Browsing by Author "Tomson, Mason"
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Item A New Kinetic Assay Method for Effective Scale Inhibitor Concentration Determination with Low Detection Limit(SPE, 2022) Dai, Zhaoyi; Ko, Saebom; Wang, Xin; Dai, Chong; Paudyal, Samridhdi; Zhao, Yue; Li, Wei; Leschied, Cianna; Yao, Xuanzhu; Lu, Yi-Tsung; Kan, Amy; Tomson, MasonScale inhibitors are widely used for mineral scale control in various industries, including oil and gas productions, geothermal energy acquisitions, and heat exchanger scale control to mention a few. In most applications, these scale inhibitors are effective at substoichiometric concentrations (e.g., 1 mg/L or lower), and the optimization of these applications is based on the ability to accurately measure the effective inhibitor concentration at such low concentrations. For example, the continuous treatment injection rate, the squeeze treatment frequency, or the batch treatment schedule need to be optimized to ensure the minimum inhibitor concentration (MIC) is achieved during production. However, the non- or low-phosphorous polymeric scale inhibitor concentration determination is difficult using inductively coupled plasma (ICP)-optic emission spectroscopy/mass spectrometry or ion chromatography, especially at mg/L level concentrations due to their high detection limits. The recently developed hyamine method or high-pressure liquid chromatography (HPLC) method involves intensive labor and high costs. Furthermore, in the complex oilfield operational conditions, the presence of other chemicals (e.g., surfactants, biocides, and corrosion inhibitors), the potential degradation of scale inhibitors and the use of combination scale inhibitors require the measurement of effective scale inhibitor concentration, which cannot be accomplished by the traditional methods. In this study, a new kinetic assay method has been developed to determine the effective scale inhibitor concentration with limits of detection (LODs) less than or around 0.1 mg/L for most cases. This method uses a continuous stirring tank reactor (CSTR) apparatus and is developed based on the linear correlation between the effective inhibition concentration and the measured critical time when laser signal changes. The results show that the inhibitor concentrations of various non- or low-phosphorous polymeric scale inhibitors in synthetic field brine, laboratory solutions, and real oilfield brines can be accurately determined at mg/L level, or lower, with less than 10% error. The method is robust, accurate, and much less time- or labor-consuming than other existing methods especially for non- or low-phosphorous polymeric scale inhibitors.Item Foam rheology of zwitterionic anionic blends in porous media(2016-03-30) Muthuswamy, Aarthi; Hirasaki, George; Miller, Clarence; Verduzco, Rafael; Biswal, Lisa; Tomson, MasonBlending of certain types of surfactants is known to promote synergism as studied by bulk measurements. This study analyzes if such synergistic interactions are beneficial for foam rheology in porous media. Foam experiments were conducted systematically in porous media, at different ratios of zwitterionic and anionic surfactants, both in the presence and absence of crude oil. Interfacial studies were conducted to explain the behavior of surfactant mixtures with respect to foam rheology in porous media. The zwitterionic surfactants used in this study were C12 straight chain betaine- Lauryl betaine (LB), C12 straight chain sultaine- Lauryl sultaine (LS), C18 tailed amido betaine (Rhodia A), C 18-22 tailed amido sultaine (Rhodia B), C 18-22 tailed amido betaine - with more C 22 (Rhodia C) and C 18-22 tailed amido betaine -with more C18 (Rhodia D). LB and LS surfactants had a viscosity close to that of water ~1 cP at room temperature. On the other hand 0.5 wt% of Rhodia A, Rhodia B, Rhodia C and Rhodia D were viscoelastic and shear thinning fluids due to the presence of wormlike micelles. Rheological studies which were conducted at room temperature revealed that salinity had a prominent effect on Rhodia A. On increasing salinity from ~ 4% to 12%, the relaxation time of Rhodia A increased by three orders of magnitude, thereby causing the weakly viscoelastic surfactant solution to change to a strongly viscoelastic solution. On the other hand salinity had a negligible effect on Rhodia B, Rhodia C and Rhodia D. When 1 wt% surfactant solutions of Rhodia A, B, C or D were mixed with ~ 35% synthetic crude oil (mass basis), all surfactant solutions lost viscosity and viscoelasticity except Rhodia C. Crude oil had an adverse effect on Rhodia A perhaps due to the conversion of wormlike micelles to spherical micelles. Rhodia B and D had lower elastic and viscous moduli most likely due to the shortening of the wormlike micelles. Additional tests were done to study the flow of these complex fluids in a 100 Darcy silica sand pack. Rhodia A, B and D showed no elongational effects during flow in porous media. Their shear thinning apparent viscosities in porous media were very close to the rheometric data in shear flow. Rhodia C exhibited yield stress behavior and hence could not be injected in a porous medium. Zwitterionic surfactants Rhodia A/LB/LS were blended with anionic Alpha Olefin Sulfonate AOS 14-16 (AOS) surfactant at specific ratios - one with high and one with low bulk mass ratio of zwitterionic to anionic. Rhodia A which was weakly viscoelastic by itself, when blended with AOS in the ratio 9:1 respectively (by mass) produced a strongly viscoelastic solution. Nitrogen foam experiments were conducted in 100 Darcy silica sand at 25° C for Rhodia A and AOS blends and, in Bentheimer sandstone cores at 45° C, for LB/AOS blends and LS/AOS blends. Zwitterionic surfactants of this type have been reported to be “foam boosters” for bulk foams when added to anionic surfactant. Rhodia A betaine was a weak foamer both in the presence and absence of oil. However when blended with AOS (9:1 ratio), its foam strength significantly improved in the absence of oil. In the presence of oil the viscoelastic surfactant helped generate strong foam in fewer pore volumes (PVs- a dimensional unit of time) but took a longer time than AOS to propagate through the sand pack. In the case of LB/AOS and LS/AOS surfactant systems, the zwitterionic (LB, LS) foam by itself was weak, but AOS and the blends of zwitterionic and AOS had strong foam with comparable foam rheology. The regular solution theory approach of Rubingh combined with Rosen’s application to water-air film interfaces and its adaption to oil-water interfaces was applied to understand this behavior, especially the high foam strength observed when the poor-foaming zwitterionics were added to the strong foamer AOS. It was found that the zwitterionic-anionic blends exhibited synergistic interactions. The Gibbs surface excess calculations suggested that the synergistic interactions promoted tighter packing at the interface thereby helping the poorly foaming zwitterionic surfactant to exhibit strong foam rheology in porous media. Interestingly, AOS surfactant by itself had tight packing at the interface. The trends observed in porous media were well explained by the Gibbs surface excess calculations. However, the synergism did not lead to improvement in foam performance in porous media beyond that seen for AOS alone. Additionally foam strength in the presence of water flood residual oil was weak for the pure zwitterionic surfactants, but the blends with higher mole fraction of AOS and pure AOS had comparable foam performance. Again AOS by itself was able to achieve good mobility control in displacing residual oil. The addition of zwitterionic surfactant had apparently not boosted the foam performance of AOS in porous media in the presence of oil as well. Interfacial shear rheology for the LB/AOS and LS/AOS systems were performed and it showed that none of the surfactants possessed interfacial shear viscosity. Qualitative film drainage studies were conducted and it was observed that a small addition of LB to AOS helped in creating very stable black film and substantially increased the longevity of the film more than AOS itself. However all these thin film studies failed to offer any explanation to porous media foam studies but perhaps help develop an understanding on bulk foam studies. In the case of Rhodia A:AOS 9:1 viscoelastic blend, an injection strategy can be proposed where in a small slug of A:AOS 9:1 blend can be injected which can aid in quicker foam generation followed by a large AOS slug which can help in faster propagation and hence more efficient oil recovery. Anionic AOS 14-16 surfactant did not need a foam booster contrary to the opinion in literature that a betaine surfactant (coco amido propyl betaine) is needed to boost the foam strength of an anionic surfactant (AOS 16-18) in the presence and absence of crude oil in porous media.Item Impact of Fe(II) and Fe(III) on scale inhibitor: application to scale control in oil and gas systems(2017-04-19) Zhang, Zhang; Tomson, MasonThe effect of Fe(II) on the performance of barite scale inhibitors was tested using an improved anoxic testing apparatus. Inhibitors were tested with from 1 to 50 mg/L Fe(II) at 70oC and near neutral pH conditions. Most scale inhibitors show good Fe(II) tolerance at experimental conditions, while some phosphonates based scale inhibitors were significantly impaired by Fe(II). The formation of insoluble precipitates between Fe(II) and phosphonate is very likely the reason behind this detrimental effect. Fe(III) can significantly impair the performance of all scale inhibitors even at extremely low concentrations. However, the mechanism of this detrimental effect has not been studied. In this research, an analytical ultracentrifuge was utilized to separate ferric hydroxide nanoparticles from the aqueous phase. Scale inhibitor concentration in the aqueous and particle phases were measured and compared with barite induction time data. The mechanism of Fe(III) effect on scale inhibitor was experimentally shown a result of adsorption of scale inhibitor onto ferric hydroxide nanoparticles in solution. If inhibitors are added in excess of the adsorption ability of the ferric hydroxide particles, the remaining scale inhibitors in the aqueous phase can still provide inhibition. EDTA and citric acid, two of the most common organic chelating agents used in oilfield, were tested for their ability to reverse the detrimental effect of Fe(III) on scale despite the fact the EDTA is a much stronger chelating agent. The mechanistic difference between EDTA and citrate is discussed.Item Kinetics of BaSO4-BaxSr1-xSO4-SrSO4 mineral crystallization: Prediction and control(2021-09-29) Zhao, Yue; Tomson, MasonMineral crystallization is ubiquitous in various industrial processes. Among all the mineral scales, sulfate minerals, such as barite (BaSO4) and celestite (SrSO4), are commonly discovered during the production. Due to the wide coexistence of Ba2+ and Sr2+, BaxSr1-xSO4 solid solution is also frequently discovered in industrial processes. Scale inhibitors have been widely used as one of the most efficient methods for sulfate scale control. In this work, a systematic study of the crystallization and inhibition kinetics of barite-BaxSr1-xSO4-celestite mineral systems are conducted to have a better knowledge of sulfate scale formation prediction and control. The celestite crystallization and inhibition kinetics is experimentally studied by measuring the induction time of celestite under wide ranges of celestite saturation index (SI = 0.7 – 1.9), temperature (T = 25 – 90 ℃) without and with inhibitors. Based on the experimental results and literature data, a semiempirical and a mechanistic celestite crystallization and inhibition model have been developed based upon readily available parameters such as celestite SI (or other brine compositions) and T. The celestite crystallization and inhibition mechanistic model is developed based on classical nucleation theory (CNT) and polynuclear growth mechanism. The inhibition mechanism behind this model is assumed to be Langmuir type inhibitor adsorption onto nuclei surface and the change of the interfacial energy between the nuclei and the aqueous phase due to the inhibitor adsorption. Good agreements between the experimental results and calculated results with these two models can be found. Both the semiempirical model and the mechanistic model can be applied to predict the minimum inhibitor concentration (MIC) and provide a better celestite scale management strategy. The mechanistic model could also be widely adopted in other disciplines, such as elucidation of the inhibition mechanisms or new scale inhibitors design guidance. The mechanistic model developed is also applied to barite crystallization and inhibition kinetics predictions based on the barite induction time measurements at the conditions of barite SI 0.81 – 3.26 and T 4 to 90 °C with or without inhibitors. The induction times predicted with this newly developed model matches well with the experimental results. The barite mechanistic model could help us further understand the mechanisms of the scale inhibition. The effects of other commonly seen species, silica and the related divalent ion-silicate (Ca, Mg-silicate and Fe(II)-silicate), on barite inhibition were also investigated. It can be found that Fe2+ ions shows detrimental impacts on the phosphonate inhibitor; while the formation of Fe(II)-silicate complex/interactions helps partially recover the detrimental impacts of Fe2+ on phosphonate inhibitors. The studies about barite in this work could help provide a more accurate barite scale management strategy during productions. The induction times of BaxSr1-xSO4 solid solution were also measured without or with scale inhibitors at the conditions of barite saturation index (SI) from 1.5 to 1.8, temperature (T) from 40 to 70 ℃, [Sr2+]/[Ba2+] ratios from 0 to 15 with celestite SI < 0. The results showed that the BaxSr1-xSO4 solid solution's induction time increases with [Sr2+]/[Ba2+] ratio at a fixed experimental condition. Based on the experimental results, a semiempirical Ba-Sr-SO4 solid solution crystallization and inhibition model is firstly developed with good predictions results. Then, to have a better understanding of the mechanisms of BaxSr1-xSO4 solid solution crystallization and inhibition, the non-equilibrium BaxSr1-xSO4 solid solution composition empirical model is developed with the composition measurement results at the conditions of SIbarite from 0.9 to 1.5, [Sr2+]/[Ba2+] molality ratio from 0.33 to 30, temperature (T) from 50 to 90 ℃ and ionic strength (IS) from 0.01 M to 3 M as NaCl. With the composition of the BaxSr1-xSO4 solid solution predicted at a certain experimental condition, the mechanistic model developed for celestite and barite can be extrapolated to BaxSr1-xSO4 solid solution. The properties of the BaxSr1-xSO4 solid solution in the mechanistic model can be calculated with the properties of the pure end member minerals BaSO4 and SrSO4 determined. The BaxSr1-xSO4 solid solution induction time measurement results are used to evaluate the mechanistic model developed. The good agreements between the measured induction time and the calculated induction time with the mechanistic model can be found. The semiempirical and the mechanistic BaxSr1-xSO4 solid solution model proposed will significantly improve the sulfate scale management strategy when Ba2+ and Sr2+ coexist in the oilfield. Furthermore, the mechanistic BaxSr1-xSO4 solid solution model has the potential to be applied to the crystallization and inhibition kinetics predictions of BaxSr1-xSO4 solid solution with any composition or other binary mineral systems due to the sound theoretical basis behind the model.Item Modeling of Mineral Scaling in a West Texas CO2-WAG EOR Field Using Produced Water Analysis and a 1-D Reactive Mixing-Material Balance Coupled Approach(2020-03-09) Mateen, Sana; Tomson, MasonWith decreasing accessible oil and gas reserves, secondary and tertiary modes of EOR (enhanced oil recovery) are increasingly being used. WAG (water alternating with CO2 gas) injection for oil production alters the chemistry of carbonate reservoirs exacerbating the already prevalent issue of mineral scaling in oil field production wellbores, tubing, and surface equipment. In this work, produced water samples from two WAG fields in West Texas experiencing predominantly gypsum and calcite scaling are analyzed. Several analytical methods for measurement of cations (calcium and magnesium) and anions (chloride, sulfate, and alkalinity) are compared. The detection limit for very low-level sulfate measurement in high ionic strength brines using ion chromatography is established. Gypsum and calcite saturation indices are calculated and interpreted at varying field conditions and empirically validated with solid scale sample analysis. As it was determined that scaling occurs in well and tubing prior to already equilibrated water being sampled at surface, a 1-D Reactive Mixing-Material Balance Coupled Model is developed to provide insights on the scaling in the West Texas fields. An aerial streamlining mixing mechanism in which slow moving equilibrated carbonated injection water mixes with faster moving formation water right at the wellbore is deduced to be the in-situ mixing mechanism resulting in the observed scaling at the West Texas field. Based on 12 model runs with 4 different injection water fractions and 3 different analyzed surface sample compositions, 11 out of 12 runs qualitatively validated the observed calcium sulfate and calcium carbonate scaling in the field. In these 11 runs, the model’s predicted surface calcium concentrations differed from measured calcium concentrations by 8.3% to 27%. This study also includes preliminary scale inhibitor testing and scale inhibition recommendations.Item Non-equilibrium BaxSr1-xSO4 solid solution compositions at elevated Sr2+ concentration, ionic strength, and temperature(Elsevier, 2022) Zhao, Yue; Dai, Zhaoyi; Wang, Xin; Dai, Chong; Paudyal, Samridhdi; Ko, Saebom; Li, Wei; Kan, Amy T.; Tomson, MasonThe BaxSr1-xSO4 solid solution is ubiquitously present in both geological and industrial processes, where they mostly form under non-equilibrium conditions. Compared with those formed under equilibrium conditions, the BaxSr1-xSO4 solid solution formed at non-equilibrium condition has significantly higher Sr incorporation at the same aqueous phase compositions. The solid composition of BaxSr1-xSO4 formed at non-equilibrium condition is critical for the study of chemical palaeoceanography as well as the solid solution nucleation and growth kinetics. However, few studies have been conducted to investigate the composition of the BaxSr1-xSO4 solid solution when it precipitates at non-equilibrium conditions. In this study, the distribution coefficient of Ba2+ and Sr2+ between the BaxSr1-xSO4 solid solution and the aqueous phases (KD,Sr-Barite) at non-equilibrium conditions was studied with barite saturation index (SIbarite) from 0.9 to 1.5, [Sr2+]/[Ba2+] molality ratio from 0.33 to 30, temperature (T) from 50 to 90 °C and ionic strength (IS) from 0.01 M to 3 M as NaCl, with celestite being undersaturated. The composition of the BaxSr1-xSO4 solid solution formed at non-equilibrium conditions can then be calculated from the KD,Sr-Barite values. The results show that the KD,Sr-Barite value decreases with the increase of aqueous Sr2+ concentration at fixed SIbarite and T conditions. The IS effect on the KD,Sr-Barite value is small. Based on the experimental results, a new empirical model is developed to accurately predict the measured compositions of BaxSr1-xSO4 solid solution at non-equilibrium conditions under a wide T and IS conditions as follows (the plot of the predicted log10KD,Sr-Barite versus the measured log10KD,Sr-Barite with : Several theoretical models have also been compared against the experimental data. The birth and spread crystal growth model (B + S model) could accurately predict the solid composition of BaxSr1-xSO4 at higher barite SI and/or higher T conditions (barite SI = 1.5 at 70 °C and barite SI = 1.2–1.5 at 90 °C with [Sr2+]/[Ba2+] = 0.33–10). However, the B + S model predictions show larger deviations at lower SI and/or lower T conditions (barite SI = 0.9 and 1.2 at 50 °C and barite SI = 0.9 at 70 °C with [Sr2+]/[Ba2+] = 0.33–10 in this study). For other theoretical models, such as the CNT model and the BCF model, the predicted solid compositions of BaxSr1-xSO4 are significantly higher than the measured results. This quantitative study of the BaxSr1-xSO4 solid solution compositions could help reconstruct oceanic physical conditions and chemistry. It also establishes a solid foundation to further investigate the kinetics of the BaxSr1-xSO4 solid solution formation during non-equilibrium geological and industrial processes.Item Observations of CO2 Corrosion-Induced Carbonate Scale Formation and Inhibition on Mild Steel(SPE, 2022) Li, Wei; Dai, Zhaoyi; Wang, Xin; Ko, Saebom; Paudyal, Samiridhdi; Yao, Xuanzhu; Leschied, Cianna; Shen, Yu-Yi; Pimentel, Daniel; Kan, Amy T.; Tomson, MasonAqueous CO2-containing environment is ubiquitous in oil and gas production. Carbonate scales (e.g., calcite) tend to form in such an environment. Meanwhile, the CO2 corrosion of mild steel infrastructure may result in corrosion-induced scales including siderite (FeCO3). Previously, siderite was generally treated as a corrosion problem rather than a scale problem. However, the relationship between the corrosion-induced scale and other metal carbonate scales on the steel surface is unclear. For example, how does siderite influence calcite deposition on the mild steel? In this study, the mild steel corrosion and mineral carbonate scaling behaviors were investigated simultaneously in the presence of various cations such as Ca2+ and Mg2+. We observed a two-layer scale structure on the mild steel surface under simulated oilfield conditions. The inner layer is an iron-containing carbonate scale such as ankerite or siderite, while the outer layer is calcite. In addition, calcite deposition at a very low saturation index was observed when the inner layer was present. Furthermore, a common scale inhibitor [diethylenetriaminepentakis(methylenephosphonic acid) or DTPMP] can effectively mitigate calcite, siderite, and ankerite formation on the steel surface, but meanwhile, aggravate the steel corrosion because of the absence of protective scale layers.Item Embargo Thermodynamics of Electrolytes: From Infinite Dilution to Concentrated Systems(2022-12-05) Khalil, Yousef; Chapman, Walter G.; Tomson, Mason; Singer, Philip; Asthagiri, Dilip N.Salts are involved in almost everything from biological and geological systems to industrial processes. They can exist in all phases, including in the form of a pure crystal, an aqueous solution, a melt, or even as a vapor of ion pairs. The behavior of ions in solution is specific and depends on the type of ion. However, many complications manifest as we extend beyond that i.e. the limit of infinite dilution (a single ion in water). The complications begin as these specific interactions depend on the type of counter ion, namely, depending on what counter ion is in solution, the ion behaves differently. Furthermore, these interactions are also dependent and change with concentration, limiting researchers' ability to develop an underlying model that can capture and predict their physics. The composition of solvent in the system and temperature both alter the effective dielectric of the system, adding an extra layer of complexity when attempting to investigate practical systems. In this work, utilizing the quasichemical framework, the different components of the hydration free energy were investigated. The hydration free energy was broken down into a short-range ion-specific contribution and a long-range ion-nonspecific contribution. Within the quasichemical approach, the hydration free energy of an ion is decomposed into a chemical term accounting for local, specific ion-water interactions within the coordination sphere and nonspecific contributions accounting for packing (cavity creation) and long-range interactions. The change in the chemical term with a change in the radius of the coordination sphere is the compressive force exerted by the bulk solvent medium on the surface of the coordination sphere. For the ions considered here, Na$^+$, K$^+$, F$^-$, and Cl$^-$, this compressive force becomes equal for equally charged ions of the same sign at short range, namely, at a coordination radii of about 3.5~{$\AA$} for cations and 4.2~{$\AA$} for anions. This includes waters just within the first hydration shell regardless of the sign of charge. For hypothetical ions, i.e. the same ions but with double the charge, Na$^{2+}$, K$^{2+}$, F$^{2-}$ and Cl$^{2-}$ ions, the results were similar with the compressive forces equating at $r \approx 3.5~{\AA}$ for cations and $r \approx 4.2~{\AA}$ for anions. These results show that ion-specific effects, which arise primarily due to differences in the local ion-water interactions, are short-ranged and are limited to the first hydration shell of an ion. Furthermore, investigating the reorganization of the solvent matrix in the presence of the ion indicates that while ion specificity is limited to the first hydration shell, the overall effect of the ion on the solvent matrix extends to the second shell and approaches zero by the third hydration shell. The long-range interactions of the ions, through the force curves, are found to be proportional to the Born hydration model. This finding rationalizes the success of certain approaches of electrolyte modeling such as the Unified Model\cite{djamali_unified_2009} and guides future work. The Mean Ionic Activity Coefficient (MIAC) is of significant interest for practical systems investigations. Previous Molecular simulation studies of MIAC did not consider the effect of polarizability. In this work, we use the AMOEBA model that includes polarizability and describes van der Waals interactions with a Buffered 14-7 potential. We here calculate the MIAC for aqueous NaCl of varying concentrations up to near experimental saturation at 298.15 K and 1 atm. The free energy of hydration of NaCl was calculated by removing a single $Na^+$ or $Cl^-$ from the solution and gradually switching off electrostatic interactions, followed by switching off Buffered 14-7 interaction. Simulating a charge non-neutral system inevitably involves accounting for neutralizing background potential which is accounted for in the free energy calculation. Investigating, system size effects within the AMOEBA model, simulations were performed at multiple system sizes per concentration, the results of which were extrapolated to obtain the free energy if the simulation box was infinite. No significant system size effect was found beyond the lowest concentration of $m = 0.019 ~ mol/kg$. Instead, we find that using the mean value of the free energy from the multiple system size simulation per concentration provided a better estimate of the MIAC. AMOEBA model correctly estimates the experimental MIAC up to the highest concentration simulated. We propose a different method of estimating Henry's law reference standard state free energy, the Self Consistent approach. This self-consistent method provides the ability to estimate the chemical potential if experimental data are lacking. The Individual Ionic Activity Coefficient (IIAC) was also calculated and compared with previously reported work using an empirical force field. Both $Na^+$ and $Cl^-$ show some agreement with the empirical force field results, before deviating at higher concentrations. Investigating both AMOEBA's capability to predict the free energy of hydration of higher valency ions and the temperature dependence of the hydration free energy, we study the Gadolinium ion. Free Energy Perturbation is utilized to calculate the hydration free energy of Gadolinium Chloride in water using the AMOEBA polarizable force field. The hydration free energy was calculated by gradually switching off electrostatic interactions, followed by switching off Buffered 14-7 interaction. Starting with a single ion in a water box or a charge non-neutral system inevitably involves accounting for neutralizing background potential which is accounted for in the free energy calculation. System size effects were accounted for through the Wigner correction. Good agreement of the hydration free energy and its temperature dependence from 298K to 473K at saturation conditions with experimental data reproduced through the unified model was achieved. Hydration free energy at 573K showed deviation from the experimental values by $23\%$, due to AMOEBA predicting a vapor instead of a liquid phase. Findings from this work indicate that calculations with a polarizable force field fitted from ab initio calculations can capture the thermodynamics of ion solvation and its temperature dependence with good agreement.