Osmotic Membrane Distillation Crystallization of NaHCO 3

: A new crystallization process for sodium bicarbonate (NaHCO 3 ) was studied, proposing the use of osmotic membrane distillation crystallization. Crystallization takes place due to the saturation of the feed solution after water evaporation on the feed side, permeating through the membrane pores to the osmotic side. The process operational parameters, i.e., feed and osmotic velocities, feed concentration, and temperature were studied to determine the optimal operating conditions. Regarding the feed and osmotic velocities, values of 0.038 and 0.0101 m/s, respectively, showed the highest transmembrane ﬂux, i.e., 4.4 × 10 − 8 m 3 /m 2 · s. Moreover, study of the temperature variation illustrated that higher temperatures have a positive effect on the size and purity of the obtained crystals. The purity of the crystals obtained varied from 96.4 to 100% In addition, the ﬂux changed from 2 × 10 − 8 to 7 × 10 − 8 m 3 /m 2 · s with an increase in temperature from 15 to 40 ◦ C. However, due to heat exchange between the feed and the osmotic solutions, the energy loss in osmotic membrane distillation crystallization is higher at higher temperatures.


Introduction
Climate change is redirecting global objectives to regulate greenhouse gas emissions. Industry accounts for 21% of these emissions [1] Thus, in order to minimize waste production and its effect on the environment, the design of more efficient processes is required. Many industrial sectors are already focused on lower energy consumption, such as the pharmaceutical industry, food industry, fine chemicals industry, and construction. However, some of their processes are still far from sustainable [2,3]. That is the case for crystallization, a separation technique for producing or purifying solid products from a supersaturated solution. Crystals have high stability, are easy to store, and have a long life. For these reasons, there is an immense requirement for their production from industry [4].
On a larger scale, several principles are used to form crystals, such as cooling of the feed solution, evaporation of the solvent, and anti-solvent techniques. The conventional equipment for performing crystallization is a batch stirred tank, which has several drawbacks. Firstly, the conventional crystallizer cannot provide crystalline solid products of sufficient morphological quality (size, shape, and crystal size distribution), structure (polymorphism), and purity [5]. Secondly, there are some reproducibility issues such as imperfect mixing, where the solution is not homogeneous, and the supersaturation control is limited. Moreover, the points at which crystallization can be performed vary from one batch to another. Furthermore, a great deal of energy is needed either to heat/cool the solution in a conventional evaporator or to power vacuum systems, which are not efficient [6].
In addition, the stirred tank mostly operates as a batch reactor, meaning that the process is not continuous and has to be stopped to recover the products. It would be more convenient and energetically more efficient to use a continuous process [5,[7][8][9]. As conventional crystallizers have many inconveniences, research has been conducted to find alternatives allowing better control and performance during the crystallization process, and membrane distillation crystallization is one of these alternatives [4].
Osmotic membrane distillation crystallization (OMDC) is an innovative technique in which two liquids are brought into contact through a non-selective hydrophobic microporous membrane [10]. Because the concentration is not the same on both sides, this induces a water activity difference and leads to the evaporation of water from the feed to the osmotic side. Thus, the driving force is the vapor pressure gradient created by the water activity difference between the two sides of the membrane. Figure 1 depicts the mass transfer profile for the OMDC system [7,8].
Energies 2022, 15, x FOR PEER REVIEW 2 of 15 batch to another. Furthermore, a great deal of energy is needed either to heat/cool the solution in a conventional evaporator or to power vacuum systems, which are not efficient [6]. In addition, the stirred tank mostly operates as a batch reactor, meaning that the process is not continuous and has to be stopped to recover the products. It would be more convenient and energetically more efficient to use a continuous process [5,[7][8][9]. As conventional crystallizers have many inconveniences, research has been conducted to find alternatives allowing better control and performance during the crystallization process, and membrane distillation crystallization is one of these alternatives [4].
Osmotic membrane distillation crystallization (OMDC) is an innovative technique in which two liquids are brought into contact through a non-selective hydrophobic microporous membrane [10]. Because the concentration is not the same on both sides, this induces a water activity difference and leads to the evaporation of water from the feed to the osmotic side. Thus, the driving force is the vapor pressure gradient created by the water activity difference between the two sides of the membrane. Figure 1 depicts the mass transfer profile for the OMDC system [7,8]. OMDC has advantages over conventional distillation and crystallization processes. This technique has a very high specific contact area, promoting higher mass transfer with more compact equipment than in conventional crystallization or distillation. The main advantage of OMDC is lower energy consumption [11,12]. As the driving force is created through the partial pressure gradient, no additional pressure is required, which allows equipment costs to be reduced and process safety to be increased in comparison with pressure-driven processes. Residual heat or renewable energy can also be used, if available, which could reduce the overall cost and environmental impact [12][13][14]. Another benefit of OMDC is the use of polymer materials in the equipment, which decreases or even avoids erosion problems [4][5][6][7].
OMDC is presented as an alternative option for crystallizing sodium bicarbonate (NaHCO3). NaHCO3 is a salt obtained from a reaction between soda ash and carbon dioxide (CO2) [15,16]. NaHCO3 is used in various industries such as food, pharmaceuticals, agriculture, etc. However, the purity and the morphology of the obtained crystals play an important role in where the NaHCO3 salts can be used. To crystallize NaHCO3 in a conventional crystallizer, CO2 must be introduced to the tank atmosphere as NaHCO3, which can easily be converted to CO2 by heat or stirring [15]. Shifeng Jiang also studied the crystallization of NaHCO3 using a cooling crystallizer to generate more NaHCO3 crystals [17]. However, when using OMDC technology to crystallize NaHCO3, there is no need for the OMDC has advantages over conventional distillation and crystallization processes. This technique has a very high specific contact area, promoting higher mass transfer with more compact equipment than in conventional crystallization or distillation. The main advantage of OMDC is lower energy consumption [11,12]. As the driving force is created through the partial pressure gradient, no additional pressure is required, which allows equipment costs to be reduced and process safety to be increased in comparison with pressure-driven processes. Residual heat or renewable energy can also be used, if available, which could reduce the overall cost and environmental impact [12][13][14]. Another benefit of OMDC is the use of polymer materials in the equipment, which decreases or even avoids erosion problems [4][5][6][7].
OMDC is presented as an alternative option for crystallizing sodium bicarbonate (NaHCO 3 ). NaHCO 3 is a salt obtained from a reaction between soda ash and carbon dioxide (CO 2 ) [15,16]. NaHCO 3 is used in various industries such as food, pharmaceuticals, agriculture, etc. However, the purity and the morphology of the obtained crystals play an important role in where the NaHCO 3 salts can be used. To crystallize NaHCO 3 in a conventional crystallizer, CO 2 must be introduced to the tank atmosphere as NaHCO 3 , which can easily be converted to CO 2 by heat or stirring [15]. Shifeng Jiang also studied the crystallization of NaHCO 3 using a cooling crystallizer to generate more NaHCO 3 crystals [17]. However, when using OMDC technology to crystallize NaHCO 3 , there is no need for the constant addition of CO 2 . Moreover, as the solution is not heated, less NaHCO 3 is converted to CO 2 , which is the main advantage of OMDC for crystallizing NaHCO 3 .
To the best of our knowledge, no studies have been performed on the crystallization of NaHCO 3 using membrane distillation crystallization. However, OMDC has been used for other materials. Israel Ruiz Salmon et al. studied OMDC for the crystallization of sodium carbonate. It was observed that in OMDC, the main resistance was the membrane itself, and the process suffered from concentration polarization and possible wetting [18].
In this study, the main objective was to optimize the OMDC system for the crystallization of NaHCO 3 . Several operational parameters such as the feed and osmotic velocities, the effect of feed concentration, and the feed temperature were studied. Moreover, the purity, shape, and size of the crystals were analyzed using X-ray diffraction (XRD) and scanning electron microscopy (SEM).

Chemicals
The feed solution for each experiment was produced by dissolving NaHCO 3 salt (sodium bicarbonate, ≥99.7%, AnalaR NORMAPUR, Leuven, Belgium) in ultrapure water, and the osmotic solution was obtained by dissolving sodium chloride (NaCl) (sodium chloride, ≥99.9%, AnalaR NORMAPUR, Leuven, Belgium) up to the maximum solubility in ultrapure water.  Table 1. The feed and osmotic solution were in contact with a countercurrent flow. The feed solution flowed on the lumen side and the osmotic solution was on the shell side. The weight of the feed reservoir was measured constantly using a balance (LP 4202I, VWR, Milano, Italy), and is used in Equation (1) for calculating the transmembrane flux and in Equation (2) for the mass transfer coefficient calculation. The feed solution was always kept in a closed-cap container. The feed and osmotic solutions were kept at room temperature for most experiments, except for the temperature study, in which a cooler (Corio CD-900F, Julabo, Seelbach, Germany) and a water bath (VWB2 12L, VWR, Poole, UK) were used to change the temperature in the range of 15 to 40 • C. The temperature was measured using thermocouple thermometers (2000, TME, Birmingham, UK). Scanning electron microscopy (SEM) (GEMINI, Zeiss, Ultra 55) was used to observe the NaHCO3 crystals produced at different feed temperatures. The SEM images studied were taken at 500× magnification with a signal A = E2.

Equipment
X-ray diffraction (XRD) (Bruker, AXS D8 ADVANCE) was used to determine whether the feed temperature altered the crystal purity. First, a metal sputter deposition system (CEA030, Balzers, Liechtenstein) was used to coat the surface with a thin gold layer  Scanning electron microscopy (SEM) (GEMINI, Zeiss, Ultra 55) was used to observe the NaHCO 3 crystals produced at different feed temperatures. The SEM images studied were taken at 500× magnification with a signal A = E2.
X-ray diffraction (XRD) (Bruker, AXS D8 ADVANCE) was used to determine whether the feed temperature altered the crystal purity. First, a metal sputter deposition system (CEA030, Balzers, Liechtenstein) was used to coat the surface with a thin gold layer to produce a conductive surface. Subsequently, the analyses were performed with a LYNXEYE detector, with a 2Theta from 20 • to 100 • .

Overall Mass Transfer Coefficient and Transmembrane Flux Calculation
Two parameters allow characterization of the operating conditions of the membrane system, namely, the transmembrane flux (J, m 3 /m 2 ·s) and the overall mass transfer coefficient (K ov , m 3 /m 2 ·Pa.s). J was calculated by measuring the weight of the feed tank over time and recorded in intervals of 20 min. The flux shown in the figures is an average of the fluxes during the experiment, calculated by Equation (1) [12,19,20].
For calculating K ov , the following relation is used [12,19,20]: In this equation, p* and a are the vapor pressure and the activity coefficient of the feed (f ) and osmotic (o) sides, respectively, which were computed following the procedure described by Hamer et al. [21] and by Sandler [22] when the values of the osmotic coefficients were not found in the literature [23]. The vapor pressure (mmHg) was calculated using Antoine's equation, with the temperature T given in • C: where a w is the sum of the ions of the electrolyte (−), M m is the molar mass of water (kg/mol), M is the molality (mol/kg), and a w is the water activity.

Influence of the Fluid Dynamics
Improving the mass transfer is the key to having a lower required contact area and reducing capital costs. There are three resistances to mass transfer in the OMDC system: the feed boundary layer, the membrane, and the osmotic boundary layer. An increment in the velocity has a positive effect on reducing the lumen-and shell-side boundary resistances and increasing K ov . Figures 3 and 4 show the flux and K ov versus the change in the osmotic/feed velocities, respectively, while the velocity at the other side was set at a constant value. In addition to the boundary resistances, membrane crystallization is significantly affected by the phenomenon of concentration polarization (e.g., when the concentration of the salt is higher on the surface of the membrane), and therefore higher velocities in the membrane are more suitable, since they result in higher turbulence and thus better mixing of the solution in the membrane contactor. However, it can be observed in Figure 3a that overall, the feed velocity presents a maximum flux at 0.04 m/s when the osmotic solution operates at 0.01 m/s. At higher velocities of the feed solution, there is a decrease in flux. This decrease might be because of partial wetting of the membrane pores. As previously reported [17], wetting of the pores results in a lower flux and a higher resistance to mass transfer. In Figure 3b, with increasing feed velocity, K ov decreases slightly, reinforcing the idea of potential membrane wetting. The error bars for the feed flow rate of 0.01 m/s are around 13%. Regarding the osmotic velocity, K ov increases slightly when a higher velocity is used, which is an indication of more turbulence on the osmotic side and lower resistance to mass transfer. It can be observed in Figure 4a that in general, there is a rise in flux with an increase in the osmotic velocity. The maximum flux was observed at an osmotic velocity of 0.01 m/s. In Figure 4b, K ov increases when the feed flow rate is higher, to overcome the resistance in the osmotic boundary layer. However, there is a drop after 0.015 m/s due to possible membrane wetting. It can be concluded that the effect of the osmotic flow rate is higher than that of the feed flow rate, and it is more favorable to have a higher osmotic flow rate than a lower feed flow rate to avoid membrane wetting.

Influence of the Fluid Dynamics
Improving the mass transfer is the key to having a lower required contact area and reducing capital costs. There are three resistances to mass transfer in the OMDC system: the feed boundary layer, the membrane, and the osmotic boundary layer. An increment in the velocity has a positive effect on reducing the lumen-and shell-side boundary resistances and increasing Kov. Figures 3 and 4 show the flux and Kov versus the change in the osmotic/feed velocities, respectively, while the velocity at the other side was set at a constant value. In addition to the boundary resistances, membrane crystallization is significantly affected by the phenomenon of concentration polarization (e.g., when the concentration of the salt is higher on the surface of the membrane), and therefore higher velocities in the membrane are more suitable, since they result in higher turbulence and thus better mixing of the solution in the membrane contactor. However, it can be observed in Figure 3a that overall, the feed velocity presents a maximum flux at 0.04 m/s when the osmotic solution operates at 0.01 m/s. At higher velocities of the feed solution, there is a decrease in flux. This decrease might be because of partial wetting of the membrane pores. As previously reported [17], wetting of the pores results in a lower flux and a higher resistance to mass transfer. In Figure 3b, with increasing feed velocity, Kov decreases slightly, reinforcing the idea of potential membrane wetting. The error bars for the feed flow rate of 0.01 m/s are around 13%. Regarding the osmotic velocity, Kov increases slightly when a higher velocity is used, which is an indication of more turbulence on the osmotic side and lower resistance to mass transfer. It can be observed in Figure 4a that in general, there is a rise in flux with an increase in the osmotic velocity. The maximum flux was observed at an osmotic velocity of 0.01 m/s. In Figure 4b, Kov increases when the feed flow rate is higher, to overcome the resistance in the osmotic boundary layer. However, there is a drop after 0.015 m/s due to possible membrane wetting. It can be concluded that the effect of the osmotic flow rate is higher than that of the feed flow rate, and it is more favorable to have a higher osmotic flow rate than a lower feed flow rate to avoid membrane wetting.  Another set of experiments was performed to check whether there was total membrane wetting. This would be the case if NaCl was found in the feed solution. Ultrapure water was placed in the feed container, and the conductivity of the feed was measured over time with a conductivity meter. It was concluded that there was a high mass transfer of NaCl salts to the feed container at high velocity. For example, when the feed and osmotic velocities were 0.078 and 0.02 m/s, respectively, the conductivity of the ultrapure placed in the feed container, and the conductivity of the feed was measured over time with a conductivity meter. It was concluded that there was a high mass transfer of NaCl salts to the feed container at high velocity. For example, when the feed and osmotic velocities were 0.078 and 0.02 m/s, respectively, the conductivity of the ultrapure water changed from 13 µS/cm to 32 mS/cm within 2 h. This also confirms the hypothesis of partial membrane wetting at higher flow rates. Thus, velocities of 0.038 m/s (200 mL/min) for the feed side and 0.01 m/s (~200 mL/min) for the osmotic side were chosen as the optimal conditions, leading to a high K ov without significant membrane wetting. These velocities were set as constant values for the rest of the experiments described in the following sections. Figure 5 shows the flux and K ov versus the change in NaHCO 3 concentration. The average flux decreases with an increase in concentration. This is due to a decrease in the driving force. In osmotic membrane crystallization, the driving force for water evaporation is the vapor pressure difference between the two sides of the membrane, which is influenced by the water activity. To promote flux, the driving force must be increased. This can be achieved either by increasing the osmotic concentration or by decreasing the feed concentration. An increase in the osmotic concentration implies a lower water activity, while a decrease in the feed concentration induces a lower water activity. Globally, this results in a higher driving force [7]. Therefore, we expect to see a drop in flux with an increase in feed concentration, as can be observed in Figure 5a. By calculating K ov using Equation (2), the effect of the driving force will be removed, and a constant K ov is expected with a change in concentration. However, it can be observed in Figure 5b that K ov still decreases with an increase in the concentration. The factor that causes K ov to decrease could be concentration polarization.

Influence of the Feed Temperature
The temperature of the feed solution was varied in a range between 15 °C and 40 °C, while the osmotic temperature was kept at 20 °C, equivalent to room temperature (see the evolution of temperatures shown in Appendix A). This study was limited to 40° by the membrane contactor characteristics. To investigate the effect of feed temperature on the flux and the overall mass transfer coefficient, experiments were conducted with a feed concentration of 0.8 mol/L (67.2 g/L) and an osmotic concentration of 6.16 mol/L (360 g/L). The feed flow rate and the osmotic flow rate were at their optimal values for this system. The results are presented in Figure 6. When the feed temperature increases, the flux increases due to the vapor pressure difference created by the temperature difference and the concentration difference across the membrane at the same time. After some time of operation, the feed solution and the osmotic solution reach the same temperature, since the two streams are recirculated in the experimental setup. The membrane contactor acts as an excellent heat exchanger between the feed and osmotic solutions, which unfortunately is not the desired effect, since most of the energy is lost in heating the osmotic solution rather than evaporating the water in the feed. Thus, it is more efficient if a mem-

Influence of the Feed Temperature
The temperature of the feed solution was varied in a range between 15 • C and 40 • C, while the osmotic temperature was kept at 20 • C, equivalent to room temperature (see the evolution of temperatures shown in Appendix A). This study was limited to 40 • by the membrane contactor characteristics. To investigate the effect of feed temperature on the flux and the overall mass transfer coefficient, experiments were conducted with a feed concentration of 0.8 mol/L (67.2 g/L) and an osmotic concentration of 6.16 mol/L (360 g/L). The feed flow rate and the osmotic flow rate were at their optimal values for this system. The results are presented in Figure 6. When the feed temperature increases, the flux increases due to the vapor pressure difference created by the temperature difference and the concentration difference across the membrane at the same time. After some time of operation, the feed solution and the osmotic solution reach the same temperature, since the two streams are recirculated in the experimental setup. The membrane contactor acts as an excellent heat exchanger between the feed and osmotic solutions, which unfortunately is not the desired effect, since most of the energy is lost in heating the osmotic solution rather than evaporating the water in the feed. Thus, it is more efficient if a membrane with a lower heat conductivity is used. Unlike the flux, the mass transfer coefficient decreases when the temperature increases, which could be explained by the presence of the temperature polarization effect. These phenomena were also observed by Salmon et al. [18] and by Boubakry et al. [24]. evolution of temperatures shown in Appendix A). This study was limited to 40° by the membrane contactor characteristics. To investigate the effect of feed temperature on the flux and the overall mass transfer coefficient, experiments were conducted with a feed concentration of 0.8 mol/L (67.2 g/L) and an osmotic concentration of 6.16 mol/L (360 g/L). The feed flow rate and the osmotic flow rate were at their optimal values for this system. The results are presented in Figure 6. When the feed temperature increases, the flux increases due to the vapor pressure difference created by the temperature difference and the concentration difference across the membrane at the same time. After some time of operation, the feed solution and the osmotic solution reach the same temperature, since the two streams are recirculated in the experimental setup. The membrane contactor acts as an excellent heat exchanger between the feed and osmotic solutions, which unfortunately is not the desired effect, since most of the energy is lost in heating the osmotic solution rather than evaporating the water in the feed. Thus, it is more efficient if a membrane with a lower heat conductivity is used. Unlike the flux, the mass transfer coefficient decreases when the temperature increases, which could be explained by the presence of the temperature polarization effect. These phenomena were also observed by Salmon et al. [18] and by Boubakry et al. [24].  The results of previous studies on membrane crystallization are presented in Table 2, for comparison with the results obtained in this study. It can be observed that the flux obtained in this work was in good agreement with the values obtained with the same type of hollow fibers but was inferior to the flux obtained in bigger membrane contactors. The fact that most of the studies did not report the mass transfer coefficient is a critical limitation, in terms of making a fair comparison. Sparenberg et al. [20] used the same type of membrane contactor for direct contact and vacuum membrane crystallization. The vacuum membrane crystallization had a higher flux in comparison to OMCD and DCMD, as the heat losses during the process were lower. The same applied to K ov : the values obtained in previous studies using the same type of hollow fibers were near the values obtained in this study, ranging from 4.8 × 10 − 11 m 3 /m 2 ·Pa·s to 6.53 × 10 − 11 m 3 /m 2 ·Pa·s.

Crystalline Phases
Commercial crystals were observed via SEM for comparison with the crystals produced at 15, 20, 30, 35, and 40 • C. The images produced via SEM are shown in Figure 7a-f. Commercial sodium bicarbonate is a powder consisting of flat sheet crystals with no preferential shape, while the crystals produced by membrane distillation crystallization were in the form of squares, sticks, and other shapes. The shape of the crystals obtained in this study was similar to that of crystals obtained in the literature using other novel crystallization processes. Therefore, the effect of OMDC on the shape of the crystals was not significant [17,29,30]. The temperature influenced the morphology and the size of the crystals, giving bigger crystals at 35 • C. This is due to the fact that temperature has a great effect on the nucleation and growth rate of crystals [16]. The experiment at 35 • C gave larger crystals. This experiment was repeated four times, and it was observed that on two occasions the crystal size was similar to the size in the experiment at 40 • C, while on the other two occasions bigger crystals were obtained. For this reason, the average size should be taken carefully. This is due to the effect that temperature, or the residence time of the crystals in the tank, has on the nucleation and growth rate of crystals. The crystal size obtained in this study agreed with the crystal size obtained by Adnan Abdel-Rahaman et al. [31]. To find an optimal temperature, higher temperatures may have to be tested, but this was not possible in this study due to the thermal limitations of the material of the module.

Crystalline Phases
Commercial crystals were observed via SEM for comparison with the crystals produced at 15,20,30,35, and 40 °C. The images produced via SEM are shown in Figure 7a-f. Commercial sodium bicarbonate is a powder consisting of flat sheet crystals with no preferential shape, while the crystals produced by membrane distillation crystallization were in the form of squares, sticks, and other shapes. The shape of the crystals obtained in this study was similar to that of crystals obtained in the literature using other novel crystallization processes. Therefore, the effect of OMDC on the shape of the crystals was not significant [17,29,30]. The temperature influenced the morphology and the size of the crystals, giving bigger crystals at 35 °C. This is due to the fact that temperature has a great effect on the nucleation and growth rate of crystals [16]. The experiment at 35 °C gave larger crystals. This experiment was repeated four times, and it was observed that on two occasions the crystal size was similar to the size in the experiment at 40 °C, while on the other two occasions bigger crystals were obtained. For this reason, the average size should be taken carefully. This is due to the effect that temperature, or the residence time of the crystals in the tank, has on the nucleation and growth rate of crystals. The crystal size obtained in this study agreed with the crystal size obtained by Adnan Abdel-Rahaman et al. [31]. To find an optimal temperature, higher temperatures may have to be tested, but this was not possible in this study due to the thermal limitations of the material of the module. analyzed were NaHCO 3 crystals obtained after membrane crystallization distillation at 15,20,30,35, and 40 • C for the feed solution. A comparison of the different XRD spectra is shown in Figure 8. As previously reported [32,33], all the spectra compared showed peaks at 29.7,35.4,and 40.8 (2Theta), attributed to the NaHCO 3 crystal phase. XRD analysis was performed on various bicarbonate crystals. The first was the original sodium bicarbonate powder from the industrial supplier. The second to the sixth samples analyzed were NaHCO3 crystals obtained after membrane crystallization distillation at 15,20,30,35, and 40 °C for the feed solution. A comparison of the different XRD spectra is shown in Figure 8. As previously reported [32,33], all the spectra compared showed peaks at 29.7,35.4,and 40.8 (2Theta), attributed to the NaHCO3 crystal phase. The purity of the crystals obtained was in a range between 96.4 and 100%. While the crystals obtained at 30° had the lowest purity, showing a composition of 96.4% pure Na-HCO3 and 3.6% hydrated Na2CO3, the highest purity was observed at 20, 35, and 40 °C, with crystals of 100% NaHCO3. The quantitative analysis of purity is included in Appendix B. As observed by Wang et al. [34], two factors influence the decomposition process of NaHCO3 to Na2CO3 + CO2 + H2O: temperature and water activity. The change in water activity is sensitive to both temperature and the composition of the liquid. The variation in the purity of the crystal can be explained by the membrane system's energy losses while heating the osmotic solution. This produces a slight variation along the membrane that can induce decomposition of NaHCO3 to Na2CO3. The purity of the crystals obtained was in a range between 96.4 and 100%. While the crystals obtained at 30 • had the lowest purity, showing a composition of 96.4% pure NaHCO 3 and 3.6% hydrated Na 2 CO 3 , the highest purity was observed at 20, 35, and 40 • C, with crystals of 100% NaHCO 3 . The quantitative analysis of purity is included in Appendix B. As observed by Wang et al. [34], two factors influence the decomposition process of NaHCO 3 to Na 2 CO 3 + CO 2 + H 2 O: temperature and water activity. The change in water activity is sensitive to both temperature and the composition of the liquid. The variation in the purity of the crystal can be explained by the membrane system's energy losses while heating the osmotic solution. This produces a slight variation along the membrane that can induce decomposition of NaHCO 3 to Na 2 CO 3 .

Conclusions
Osmotic membrane distillation crystallization (OMDC) is a novel technology considered as an alternative to conventional crystallizers. OMDC has been studied for crystallization of sodium bicarbonate, due to its advantages such as lower energy and material consumption, control over the operational parameters, and larger evaporation surface area, among others. Several parameters such as the feed and osmotic velocities, feed concentration, and feed temperature were optimized. Regarding the feed and osmotic velocities, as the velocity increases the possibility of membrane wetting increases significantly. Therefore, a feed velocity of 0.078 m/s and an osmotic velocity of 0.01 m/s were chosen as the optimal conditions, which resulted in obtaining a K ov of 5.4 × 10 − 11 m 3 /Pa·m 2 ·s. In addition, since the driving force in OMDC is the difference in concentration, an increase in feed concentration reduces the driving force and results in a reduction in the flux. However, when studying K ov and removing the driving force effect, the process was found to be affected by concentration polarization, and K ov still decreased by 23.6%. Finally, the effect of the temperature on water evaporation showed that the driving force of the system increased with temperature, as the flux increased from 2.45 × 10 −8 to 7.49 × 10 −8 m 3 /m 2 ·s, but a great deal of energy was lost via the heat exchange between the feed and osmotic solutions. It was also observed that the size and the purity of the crystals were affected by the temperature, with larger sizes and higher purities obtained at higher temperatures.

Patents
The process presented here is registered under the patent application EP 2021163.

Conflicts of Interest:
The authors declare no conflict of interest.

Appendix A
effect of the temperature on water evaporation showed that the driving force of the system increased with temperature, as the flux increased from 2.45 × 10 −8 to 7.49 × 10 −8 m 3 /m 2 ·s, but a great deal of energy was lost via the heat exchange between the feed and osmotic solutions. It was also observed that the size and the purity of the crystals were affected by the temperature, with larger sizes and higher purities obtained at higher temperatures.

Patents
The process presented here is registered under the patent application EP 2021163.            Figure A6. XRD quantitative analysis for crystals produced at 40 • C.