Comparing Fly Ash Samples from Different Types of Incinerators for Their Potential as Storage Materials for Thermochemical Energy and CO2

This study aims to investigate the physical and chemical characterization of six fly ash samples obtained from different municipal solid waste incinerators (MSWIs), namely grate furnaces, rotary kiln, and fluidized bed reactor, to determine their potential for CO2 and thermochemical energy storage (TCES). Representative samples were characterized via simultaneous thermal analysis (STA) in different atmospheres, i.e., N2, air, H2O, CO2, and H2O/CO2, to identify fly ash samples that can meet the minimum requirements, i.e., charging, discharging, and cycling stability, for its consideration as TCES and CO2-storage materials and to determine their energy contents. Furthermore, other techniques, such as inductively coupled plasma optical emission spectroscopy, X-ray fluorescence (XRF) spectrometry, X-ray diffraction (XRD), scanning electron microscopy, leachability tests, specific surface area measurement based on the Brunauer–Emmett–Teller method, and particle-size distribution measurement, were performed. XRF analysis showed that calcium oxide is one of the main components in fly ash, which is a potentially suitable component for TCES systems. XRD results revealed information regarding the crystal structure and phases of various elements, including that of Ca. The STA measurements showed that the samples can store thermal heat with energy contents of 50–394 kJ/kg (charging step). For one fly ash sample obtained from a grate furnace, the release of the stored thermal heat under the selected experimental conditions (discharging step) was demonstrated. The cycling stability tests were conducted thrice, and they were successful for the selected sample. One fly ash sample could store CO2 with a storage capacity of 27 kg CO2/ton based on results obtained under the selected experimental conditions in STA. Samples from rotary kiln and fluidized bed were heated up to 1150 °C in an N2 atmosphere, resulting in complete melting of samples in crucibles; however, other samples obtained from grate furnaces formed compacted powders after undergoing the same thermal treatment in STA. Samples from different grate furnaces showed similarities in their chemical and physical characterization. The leachability test according to the standard (EN 12457-4 (2002)) using water in a ratio of 10 L/S and showed that the leachate of heavy metals is below the maximum permissible values for nonhazardous materials (except for Pb), excluding the fly ash sample obtained using fluidized bed technology. The leachate contents of Cd and Mn in the fly ash samples obtained from the rotary kiln were higher than those in other samples. Characterization performed herein helped in determining the suitable fly ash samples that can be considered as potential CO2-storage and TCES materials.


Introduction
Global population growth, massive urbanization, and economic growth have increased the consumption of natural raw materials and energy, resulting in huge amounts of waste. Since the resources are limited, sustainable resource management is necessary to secure the physical basis of society and economy in the long run [1]. Waste incineration is a key element in sustainable waste management, which decreases the amount and volume of solid waste and sanitizes the waste during incineration [2]. However, waste incinerators produce bottom ash and fly ash. The bottom ash can be deposited in nonhazardous-waste landfills or used as a road construction material.
Fly ash is particulate matter carried over from the combustion chamber and removed from the flue-gas stream prior to the addition of any type of sorbent material [3].
The composition and utilization of these fly ash samples depend on various factors, such as the fuel composition (feed), type of incinerator, air pollution control devices, and operating parameters. Therefore, these fly ash samples have diverse compositions.
In most cases, municipal solid waste is treated in grate furnace combustors [4], whereas sewage sludge and hazardous waste are mainly treated in fluidized bed combustors and rotary kilns, respectively [5][6][7][8]. Since current management practices for incinerating fly ash samples are associated with considerable environmental impacts [9], the utilization of these residues is desirable. From this viewpoint, the possible applications for fly ash samples generated from municipal solid waste incinerators MSWIs have been the focus of many researchers during the last decade. For example, Ferreira et al. categorized the possible applications of fly ashes and discussed the advantages and disadvantages of their use in road construction, cement production, and pozzolanic materials [10]. Astrup et al. reported the management and utilization of fly ash in different European countries [11]. Generally, the application of municipal solid waste (MSW) fly ash samples are challenging, owing to their high chlorine concentrations, heavy metal content, and presence of persistent organic pollutants such as dioxin and furans, which increase the treatment and management costs.
Nonetheless, there are approaches that revalorize MSW fly ash and bottom ash in thermal energy storage, particularly in sensible heat storage, owing to the pozzolanic properties of ashes [12,13]. Cherbasnki et al. presented the CO 2 sorption properties of fly ash for methane steam reforming [14]. Moreover, a possible application for MSWI fly ash samples as thermochemical energy storage (TCES) materials was reported by Setoodeh et al. [15]. TCES technology has been under development worldwide during the last decades, and interest in the industrial implementation of this type of energy storage system is increasing. In comparison with sensible and latent heat storage, TCES possesses advantages such as high energy density and unlimited energy storage duration without loss. However, TCES requires suitable and affordable materials for its operation to be comparable with other existing state-of-the-art storage technologies, such as sensible and heat energy storage. Investigations show that well-known TCES materials are suitable for different temperature levels [16][17][18][19][20]. Nonetheless, the screening of TCES materials has focused only on raw or doped materials. Overall, raw TCES materials possess drawbacks, such as sintering [21][22][23], slow conversion rates [22], low cycling stability [17], low thermal conductivity [17], and high costs [17,24], and researchers have attempted to overcome these drawbacks by doping or mixing raw TCES materials with other TCES/sensible heat storage materials [24][25][26][27][28]. For instance, the cycling stability of a calcium oxide (CaO)/CaCO 3 system decreased with the number of cycles because the carbonation of CaO to form CaCO 3 was significantly slow and sintering of material occurred at high temperatures [29]. Therefore, researchers investigated and improved the durability of the CaO/CaCO 3 system by adding inert materials, such as TiO 2 [33]. Chen et al. studied the impact of SiO 2 doping on the CaO/CaCO 3 system and reported an enhanced cycling stability, reduction of energy storage times, and higher released heat owing to the high thermal conductivity of SiO 2 [26].
However, a material that can meet all the TCES requirements from the technical, environmental, and economic viewpoints remains under development. To the best of our knowledge, wastes or byproducts from industries have not yet been studied for use as TCES materials; however, the chemical compositions of MSW fly ash samples, their reduced or zero cost, harmful environmental impact, and amount produced per year make them an interesting material for further investigation regarding their revalorization as thermochemical and CO 2 storage materials.
CaO, along with Al 2 O 3 , SiO 2 , and metal salts, is a main component of fly ash and a promising potential candidate for TCES systems [15]. One special feature of CaO is its ability to reversibly react with water vapor (H 2 O (g) ) and carbon dioxide (CO 2 ) to build two TCES systems (Equations (1) and (2) Figure 1 shows the basic principle of a TCES system [20]. Excess thermal heat from any plant, such as a concentrated solar power system, steam reforming plant, or MSWI, can be used as input heat to decompose a chemical component or mixture of different chemicals A (s) (fly ash herein) into their components (B (s) and C (g) ) through endothermic reactions, known as the charging step (first requirement). The charged component B (s) can be used for a period of time to produce component A (s) on providing the required heat while reacting with gas component C (g) through exothermic reactions, which is known as the discharging step (second requirement). The charging and discharging step involve heat consumption and release, respectively (Equations (1) and (2)). Figure 2 shows the comparison of the energy contents of different types of heat storage technologies compared with those of Ca(OH) 2 and CaCO 3 [34].  [26]. However, a material that can meet all the TCES requirements from the technical, environmental, and economic viewpoints remains under development. To the best of our knowledge, wastes or byproducts from industries have not yet been studied for use as TCES materials; however, the chemical compositions of MSW fly ash samples, their reduced or zero cost, harmful environmental impact, and amount produced per year make them an interesting material for further investigation regarding their revalorization as thermochemical and CO2 storage materials.
CaO, along with Al2O3, SiO2, and metal salts, is a main component of fly ash and a promising potential candidate for TCES systems [15]. One special feature of CaO is its ability to reversibly react with water vapor (H2O(g)) and carbon dioxide (CO2) to build two TCES systems (Equations 1 and 2/at 25 °C). Figure 1 shows the basic principle of a TCES system [20]. Excess thermal heat from any plant, such as a concentrated solar power system, steam reforming plant, or MSWI, can be used as input heat to decompose a chemical component or mixture of different chemicals A(s) (fly ash herein) into their components (B(s) and C(g)) through endothermic reactions, known as the charging step (first requirement). The charged component B(s) can be used for a period of time to produce component A(s) on providing the required heat while reacting with gas component C(g) through exothermic reactions, which is known as the discharging step (second requirement). The charging and discharging step involve heat consumption and release, respectively (Equations 1 and 2). Figure 2 shows the comparison of the energy contents of different types of heat storage technologies compared with those of Ca(OH)2 and CaCO3 [34].   Based on Equation 2, fly ash can be carbonated by simultaneously harvesting energy. Hence, MSWI fly ash can be considered as a carbon capture and storage (CCS) material. The application of fly ash generated from coal-fired power plants (CFPPs) for CO2 capture and storage is discussed and reviewed earlier by Wee et al. and later by Dindi et al. [35,36]. Both papers concluded that fly ash from CFPPs can be considered as CCS materials in the raw or synthesized forms, such as zeolite or silica. Furthermore, they reported carbonation effect on the stabilization of fly ash for use as an admixture in cement (Dindi et al.) or for stabilizing harmful components in fly ash, such as Cd, Pd, As, and S [35,36].
Harvesting and storing heat energy through reversible exothermic carbonation and endothermic decarbonation of fly ash is another advantage along with the aforementioned carbonation effect.
In our earlier investigation, three fly ash samples from the same technology (grate furnaces) were chemically characterized for their application as TCES materials. Results revealed that all three fly ash samples could store heat, and one fly ash could release the stored heat under designated conditions [15]. To obtain the complete spectra of various fly ash samples obtained from different types of incinerators to determine their TCES and CO2 storage potential, extensive characterization of samples from grate furnaces, rotary kiln, and fluidized bed was performed.
Different waste and biomass combustion technologies are shown in Figure 3 (left), which can provide fly ash for storage purposes. Fine fly ash particles can be separated from the flue-gas stream at the heat exchanger or at particle separators as boiler ash and cyclones or filters, respectively. Fly ash is stored in appropriate storage facilities according to the intended storage duration (short time or seasonal storage). Charging and discharging/CO2 binding of fly ash can be accomplished as an external process (using separate reactors) or by applying an in situ approach; discharging and CO2 fixation can be done by entering the charged (decarbonated) fly ash into the heat exchanger part of the plant and exposing it to CO2 in the flue gas. Charging is conducted by feeding the discharged (carbonated) fly ash into the burning chamber. As an alternative, discharging can also be conducted in a slurry reactor (achieving ash stabilization subsequently). It is also possible to utilize the energy storage material off-site by transporting it to remote energy extraction facilities by truck, train, or pipeline to make use of the stored thermal energy. Aged or excess fly ash can be used in cement industries and construction sites or as a stabilization material (binder) in landfill operations. Stabilized fly ash could also be landfilled directly.  (2), fly ash can be carbonated by simultaneously harvesting energy. Hence, MSWI fly ash can be considered as a carbon capture and storage (CCS) material. The application of fly ash generated from coal-fired power plants (CFPPs) for CO 2 capture and storage is discussed and reviewed earlier by Wee et al. and later by Dindi et al. [35,36]. Both papers concluded that fly ash from CFPPs can be considered as CCS materials in the raw or synthesized forms, such as zeolite or silica. Furthermore, they reported carbonation effect on the stabilization of fly ash for use as an admixture in cement (Dindi et al.) or for stabilizing harmful components in fly ash, such as Cd, Pd, As, and S [35,36].

Based on Equation
Moreover, the carbonation of MSW fly ash and its positive impact on immobilizing heavy metals, such as lead and zinc, have been studied previously [37][38][39][40][41].
Harvesting and storing heat energy through reversible exothermic carbonation and endothermic decarbonation of fly ash is another advantage along with the aforementioned carbonation effect.
In our earlier investigation, three fly ash samples from the same technology (grate furnaces) were chemically characterized for their application as TCES materials. Results revealed that all three fly ash samples could store heat, and one fly ash could release the stored heat under designated conditions [15]. To obtain the complete spectra of various fly ash samples obtained from different types of incinerators to determine their TCES and CO 2 storage potential, extensive characterization of samples from grate furnaces, rotary kiln, and fluidized bed was performed.
Different waste and biomass combustion technologies are shown in Figure 3 (left), which can provide fly ash for storage purposes. Fine fly ash particles can be separated from the flue-gas stream at the heat exchanger or at particle separators as boiler ash and cyclones or filters, respectively. Fly ash is stored in appropriate storage facilities according to the intended storage duration (short time or seasonal storage). Charging and discharging/CO 2 binding of fly ash can be accomplished as an external process (using separate reactors) or by applying an in situ approach; discharging and CO 2 fixation can be done by entering the charged (decarbonated) fly ash into the heat exchanger part of the plant and exposing it to CO 2 in the flue gas. Charging is conducted by feeding the discharged (carbonated) fly ash into the burning chamber. As an alternative, discharging can also be conducted in a slurry reactor (achieving ash stabilization subsequently). It is also possible to utilize the energy storage material off-site by transporting it to remote energy extraction facilities by truck, train, or pipeline to make use of the stored thermal energy. Aged or excess fly ash can be used in cement industries and construction sites or as a stabilization material (binder) in landfill operations. Stabilized fly ash could also be landfilled directly. Owing to the existence of CaO in different phases, such as aluminate, silicate, and carbonate, all the fly ash samples were analyzed via X-ray diffraction (XRD). The determination of the particle-size distribution (PSD) and specific surface analysis based on the Brunauer-Emmett-Teller (BET) method were performed in addition to XRF, inductively coupled plasma optical emission spectroscopy (ICP-OES), and simultaneous thermal analysis (STA). STA measurements were performed to obtain information regarding the reactivity of fly ash samples in different atmospheres and to identify the fly ash samples that could meet the following criteria for a TCES material.
• Charging (endothermic reactions through thermal treatment) o A(s) (fly ash/discharged) + heat  B(s) (fly ash/charged) + C(g) • Discharging (exothermic reaction by reacting with reactive gases, such as H2O and CO2) o B(s) (fly ash/charged) + C(g)  A(s) (fly ash/discharged) + heat • Cycling stability test (various charging and discharging of heat) Furthermore, leachability test was performed to evaluate the environmental impact of fly ash. Scanning electron microscopy (SEM) analysis was conducted to determine the morphology changes before and after STA treatment up to 1150 °C in an N2 atmosphere. Owing to the existence of CaO in different phases, such as aluminate, silicate, and carbonate, all the fly ash samples were analyzed via X-ray diffraction (XRD). The determination of the particle-size distribution (PSD) and specific surface analysis based on the Brunauer-Emmett-Teller (BET) method were performed in addition to XRF, inductively coupled plasma optical emission spectroscopy (ICP-OES), and simultaneous thermal analysis (STA). STA measurements were performed to obtain information regarding the reactivity of fly ash samples in different atmospheres and to identify the fly ash samples that could meet the following criteria for a TCES material.

•
Charging (endothermic reactions through thermal treatment) A (s) (fly ash/discharged) + heat B (s) (fly ash/charged) + C (g) • Discharging (exothermic reaction by reacting with reactive gases, such as H 2 O and CO 2 ) B (s) (fly ash/charged) + C (g) A (s) (fly ash/discharged) + heat • Cycling stability test (various charging and discharging of heat) Furthermore, leachability test was performed to evaluate the environmental impact of fly ash. Scanning electron microscopy (SEM) analysis was conducted to determine the morphology changes before and after STA treatment up to 1150 • C in an N 2 atmosphere.

Fly Ash Sampling and Waste Incineration Plants
Herein, six fly ash samples from five different types of waste incineration plants, i.e., rotary kiln, fluidized bed, and grate furnaces, were selected. Samples were collected at regular intervals over a period of four years. To obtain representative samples, the fly ash samples were combined and homogenized prior to their use for different analyses. As mentioned previously, fly ash characterization depends on the number of plant-linked parameters. Therefore, brief descriptions of the plants are given below.
Plant A In plant A, MSW is treated in a grate furnace. Downstream from the boiler, activated coke is injected into the flue-gas stream to adsorb Hg, and this pollutant-loaded activated coke is separated together with fly ash from the flue gas using a filter separator. This filter ash is removed from the plant together with boiler ash. Furthermore, the dedusted flue gas is cleaned using a multi-stage scrubber and selective catalytic reduction (SCR) device.
Plant B In plant B, MSW is treated in a grate furnace. The air pollution control and fly ash removal systems are identical to those in plant A.
Plant C In plant C, MSW is treated in a grate furnace. Downstream from the boiler, ash is separated from the flue-gas stream using an electrostatic precipitator (ESP). In this plant, boiler ash and ESP ash can be removed and stored separately. Therefore, the two different ashes were sampled separately. Furthermore, the dedusted flue gas is cleaned in a multi-stage scrubber, SCR device, and fixed-bed activated coke filter.
Plant D Plant D uses rotary kiln technology for treating hazardous waste. Downstream from the boiler, ash is separated from the flue-gas stream using an ESP. This filter ash is removed from the plant together with boiler ash. Then, the dedusted flue gas is cleaned using a multi-stage scrubber, SCR device, and fixed-bed activated coke filter.
Plant E In plant E, refuse-derived fuel is treated in a fluidized bed combustor. Downstream of the boiler, ash is separated from the flue-gas stream using an ESP. This filter ash is removed from the plant together with boiler ash. Then, the dedusted flue gas is cleaned using a multi-stage scrubber, SCR device, and fixed-bed activated coke filter.

Chemical and Physical Analysis of Fly Ash Samples
Specific surface measurement was performed through physisorption (ASAP 2020, Micromeritics GmbH, Unterschleißheim, Germany). N 2 gas was used, and the bath temperature used during the analysis was 195 • C. To eliminate the adsorbed gases and moisture from the sample, the sample was heated to 120 • C under vacuum overnight. The sample masses were 0.2-0.8 g.
PSD was measured using a laser diffraction analyzer (Mastersizer 2000, Malvern PANalytical, Almelo, Netherlands) and red and blue helium-neon light source at 633 and 466 nm, respectively. With this setup, it was possible to measure particle sizes in 50 different classifications of 0.02-2000 µm. All the samples analyzed herein were dry-dispersed at an injector air pressure of 2 bar. A sample mass between 2 and 10 g was placed on the vibrating gutter, and at least six measurements were performed for each sample to calculate an average value.
For the total content analysis of nonmatrix elements, fly ash samples were digested in aqua regia according to EN 13657 (2002) and subsequently analyzed according to EN 11885 (2009) using an ICP-OES (Optima 8300 ICP-OES spectrometer equipped with an SC-2 DX FAST sample preparation system) (Perkin Elmer, Waltham, MA, USA). A customized single-element standard was used for the calibration.
To determine the total content of matrix elements, samples were milled to a grain size of 250 µm and subsequently analyzed via X-ray fluorescence spectrometry (XRF, NITON XL3t Air) (Thermo Fischer Scientific, Waltham, MA, USA).
Powder XRD measurements were performed on a PANalytical X'pert-Pro diffractometer (CuKα, 45 kV, 40 mA, continuous scan, Soller slits 0.04 rad, Bragg-Brentano HD mirror, X'Celerator detector, 2Θ range 5 • -70 • , 200 s/step measurement time) (PANalytical, Almelo, Netherlands). The representative samples were manually ground in an agate mortar for 5-10 min and mounted on a zero-background sample holder with minute amounts of grease. Evaluation and phase identification were performed using the search and match routine of the PANalytical HighScore Plus Program Suite on the ICDD database (ICDD, 2017) [42]. This was followed by Rietveld refinement with TOPAS software (Brucker, Billerica, MA, USA) using CIF files from the ICSD database [43,44].
The STA data obtained in the different atmospheres were generated on a Netzsch STA 449 Jupiter instrument equipped with a TGA-DSC sample holder (Erich Netzsch GmbH & Co. Holding KG, Selb, Germany). This instrument maintained a water-vapor furnace, including an air-cooled double jacket, heated vapor inlet, heated transfer line, and heated collar. The oven had the capacity to operate between 25 • C and 1250 • C, regulated by an S-type thermocouple. All samples were measured in aluminum oxide crucibles using various gas atmospheres (N 2 , N 2 /O 2 (air), CO 2 , H 2 O, and CO 2 /H 2 O). Some samples, which demonstrated melting or were not separable from the crucible after decomposition (fly ash samples D and E), were not tested in all conditions (see Table 1). The oven was heated at 30 • C/min to 1240 • C, setting a sample temperature of approximately 1150 • C for all experiments. Table 1 lists an overview of the performed experiments.
A cycling stability test was performed for the selected fly ash sample. The sample (30 mg) was heated to 880 • C at a heating rate of 30 • C/min in an N 2 atmosphere (charging step). After a stabilization time of 30 min, the atmosphere was changed to a mixture of CO 2 (100 ml/min) and water vapor (1 g/h), cooled at 10 • C/min from 880 • C to 350 • C and maintained at 350 • C for 30 min. This cycle was repeated thrice.
A FEI Quanta 250 FEGSEM microscope (FEI, Hillsboro, OR, USA) was used for SEM images. These were recorded at a 5-kV acceleration voltage under a high vacuum of 6 × 10 −6 mbar. A magnification of 1000 shows the thermal treatment of samples very well compared with higher resolutions. In accordance with the standard EN 12457-4 (2002), the leachability test was performed on the original samples.

BET Surface Area
The BET surface areas are listed in Table 2. Fly ash samples A and B (grate furnaces) display the highest surface areas of 3.6 and 4.3 m 2 /g, respectively, followed by fly ash C (filter ash from grate furnace) with a surface area of 2.1 m 2 /g. Other fly ash samples have average surface areas of 1.6 ± 0.1 m 2 /g. Fly ash samples A and B have higher BET surface areas owing to the higher unburned carbon contents or activated carbon added to the fly ash sample in the air pollution control system. The lower BET surface areas of fly ash samples correspond to the finest fractions, which contain less unburned carbon and higher inorganic content [45].

PSD Analysis
PSD analysis of fly ash samples plays a vital role in assessing and evaluating their potential utilization and environmental impact since it directly influences their characteristics [46]. A comparison of PSD results is shown in Figure 4, which indicates that only boiler ash sample C-boiler has a bimodal distribution with modes at 4 and 315 µm and large fraction of coarse particles reaching 2000 µm.
Fly ash sample C-filter has a multimodal distribution with modes at every magnitude from 1 to 100 µm. It is noteworthy that there are no particles larger than 1000 µm. Samples A and B are from different plants having the same combustion process and parameters. Both show a bimodal distribution of 0.2-1000 µm with modes at approximately 1, 10, and 100 µm. Fly ash sample E shows unimodal distribution in the range 1-2000 µm with mode at 400 µm. Fly ash sample D also shows a multimodal distribution in the range 1-2000 µm with notable mode at 315 µm. Regarding the E, D, and C boilers, coarse particles reach 2000 µm. It can be interesting to investigate their elemental compositions to identify the size fractions, wherein elements such as Ca accumulate; the same is applicable to the fine grain size fraction of approximately 1 µm of the A, B, and C-filters.

Chemical Composition of Fly Ash Samples
The total content of matrix elements determined by XRF is listed in Table 3, and the total content of nonmatrix elements determined by ICP-OES is listed in Table 4. Regarding the XRF results, the elemental content is calculated for the oxide form. Most elements should exist in their oxide form;

Chemical Composition of Fly Ash Samples
The total content of matrix elements determined by XRF is listed in Table 3, and the total content of nonmatrix elements determined by ICP-OES is listed in Table 4. Regarding the XRF results, the elemental content is calculated for the oxide form. Most elements should exist in their oxide form; however, some are present as carbonates, sulfates, and possibly chlorides. Investigated fly ash samples mainly comprise Na 2 O, SiO 2 , Al 2 O 3 , SO 3 , Cl, and CaO. The boiler ash from plant C shows the highest content of CaO, which appears to be the most suitable compound for TCES investigations. The remaining fly ash samples have similar CaO-content ranges, except for fly ash sample D, which contains less CaO than all the other samples. Fly ash samples D and E have the highest SiO 2 and sulfur contents, which, in fly ash sample E, is due to the high velocity in the fluidized bed reactor, partially removing the bed material (sand), a major source of SiO 2 . Plants A, B, C-filter, and E produce fly ash with similar CaO contents.  Furthermore, based on the ICP-OES analysis, plant C-boiler ash shows low values of potentially hazardous elements, such as Pb, Cd, Hg, and As, in comparison with other fly ash samples from grate furnaces (A, B, C-filter). Fly ash samples A, B, and C-filter show similarities in their matrix and nonmatrix elements. Fly ash sample D shows a higher Pb content than the other fly ash samples.
All fly ash samples contain high zinc contents, exceeding 18000 mg/kg, except those from plants C-boiler and E. Zn can be recovered using the FLUWA/FLUREC process, which has already been fully applied in Switzerland [47][48][49]. Similar research was conducted by Fellner et al. on zinc (Zn) recovery from fly ash samples in Europe [4].

XRD Analysis
Qualitative phase analysis shows that all samples contained extremely complex phase compositions (Figures 5 and 6). The peak search routines were only helpful for the 4-6 main compounds, but Rietveld refinements revealed that various additional phases must be present. The six compounds mostly comprised different amounts of quartz, anhydrite, calcite, halite, and sylvite. Aluminosilicates were present in the form of belite, mayenite, and gehlenite; however, feldspars and pyroxenes were also found in some samples. If phosphate is present in larger amounts, it gets crystallized as whitlockite. Most samples contained metallic aluminum in low amounts, and iron was found in the form of hematite (see Table 5).  Table 5) are included. A visible difference in the background height is due to sample fluorescence (Fe) and possible differences in the amorphous content.  Table 5) are included. A visible difference in the background height is due to sample fluorescence (Fe) and possible differences in the amorphous content.  The difference curve shows a good fit for the main peaks; however, minor phases that could not be clearly identified probably exist. Table 5. XRD-Rietveld refinement results of six compounds (given in wt % and normalized to 100%). Amorphous contents and unidentified minor components are probably present but could not be accounted for. Therefore, the quantification error is estimated at 20% relative and minimum of 2% absolute. Samples C-filter, A, and B had very similar phase contents, containing large amounts of salts (NaCl, KCl, and CaSO 4 ). Sample D mainly contained salts in the form of sulfates (Na 2 SO 4 and K 3 Na(SO 4 ) 2 ).

Compound
Most samples contain portlandite (Ca(OH) 2 ), which is probably an alteration product of free lime (CaO), which reacts very quickly with moisture in the air.

Thermogravimetric Analysis and Differential Scanning Calorimetry (TGA/DSC) of Fly Ash Samples
The fly ash samples from grate furnaces, rotary kiln, and fluidized bed combustors were analyzed by STA in different atmospheres, such as N 2 , synthetic air, CO 2 , H 2 O, and H 2 O/CO 2 .
The STA results are given in Figures 7-9. Fly ash samples A, B, and C-filter from grate furnaces demonstrate three similar steps of mass change (mass loss) within the investigated temperature range (30 • C-1150 • C). The mass loss was constant at 1150 • C for 30 min at this temperature. 0.5% mass loss up to 300 °C can be observed, which is related to the desorption of physically and chemically adsorbed water. This type of fly ash contains more sulfates and sodium, such as Na2SO4 and K3Na(SO4)2, confirmed by XRD, and less Ca, as confirmed by XRF analysis. A mass loss of 11.3% occurs over the entire temperature range for this type of fly ash. Fly ash sample E shows three steps of mass loss over the total temperature range up to 1150 °C with the least mass loss of below 10% in total. This can be attributed to fly ash sample E having the highest silicon oxide content based on XRF analysis.  The relative mass changes with the appropriate temperature ranges and reaction types are listed in Table 6. Table 6. Temperature range and percent mass loss for each fly ash and reaction type; temperature range (TR), reaction type (RT), endothermic reaction (Endo), and exothermic reaction (Exo). The different mass loss trends can be explained based on the variations in feed, combustion technology, bed temperature, and gas cleaning system.

TR /°C
After conducting the first TGA experiment on all fly ash samples in a N2 atmosphere, it was    Figure 9 shows the thermogravimetric (TG) signals of the experimental samples in N2, synthetic air, H2O, and CO2 atmospheres. In N2 atmosphere, the fly ash sample generated from the grate furnace in plant B showed the maximum mass loss and that from fluidized bed E showed the minimum mass loss. As mentioned previously, fly ash samples D and E were not subjected to STA in atmospheres other than N2 because they exhibited a phase change during heating in N2 atmosphere, questioning their suitability as TCES materials. In synthetic air, CO2, and H2O atmospheres, fly ash sample B exhibited the highest mass loss and fly ash sample C-boiler exhibited the lowest mass loss. The percentage mass changes in fly ash samples in different atmospheres are shown in Figure 9.   Figure 9 shows the thermogravimetric (TG) signals of the experimental samples in N2, synthetic air, H2O, and CO2 atmospheres. In N2 atmosphere, the fly ash sample generated from the grate furnace in plant B showed the maximum mass loss and that from fluidized bed E showed the minimum mass loss. As mentioned previously, fly ash samples D and E were not subjected to STA in atmospheres other than N2 because they exhibited a phase change during heating in N2 atmosphere, questioning their suitability as TCES materials. In synthetic air, CO2, and H2O atmospheres, fly ash sample B exhibited the highest mass loss and fly ash sample C-boiler exhibited the lowest mass loss. The percentage mass changes in fly ash samples in different atmospheres are shown in Figure 9.  Figure 10 shows the charging and discharging steps for all fly ash samples. The charging steps were performed in N2 atmosphere up to 880 °C, whereas discharging was performed in CO2 and H2O atmosphere, and samples were cooled to 70 °C at a rate of 10 °C/min. All fly ash samples underwent exothermic reactions followed by mass loss, despite fly ash sample D showing no endothermic peaks in its DSC signal. Only fly ash sample C-boiler showed the reverse reaction under these experimental conditions. Up to 880 °C, the fly ash can store 226 kJ/kg (integrations of DSC peaks with linear base line) followed by a mass loss of 10.3%. The thermal energy released during the reverse reaction was 86 kJ/kg based on 38% conversion according to the mass signal. The first mass loss up to 500 • C occurs because of desorption of physically and chemically adsorbed water combined with volatilization of organic components and volatile elements existing in fly ash samples [15,50,51]. The mass loss continues in the temperature range 530 • C-770 • C, and an average mass loss of approximately 4% is observed for fly ashes A, B, and C-filter. This step demonstrates the decomposition of Ca(OH) 2 or other metal hydroxides existing in fly ash samples [15]. The last step of 770 • C-1150 • C indicates the breakdown of carbonate, sulfate, aluminum salts, and chlorides [15,50,51]. The DSC signals confirm endothermic reactions at the second and third steps of the mass loss for fly ash samples A, B, and C-filter, which are related to the dehydration of hydroxides and decomposition of carbonates and sulfates, respectively. C-filter differs in mass loss in the third step compared to fly ashes A and B due to differences in the sulfate, carbonate, and chloride contents.
Fly ash sample C-boiler shows four steps of mass loss. The total mass change of fly ash sample C-boiler is significantly less than those of A, B, and C-filter. XRF analysis indicated high SiO 2 and Al 2 O 3 contents in fly ash sample C-boiler in comparison with the other fly ash samples. These compounds contribute less toward the mass loss with respect to the inert behaviors of these components.
Fly ash sample D from a rotary kiln shows an almost continuous mass loss. A small step with 0.5% mass loss up to 300 • C can be observed, which is related to the desorption of physically and chemically adsorbed water. This type of fly ash contains more sulfates and sodium, such as Na 2 SO 4 and K 3 Na(SO 4 ) 2 , confirmed by XRD, and less Ca, as confirmed by XRF analysis. A mass loss of 11.3% occurs over the entire temperature range for this type of fly ash. Fly ash sample E shows three steps of mass loss over the total temperature range up to 1150 • C with the least mass loss of below 10% in total. This can be attributed to fly ash sample E having the highest silicon oxide content based on XRF analysis.
The relative mass changes with the appropriate temperature ranges and reaction types are listed in Table 6. Table 6. Temperature range and percent mass loss for each fly ash and reaction type; temperature range (TR), reaction type (RT), endothermic reaction (Endo), and exothermic reaction (Exo). The different mass loss trends can be explained based on the variations in feed, combustion technology, bed temperature, and gas cleaning system.
After conducting the first TGA experiment on all fly ash samples in a N 2 atmosphere, it was observed that samples from rotary kiln D and fluidized bed E were melted and they were not removable from the crucibles. Figure 8 shows the TGA curves of fly ashes from plants A, B, C-filter, and C-boiler in different atmospheres, namely N 2 , air, H 2 O, and CO 2 . Fly ash samples A, B, and C-filter show the same trend of curves in different atmospheres, whereas fly ash C-boiler shows a different trend. The TGA signal of fly ash C-boiler in a CO 2 atmosphere exhibits different behavior. It is noteworthy that at 410 • C, fly ash samples A, B, and C-filter displayed mass losses, whereas C-boiler ash showed a 2.7% (w/w) mass increase. This direct carbonation with L/S = 0 shows a CO 2 -storage capacity of 27 kg CO 2 /ton fly ash. CO 2 sequestration of coal power plants varies in the range between 265 kg CO 2 to 25.2 kg/ton fly ash depending on the chemical composition and carbonation procedures performed, i.e., direct or indirect [36].
The trend of reduced mass loss was observed during all the experiments that were conducted in synthetic air. The total mass loss is least in the synthetic air atmosphere due to oxidation of metals, which reduces the mass change. The maximum mass changes in all fly ash samples were detected in the N 2 atmosphere. The total mass loss for fly ashes A, B, and C-filter in water vapor and CO 2 atmospheres showed intermediate behavior with respect to the total mass loss in comparison to those in N 2 and O 2 atmospheres. The total mass loss was constant for fly ash C-boiler in CO 2 and water vapor and N 2 atmospheres. Figure 9 shows the thermogravimetric (TG) signals of the experimental samples in N 2 , synthetic air, H 2 O, and CO 2 atmospheres. In N 2 atmosphere, the fly ash sample generated from the grate furnace in plant B showed the maximum mass loss and that from fluidized bed E showed the minimum mass loss. As mentioned previously, fly ash samples D and E were not subjected to STA in atmospheres other than N 2 because they exhibited a phase change during heating in N 2 atmosphere, questioning their suitability as TCES materials. In synthetic air, CO 2 , and H 2 O atmospheres, fly ash sample B exhibited the highest mass loss and fly ash sample C-boiler exhibited the lowest mass loss. The percentage mass changes in fly ash samples in different atmospheres are shown in Figure 9. Figure 10 shows the charging and discharging steps for all fly ash samples. The charging steps were performed in N 2 atmosphere up to 880 • C, whereas discharging was performed in CO 2 and H 2 O atmosphere, and samples were cooled to 70 • C at a rate of 10 • C/min. All fly ash samples underwent exothermic reactions followed by mass loss, despite fly ash sample D showing no endothermic peaks in its DSC signal. Only fly ash sample C-boiler showed the reverse reaction under these experimental conditions. Up to 880 • C, the fly ash can store 226 kJ/kg (integrations of DSC peaks with linear base line) followed by a mass loss of 10.3%. The thermal energy released during the reverse reaction was 86 kJ/kg based on 38% conversion according to the mass signal.

Energy Density
To determine the energy content of fly ash samples on thermal treatment up to 1150 °C, the endothermic peaks generated in DSC signals were integrated with a linear base line; results are listed in Table 7.
Fly ash sample D shows no endothermic peak, whereas fly ash sample C shows the highest energy content of 394 kJ/kg.

Energy Density
To determine the energy content of fly ash samples on thermal treatment up to 1150 • C, the endothermic peaks generated in DSC signals were integrated with a linear base line; results are listed in Table 7. Fly ash sample D shows no endothermic peak, whereas fly ash sample C shows the highest energy content of 394 kJ/kg. The measured energy content of fly ash C-boiler (394 kJ/kg) is not negligible in comparison with potential metal oxide candidates at high temperatures, such as Co 3 Figure 11 shows cycling stability test results for three cycles of selected fly ash C-boiler because this meets the first (charging) and second requirements (discharging).  The measured energy content of fly ash C-boiler (394 kJ/kg) is not negligible in comparison with potential metal oxide candidates at high temperatures, such as Co3O4/CoO, CuO/Cu2O, Mn2O3/Mn3O4, and MnO2/Mn2O3 with energy content values of 844, 810, 202, and 480 kJ/kg, respectively, in TCES [27,28,34]. Figure 11. shows cycling stability test results for three cycles of selected fly ash C-boiler because this meets the first (charging) and second requirements (discharging). Figure 11. Cycling stability test of fly ash C-boiler heated to 800 °C at a heating rate of 30 °C/min in a N2 atmosphere (charging step) and cooled from 800 °C to 350 °C at a cooling rate of 10 °C/min in CO2 (100 ml/min) and H2O (1 g/h) atmosphere.

Cycling Stability Test
The initial mass loss of 15% up to 880 °C in a N2 atmosphere (charging) is due to the decomposition of organic compounds, hydroxides, carbonates, and sulfates, and vaporization of light heavy metals, such as Zn, Cd, and their chloride compounds [15,51,52]. The reverse reaction occurs through the carbonate of fly ash with a mass gain of 3.9%, starting at 100 min for the first cycle. The second discharging cycle continued at 200 min with a mass loss of 4% in N2 atmosphere, and the reverse carbonation reaction was completed at 300 min with an expected mass increase of 4%. The same trend of mass changes was observed for the third discharging and charging steps. Hence, based on the experiment results, the third requirement for TCES material, i.e., cycling stability (charging and discharging), can be met by fly ash C-boiler for three cycles. The carbonation reaction time under the designated experimental conditions was set at 85 min for each cycle (cooling from 880 °C to 350 °C and maintaining at 35 °C for 30 min). Results showed that the reaction for each step was completed faster, i.e., in 40 min, than the set time of 85 min. Table 8 lists the specific energy contents of decomposition (charging) up to 880 °C and reverse reaction of the decomposed form of fly ash C-boiler with gas components (100 ml/min CO2 and 1 g/h H2O). The measured energy content for charging is based on integration of DSC peaks with a linear baseline and that for discharging is obtained from the mass signal. Figure 11. Cycling stability test of fly ash C-boiler heated to 800 • C at a heating rate of 30 • C/min in a N 2 atmosphere (charging step) and cooled from 800 • C to 350 • C at a cooling rate of 10 • C/min in CO 2 (100 ml/min) and H 2 O (1 g/h) atmosphere.
The initial mass loss of 15% up to 880 • C in a N 2 atmosphere (charging) is due to the decomposition of organic compounds, hydroxides, carbonates, and sulfates, and vaporization of light heavy metals, such as Zn, Cd, and their chloride compounds [15,51,52]. The reverse reaction occurs through the carbonate of fly ash with a mass gain of 3.9%, starting at 100 min for the first cycle. The second discharging cycle continued at 200 min with a mass loss of 4% in N 2 atmosphere, and the reverse carbonation reaction was completed at 300 min with an expected mass increase of 4%. The same trend of mass changes was observed for the third discharging and charging steps. Hence, based on the experiment results, the third requirement for TCES material, i.e., cycling stability (charging and discharging), can be met by fly ash C-boiler for three cycles. The carbonation reaction time under the designated experimental conditions was set at 85 min for each cycle (cooling from 880 • C to 350 • C and maintaining at 35 • C for 30 min). Results showed that the reaction for each step was completed faster, i.e., in 40 min, than the set time of 85 min. Table 8 lists the specific energy contents of decomposition (charging) up to 880 • C and reverse reaction of the decomposed form of fly ash C-boiler with gas components (100 ml/min CO 2 and 1 g/h H 2 O). The measured energy content for charging is based on integration of DSC peaks with a linear baseline and that for discharging is obtained from the mass signal.

Scanning Electron Microscopy
SEM analysis was performed to determine the changes in the particle morphology after STA treatment. Figure 12 shows the thermal effects on all samples. Fly ash samples from rotary kiln (fly ash sample D) and fluidized bed (fly ash sample E) were melted. In all the other samples, agglomeration and sintering were observed; however, samples were in compact powder form and could be removed from the crucible. On the contrary, fly ash C-boiler was less affected by thermal treatment from an optical viewpoint. Agglomeration and sintering effects can negatively impact the cycling stability of a material in TCES, which should be considered in further investigations.

Scanning Electron Microscopy
SEM analysis was performed to determine the changes in the particle morphology after STA treatment. Figure 12 shows the thermal effects on all samples. Fly ash samples from rotary kiln (fly ash sample D) and fluidized bed (fly ash sample E) were melted. In all the other samples, agglomeration and sintering were observed; however, samples were in compact powder form and could be removed from the crucible. On the contrary, fly ash C-boiler was less affected by thermal treatment from an optical viewpoint. Agglomeration and sintering effects can negatively impact the cycling stability of a material in TCES, which should be considered in further investigations.
Fly ash sample A Fly ash sample B Fly ash sample C-filter

Leaching Test
Ashes from combustors are exposed to different atmospheres and natural processes throughout storage, utilization, or disposal, which may trigger contamination of water sources by the leaching of heavy metals [53]. Different leaching tests have been conducted to determine the affinity of these metals with their surroundings. The leaching capacity of these metals is pH dependent; therefore, pH is the dominant factor in defining their leaching rate [54]. Leaching analysis plays a vital role in assessing the utilization and treatment of fly ash samples [3,53].
The leaching test results (EN 12457-4) are presented in Table 9. The limit values are the lower limits for non-hazardous-waste landfill, whereas the highest limits are listed in brackets, as set by the Austrian landfill ordinance [15,55]. The Pb leaching values of samples A, B, and C-filter are considerably higher than in the nonhazardous-waste category. The Mn and Cd leaching contents from fly ash sample D from a rotary kiln were significantly higher than the limit values or values

Leaching Test
Ashes from combustors are exposed to different atmospheres and natural processes throughout storage, utilization, or disposal, which may trigger contamination of water sources by the leaching of heavy metals [53]. Different leaching tests have been conducted to determine the affinity of these metals with their surroundings. The leaching capacity of these metals is pH dependent; therefore, pH is the dominant factor in defining their leaching rate [54]. Leaching analysis plays a vital role in assessing the utilization and treatment of fly ash samples [3,53].
The leaching test results (EN 12457-4) are presented in Table 9. The limit values are the lower limits for non-hazardous-waste landfill, whereas the highest limits are listed in brackets, as set by the Austrian landfill ordinance [15,55]. The Pb leaching values of samples A, B, and C-filter are considerably higher than in the nonhazardous-waste category. The Mn and Cd leaching contents from fly ash sample D from a rotary kiln were significantly higher than the limit values or values from other fly ash samples. The leaching contents of other elements and components were all below the limit values.

Conclusions
Herein, a detailed chemical and physical characterization of fly ash samples obtained from MSWI, such as grate furnaces, fluidized beds, and rotary kilns, was performed to determine the possible utilization of fly ash as TCES and CO 2 -storage materials. The main conclusions from the performed analyses are summarized as follows: • Based on the SSA results obtained between 1.5 and 4.3 m 2 /g, no specific relation between their values and potential usability of fly ashes for TCES and CO 2 storage was found. To determine the sorption potential, further analysis on the pore volume, pore size distribution, average pore diameter, and narrow microporosity parameters should be performed.

•
The PSDs of fly ash samples E (fluidized bed), C-boiler (grate furnace), and D (rotary kiln), showed unimodal, bimodal, and multimodal distributions, respectively. Fly ashes A and B from grate furnace technologies with the same combustion processes showed the same PSDs with modes at appropriately 1, 10, and 100 µm.

•
The fly ash sample C-boiler differs in Ca amount compared to other fly ash samples via XRF analysis. According to XRD results, no free CaO was detectable. However, portlandite Ca(OH) 2 and calcite (CaCO 3 ), which are most likely the alteration products of free CaO, were present in most samples. Alteration and its effect on free CaO content and subsequently on its potential for TCES and CO 2 capture should be investigated separately.

•
Based on TGA results up to 1150 • C in N 2 atmosphere, fly ashes A, B, C-filter, C-boiler (grate furnace), D (rotary kiln), and E (fluidized bed) achieved total mass losses of 37%, 40%, 32%, 13%, 11%, and 9%, respectively. Fly ash sample C-boiler had the highest energy content of 394 kJ/kg, and no endothermic peaks were detected for fly ash sample D. Fly ash samples A, B, C-filter, and E possessed energy contents of 94, 85, 98, and 50 kJ/kg, respectively. This showed that all fly ash samples, except fly ash sample D from a rotary kiln, met the first requirement of TCES under the selected experimental conditions, which is to store thermal heat through endothermic reactions.

•
The second requirement for a TCES material (exothermic reaction by reaction with reactive gas components (H 2 O and CO 2 )) was met by fly ash sample C-boiler. The energy content in fly ash sample C-boiler obtained by thermal treatment up to 880 • C was approximately 226 kJ/kg, approximately 86 kJ/kg of which could be released under the selected operational conditions in STA.

•
Cycling stability tests, i.e., various charging and discharging of heat, as the third requirement for TCES materials, were accomplished for fly ash sample C-boiler for three cycles in STA. The charging step occurred at a heating rate of 30 • C/min up to 880 • C for 30 min, followed by heat storage between 99 and 290 kJ/kg. Discharging started at a cooling rate of 10 • C/min from 880 • C to 350 • C, maintaining at 350 • C for 30 min in CO 2 and H 2 O vapor atmospheres, and followed by heat release between 73 and 101 kJ/kg.

•
Fly ash sample C-boiler could store CO 2 with a storage capacity of 27 kg CO 2 /ton fly ash.

•
According to ICP-OES analysis and leachability test, the fly ash C-boiler showed that this kind of fly ash may be considered to be nonhazardous, making this fly ash more feasible since it does not exceed the limits for disposal in standard above-ground landfills. However, before it can be considered to be a nonhazardous material such as total organic carbon, further analysis of its total dissolved solids needs to be performed. • SEM analysis of all samples before and after thermal treatment by STA up to 1150 • C in N 2 atmosphere revealed sintering, agglomeration, and melting of particles. However, fly ash samples were in compact powder form and easily removable from the crucible, except for fly ashes D (rotary kiln) and E (fluidized bed) because they melted.
It can be concluded that among all fly ash samples analyzed herein, fly ash sample C-boiler could meet the minimum requirements, i.e., charging, discharging, and cycling stability, for consideration as TCES material and can also be considered as CO 2 storage material based on direct and dry carbonation results in a TGA experiment. This study aims to bring awareness among researchers in the field of TCES to focus on raw or doping materials for producing an optimal TCES material and to take into account the byproducts and waste from industries as well. Furthermore, this study can contribute toward developing the practical application of an environmentally-sustainable solid waste management strategy. However, due to issues such as legislation, which varies from country to country, reasonable system integration considering all points regarding the potential uses of TCES, including CCS, stabilization of fly ash through carbonation by simultaneously harvesting energy, economic aspects, and life cycle assessment, must be separately investigated.