimation of the storage capacity of the reservoir.
In the case of CO 2 storage in a deep saline aquifer, γ b,CO 2 governs fluid distribution in the porous media and is a key parameter in reservoir simulations to estimate the water displacement by a CO 2 injection. For a given height of stored CO 2 , the underestimation of γ b,CO 2 leads to an overestimation of the displacement efficiency of a CO 2 flooding in a deep saline aquifer; hence, it increases the amount of displaced brine and could erroneously increase the available reservoir storage volume for CO 2 . Figure 5 shows the cumulative brine production for CO 2 flooding in a carbonate core saturated with brine, at two different salinities (from Egermann et al. [30]). These experiments were carried out at the same pressure and temperature, P = 100 bars and T = 80°C, and two different salinities: 5000 ppm and 150 000 ppm. This figure shows that when the cumulative brine production has reached a constant value, this value is 13% higher for the lowest brine salinity, hence the available reservoir storage volume for CO 2 is 13% higher. According to Egermann et al. [30], this difference is due to the difference in the interfacial tension: it is possible to perform a satisfactory history match from reservoir simulations of both experiments, with the same k r and P c curves, if the P c curves are corrected using γ b,CO 2 values which take into account the salinity.

IFT Modeling
For water-pure hydrocarbon systems, Firoozabadi and Ramey [31] presented some examples using the Parachor model for multicomponents systems [32] (see Eq. 4). According to the authors this equation fails to predict the IFT for several water-hydrocarbon systems.
Firoozabadi and Ramey [31] proposed a correlation analogous to the Parachor model because it correlates the IFT to the density difference, with an exponent 4 (critical scaling exponent). Two correlation parameters have been used by Firoozabadi and Ramey [31]: the density difference between the hydrocarbon phase and the water phase and the reduced temperature. In this correlation the y-axis is: (5) and the x-axis is the density difference, Δρ. Although Firoozabadi and Ramey [31] showed that when using this correlation, the interfacial tension of several water-hydrocarbon systems at different thermodynamic conditions, is represented by a single curve; however it is not the case for some gases such as n-propane, ethylene and CO 2 . To develop this correlation the effect of gas dissolved in water or water dissolved in gas is not taken into account. This correlation originates from an assumed similarity between the water-liquid hydrocarbon IFT and the surface tension of the hydrocarbon at the same thermodynamic conditions [23]. Subsequently, Argaud [25] proposed to use the Parachor number to molar mass ratio of the hydrocarbon and an exponent, α, as a corrective factor to the correlation proposed by Firoozabadi and Ramey [31] as follows: (6) This corrective factor is based on the McLeod equation for pure compounds [33] reviewed by Fowler [34]: where Δρ lv is the density difference between the liquid and vapour phases of a pure hydrocarbon.
From Equation (6), Argaud [25] obtained a better fit to available IFT data for other gases compared with Firoozabadi and Ramey [31]. The idea is that Δρ is not the only parameter to be used for IFT prediction and additional information has to be sought from the chemical structure of the hydrocarbon through its hydrocarbon Parachor number.
The experimental results of this study indicate that γ b,CO 2 is strongly correlated with Δρ (see Fig. 6). The density difference takes into account the combined effects of pressure and temperature, and part of the salt effect as well. Nevertheless, Δρ is not enough to predict the γ b,CO 2 . Figure 7 show that for the same Δρ, different IFT can be obtained. This is mainly due to the salt effect. The observed existence of a plateau in the γ b,CO 2 is strongly related with the density difference. For density differences below 0.6 g/cm 3 , a stabilization in the has been observed, and the only parameter that affects the γ b,CO 2 is the salt concentration.
In order to model the interfacial tension, it is necessary to separate its variation with the density difference in two parts (see Fig. 7). The first part (high Δρ) could be correlated with equations similar to the Parachor model for pure compounds (Eq. 7). The second part (low Δρ), which corresponds to the plateau, has to be correlated using the γ w,CO 2 , once the plateau is reached (γ Wplateau ), and a linear relationship, to match the increase due to the presence of dissolved salts. Then, γ b,CO 2 can be explicitly described as: (8) where λ, β‚ θ are regression coefficients obtained from a least-squares fit of our results. The values of these coefficients are presented in Table 1 Table 2. P and M are respectively the Parachor number and the molar mass of CO 2 . As "α" exponent was always close to 1 it was decided not to use the "α" exponent or the P/M factor (Eq. 6) and a good regression fit of the results was obtained. It can be considered as arbitrary not to use the density difference with an exponent 4; but as Schechter and Guo [35] explained in a comprehensive review of the Parachor model and its use in IFT prediction of fluids, the IFT of several systems deviates from a slope of 4 to higher values. This behavior is attributed to molecules which rapidly adsorb at the interface. In this case the IFT would be significantly reduced although the density difference between the bulk phases would change very little (Fig. 7, part 1).
In the proposed correlation, T r was only used as a corrective factor because at lower pressures (Fig. 6, part 1), the IFT increase due to the presence of dissolved salts becomes higher with temperature. Hence, the use of a constant parameter related to salts effects (λ, Tab. 1) is compensated with the use of the T r .
The correlation proposed in Equation (7) takes into account pressure, temperature and salt effects, as well as the influence of the chemical structure of the CO 2 . Figure 8 shows the modeled γ b,CO 2 using Equation (8) vs the experimental data, under the same conditions. From the regression fit of our experimental results, it is possible to predict the γ b,CO 2 , using only three regression coefficients with a mean deviation of 2.5% and more than 96% of the calculated values below a deviation of 6% from the experimental values.

Visualization Experiments
In order to study the fluid flow and distribution in the porous media for different wettability conditions, glass micromodels were used. The tests were conducted with water-wet, intermediate-wet and oil-wet micromodels. The micromodels were initially fully saturated with water and then flooded with CO 2 under different thermodynamic conditions.  Variation of the interfacial tension of brine-CO 2 systems with density difference.  allows the pore-scale multiphase displacement to be observed and recorded. For this study, the micromodels consist of a porous area of 6.5 cm × 1.25 cm. For the used heterogeneous network the solid surface is represented by round grains, and the fluid path by the space between these grains. The design corresponds to a random grain size and location (Fig. 10).

Experimental Facilities
Glass micromodels are originally water-wet. In order to obtain an intermediate wettability the entire porous medium has been aged with a heavy crude oil. In order to obtain an oil-wet medium we treated the surface with a silane. Details of this treatment can be found elsewhere [36].

Experimental Procedure
The micromodel was initially saturated with distilled water. Then CO 2 was injected at a low rate. The injection rate at all stages was 1cc/h (0.5 PV/h). Experiments were video recorded until the fluid distribution in the porous media was static. At the end of each experiment the micromodel was flushed with distilled water until reaching a 100% water saturation. Then thermodynamic conditions of the set-up were changed for the next experiment. Table 3 presents the thermodynamic conditions of all experiments carried out in this study. These conditions have been chosen in order to be able to visualize the fluid distribution for all the CO 2 physical states: gaseous, liquid and supercritical. A more detailed description of our results, including all images, could be found elsewhere [37].

Water-Wet
In the water-wet experiment we observed that the water is always the wetting fluid. This looks obvious from the shape of the interfaces; it is also possible to draw this conclusion from the existence of very thin water films around the grains (see Fig. 10). Chiquet et al. [13], reported water-CO 2 contact angle values on silica surfaces (quartz and mica). By means of contact angle measurements, the authors showed that the  water-wettability of minerals representative of shales, such as mica and quartz, is significantly altered by the presence of CO 2 , under pressures representative of geological storage conditions (100 bars). Therefore, those minerals, known to be strongly water-wet in the presence of oil, turn out to be intermediate-wet in the presence of dense CO 2 . The authors explain this change in wettability using the DLVO theory [38]. According to this theory, the stability of the water films on the solid surface (an indicator of the wettability) can be estimated from van der Waals and double layer forces. According to Chiquet [14], the change in double-layer forces is due to a reduction in the pH of water phase, which is a consequence of CO 2 dissolution into water. This makes the water film unstable, so altering the wettability of the system. Our study has not been performed with the planar substrates, however being all silica surfaces a comparison should be possible. At the pore scale we do not see any significant alteration in the wettability while increasing the pressure of the system. We observe similar shape of the interfaces, as well as the existence of thin water films around the solid surface for gaseous (low density) as well as for liquid or supercritical (high density) CO 2 . This indicates that for all these experiments the system could be considered as strongly water-wet. For all our experiments, none of the two phases was observed as a dispersed phase in the porous media. Both phases were well connected. One factor that could explain the differences of our results compared with those of Chiquet, is fluid phase equilibriums, which have a significant impact on interfacial properties.

Intermediate-Wet
In the intermediate-wet conditions the fluid distribution depends strongly on Pressure and Temperature conditions. At low pressure and low temperature, P = 60 bars and T = 25 °C, some interfaces show a strong water-wet behavior (analogous to that showed in Fig. 10). Other interfaces have a contact angle close to 90°which corresponds to an intermediate-wet behavior. These differences could be explained from a nonuniform efficiency of the wettability alteration process. At this scale no water or CO 2 film has been observed. In some areas, the water phase does not seem to be connected, however it is tough to say if it is a dispersed phase because water saturation is still important. Figure 15 shows a CO 2 flooding at P = 100 bars and T = 60°C. Figure 11 shows a CO 2 flooding at P = 100 bars and T = 25°C. Under these conditions, most of the interfaces show that the wetting fluid is the CO 2 instead of the water. The water saturation is very low and it is clear that the water phase is present only as a dispersed phase. This wetting   behavior of CO 2 was also observed at the same pressure but a higher temperature (P = 100 bars and T = 60°C). At this temperature we have not observed the water as a dispersed phase as observed at T = 25 °C. This wetting behavior of the CO 2 could be explained from the solubility of CO 2 into water, which leads to a lower pH value of the aqueous phase. This affects negatively the stability of any water film present on the solid surface [13]. Chiquet et al. [14] have shown this effect by modeling experimental contact angles, using the DLVO theory. This CO 2 behavior should be stronger for an altered surface because of a lower affinity to water. Nevertheless, considering all the assumptions, this modeling should not be seen as predictive. As has been showed by Chang et al. [39] the solubility is considerably higher for low temperatures. This could explain the difference in wettability and distribution of the phases between our results at 100 bars and temperatures of 25 °C and 60°C

Oil-Wet
Observations for the oil wet micromodels are analogous to those for the intermediate wet as shown in Figure 12. The reason why there is not a stronger CO 2 wettability for the oilwet micromodel, is probably related to a low efficiency of the treatment (silanization).

Core Experiments -Rock and Fluid Properties
To investigate the influence of wettability on CO 2 /brine displacement, parallel to the pore-scale micromodel experiments, coreflood displacements were conducted. All the experiments were performed on a limestone sample. It was selected for its good level of homogeneity at the core scale. This is highly important when results of core flooding data, conducted at different conditions, have to be compared. The main properties of this sample are gathered in Table 4. A mercury porosimetry curve obtained on an end-cut of the sample and the NMR T2 response of the sample indicated that the pore distribution exhibited a mono-modal behavior. An initial P c curve was also estimated from the mercury porosimetry curve, using the Leverett function. An immiscible gas/water k r curve was obtained by the UnSteady-State method, while performing an history match of the experimental data with a 1-D numerical simulator. A Pore Network Model (PNM) approach [40] was also applied to double check that these k r and P c curves were representative of the rock-type of the sample. Table 5 presents the injecting fluid, N 2 or CO 2 , and the operating conditions of each coreflood experiment. Wettability indices were deduced from P c curves obtained by centrifuge. The indices were calculated using the USBM method. As seen in Table 5, in one case the sample is strongly water-wet and in the other cases it is intermediatewet. The intermediate wettability was obtained while aging the sample in crude oil at 60°C during one month.
The used brine was composed of 5 g/L NaCl.

Coreflood Experiments
In order to obtain P c data at different wettability states CO 2 and N 2 multi-rate injections were performed in the selected sample. These UnSteady-State coreflood were performed in drainage, at reservoir conditions (Tab. 5). The local saturation of both phases was recorded continuously. For the interpretation of the experiments, the heterogeneous approach was applied. More information about the heterogeneous approach can be founded elsewhere [41]. Figures 13, 14 and 15 present the P c curves obtained for each core flooding. Figure 13 shows that the experimental P c data match the P c curve derived from the mercury porosimetry curve (using the Leverett function for a contact angle of 0°), especially for the low and medium flow rates. Hence, at reservoir conditions, the obtained P c data indicates a strongly water-wet system for an initially water-wet sample. In Figure 14, the same behavior can be observed, but in this case, with an intermediate-wet sample. Therefore, according to the P c , N 2 does not wet the rock surface, even if the rock has an intermediate wettability. The case of a CO 2 injection in the intermediate-wet sample (Fig. 15) is different: it is necessary to use a contact angle of 55°, in the Leverett function, to match the experimental values. This indicates that for an intermediate-wet sample, the CO 2 partially wets the solid surface. These data are coherent with the visual experiments presented previously in this paper. Nevertheless, it is interesting to notice that at the macro scale (sample scale, i.e. Darcy scale), the wetting behavior of the CO 2 seems to be less important compared to the one observed at the pore scale (micromodels). A similar trend can be identified while comparing the contact angle evolution reported by Chiquet et al. [13] with the results obtained in this study at the pore scale (see Sect. 2). The contact angle measurements suggest a change in wettability of the systems while increasing pressure. At a larger scale, the pore scale, some changes were observed in the distribution of the phases and in the shape of the interfaces, but the media seemed to keep water wettability while increasing pressure.

Results and Discussion
In Figures 13 to 15, at the highest rate, a deviation exists between the values obtained at reservoir conditions and the curve derived from the Purcell data. In these experiments, the injected CO 2 or N 2 is limited by the volume of the CO 2 or N 2 cell (1 liter). It means that for a rate of 100 cm 3 /h, there is always the risk to have to stop the experiment before the system has reached a complete stabilization, both in the cumulative brine production and in the pressure drop. In order to verify the hypothesis that this deviation is, at least partly, due to a stabilization problem, the pressure drop was extrapolated to longer times, using an exponential law. This was done for the N 2 injection experiments because of the availability of more data points at the higher rate, compared to the experiments with CO 2 . Figure 16 (to be compared to Fig. 14) shows a good agreement between the Purcell curve, the experimental (5 cc/h and 25 cc/h) and extrapolated (100 cc/h) data. The deviation was effectively due to a stabilization issue.        k r curves for the CO 2 core flooding experiments.
For each coreflood, the P c (S g ) values presented in Figures 1 to 16 were introduced into the simulation model as local P c curves, for different sections of the sample, in order to match the heterogeneities observed in the saturation profiles. For the CO 2 injection in a WW sample, Figure 17 shows the good agreement between the measured saturation profiles and the profiles obtained by history match. Figure 17 must be compared to Figure 18 in order to appreciate the degree of improvement in this history matching. Only one iteration was needed to obtain these results. This demonstrates the ability of the pressure data to account for the heterogeneities.

Possible implications of a wetting CO 2 in geological storage
According to the previous pore and core scale observations the CO 2 can wet the surface if this surface is not strongly water-wet. In terms of capillary-sealing efficiency, the effect of a wetting CO 2 at reservoir conditions is detrimental to CO 2 underground storage. Actually, from Equation (3), this implies to lower the threshold value of the capillary pressure. Hence a lower amount of CO 2 could be stored in a given intermediate-wet reservoir, compared to a strongly water-wet one, because of an earlier breakthrough in the caprock.
In terms of CO 2 displacement efficiency, the performed experiments showed a water cumulative production 20% higher for the intermediate-wet scenario compared to the water-wet scenario. Therefore, it is possible to reach higher CO 2 saturations in the reservoir if CO 2 partially wets the rock. This is coherent with the micromodel observations of a water dispersed phase. Figure 19 shows the k r data obtained for each CO 2 core flooding experiment. A higher k rw was obtained for the CO 2 injection in the case of the intermediate-wet sample. Therefore, the higher displacement efficiency cannot only be attributed to a lower P c , but also to a higher mobility of the water phase. k rg curves have also be estimated, but no significant difference has been observed between the WW and IW cases.
The increase in the displacement efficiency could be considered as an advantage for the CO 2 storage in oil depleted reservoirs presenting an intermediate wettability.
But an intermediate wettability could be hardly found in an aquifer.   Figure 17 History matching of the saturation profiles with local P c data. CO 2 injection in a WW sample.

Figure 18
Initial history matching (homogeneous model) of the saturation profiles. CO 2 injection in a WW sample.

CONCLUSIONS
The first part of this paper presents a complete set of experimental values of brine-CO 2 interfacial tension, at pressure and temperature conditions that can be considered as representative of those of a CO 2 storage operation. The objective of this systematic study was to enable estimation of the brine-CO 2 interfacial tension at reservoir conditions, and to evaluate the evolution of this physical property with different reservoir parameters: temperature, pressure and salinity. A correlation has been proposed in order to model IFT values with a low deviation from experimental data. The second part of this paper presents an original experimental study of the impact of wettability on CO 2 storage. Experiments were carried out under representative thermodynamic conditions, at two different physical scales: -the pore scale by means of a qualitative study in glass micromodels; -the core scale by means of a quantitative study in a carbonate sample.
Only the drainage process was investigated in this study. In a limestone rock under reservoir conditions, the CO 2 partially wets the surface when the surface is IW or OW. This wetting behavior of the CO 2 induces a lower capillary pressure and a higher mobility of the brine phase. The observations at the pore scale in glass micromodels are consistent with the results obtained at the core scale concerning the wetting behavior of the CO 2 at reservoir conditions. At the pore-scale the contact angle, the shape of the interfaces and the presence of the water phase as a dispersed phase provide clear evidences of this wettability change. Among the effects of a partial wetting of the CO 2 there is a lower capillary breakthrough pressure of the caprock, as can be deduced from Equation (1). This has negative impact on the capacity of the reservoir, hence on the amount of CO 2 that can be stored.
Future work: the imbibition process has not been evaluated. The knowledge and quantification of the k r hysteresis between the drainage and the imbibition curves is very important to estimate the capillary trapping of CO 2 [42,43]. This issue has been investigated by simulation [43][44][45]. Few experimental relative permeability determinations, specifically for that point, are available. Therefore future experimental work should be done to further investigate drainage and imbibition processes, in order to improve the estimation of the amount of CO 2 that is susceptible to be safely injected.