CO 2 Curing of Ca-Rich Fly Ashes to Produce Cement-Free Building Materials

: In this study, ﬂy ash (FA) compacts were prepared by accelerated carbonation as a potential sustainable building material application with the locally available ashes (oil shale ash (OSA), wood ash (WA) and land ﬁlled oil shale ash (LFA)) of Estonia. The carbonation behaviour of FAs and the performance of 100% FA based compacts were evaluated based on the obtained values of CO 2 uptake and compressive strength. The inﬂuence of different variables (compaction pressure, curing temperature, CO 2 concentration, and pressure) on the CO 2 uptake and strength development of FA compacts were investigated and the reaction kinetics of the carbonation process were tested by different reaction-order models. A reasonable relation was noted between the CO 2 uptake and compressive strength of the compacts. The porous surface structure of the hydrated OSA and WA compacts was changed after carbonation due to the calcite formations (being the primary carbonation product), especially on portlandite crystals. The increase of temperature, gas pressure, and CO 2 concentration improved the CO 2 uptake levels of compacts. However, the positive effect of increasing compaction pressure was more apparent on the ﬁnal strength of the compacts. The obtained compressive strength and CO 2 uptake values of FA compacts were between 10 and 36 MPa and 11 and 13 wt%, respectively, under various operation conditions. Moreover, compacts with mixed design (OSA/LFA and WA/LFA) resulted in low-strength and density compared to the single behaviour of OSA and WA compacts, yet a higher CO 2 uptake was achieved (approximately 15% mass) with mixed design. The conformity of Jander equation (3D-diffusion-limited reaction model) was higher compared to other tested reaction order models for the representation of the carbonation reaction mechanism of OSA and WA. The activation energy for OSA compact was calculated as 3.55 kJ/mol and for WA as 17.06 kJ/mol.


Introduction
Since the manufacture of cement, CO 2 emissions of the cement industry have been on a large scale and the direct CO 2 intensity of cement production increased 1.8% annually during 2015-2020 [1,2]. Cement production is estimated to increase even more, and thus reducing CO 2 emissions while producing enough cement to meet demand will be challenging until 2030 due to EU restrictions [1,2]. Carbon capture and storage at cement production plants could be a solution to this problem, yet there is no commercially available full-scale application until today [3,4]. Researchers throughout the world have been searching for alternatives to cement among waste materials to cut cement dependency and lower the related CO 2 emissions [3,5]. Primarily, fly ash (FA), which is generally disposed of in landfills, has always been an alternative to cement, as it is considered a supplementary cementitious material which provides one of the most feasible routes for concrete production with reduced CO 2 emissions [6].
The suitability of FA depends on the chemical and mineralogical composition such as the content of siliceous or siliceous-and-aluminous material, lime, portlandite, and its physical properties [7]. Although FA has several advantages on concrete properties, there are still several drawbacks that limit the applications on a big scale due to the reduction of mechanical properties of the concrete and its durability. As FA amounts increase in concrete, the mechanical properties of the concrete decrease, which means that remarkable replacement ratios are infeasible in today's construction applications [6][7][8].
With the increase of environmental consciousness, the building sector is evolving with the integration of circular economy concepts for better waste utilization and zero carbon emissions. Mineral carbonation is at the forefront due to recent progress when it comes to the utilization of both industrial alkaline waste materials and CO 2 gas without using traditional binders towards sustainable construction materials [9][10][11][12][13]. Considering the vast amount of ashes generated from both fossil and renewable fuels, and for the applications of non-traditional construction materials, the usage of FAs via carbonation activation could be a promising alternative for producing cement-free building materials.
Calcium (Ca) and magnesium (Mg) are considered as two of the most dominant and reactive (with respect to CO 2 ) alkaline earth metals found in industrial residues [14][15][16]. Based on the chemical composition of the ashes, Ca and Mg-rich FAs are found to be potential candidate materials for CO 2 mineralization due to their high alkalinity. The average CO 2 uptake level of most of the alkaline solid wastes including ashes can also be directly connected to the contents of Ca and Mg [12,15,17].
In Estonia, Ca-rich ashes; oil shale ash (OSA), and wood ash (WA) are widely produced, constituting more than 70% of the total residues generated by power plants. As a result of the past industrial processes involving oil shale (OS) combustion and retorting (approximately 100 years) and due to the limited ash utilization applications, there are more than 300 million tonnes of land filled OS ash (LFA) in plateau-like waste depositories [18,19]. The ash problem and CO 2 emissions, which are elevated by high carbonate content in OS, are key issues undermining the long-term sustainability of the energy sector of Estonia. Therefore, valorisation of the ashes in environmentally sound applications is of clear strategic interest to the country. The utilization of local alkaline waste streams together with CO 2 via mineral carbonation can contribute to the circular economy and sustainable development.
In an early investigation on typical residues from the OS industry of Estonia, a mineral carbonation approach was studied for the first-time to evaluate the suitability and reactivity of available OSAs. The preliminary findings on CO 2 uptake (up to 9%) were promising, reflecting on the improved strength  as a result of mainly the carbonation of Ca(OH) 2 forming CaCO 3 crystals [20]. With respect to this positive outcome, principally OSA, WA, and LFA could be useful waste materials for both capture and permanent sequestration of CO 2 through the formation of CaCO 3 , as these waste streams contain high amounts of calcium mainly due to the presence of free lime and portlandite.
It is also known that the formation of the CaCO 3 phase has a positive effect on construction materials because of the increased density through a filling effect, which improves the microstructure, lowers the permeability, and improves strength [21,22]. This behaviour of strength development has been studied with different waste materials including steel slag, blast furnace slag, construction demolition waste, municipal solid waste, coal combustion FA, and ashes from wood and peat combustion under controlled process conditions [21][22][23][24][25][26]. In most of these studies, carbonation tests of compacted or granulated pellets, blocks, etc., were carried out both in a CO 2 rich and lean atmosphere for modelling flue gas (FG) curing as well. It has been shown that there is a direct relation with the CO 2 uptake level and the strength gain in compacts. Since carbonation is a dynamic process involving transport of CO 2 through a compact body and dissolution of Ca, studies have shown that the extent of carbonation reactions are influenced by various parameters (reaction time, curing temperature and pressure, relative humidity (RH), CO 2 concentration, physical properties of residues etc.) [12,16,22]. However, both an excess and a scarcity of the above-mentioned parameters can result in negative effects for the entire process relating to CO 2 uptake and strengthening of the compacts.
Additionally, the achievement of the most effective CO 2 curing process and improvement in mechanical properties of compacts are highly dependent on the chemical composition and mineralogy of industrial residues [17]. It is important to bear in mind that these operation parameters must be optimized for each waste, as well as the relevant process stages for homogeneous carbonation and to lower the operational energy costs. Therefore, there is a necessity to address a research study focusing on the utilization of Ca-rich FAs in an Estonian context (OSA, WA, LFA) to gain in-depth understanding of the impacts of operation conditions during CO 2 curing to produce cement-free building materials.
The main aim of the study is to evaluate and characterize the carbonation behaviour of selected ashes based on the obtained values of CO 2 uptake and compressive strength while providing a comparative crosscheck on the rate of carbonation and mechanical performance of compacts. This study undertakes parametric investigations to understand the effects of compaction pressure, curing temperature, CO 2 concentration, and pressure on the carbonation extent and related strength development of the compacts. The reaction kinetics of the carbonation process were also tested by different reaction-order models in order to identify the carbonation reaction behaviour of Ca-rich FAs. Furthermore, the preliminary tests with LFA and impacts of mixing LFA with OSA and WA are presented for future perspectives of potential sustainable building material applications with local available ashes.

Materials
Three different types of ash samples were selected from Estonia (OSA, WA, and LFA). OSA was obtained from Auvere Power Plant [27], which is operated by the direct combustion of OS in CFB boiler for power production, and ash was collected from the electrostatic precipitators. WA was obtained from Utilitas District Heating Plant [28] which is operated by forestry wood (a mix of pine chips and bark residues) and ash was collected from bag filters located in the post-combustion zones of the grate combustor. The LFA samples were taken from a drill core made on the rim of the ash disposal site at Eesti Power Plant [29], north-eastern Estonia ( Figure 1). The selected LFA is the ash taken from the depths of 32.4-32.6 m, where mainly burnt OS FA residues exist from electricity production without including shale oil processing residues. studies have shown that the extent of carbonation reactions are influenced by various parameters (reaction time, curing temperature and pressure, relative humidity (RH), CO2 concentration, physical properties of residues etc.) [12,16,22]. However, both an excess and a scarcity of the above-mentioned parameters can result in negative effects for the entire process relating to CO2 uptake and strengthening of the compacts. Additionally, the achievement of the most effective CO2 curing process and improvement in mechanical properties of compacts are highly dependent on the chemical composition and mineralogy of industrial residues [17]. It is important to bear in mind that these operation parameters must be optimized for each waste, as well as the relevant process stages for homogeneous carbonation and to lower the operational energy costs. Therefore, there is a necessity to address a research study focusing on the utilization of Ca-rich FAs in an Estonian context (OSA, WA, LFA) to gain in-depth understanding of the impacts of operation conditions during CO2 curing to produce cement-free building materials.
The main aim of the study is to evaluate and characterize the carbonation behaviour of selected ashes based on the obtained values of CO2 uptake and compressive strength while providing a comparative crosscheck on the rate of carbonation and mechanical performance of compacts. This study undertakes parametric investigations to understand the effects of compaction pressure, curing temperature, CO2 concentration, and pressure on the carbonation extent and related strength development of the compacts. The reaction kinetics of the carbonation process were also tested by different reaction-order models in order to identify the carbonation reaction behaviour of Ca-rich FAs. Furthermore, the preliminary tests with LFA and impacts of mixing LFA with OSA and WA are presented for future perspectives of potential sustainable building material applications with local available ashes.

Materials
Three different types of ash samples were selected from Estonia (OSA, WA, and LFA). OSA was obtained from Auvere Power Plant [27], which is operated by the direct combustion of OS in CFB boiler for power production, and ash was collected from the electrostatic precipitators. WA was obtained from Utilitas District Heating Plant [28] which is operated by forestry wood (a mix of pine chips and bark residues) and ash was collected from bag filters located in the post-combustion zones of the grate combustor. The LFA samples were taken from a drill core made on the rim of the ash disposal site at Eesti Power Plant [29], north-eastern Estonia ( Figure 1). The selected LFA is the ash taken from the depths of 32.4-32.6 m, where mainly burnt OS FA residues exist from electricity production without including shale oil processing residues.

Characterization of Materials (Initial and Compacts)
All samples were obtained in fine fractions, which did not require pre-treatment (drying, milling, or grinding etc.) except the LFA samples, which were milled by Tartu

Characterization of Materials (Initial and Compacts)
All samples were obtained in fine fractions, which did not require pre-treatment (drying, milling, or grinding etc.) except the LFA samples, which were milled by Tartu University. Mean samples were taken from each collected ashes, and a size fraction below 200 µm (by sieving) was used for material characterization and further sample preparation. The physical characterization of the selected waste streams included particle size distribution (PSD) measurements. Horiba Laser Scattering instrument (LA-950) (Kyoto, Minerals 2022, 12, 513 4 of 24 Japan) was used for PSD measurement (with ethanol suspension). The BET-N 2 sorption method was used to measure the specific surface area (SSA) with Kelvin 1042 sorptiometer (Tallinn, Estonia). The chemical and mineralogical characterization of the selected waste streams included X-ray fluorescence (XRF) and X-ray diffraction (XRD) analyses with Bruker S4 Pioneer (Karlsruhe, Baden-Württemberg, Germany) and Bruker D8 (Karlsruhe, Baden-Württemberg, Germany) diffractometers, respectively, using Cu Kα radiation with a Göbel mirror monochromator and LynxEye positive sensitive detector over a 2 • -70 • 2θ range. The thermogravimetric (TGA) and mass spectrometric (MS) analysis were also carried out to obtain thermal characterization of both carbonated and un-carbonated compacted samples (mainly for the calculation of CO 2 uptake) by using the Setaram Labsys 2000 thermoanalyzer (Geneva, Switzerland) (10 K/min, sample mass: 20 ± 1 mg, 21% O 2 /79% Ar) with alumina (Al 2 O 3 ) crucible. The SEM images of carbonated compacts were obtained from the polished samples using a ZEISS Evo MA 15 (Oberkochen, Baden-Württemberg, Germany) for the investigation of the microstructure. The mineralogical composition was determined using XRD analysis to compare mineralogical changes after carbonation curing. The compressive strength measurements were performed with Toni TechnikD-13355 (Berlin, Brandenburg, Germany). The measurements of pH were conducted according to EN 12457-2 on compacts. Tube test duration was 24 h with distilled water, 1/10 solid/liquid ratio, 32 rpm rotation speed, and 0-4 mm grain size particles were used. SevenGo Duo pH/Cond meter SG23 (Greifensee, Switzerland) was used for the pH measurements.

Physical Characterization
OSA, WA, and LFA samples have BET SSA of 5.8 m 2 /g, 11.9 m 2 /g, and 20.6 m 2 /g respectively, which can indicate higher carbonation ability for LFA compared to other ashes, since the carbonation reaction is promoted by the presence of a higher number of sites available in the initial material [30] (see Figure 2). Although the SSA of LFA and WA was higher than OSA, due to the phases formed during natural hydration and biomaterial nature of WA respectively, it was revealed that the median particle diameter is 79.2 µm for LFA, 54.6 µm for WA, and 23.4 µm for OSA.
University. Mean samples were taken from each collected ashes, and a size fraction below 200 μm (by sieving) was used for material characterization and further sample preparation. The physical characterization of the selected waste streams included particle size distribution (PSD) measurements. Horiba Laser Scattering instrument (LA-950) (Kyoto, Japan) was used for PSD measurement (with ethanol suspension). The BET-N2 sorption method was used to measure the specific surface area (SSA) with Kelvin 1042 sorptiometer (Tallinn, Estonia). The chemical and mineralogical characterization of the selected waste streams included X-ray fluorescence (XRF) and X-ray diffraction (XRD) analyses with Bruker S4 Pioneer (Karlsruhe, Baden-Württemberg, Germany) and Bruker D8 (Karlsruhe, Baden-Württemberg, Germany) diffractometers, respectively, using Cu Kα radiation with a Göbel mirror monochromator and LynxEye positive sensitive detector over a 2°-70° 2θ range. The thermogravimetric (TGA) and mass spectrometric (MS) analysis were also carried out to obtain thermal characterization of both carbonated and un-carbonated compacted samples (mainly for the calculation of CO2 uptake) by using the Setaram Labsys 2000 thermoanalyzer (Geneva, Switzerland) (10 K/min, sample mass: 20 ± 1 mg, 21% O2/79% Ar) with alumina (Al2O3) crucible. The SEM images of carbonated compacts were obtained from the polished samples using a ZEISS Evo MA 15 (Oberkochen, Baden-Württemberg, Germany) for the investigation of the microstructure. The mineralogical composition was determined using XRD analysis to compare mineralogical changes after carbonation curing. The compressive strength measurements were performed with Toni TechnikD-13355 (Berlin, Brandenburg, Germany). The measurements of pH were conducted according to EN 12457-2 on compacts. Tube test duration was 24 h with distilled water, 1/10 solid/liquid ratio, 32 rpm rotation speed, and 0-4 mm grain size particles were used. SevenGo Duo pH/Cond meter SG23 (Greifensee, Switzerland) was used for the pH measurements.

Physical Characterization
OSA, WA, and LFA samples have BET SSA of 5.8 m 2 /g, 11.9 m 2 /g, and 20.6 m 2 /g respectively, which can indicate higher carbonation ability for LFA compared to other ashes, since the carbonation reaction is promoted by the presence of a higher number of sites available in the initial material [30] (see Figure 2). Although the SSA of LFA and WA was higher than OSA, due to the phases formed during natural hydration and biomaterial nature of WA respectively, it was revealed that the median particle diameter is 79.2 μm for LFA, 54.6 μm for WA, and 23.4 μm for OSA.

Chemical Characterization
According to XRF analysis, all three types of samples were composed of mainly Ca and Si, adding up to 59-64% (see Table 1). The XRD analysis showed that OSA and WA contain a considerable amount of free lime (17-20%) with a small amount of portlandite (1.4-3%), which are supposed to be the main phases to react with CO 2 (see Table 2). Dicalcium silicate, 'C 2 S', which is an important well-known component of clinker in cement industry, constitutes 13.9% of OSA and 4.1% of WA. Differently in LFA, hydration of CaO under natural water produced Ca(OH) 2 , which constitutes 18% of the phases. Similarly, dicalcium silicates in LFA are also hydrated and formed CSH (Calcium silicate hydrate), which is composed of 45% of the phase composition due to atmospheric water reacting with the constituents of the ash in the disposal area. Cement powders require the presence of C 2 S in the clinkers for strength development in concrete. These materials react vigorously with water to produce the cement paste formed in the final product. Within the building industry, the term "pozzolan" covers all the materials that react with lime and water, producing calcium silicate and aluminate hydrates. All pozzolans must be rich in reactive silica or alumina plus silica [31]. SiO 2 , Al 2 O 3 , and Fe 2 O 3 constitute 22-45% of the samples of which are described as main constituents of pozzolans. An internal sulphate attack is a deterioration mechanism of concrete. High percentages of SO 3 in the cement increase the risk of delayed ettringite formation, which can lead to significant deterioration of the concrete structure [32]. ASTM C618 (Standard specification for coal FA use in concrete) limits the sulphate content of fly ash to 5% SO 3 when the material is to be used in concrete [33].

Sample Preparation and Carbonation Apparatus
OSA and WA were selected as the two main samples for planned experiments within this study. LFA was included only for preliminary evaluation and for its capabilities as a potential mix design with OSA and WA at a ratio of 50/50.
In the first step, the hydrated OSA and WA samples have been prepared with a liquid to solid ratio of 0.25 w/v and LFA has been prepared with the liquid to solid ratio of 0.15 w/v (to ensure 10 ± 1% moisture content for all samples before curing). The moisture content has been measured using MB23 moisture analyser. The semi-batch Eirich EL1 type intensive mixer was used for mixing. The samples were homogeneously mixed with water at the fixed rotation speed (600 rpm) and time (20 min). Later, the samples were left to hydrate/cure in sealed and vacuumed containers at room temperature and were compacted on the following day using a hydraulic press into cylinders with diameter 20 ± 1 mm and height 20 ± 1 mm ( Figure 3). Each batch of samples included minimum four cylindrical compacts and their average strength values are given in the results for each tested parameter.

Sample Preparation and Carbonation Apparatus
OSA and WA were selected as the two main samples for planned experiments within this study. LFA was included only for preliminary evaluation and for its capabilities as a potential mix design with OSA and WA at a ratio of 50/50.
In the first step, the hydrated OSA and WA samples have been prepared with a liquid to solid ratio of 0.25 w/v and LFA has been prepared with the liquid to solid ratio of 0.15 w/v (to ensure 10 ± 1% moisture content for all samples before curing). The moisture content has been measured using MB23 moisture analyser. The semi-batch Eirich EL1 type intensive mixer was used for mixing. The samples were homogeneously mixed with water at the fixed rotation speed (600 rpm) and time (20 min). Later, the samples were left to hydrate/cure in sealed and vacuumed containers at room temperature and were compacted on the following day using a hydraulic press into cylinders with diameter 20 ± 1 mm and height 20 ± 1 mm ( Figure 3). Each batch of samples included minimum four cylindrical compacts and their average strength values are given in the results for each tested parameter. The physically bound water (moisture content) after overnight hydration (24 h) was measured to be 10 ± 1% for all samples before compaction, which was found to be a critical parameter for optimum compaction (without having any cracks due to dryness or erosion on the surfaces due to excessive water) based on previous experiences [20]. As press moulding of compacts was carried out with manual hand operated hydraulic press, serious attention has been given to the uniform preparation of samples. Two different compaction pressures (150 ± 10 and 300 ± 10 kgf/cm 2 ) were applied to investigate the effect of compaction pressure. Carbonation experiments were performed in an automated carbonation unit ( Figure 4) (stainless-steel 400 mL jacketed pressure vessel), consisting of apparatus controlling temperature (Circulator C-400) and monitoring CO2 gas consumption (Buchi pressflow gas controller (bpc)). The physically bound water (moisture content) after overnight hydration (24 h) was measured to be 10 ± 1% for all samples before compaction, which was found to be a critical parameter for optimum compaction (without having any cracks due to dryness or erosion on the surfaces due to excessive water) based on previous experiences [20]. As press moulding of compacts was carried out with manual hand operated hydraulic press, serious attention has been given to the uniform preparation of samples. Two different compaction pressures (150 ± 10 and 300 ± 10 kgf/cm 2 ) were applied to investigate the effect of compaction pressure. Carbonation experiments were performed in an automated carbonation unit ( Figure 4) (stainless-steel 400 mL jacketed pressure vessel), consisting of apparatus controlling temperature (Circulator C-400) and monitoring CO 2 gas consumption (Buchi pressflow gas controller (bpc)).  Different sets of experimental conditions were applied, and parallel comparative tests were carried out to investigate the effects of different curing temperatures (25, 50, 75 °C), curing with typical flue gas CO2 concentration (15% CO2/6% O2/N2) compared to 100% CO2, and different gas pressures (5, 10, and 15 bar) (see Table 3). To maintain stable CO2 concentration during FG curing, the flushing and refilling steps were followed every 20 Different sets of experimental conditions were applied, and parallel comparative tests were carried out to investigate the effects of different curing temperatures (25,50, 75 • C), curing with typical flue gas CO 2 concentration (15% CO 2 /6% O 2 /N 2 ) compared to 100% CO 2 , and different gas pressures (5, 10, and 15 bar) (see Table 3). To maintain stable CO 2 concentration during FG curing, the flushing and refilling steps were followed every 20 min. Furthermore, all tests were performed with the strategy of controlling the humidity using the potassium iodide saturated solution, which inhibits excessive humid conditions and maintains a RH between (61-68%) at different curing temperatures [34]. Density measurements were done with solid compacted cylinders. The forming compaction pressure of the FA in powder form prior to carbonation influences the physical properties of the compacted bodies and the mechanical properties of the resultant compacts. The porosity and permeability of the solid decrease when the compaction pressure is increased [35], which leads to a stronger structure and greater strength due to eliminated internal surface areas. Conversely, the lower gas permeability inhibits the penetration of the CO 2 passing through the inner surfaces of the compacted bodies. Thus, the efficiency of the accelerated carbonation process can be affected negatively due to the physical limitations of CO 2 permeability, diffusivity, and solubility, resulting in a lower amount of crystallized CaCO 3 formations and lower strength development. According to the obtained strength values of OSA, WA, and LFA there is a somewhat similar phenomenon as mentioned above. The results of compressive strength and CO 2 uptake of OSA, WA, and LFA together with mixed design compacts are presented in Figures 5 and 6.
The potential negative impact of increased compaction pressure on the CO 2 uptake of OSA compacts is negligible at the applied compaction pressure ranges. However, there are slight decreases on the CO 2 uptake level of WA and LFA compacts ( Figure 5). The CO 2 uptake level of LFA with compaction pressure of 150 kg/cm 2 is 14.7% while samples with 300 kg/cm 2 compaction pressure is 11.9%, being the highest compared to the other ashes.
It is observed that a higher pressure of compaction (from 150 kg/cm 2 to 300 kg/cm 2 ) leads to higher compressive strength in all prepared samples. The increase in compaction pressure results in an average compressive strength increase of 63% in OSA compacts, 71% in WA compacts, and 25% in LFA compacts ( Figure 6). Compressive strength values of LFA compacts are 7.8 and 10.8 MPa for a compaction pressure of 150 and 300 kg/cm 2 showing the lowest values compared to other ashes. This is mainly due to LFA being composed of already formed CSH before compaction, which can reduce the compressive strength development.
leads to higher compressive strength in all prepared samples. The increase in compaction pressure results in an average compressive strength increase of 63% in OSA compacts, 71% in WA compacts, and 25% in LFA compacts ( Figure 6). Compressive strength values of LFA compacts are 7.8 and 10.8 MPa for a compaction pressure of 150 and 300 kg/cm 2 showing the lowest values compared to other ashes. This is mainly due to LFA being composed of already formed CSH before compaction, which can reduce the compressive strength development.  leads to higher compressive strength in all prepared samples. The increase in compaction pressure results in an average compressive strength increase of 63% in OSA compacts, 71% in WA compacts, and 25% in LFA compacts ( Figure 6). Compressive strength values of LFA compacts are 7.8 and 10.8 MPa for a compaction pressure of 150 and 300 kg/cm 2 showing the lowest values compared to other ashes. This is mainly due to LFA being composed of already formed CSH before compaction, which can reduce the compressive strength development.  Two different types of mixed compacts were also designed; one containing 50% OSA/50% LFA (denoted by M1) and the other containing 50% WA/50% LFA (denoted by M2) (Figure 7). M1 compacts have an average compressive strength of 9.2 MPa while having a CO 2 uptake level of 13.1%. This indicates that LFA is slightly increasing the CO 2 uptake while reducing the compressive strength of the samples compared to 100% OSA compacts. M2 compacts have an average compressive strength of 10.4 MPa and CO 2 uptake level of 12.3%. A similar trend is observed with the strength and CO 2 uptake values of M2 compacts compared to 100% WA compacts. Both types of mixed designs exhibit more or less similar compressive strength and CO 2 uptake levels. LFA compacts exhibited overall lower density (1340 kg/m 3 ) compared to OSA (1595 kg/m 3 ) and WA (1830 kg/m 3 ) compacts. Higher compaction pressure of 300 kg/cm 2 increased the density to 1470 kg/m 3 , which may show the potential usage of LFA for low density building material applications. Mixed designs demonstrate a median density based on the constituents. The M1 have an average density of 1380 kg/m 3 and the M2 compacts have and average density of 1420 kg/m 3 (see Table 4). overall lower density (1340 kg/m ) compared to OSA (1595 kg/m ) and WA (1830 kg/m compacts. Higher compaction pressure of 300 kg/cm 2 increased the density to 1470 kg/m which may show the potential usage of LFA for low density building material applic tions. Mixed designs demonstrate a median density based on the constituents. The M have an average density of 1380 kg/m 3 and the M2 compacts have and average density 1420 kg/m 3 (see Table 4).  CO2 partial pressure and CO2 concentration are factors affecting the rate of CO2 u take due to their effect on physisorption process at the interface between the solid and t gas reactant where the formation and growth of a solid product layer of CaCO3 occu [36]. The influence of the CO2 gas pressure and CO2 concentration was examined by ev uating CO2 uptake levels and compressive strength of OSA and WA compacts. With t increase of gas pressures from 5 to 15 bar, the final CO2 uptake levels as well as compre sive strength increases in both the OSA and WA compacts. This could be explained w the improved gas penetration of CO2 into the compact under high pressures, which vours the extent of carbonation reaction. At 5 bar, the CO2 uptake percentage for OSA 10.7% and for WA it is 8.2%. At 15 bar, the CO2 uptake values are improved to 12.2% f OSA and 10.2% for WA (Figure 8   CO 2 partial pressure and CO 2 concentration are factors affecting the rate of CO 2 uptake due to their effect on physisorption process at the interface between the solid and the gas reactant where the formation and growth of a solid product layer of CaCO 3 occurs [36]. The influence of the CO 2 gas pressure and CO 2 concentration was examined by evaluating CO 2 uptake levels and compressive strength of OSA and WA compacts. With the increase of gas pressures from 5 to 15 bar, the final CO 2 uptake levels as well as compressive strength increases in both the OSA and WA compacts. This could be explained with the improved gas penetration of CO 2 into the compact under high pressures, which favours the extent of carbonation reaction. At 5 bar, the CO 2 uptake percentage for OSA is 10.7% and for WA it is 8.2%. At 15 bar, the CO 2 uptake values are improved to 12.2% for OSA and 10.2% for WA (Figure 8). At 5 bar, the compressive strength value for OSA is 21.5 MPa and for WA it is 10.1 MPa. At 15 bar, the compressive strength values are increased to 34.5 MPa for OSA and 16.7 MPa for WA ( Figure 9). For both samples, linear increasing dependency is observed at similar rates for CO 2 uptake and compressive strength measurements under increasing curing pressures (cured for 2 h).
It is also known that the CO 2 gas penetration into cementitious materials under high and low CO 2 concentration levels would be different, which affects the total CO 2 uptake levels. [37]. The CO 2 uptake value for OSA is 10.8% and for WA it is 9.4% at the curing with 100% CO 2 concentration. The CO 2 uptake values are decreased to 7.6% for OSA and 7.9% for WA (Figure 10) at the curing with FG (16% CO 2 ). The compressive strength of samples cured in 100% CO 2 are higher than the samples cured in FG, which is in line with less CO 2 uptakes. Due to the higher content of Ca-Mg silicates, which participate in hydraulic or pozzolanic reactions in OSA compacts, the compressive strength values were higher than WA compacts. At longer curing periods, CO 2 uptake values of FG curing can reach the same level as 100% CO 2 curing.
with 100% CO2 concentration. The CO2 uptake values are decreased to 7.6% for OSA and 7.9% for WA ( Figure 10) at the curing with FG (16% CO2). The compressive strength of samples cured in 100% CO2 are higher than the samples cured in FG, which is in line with less CO2 uptakes. Due to the higher content of Ca-Mg silicates, which participate in hydraulic or pozzolanic reactions in OSA compacts, the compressive strength values were higher than WA compacts. At longer curing periods, CO2 uptake values of FG curing can reach the same level as 100% CO2 curing.   with 100% CO2 concentration. The CO2 uptake values are decreased to 7.6% for OSA and 7.9% for WA ( Figure 10) at the curing with FG (16% CO2). The compressive strength of samples cured in 100% CO2 are higher than the samples cured in FG, which is in line with less CO2 uptakes. Due to the higher content of Ca-Mg silicates, which participate in hydraulic or pozzolanic reactions in OSA compacts, the compressive strength values were higher than WA compacts. At longer curing periods, CO2 uptake values of FG curing can reach the same level as 100% CO2 curing.

Temperature
It is noted in previous studies that the temperature during carbonation influences the dissolution rate of constituents, the solubility of CO2 and the morphology and mineralogy of the carbonates [23]. An increase in process temperature simultaneously increases the rates of all the chemical processes but reduces the CO2-solubility in water and thus CO2availability [38]. The influence of temperature was examined by evaluating CO2 uptake levels ( Figure 11) and compressive strength (Figure 12). In both samples, the CO2 uptake levels are elevated at higher temperatures; however, the same is not true for strength development. This indicates that a higher CO2 uptake does not always validate higher strength development. A higher carbonation degree at high temperature can cause the

Temperature
It is noted in previous studies that the temperature during carbonation influences the dissolution rate of constituents, the solubility of CO 2 and the morphology and mineralogy of the carbonates [23]. An increase in process temperature simultaneously increases the rates of all the chemical processes but reduces the CO 2 -solubility in water and thus CO 2availability [38]. The influence of temperature was examined by evaluating CO 2 uptake levels ( Figure 11) and compressive strength ( Figure 12). In both samples, the CO 2 uptake levels are elevated at higher temperatures; however, the same is not true for strength development. This indicates that a higher CO 2 uptake does not always validate higher strength development. A higher carbonation degree at high temperature can cause the double-chain silicate anion structure of CSH to decompose and consequently slow the compressive strength gain [39]. It is known that with increased carbonation, the micromechanical property of CSH is weakened [40]. For OSA, the highest compressive strength value (24.8 MPa) is attained at 50 • C. For WA, the highest compressive strength (14.7 MPa) is attained at 25 • C. For both samples, the lowest strength value is attained at the highest temperature. Reduction in compressive strength at higher temperatures in both samples can also be explained by the initial fast CO 2 uptake, causing weaker carbonate crystals in compacts. The temperature effect on the stability of carbonates is further discussed in the thermal analysis section.

Temperature
It is noted in previous studies that the temperature during carbonation influences the dissolution rate of constituents, the solubility of CO2 and the morphology and mineralogy of the carbonates [23]. An increase in process temperature simultaneously increases the rates of all the chemical processes but reduces the CO2-solubility in water and thus CO2availability [38]. The influence of temperature was examined by evaluating CO2 uptake levels ( Figure 11) and compressive strength ( Figure 12). In both samples, the CO2 uptake levels are elevated at higher temperatures; however, the same is not true for strength development. This indicates that a higher CO2 uptake does not always validate higher strength development. A higher carbonation degree at high temperature can cause the double-chain silicate anion structure of CSH to decompose and consequently slow the compressive strength gain [39]. It is known that with increased carbonation, the micromechanical property of CSH is weakened [40]. For OSA, the highest compressive strength value (24.8 MPa) is attained at 50 °C . For WA, the highest compressive strength (14.7 MPa) is attained at 25 °C . For both samples, the lowest strength value is attained at the highest temperature. Reduction in compressive strength at higher temperatures in both samples can also be explained by the initial fast CO2 uptake, causing weaker carbonate crystals in compacts. The temperature effect on the stability of carbonates is further discussed in the thermal analysis section.

Thermal Analysis
Based on the TGA/DTG curves of uncarbonated samples, there are three major mass loss steps which occur: First, related to water loss due to evaporation and later dehydration of crystalline and amorphous components i.e., ettringite (up to 200 °C ); second, dehydration of Ca(OH)2 (up to 500 °C ) (Equation (1)); and third, CO2 loss due to decomposition of CaCO3 (between 550-900 °C ) (Equation (2)) ( Figures 13 and 14).

Thermal Analysis
Based on the TGA/DTG curves of uncarbonated samples, there are three major mass loss steps which occur: First, related to water loss due to evaporation and later dehydration of crystalline and amorphous components i.e., ettringite (up to 200 • C); second, dehydration of Ca(OH) 2 (up to 500 • C) (Equation (1)); and third, CO 2 loss due to decomposition of CaCO 3 (between 550-900 • C) (Equation (2)) ( Figures 13 and 14).
Minerals 2022, 12, x FOR PEER REVIEW 13 of 26 well crystalline form of calcite [41]. This may show different thermal stability of the formation of new CaCO3 phases at above room temperatures within the applied curing conditions. This can also be attributed to poor transformation of amorphous CaCO3 into calcite, which generally has more stable formations at room temperature [42]. However, it is also known that the thermal stability of amorphous calcium carbonate could eventually increase and spontaneously crystallize.

Kinetic Analysis
The experimental real time gas monitoring results of both OSA and WA compact carbonation are shown in Figures 15 and 16, where the CO2 consumption kinetics are plotted at different temperatures. The carbonation reaction in OSA and WA compact are both There are mainly two mass loss step (water evaporation and CO 2 release from CaCO 3 ) for carbonated samples as the mass loss related to water from Ca(OH) 2 is not significant due to the carbonation of Ca(OH) 2 (Equation (3)), except for OSA carbonated at 25 • C. MS curves of OSA compacts cured at 75 • C are supporting the outcomes of the TGA curves ( Figure 13). Ca(OH) 2(s) + CO 2(g) → CaCO 3(s) + H 2 O (g) ∆H 298K = −113 kJ/mol.
As can be seen from the third mass loss step of uncarbonated samples, both ashes already include CaCO 3 in their initial forms (before hydration and carbonation). Therefore, the net CO 2 uptake is calculated by subtracting the initial (uncarbonated) mineral CO 2 related mass loss from the total CO 2 related mass loss of carbonated samples. Samples cured at 25 • C had a CO 2 uptake of 9.1 and 8.5%, respectively, for OSA and WA.
In connection with previous section, the effect of curing temperature can also be followed by both TGA/DTG curves, showing that there is clear increase in CO 2 uptake values with increased curing temperatures of 25, 50, and 75 • C. Besides, the thermal stability of the newly formed CaCO 3 can also be characterized by looking at the TG/DTG curves. The onset temperatures (for OSA, 520 • C for curing temperatures of 25, 50 and 75 • C and 580 • C for initial sample. For WA, 510 • C for curing temperatures of 25, 50 and 75 • C and 580 • C for initial sample (Figure 14)) of the DTG curves representing the initial stage of decomposition CaCO 3 of carbonated samples are slightly lower than the detected onset temperatures of uncarbonated samples. Several authors have also presented similar findings of low thermal decomposition temperatures for CaCO 3 in case of occurrence in the not well crystalline form of calcite [41]. This may show different thermal stability of the formation of new CaCO 3 phases at above room temperatures within the applied curing conditions. This can also be attributed to poor transformation of amorphous CaCO 3 into calcite, which generally has more stable formations at room temperature [42]. However, it is also known that the thermal stability of amorphous calcium carbonate could eventually increase and spontaneously crystallize.

Kinetic Analysis
The experimental real time gas monitoring results of both OSA and WA compact carbonation are shown in Figures 15 and 16, where the CO 2 consumption kinetics are plotted at different temperatures. The carbonation reaction in OSA and WA compact are both fast at the initial stage, which can be explained by the available open porous surfaces and sufficient amount of physically bound water in the open pore structures of the specimens providing a fast start of carbonation. After this stage, a stage with a slower reaction rate takes place due to the diffusion limitation through the product layer, as carbonation proceeds from the outer surface into the internal spaces. Besides, initial fast exothermic carbonation reaction also influences the particle temperatures, which can accelerate the evaporation of the physically bound water. This would cause a restriction on the diffusion of CO 2 and carbonic acid formation. Although there is no clear temperature dependency at the initial stage of the carbonation reaction, there is a positive effect of increasing temperature on CO 2 uptake especially in the diffusion-controlled stage of OSA. The CO 2 consumption trend in terms of the carbonation rate is slightly different in WA compared to OSA and varies in different temperatures. The positive effect of increasing temperature on the rate growth of WA carbonation is more apparent, pointing out more kinetic controlled reaction phenomena, already at the early carbonation stage. The increase in temperature elongates the time of the fast carbonation period, provided that the WA reacts for a longer time, before the process reaches a more diffusion-controlled stage. The trolled reaction phenomena, already at the early carbonation stage. The increase in temperature elongates the time of the fast carbonation period, provided that the WA reacts for a longer time, before the process reaches a more diffusion-controlled stage. The CO2 uptake values obtained from the gas monitoring results support the total CO2 uptake values detected in thermal analysis. The final conversion values after 2 h of curing are for OSA 0.57-0.63 and for WA 0.42-0.61. The extrapolation of graphs show that full conversion can be achieved in 12-14 h for OSA and 13-16 h for WA.  By using real time gas monitoring results obtained at three different temperatures, the reaction kinetics of the carbonation conversion were tested by different diffusion-controlled reaction-order models [43]. It is known that carbonation of Ca-Mg silicates is less reactive at alkali conditions compared to Ca(OH)2, where pH values should drop to 10 according to equilibrium calculations [6]. The obtained pH values could be considered to understand whether all Ca and Mg bearing phases are participating into carbonation reactions (see Appendix A). As the obtained pH values are around 11.5, the participation of Ca-Mg silicates into carbonation reaction should be negligible. Therefore, the amount of total CO2 that can bound during carbonation is calculated according to most reactive available phases of the ashes, which are CaO and Ca(OH)2 without including Ca-Mg silicates. The quantitative XRD analysis (see Table 2) results of initial OSA and WA were used as the basis for the calculation with Equation (4) given below. In order to estimate and compare the CO2 binding ability of different samples, CO2max, the maximal possible CO2 up- By using real time gas monitoring results obtained at three different temperatures, the reaction kinetics of the carbonation conversion were tested by different diffusion-controlled reaction-order models [43]. It is known that carbonation of Ca-Mg silicates is less reactive at alkali conditions compared to Ca(OH) 2 , where pH values should drop to 10 according to equilibrium calculations [6]. The obtained pH values could be considered to understand whether all Ca and Mg bearing phases are participating into carbonation reactions (see Appendix A). As the obtained pH values are around 11.5, the participation of Ca-Mg silicates into carbonation reaction should be negligible. Therefore, the amount of total CO 2 that can bound during carbonation is calculated according to most reactive available phases of the ashes, which are CaO and Ca(OH) 2 without including Ca-Mg silicates. The quantitative XRD analysis (see Table 2) results of initial OSA and WA were used as the basis for the calculation with Equation (4) given below. In order to estimate and compare the CO 2 binding ability of different samples, CO 2 max, the maximal possible CO 2 uptake capacity of the samples was calculated on the basis of the Ca(OH) 2 (taking into account its CaO as free CaO) and free CaO content of initial sample.
Previous studies have shown that carbonation kinetics of industrial alkaline solid wastes [44,45] can be sufficiently demonstrated by two solid-state kinetic models, which were combined into Equation (5) [46]: where k is the rate constant, t is the reaction time, n is a (parametrizable) index of the rate determining step, and α is the conversion degree (carbonation turnover, α = 1 for full carbonation) according to Equation (6).
where, m 0 is the initial weight, m t is the weight at time t, and m f is the final weight. By adapting the exponent n in Equation (5), two kinetic models can be defined. For n = 1, Equation (5) represents a purely phase-boundary controlled reaction that applies to the initial stages of carbonation. For n = 2, Equation (5) applies to a diffusion-limited reaction (Jander equation), where the rate-limiting step is diffusion through the growing layer of precipitated CaCO 3 . The conformity between experimental data and the kinetic model was expressed by the correlation coefficients (R 2 ).
The Arrhenius equation is presented below.
where k is the rate constant, A is the pre-exponential (frequency) factor, e is Euler's number, E a is the activation energy, T is absolute temperature, and R is the gas constant. The activation energy can be determined from the slope of the transformed equation ln(k) = ln(A) − E a /RT (8) with the linear fitting of ln(k) and 1/T (See Appendix B). The activation energy (E a ) for OSA has been calculated as 3.55 kJ/mol and for WA as 17.06 kJ/mol. The activation energy values exhibited in literature for CaO and Ca(OH) 2 carbonation reactions are in line with the calculated values in this work [47]. Figure 17 shows the converted experimental data of the carbonation tests (i.e., ln(1 − (1 − α) 1/3 ) vs. ln(t). A relatively high R 2 value indicates that the model adequately represents the kinetics of carbonation. The values of Equation (5) to the converted data suggest that the reaction is phase-boundary controlled during the initial stages of accelerated carbonation for OSA (ln(t) < 2.5) and WA (ln(t) < 2.9) samples. After the change in reaction rate, carbonation becomes controlled by diffusion through the product-layer. The transition between the two kinetic models is illustrated by the change of the slope for the plot of ln(1 − (1 − α) 1/3 ) vs. ln(t). For WA reaction conditions, the change in slope seems to be less pronounced and later than OSA, which can be related to higher SSA of WA delaying the beginning of the diffusion phase, which is in line with the CO 2 monitoring graphs (Figures 14 and 15). This indicates that rate limitations by diffusion through a growing layer of precipitated CaCO 3 are less important when the solid is in motion (exposure of internal surfaces), corroborating the higher CO 2 -uptake. rate, carbonation becomes controlled by diffusion through the product-layer. The transition between the two kinetic models is illustrated by the change of the slope for the plot of ln(1 − (1 − α) 1/3 ) vs. ln(t). For WA reaction conditions, the change in slope seems to be less pronounced and later than OSA, which can be related to higher SSA of WA delaying the beginning of the diffusion phase, which is in line with the CO2 monitoring graphs (Figures 14 and 15). This indicates that rate limitations by diffusion through a growing layer of precipitated CaCO3 are less important when the solid is in motion (exposure of internal surfaces), corroborating the higher CO2-uptake.

XRD Analysis
XRD analysis was performed to confirm the products of carbonation and to identify what phases were consumed in the reaction. Evidence suggested that Portlandite was consumed almost completely, while calcite was the primary product. The XRD patterns of the hydrated samples in Figures 18 and 19 show evidence of some pre-existing carbonates present as calcite in the hydrated ashes, while the sample patterns included clear portlandite peaks for both OSA and WA. A good match was found in comparing the XRD pattern of the carbonated compacts to the XRD pattern of natural calcite, which confirmed that the major carbonation product was calcite. The carbonated samples showed new and more intense XRD peaks corresponding to calcite. The trace amount of Aragonite was detected with minimal intensities, which are not displayed here. Pre-existing Quartz peaks were identified in both OSA (higher intensity) and WA. CSH peaks were identified in both hydrated and carbonated samples, which indicates that CS were hydrated by the hydration process. Anhydrite and Ettringite were present in the OSA samples only.

XRD Analysis
XRD analysis was performed to confirm the products of carbonation and to identify what phases were consumed in the reaction. Evidence suggested that Portlandite was consumed almost completely, while calcite was the primary product. The XRD patterns of the hydrated samples in Figures 18 and 19 show evidence of some pre-existing carbonates present as calcite in the hydrated ashes, while the sample patterns included clear portlandite peaks for both OSA and WA. A good match was found in comparing the XRD pattern of the carbonated compacts to the XRD pattern of natural calcite, which confirmed that the major carbonation product was calcite. The carbonated samples showed new and more intense XRD peaks corresponding to calcite. The trace amount of Aragonite was detected with minimal intensities, which are not displayed here. Pre-existing Quartz peaks were identified in both OSA (higher intensity) and WA. CSH peaks were identified in both hydrated and carbonated samples, which indicates that CS were hydrated by the hydration process. Anhydrite and Ettringite were present in the OSA samples only.   Figure 20a shows the microstructure of an area near the surface of the hydrated OSA compact. Figure 20b shows the 5000× magnified surface of compact cured at 25 °C. Although the particles are not definitively separate and the hydrated products seem to be fused together, the hexagonal portlandite lamellar appears to be covered by irregular, flaky, and grainy products with dimensions in the order of 1 µ m. The porous surface structure of the hydrated OSA compact changes after carbonation and becomes more compact. No visible portlandite crystals are identified in the carbonated compacts, which agrees with the near total conversion suggested by the XRD data. The carbonated products have fused into a coating that makes it difficult to discern the shape or location of the original OSA particles. It has been suggested [48] that the carbonation reaction products end up becoming intermixed into calcium silicate hydrate, such that it is unable to identify distinct carbonation product morphologies with SEM analyses. Nevertheless, the gel and the carbonation products have filled the spaces between the particles or even fused them together. The effect of fast carbonation in higher temperatures is observed as micro crack formations, which can explain the lower strength values attained at the highest temperature (75 °C) (Figure 21). Similarly, the microstructure of the hydrated WA specimen, as seen in Figure 22a, displays distinct morphological evidence of a more open structure near the surface of the hydrated WA compact. Figure 22b shows more compact structure of the WA compact cured at 25 °C, covered with globular formations. Some acicular or flaky products can be seen and were identified as calcium carbonates. Agglomeration of calcium silicate hydrate particles forming gel like structures surrounding the calcium carbonates can be observed. In carbonated compacts, no portlandite crystals are identified, which agrees with the near total conversion suggested by the XRD data.  Figure 20a shows the microstructure of an area near the surface of the hydrated OSA compact. Figure 20b shows the 5000× magnified surface of compact cured at 25 • C. Although the particles are not definitively separate and the hydrated products seem to be fused together, the hexagonal portlandite lamellar appears to be covered by irregular, flaky, and grainy products with dimensions in the order of 1 µm. The porous surface structure of the hydrated OSA compact changes after carbonation and becomes more compact. No visible portlandite crystals are identified in the carbonated compacts, which agrees with the near total conversion suggested by the XRD data. The carbonated products have fused into a coating that makes it difficult to discern the shape or location of the original OSA particles. It has been suggested [48] that the carbonation reaction products end up becoming intermixed into calcium silicate hydrate, such that it is unable to identify distinct carbonation product morphologies with SEM analyses. Nevertheless, the gel and the carbonation products have filled the spaces between the particles or even fused them together. The effect of fast carbonation in higher temperatures is observed as micro crack formations, which can explain the lower strength values attained at the highest temperature (75 • C) ( Figure 21). Similarly, the microstructure of the hydrated WA specimen, as seen in Figure 22a, displays distinct morphological evidence of a more open structure near the surface of the hydrated WA compact. Figure 22b shows more compact structure of the WA compact cured at 25 • C, covered with globular formations. Some acicular or flaky products can be seen and were identified as calcium carbonates. Agglomeration of calcium silicate hydrate particles forming gel like structures surrounding the calcium carbonates can be observed. In carbonated compacts, no portlandite crystals are identified, which agrees with the near total conversion suggested by the XRD data.

Current Results in the Context of Sustainable Building Materials
The construction materials sector needs to become more diversified and sustainable, as well as safe and performant, in order to meet the stringent environmental and technical demands [49][50][51]. Furthermore, based on the type and availability of secondary raw materials from various industrial units, the manufacturing of new construction materials should be customized to local resources.
There are a variety of commercial technologies that combine CO2 with solid waste streams due to the growing interest in waste mineralization as a feasible carbon capture

Current Results in the Context of Sustainable Building Materials
The construction materials sector needs to become more diversified and sustainable, as well as safe and performant, in order to meet the stringent environmental and technical demands [49][50][51]. Furthermore, based on the type and availability of secondary raw materials from various industrial units, the manufacturing of new construction materials should be customized to local resources.
There are a variety of commercial technologies that combine CO2 with solid waste streams due to the growing interest in waste mineralization as a feasible carbon capture

Current Results in the Context of Sustainable Building Materials
The construction materials sector needs to become more diversified and sustainable, as well as safe and performant, in order to meet the stringent environmental and technical demands [49][50][51]. Furthermore, based on the type and availability of secondary raw materials from various industrial units, the manufacturing of new construction materials should be customized to local resources.
There are a variety of commercial technologies that combine CO2 with solid waste streams due to the growing interest in waste mineralization as a feasible carbon capture

Current Results in the Context of Sustainable Building Materials
The construction materials sector needs to become more diversified and sustainable, as well as safe and performant, in order to meet the stringent environmental and technical demands [49][50][51]. Furthermore, based on the type and availability of secondary raw materials from various industrial units, the manufacturing of new construction materials should be customized to local resources.
There are a variety of commercial technologies that combine CO 2 with solid waste streams due to the growing interest in waste mineralization as a feasible carbon capture and utilization technology. For instance, an accelerated carbonation technique was developed by Carbon8 Systems Ltd. (Gillingham, UK) for the remediation of industrial wastes and contaminated soils to produce construction products [52]. Additionally, Carbicrete (Montreal, Canada) uses a mineral carbonation method to create a concrete manufactured from mainly steel slags and CO 2 (8% from flue gas) with a compressive strength 50% higher than ordinary concrete [53]. In addition, Carbstone Innovation (Genk, Belgium) uses CO 2 to cure slags from electric arc furnaces and basic oxygen furnaces for use as building material [54]. Similar to the commercialized technologies above, when the results of this study are considered for a specific target product, the process can be improved and optimized in line with the associated standards.
Compressive strength of 10-36 MPa and CO 2 uptake of 11-15% mass was achieved by mineral carbonation. These findings show that there is a room for improvement and potential for future applications such as kerbstone paver and paving blocks. The findings exhibited better performance of compressive strength compared to previous explorations of cementitious properties of similar FAs [20]. Telesca et al. [55,56] studied coal FA as a raw material to produce ettringite-based construction materials and discovered that it has the potential to be used in this method. They obtained a maximum compressive strength of around 6 MPa, which was achieved after 16 h of curing. Self-cementitious characteristics and pozzolanic reactivity of FA were examined by Li et al. [57]. They achieved a compressive strength of 11.4 MPa without chemical modifiers after 28 days, and 22.4 MPa with chemical modifiers and particle size distribution optimization. Ohenoja et al. [58] discovered that compressive strength was dependent on the selectively soluble calcium, aluminium, silicate, and sulphate content. Tests including different FAs have achieved a compressive strength of up to 6 MPa after 28 days.

Conclusions
This study analyses the performance of compacts produced from locally sourced distinct FAs such as OSA, WA, and LFA, in terms of CO 2 uptake and compressive strength under numerous process conditions (i.e., 25-75 • C, 5-15 bar, 15-100% CO 2 , and compaction pressures of 150 and 300 kgf/cm 2 ).
Among the two main samples, OSA compacts exhibited 10-12 wt% CO 2 uptake with a compressive strength of 16-36 MPa, whereas WA compacts show a wider range of 8-13 wt% CO 2 uptake with a compressive strength of 10-16 MPa. Preliminary findings of LFA indicate that there is a future potential for applications of lightweight building materials by utilizing previously deposited combustion residues, binding~15 wt% CO 2 .
Changes in the curing conditions have a direct effect on the CO 2 uptake levels and related strength development; • Increase in gas pressure and CO 2 concentration exhibited positive correlation with the CO 2 uptake and compressive strength values; • Compaction pressure as a pre-processing parameter is mainly related to compressive strength. However, due to its physical effect on diffusivity, the compaction pressure increase showed an increase in strength while limiting CO 2 penetration in a small amount, causing less CO 2 uptake; • Despite higher carbonation degrees at elevated curing temperatures, the compressive strength did not increase accordingly. High temperatures can increase the risks of micro cracks and change the micro-mechanical property of CSH, which in turn weakens the compressive strength; • Additionally, at high temperatures, due to the reduction of liquid water in compacts, uneven and fast formation of particulates (amorphous formations of calcite polymorphs) on the surfaces of mainly Ca(OH) 2 can appear, yet such determination is rather complex for short curing times (2 h); • SEM and XRD analysis further proved that Calcite was the dominant phase after carbonation and portlandite was almost completely consumed; • Reaction mechanism corresponds to 3D-diffusion-controlled reaction order model for both OSA and WA. CO 2 diffusion through the product layer was estimated to be the rate-controlling step and surface passivation was clearer for OSA, except for WA, due to the short curing time. Calculated apparent activation energies are given for OSA as 3.55 kJ/mol and for WA as 17.06 kJ/mol.
The prospective result of this study enables greater insight into the CO 2 curing processes of ashes, which can be transferred to the industrial building material applications for tailoring of the locally available Estonian ash as well as similar ash elsewhere.

Conflicts of Interest:
The authors declare no conflict of interest. The funders had no role in the design of the study; in the collection, analyses, or interpretation of data; in the writing of the manuscript, or in the decision to publish the results. Appendix B Figure A1. Arrhenius chart for OSA compacts.    Figure A1. Arrhenius chart for OSA compacts.