CO2 Hydrogenation Induced by Mechanochemical Activation of Olivine With Water Under CO2 Atmosphere

Introduction

Fossil fuels are still the primary energy source in the world. However, the energy demand, in continuous growth, has led to increased fuel consumption and then to the release of a huge amount of carbon dioxide, CO₂, into the atmosphere (Koukouzas et al., 2009). It is well-known that CO₂ is the greenhouse gas with the major contribution to global warming. It is also recognized that natural processes cannot absorb all the anthropogenically produced carbon dioxide. As a consequence, the development of new technologies for capture and conversion is urgently required (Falkowski et al., 2000).

Global emissions of CO₂ have been increasing steadily in the past decades and reached values 60% above 1990 levels, when the Kyoto Protocol was stated. In order to limit the global temperature rise, CO₂ emissions should be reduced by at least 50% by 2050 (Stocker et al., 2014; Cuéllar-Franca and Azapagic, 2015).

Among the various strategies under investigation, Carbon Capture Storage (CCS) and, more recently Carbon Capture Utilization (CCU), have attracted the attention of scientists worldwide. The aim of such approaches is to capture emissions from point sources but the main difference is the destination of captured CO₂. While in CCS it is transferred to a suitable site for long-term storage, in CCU it is converted into valuable products (e.g., chemicals and fuels), contributing to mitigate climate change (Metz et al., 2005; Weisser, 2007; Hertwich et al., 2008; Cooper, 2009; Nagashima et al., 2011; Styring and Jansen, 2011; Markewitz et al., 2012; Zapp et al., 2012).

As for the CCS, i.e., CO₂ geological storage, it involves the injection of CO₂ into geological formations, such as depleted oil and gas reservoirs at great depths. Such sequestration technique is, at present, probably one of the most promising options due to the previous experience by the oil and gas industry. In fact, the industry has a good understanding of the structural characteristics and behavior of depleted oil and gas reservoirs, and the existing well-drilling and injection techniques can be adapted for carbon storage applications (Metz et al., 2005) (e.g., CO₂-injection at Sleipner) (Leung et al., 2014; Furre et al., 2017). The main issues with CO₂ storage are their possible leaks and the related damage that would cause if a concentrated stream escaped into the environment. This possibility depends on the permeability of the geological structure and its faults or defects. According to the literature, annual leakage rates are in the range from 0.00001 to 1% (Metz et al., 2005; Pehnt and Henkel, 2009; Singh et al., 2011).

Finally, mineral carbonation, also known as “mineral sequestration,” can be considered as a storage and utilization option, because it involves CO₂ conversion into carbonates through the reaction with metal oxides, such as magnesium or calcium oxide (Metz et al., 2005; Von Der Assen et al., 2013). The carbonation is an exothermic reaction that releases enough heat to make the whole carbonation process, at least in theory, self-sustaining (Von Der Assen et al., 2013). The main advantage of mineral carbonation is the formation of stable carbonates capable of storing CO₂ for long periods, without the risk of CO₂ leakage as in CCS (Metz et al., 2005; Styring and Jansen, 2011; Von Der Assen et al., 2013).

Olivine and Serpentine minerals are the most promising candidates for carbon sequestration because of their high contents of magnesium. The main carbonation reactions of these two minerals are described by the following reactions (Equations 1–3):

$\begin{array}{ll}{(Mg,Fe)}_{2}Si{O}_4+2C{O}_2\to 2(Mg,Fe)C{O}_3+Si{O}_2& (1)\end{array}$

$\begin{array}{l}6{(Mg,Fe)}_{2}Si{O}_4+12H_{2}O+6C{O}_2\to 2{(Mg,Fe)}_{3}S{i}_2{O}_5{(OH)}_4\\ +2F{e}_3{O}_4+8H_2+6MgC{O}_3+2Si{O}_2& (2)\end{array}$

$\begin{array}{ll}{(Mg,Fe)}_{3}S{i}_2{O}_5{(OH)}_4+3C{O}_2\to 3(Mg,Fe)C{O}_3+2Si{O}_2+2H_{2}O& (3)\end{array}$

In nature, around 100 million tons of carbon per year, according to a slow weathering process, is bound by these minerals (Oelkers et al., 2008). The CO₂ sequestration in natural silicates is sometimes accompanied by the occurrence of the serpentinization process. This is a widespread phenomenon on the Earth's mantle that occurs generally at temperatures <300°C (Oelkers et al., 2008; McCollom and Bach, 2009; Neubeck et al., 2011; Holm et al., 2015), and during which, mineral based silicates of Fe and Mg react with water to give H₂ and minerals of the serpentine group [(Mg,Fe)₃Si₂O₅(OH)₄] (Equation 2). This involves the formation of extremely reducing fluids, rich in hydrogen, so any species present, such as inorganic C, can be reduced. Therefore, CO₂ can react with H₂, through a Fischer-Tropsch type (FTT) or Sabatier mechanism, to form CH₄ and light hydrocarbons (Holm et al., 2015) (Equation 4).

$\begin{array}{ll}C{O}_2+4H_2\to C{H}_4+2H_{2}O& (4)\end{array}$

Although the whole process is thermodynamically favored, the rate of the reaction is very slow, and, accordingly, the natural process does not allow control of CO₂ emission levels into the atmosphere. The possibility to increase the kinetics of such processes deserves interest, and to this regard, preliminary treatment of the olivine mineral, such as mechanical activation, has been demonstrated to be successful. If, on the one hand, the CO₂ absorption process during olivine serpentinization had been experimentally investigated, on the other hand, literature data (Kleiv and Thornhill, 2006; Baláž et al., 2008; Fabian et al., 2010; Sandvik et al., 2011; Power et al., 2013; Turianicová et al., 2013; Li and Hitch, 2015; Rigopoulos et al., 2015) are not homogeneous and refer to the effects of mechanical activation on olivine, focusing mainly on its structural and surface transformation, in order to facilitate CO₂ storage. In particular, it has been shown that the mechanical grinding of olivine significantly increases its ability to form iron and magnesium carbonates making the CO₂ capture a potential stable storage method for long periods. The mechanical activation was found to be more effective if the treatment occurs in the presence of liquids, such as water (Turianicová and Baláz, 2008) or ethanol (Rigopoulos et al., 2015), as a consequence of the greater surface area generated in wet conditions. Conversely, less attention has been paid, in such studies, to the chemical reduction of CO₂, to yield light hydrocarbons and corresponding oxygenated compounds. The present work just deals with such issues, and, for the first time to the best of our knowledge, the attention has been focused on the mechanically induced production of methane and light hydrocarbons during the interaction between olivine and water under CO₂ atmosphere.

Materials and Methods

Olivine powders were provided by SATEF-HA (Italy). Chemical analysis reported by the supplier indicated the following relative composition expressed as weight % of oxide of each element contained in the material: 50.00% MgO, 41.50% SiO₂, 7.30% Fe₂O₃, 0.29% Cr₂O₃, 0.40% Al₂O₃, 0.30% NiO, 0.10% MnO, 0.10% CaO.

High purity Carbon dioxide gas (≥99.995%) was provided by Sapio (Italy).

Materials Processing

The mechanical activation was carried out by a Spex Mixer Mill mod.8000, which was suitably modified to control the milling dynamic parameters (Delogu et al., 2004).

As a mechanochemical reactor, we employed a stainless-steel vial (76 cm³) equipped with two circular bases which were fitted with sealing valves. On one side, these valves allowed the connection to the gas reservoir (CO₂), and on the other side, to the GC apparatus for the analyses of gaseous reagents and products. The mechanical treatments were carried out on fresh powders at selected milling times. In order to remove the residual air from the vial, a dynamic vacuum of 10⁻³ mbar for 10 min was applied, before introducing CO₂. Gas sampling was then performing 30 min after stopping milling and the gases analyzed by gas chromatography.

Three series of experiments have been performed by charging the vial with 2 g of olivine, 0.3 ml of deionized H₂O, three stainless steel balls of 3.80 g each, and a rotation speed of 875 rpm. The reactor was then closed under CO₂ atmosphere under different conditions: (a) applying a constant pressure of 1.5 bar; (b) pressurizing the milling vial with an initial pressure of 1.5 bar; (c) filling the reactor with 1.0 bar. All the mechanochemical processes were conducted under low pressure of CO₂, in order to reproduce the reaction conditions expected under a real environment.

Methane, Hydrogen, and Light Hydrocarbons Evolution

Gas withdrawal from the reactor and injection in the gas sampling valves of gas chromatographs (GC) were performed by a gastight syringe. A GC Perkin Elmer 8600 equipped with a capillary column (GSQ 115-3432-J&W Scientific) and an FID detector, was used for CH₄ and light hydrocarbons detection. A Fisons 8000 equipped with a molecular sieves column (10 Å) and a hot wire detector (HWD), was used to evaluate H₂ and permanent gases. The conversion of CO₂, expressed as percentage (%), was calculated using the following equation:

$\begin{array}{ll}C{O}_{2}conversion(\%)=\frac{{C{O}_2}_{initial}-{C{O}_2}_{final}}{{C{O}_2}_{initial}}*100& (5)\end{array}$

where C_O2initial and C_O2final correspond to the area of the peak showed by GC measurements before and after the mechanical treatment, respectively.

Quantitative analyses were carried out through calibration curves setup by resorting to analytical standards, provided by Linde Gas Italia S.R.L.

Solid-State Samples Characterization

Powders were structurally characterized by means of a Rigaku SmartLab X-ray Diffractometer (XRD) with a Bragg–Brentano geometry using Cu Kα radiation (λ = 1.54178 Å) and a graphite monochromator in the diffracted beam. Quantitative evaluation of phase abundance and structural features were obtained for all the XRD patterns, by non-linear least-square refinement procedure, according to Rietveld method, and using the MAUD (Materials Analysis Using Diffraction) software (Young, 1993).

The thermogravimetric analyses were carried out by a Setaram Labsys DTA-TGA under Argon flux, by heating the specimens from room temperature to 1,000°C, at a scanning rate equal to 5°C/min.

Results

The crystallographic characterization of the olivine powders in the as-received state was performed by XRD using the Rietveld refinement method (Figure 1). In this way, phases were identified and their relative abundance and microstructural features were evaluated (Table 1). The Mg-rich Olivine used in these tests (from now Olivine) consists of three phases: Forsterite (Fe_0.2Mg_1.8SiO₄), space group (s.g.) Pbnm, Enstatite ferroan (Fe_0.2Mg_0.8SiO₃), s.g. Pbca, and Clinochlore (Al_1.84Fe_0.5H₈Mg_4.5O₁₈Si_3.16), s.g. C-1. The Forsterite is the majority phase in the as-received olivine powders (91 wt%), with Enstatite as secondary phase (7.5 wt%).

FIGURE 1

Figure 1. CuKα XRD pattern of the Olivine in the as received state. The structural refinement procedure by Rietveld method, allowed to quantitatively evaluate the contribution of the three phases indicated in the Figure: Forsterite (green line), Enstatite ferroan (blue line), Clinochlore (red trace).

TABLE 1

Table 1. Phase composition and structural parameters of Olivine in the as-received state.

As a general behavior, mechanical activation tests of olivine with water under CO₂ atmosphere led to the production of different gas-phase products, which were detected by gas chromatography. The main hydrocarbons produced were methane, CH₄, ethane, C₂H₆, and ethylene, C₂H₄. As an example, the gas-chromatographic trace of olivine mechanically treated for 150 min is shown (Figure 2). The relative concentration of light hydrocarbons and other gas phase compounds, within the mechanochemical reactor, was evaluated by a calibration line obtained using certificated standard gas mixtures. Data plotted in Figure 2 indicate that the relative amount is: 0.23% v/v of methane, 0.036% v/v of ethane, and 0.099% v/v of ethylene. Moreover, it is safe to say that, at present, we cannot exclude the formation of traces of further heavier products, which could be in condensed liquid phase, or chemisorbed on the powder surfaces: this point is still under investigation. However, concerning the present work, we focused our attention mainly on the formation of methane. It should also be noted that, in absence of CO₂, there was no methane formation, during two blank tests carried out by filling the jar with air or Argon.

FIGURE 2

Figure 2. Gas-chromatographic analysis, by FID, of the gas phase sampled from the mechanochemical reactor. Experimental data, reported as pink line, are compared with the relevant standard mixture data (STD), relative to 1% concentration value.

The evolution of methane during the experiments performed under a constant pressure of 1.5 bar of CO₂ (with continuous flow) is presented in Figure 3. Data are reported in the graph as a degree of conversion α, vs. the milling time. The kinetics of evolution of methane concentration followed a sigmoidal shape, a trend often observed in chemical reactions involving solids as well as in gas-solid interaction processes, also activated by mechanical treatment (Delogu et al., 2004; Ahmedabadi and Kain, 2019). The data suggest that methane formation rate, initially slow (α = 8.3·10⁻³), increased up to reaching its maximum value after about 150 min of milling, and then CO₂ to CH₄ conversion progressively slows down, asymptotically approaching α = 1, which corresponds to the CH₄ maximum concentration value, between 0.18 and 0.2% v/v. Experimental points can be fitted by the empirical equation α = 1−(1+kt)exp(−kt), in which t represents the milling time, and k represents the apparent kinetic constant of the process and has a value of 1.484^*10⁻² min⁻¹. Apart from the empirical approach, it should be noted that the actual process is rather complex, as it involves several steps, including surface adsorption of H₂O and CO₂, with molecular dissociation occurring over the surface, or after diffusion phenomena through the bulk. Such steps are accompanied by the creation of highly activated and freshly renewed surfaces due to the milling process, corresponding to sites where CO₂ conversion can take place. Despite the complexity of the process, which makes it difficult to reliably define the different reaction steps, some hints can be obtained by analyzing the experimental results, as described below.

FIGURE 3

Figure 3. Methane concentration values in the gas phase mixture, reported as degree of conversion α, as a function of mechanical treatment time, t. Blue dots refer to experimental data, while continuous line represents the fitting curve according to the empirical equation reported in the text.

In order to evaluate structural and microstructural changes of the olivine during mechanical activation, XRD analyses were performed (Figure 4). A decrease in the crystallite size of the predominant Forsterite phase due to the milling process was obtained by Rietveld refinement (Table 2). XRD patterns presented in Figure 4 do not evidence the formation of a Serpentine phase. However, these patterns display, together with the residual Forsterite, the formation of two Mg-based phases, which can be identified as the trigonal MgCO₃, Magnesite, s.g. R-3C, and the orthorhombic MgSiO₃, Enstatite, s.g. Pbca. Such phases were observed in all the samples at the end of the mechanochemical trials, as displayed in Table 3. An example is the XRD pattern of the olivine subjected to 90 min of mechanochemical activation (central trace of Figure 4). The data suggest that the transformation process of olivine was accompanied by CO₂ adsorption on the mineral surface, and further activation, which induces the formation of Magnesium carbonates phases. No Fe-based carbonates were detected. However, after heat treatment up to 1,000°C of this as-activated olivine (upper trace of Figure 4), the precipitation of two crystalline Fe-oxide phases, namely Hematite Fe₂O₃, s.g. R-3C, and Magnetite Fe₃O₄, s.g. Fd-3m was observed.

FIGURE 4

Figure 4. The CuKα XRD patterns sequence displays, from the bottom, the analyses of the Olivine in the as received state, the one of the sample at the end of 90 min of mechanical activation in the first series of runs, and the one further subjected to the thermogravimetric analysis. Experimental points are fitted by the Rietveld refinement procedure.

TABLE 2

Table 2. Crystallite size of the Forsterite phase, evaluated by Rietveld analysis of each sample, as a function of the milling time.

TABLE 3

Table 3. Phase composition, as evaluated by Rietveld analysis, of different samples after selected time of mechanical treatment, in the first series of tests.

Figure 5 shows the TGA curves of the pristine olivine and the samples previously subject to different milling times. Whereas, for pristine olivine, which did not display significant changes in weight, all the other TG curves are characterized by two weight loss phenomena, occurring within three main temperature ranges (20–100, 100–400, and 400–1,000°C). The comparison with literature data suggests that the weight loss occurring at lower temperature ranges is related to H₂O desorption by the sample surface (Maroto-Valer et al., 2005); the subsequent signal, whose onset is observable at about 107°C can be related to the dehydration of the bulk; the last weight loss (around 450°C) can be conversely related to CO₂ evolution after decomposition of carbonate phases (Bisbal et al., 2015; Stopic et al., 2018). It can, thus, be argued that the heat treatment allowed H₂O and CO₂ evolution from these compounds, and that the decomposition of MgCO₃ (Magnesite) induced the increase of MgSiO₃ concentration (Enstatite) up to about 8%. The precipitation and grain growth of Hematite and Magnetite phases, whose relative amount are reported in Table 3, deserve further analysis.

FIGURE 5

Figure 5. TGA traces carried out over selected samples at the end of the first series runs, i.e., mechanochemical tests carried out under a CO₂ pressure head equal to 1.5 bar.

It is noteworthy that the above findings are in agreement with Klein (2014) and Jones et al. (2010) who reported the treatment of olivine with H₂O and CO₂, under hydrothermal conditions, at low-temperatures and in presence of an excess ${\text{CO}}_3^{2-}$ ions. In that case, Fe²⁺ ions were rapidly incorporated to form carbonates, silicates and hydroxides, rather than being oxidized to Fe³⁺, and can also be included within the serpentine, thus not leading to the precipitation of appreciable amounts of Magnetite. According to this, it could be surmised that, in our tests, the Magnesite carbonate phase, that formed as a consequence of mechanical activation of olivine with H₂O and CO₂, is not a pure Mg²⁺ based phase, but includes Fe ions. This is confirmed by crystallographic features: values of lattice parameters a and c of the R-3C carbonate phase, equal to 4,682 and 15,218 Å, respectively, are consistent with a ca. equimolecular mixture of the two Fe- and Mg-carbonate phases whose corresponding lattice parameters are a = 4,686 Å, c = 15,383 Å, and a = 4,635 Å, c = 15,023 Å, respectively.

The driving force of the serpentinization process lies in the oxidation of Fe²⁺ to Fe³⁺ that leads to the reduction of water and the formation of molecular hydrogen. As a matter of fact, the whole analysis of gaseous mixture, from the mechanochemical reactor at the end of tests, allowed for confirmation of the occurrence of a significant amount of gaseous H₂. This hydrogen appeared due to H₂O activation and dissociation, and it was made available, within the vial, as a consequence of its desorption from powders. Its kinetic trend parallels the shape of CO₂ to CH₄ transformation (Figure 6), and its value is relevant to samples mechanically treated up to 150 min, which show that the H₂ concentration rises up to about 20% v/v. Assuming 1 atm pressure inside the vial, the amounts of H₂ detected are stoichiometrically possible (54% of the theoretical maximum) based on the available Fe²⁺ amount. The CO₂ conversion (Figure 7) shows that the kinetic trend recalls that observed for H₂: the increasing rate has to be considered as the initial step of a sigmoid-shaped curve, while the observed conversion values indicate, on one hand, the efficiency of the mechanochemical process as a tool for CO₂ storage, and on the other hand, confirm that CO₂ absorption and activation steps are necessary conditions that precede the reduction to form methane.

FIGURE 6

Figure 6. H₂ concentration in the gas phase within the mechanochemical reactor, as registered at different times of mechanical treatment, in the tests carried out with a pressure head of 1.5 bar of CO₂.

FIGURE 7

Figure 7. Conversion data of CO₂, plotted as a function of milling time, as observed during the series of mechanochemical tests performed with a pressure head of 1.5 bar of CO₂.

In order to evaluate the effect of the CO₂ pressure, as registered within the milling vial, on the transformation path under mechanochemical activation, two subsequent series of tests were carried out by changing the value of the CO₂/H₂O ratio, by setting the CO₂ initial pressure of the vial at 1.5 bar and at 1.0 bar, respectively.

The CH₄ concentration values reported in Figure 8 correspond to the above series of experiments. It emerged that CO₂ conversion trend, as well as the H₂ evolution, approach the results of formerly presented runs at corresponding times of mechanical treatment. The data of the two series have similar trends and are in the same order of magnitude, with a small increase observed in the tests carried out at an initial pressure equal to 1.5 bar. For samples milled for 120 min, the lower conversion value marks a difference in the rising trend, and it parallels the corresponding data for H₂ evolution at the same time of treatment. Although the amount of gaseous H₂ available within the vial remains much higher than the stoichiometric requirement for the hydrogenation process, the dependence of the conversion on the H₂/CO₂ ratio may be a relevant factor.

FIGURE 8

Figure 8. Methane concentration data relevant to the three different test series. Blue dots: initial CO₂ pressure equal to 1.5 bar. Red dots: initial CO₂ pressure equal to 1.0 bar. The data are replicates of two runs and error bars refers to standard deviation values.

As for the solid phases, a difference in the evolution of the phases was evidenced by XRD data (Table 3), which refer to the first series of tests performed under constant CO₂ pressure value equal to 1.5 bar. These results revealed the formation of the Mg-carbonate phase, the trigonal Mg(CO₃), Magnesite, s.g. R-3C, while no relevant signals of Nesquehonite were observed. Different finding was observed in the third series of tests (carried out at initial CO₂ pressure of 1 bar) the Nesquehonite phase appeared in all the samples except for the one milled for 150 min, and it is consistent with the reduced value of the CO₂/H₂O ratio (Table 4). This suggests the sensibility of the chemical transformation to the adopted conditions. In this regard, it is interesting to note that our findings agree with the literature data, referred to the process in a liquid medium, which indicate that the precipitation of Magnesite at room temperature is not observed, despite being the stable carbonate form. Most commonly, only the Nesquehonite mineral can precipitate from aqueous solution at 25°C and with a partial pressure of CO₂ close to ambient pressure. At higher temperatures, above 40°C, several basic carbonates were observed to precipitate, in the form of hydromagnesite. Conversely, Magnesite production takes place only if the temperature is around 60–100°, and at high CO₂ pressure (Fernández et al., 2000; Zhang et al., 2000; Kloprogge et al., 2003; Giammar et al., 2005; Hänchen et al., 2008).

TABLE 4

Table 4. Phase composition, as evaluated by Rietveld analysis, of different samples after selected time of mechanical treatment, in the second series of tests, run under the initial CO₂ pressure of 1 bar.

A further point deserves a comment: the Clinochlore phase, observed in the above tests, was present in a low amount (about 1.7 wt%) in the as-received Olivine and it was not found in the first series of experiments, where the mixed carbonate, Magnesite-type, was recovered. However, its content increased in the other series, where hydrated Nesquehonite compound was formed. In other words, during the process, decreasing the CO₂/H₂O ratio, the concentration of the resulting carbonate form decreases, and under such conditions, the formed carbonate phase is hydrated. Therefore, the absence in XRD data of the signals, related to the Serpentine, at the end of the mechanochemical runs, could be related to a possible phase amorphization during the process. A further possible interpretation is the occurrence of a consecutive process. The former step is related to olivine hydrolysis, with the induced formation of Serpentine minerals, which still evolve, in the latter step, to give carbonates when CO₂ is available in the proper amount. Otherwise, in the tests carried out with a lower value of CO₂/H₂O ratio, the kinetics of the latter step slows down, allowing to observe the rise of the Clinochlore phase concentration.

Finally it is noteworthy that Magnetite, reported as the active catalytic phase in situ generated during FTT after olivine hydrolysis under hydrothermal conditions (Giammar et al., 2005; Jones et al., 2010), was not observed during our mechanochemical runs, but only after thermal annealing at TGA. However, it is safe to say that, under mechanochemical activation, a necessary condition for the occurrence of FTT after olivine weathering process, is the presence of Fe³⁺ ions more than actual Magnetite particles.

Conclusions

The mineral carbonation technology is capturing wide interest as a useful strategy for both CO₂ storage and its utilization, and in this context, the chemical transformations driven by olivine weathering process appear worthy of investigation. In particular, while the very slow kinetics of the natural process are not practical for CO₂ storage and conversion purpose, the activation by mechanical treatment of olivine in the presence of H₂O and CO₂ has been demonstrated to be efficient to promote both the solid phases evolution and the gas-phase synthesis of light hydrocarbons, in particular of methane. The formation of carbonate solid phases and the methanation reaction, displayed faster kinetics compared to the hydrothermally activated ones and similar or higher conversion data. The whole pattern of physical and chemical transformations activated by mechanical treatment requires further deepening, but the results allowed to clarify some mechanistic aspects and suggested a possible line of future investigation. This process promoted H₂O dissociation with consequent H₂ formation, which in turn can promote FTT reactions over the mineral surface, and CO₂ hydrogenation rate can then increase, after an induction period related to CO₂ and H₂ activation, according to a sigmoidal trend often observed in mechanochemical processes. Structural evolution of solid phases suggests the occurrence of a complex process that appears to be defined by the CO₂/H₂O ratio values. The presence of a “mechanochemical effect” is evident, i.e., the occurrence of an increased system reactivity specifically related to the activation by mechanical treatment.

The observed concentration values of methane and hydrocarbons may be influenced by the experimental set up: the analyses of the effects of parameters like the geometry reactor, as well as the milling dynamic parameter, i.e., frequency of collision, will be the focus of future work aimed at improving chemical results and deepening the knowledge of the whole process.

Data Availability Statement

The datasets generated for this study are available on request to the corresponding author.

Author Contributions

VF, FT, AT, and NG carried out the experimental activities: the several tests of CO₂ hydrogenation over olivine under mechanochemical treatment, the structural, thermal, and gaseous analyses. All of them collaborated with SE, SG, FG, and GM to analyse the different data. All authors discussed the results, wrote their respective parts of the manuscript, and revised the overall manuscript.

Funding

The present work is part of the CO2MPRISE, CO₂ absorbing Materials Project-RISE, a project that has received funding from the European Union's Horizon 2020 research and innovation programme, under the Marie Skłodowska-Curie, Grant Agreement No. 734873. This work has been partially supported also by RAS, Regione Autonoma Sardegna, through the project Sistemi innovativi di conversione di anidride carbonica a metano da fonti rinnovabili, under the program L.R.n.7/2007, call Capitale Umano ad Alta Qualificazione. The activity of VF was supported by a Ph.D. program in a collaborative scheme between the University of Sassari and Cagliari of Italy, which is especially endorsed by Autonomous Regional Administration of Sardinia (RAS).

Conflict of Interest

The authors declare that the research was conducted in the absence of any commercial or financial relationships that could be construed as a potential conflict of interest.

Acknowledgments

The authors acknowledge the support of the CeSAR UNISS, Centro Servizi di Ateneo per la Ricerca of the University of Sassari, for making available several instrumental techniques to carry out materials characterization.

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