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Influence of Fuel to Oxidizer Ratio on Microwave-Assisted Combustion Preparation of Nanostructured KOH/Ca12Al14O33 Catalyst Used in Efficient Biodiesel Production

In this study, the microwave-assisted solution combustion method was utilized for the fabrication of Ca12Al14O33 as support and the amount of urea was assessed as an important parameter during synthesis of the sample. Synthesized Ca12Al14O33 with different fuel amounts was impregnated by KOH and used in the biodiesel production process with canola oil under microwave irradiation. The results presented that the crystallinity, crystalline size, specific surface area, and elemental composition of the final nanocatalysts are affected by the fuel amount. Moreover, during impregnation of potassium components, the structure of support was interestingly transformed from CaAl2O4 to Ca12Al14O33 structure due to the incorporation of potassium in an alumina lattice and more diffusion of calcium cations into a support lattice. On the other hand, when the amount of fuel passed the optimum amount (2 times the stoichiometric amount), the crystallinity was reduced due to the formation of high amounts of smoke during combustion and prevention of the entry of air (oxygen) into the system. The results of the microwave-enhanced transesterification reaction confirmed the results of the analyses that the conversion of 94.5% was obtained using an optimum sample at 450 W, 12 molar ratios of methanol/oil, 4 wt.% catalyst, and 60 min reaction time. According to the stability of the optimum sample [at least three times (>75%)], along with its unique mesoporous structure, uniform dispersion of potassium components, and high basicity sites, it can be considered as a comparable solid base nanocatalyst for biodiesel production.


INTRODUCTION
Nowadays, the production of renewable, non-toxic, eco-friendly, and environmentally friendly fuels has been of great concern to scientists and governments. Extensive research has been performed on alternative fuels, among which biodiesel has shown its high potential due to its biodegradability, similar properties to petroleum fuel, low emission profiles, excellent lubrication of the engine system, and suitability for industrial production (Mardhiah et al., 2017). Biodiesel, otherwise called fatty acid methyl ester (FAME), is commonly produced via the transesterification of vegetable oil or animal fats with methanol (Dehghani and Haghigh, 2017;Veillette et al., 2017). In fact, the viscosity of feedstocks, which has some drawbacks for engine and injection systems, is reduced by the reaction. The catalyst has an important role in the transesterification reaction, where homogeneous catalysts such as NaOH and KOH are usually utilized (Avhad and Marchetti, 2015). This reaction is carried out in a short time (about 1.5 h), while the separation process for producing the final biodiesel with an appropriate quality takes a long time (Tangy et al., 2016).
Microwave irradiation as a novel technology has been widely considered in chemical reactions (Ajamein and Haghighi, 2016;Rezaee and Haghighi, 2016) and it has been extensively studied in the field of biodiesel production in order to reduce production and separation times. Refaat et al. reported that, in addition to the reduction of the transesterification reaction time (from 75 to 4 min), the separation time was also reduced (from 60 to 3 min) (Refaat and El Sheltawy, 2008). Although microwave irradiation eases the production and separation processes, the major drawback of homogeneous catalysts is that they produce soap, and thus several separation and purification steps are required to obtain pure biodiesel. These processes could cause significant environmental problems, since wastewater is produced by the washing of biodiesel with water several times for the elimination of the soap. Therefore, heterogeneous catalysts have been suggested for biodiesel production, although they have not been meaningfully studied in the microwave system as compared to the conventional heating system Allami et al., 2019).
Heterogeneous base catalysts have extensively been proposed for biodiesel production; KOH and CaO are often used as an active phase for increasing the basicity of catalysts. Liao and Chung (2013) studied the performance of KOH/CaO in microwave-assisted biodiesel production. However, the low specific surface area and lower stability of CaO as support or during the active phase, due to a simple reaction with H 2 O and CO 2 in the air, are among the issues challenging scientists (de Sousa et al., 2016;Ye et al., 2016). The application of stable basic support was suggested to overcome this problem. Alkali earth aluminates with a general formula M x Al 2y O x+3y (M = Mg, Ba, Sr, and Ca) have some unique properties, such as high stability and thermal resistance (Quirino et al., 2016;Naderi and Nayebzadeh, 2019). It seems that calcium sources such as carbonate, nitrate, etc., due to their low prices, are a sufficient component for the preparation of alkali earth aluminate (Gupta and Agarwal, 2016;Roschat et al., 2016).
In previous studies, conventional catalyst preparation methods such as co-precipitation (Meng et al., 2013;Lu et al., 2015) and sol-gel (Selyunina et al., 2013;Mandić and Kurajica, 2015) were utilized for the fabrication of calcium aluminate. Against these long time catalyst preparation processes, the combustion method as a self-propagating high-temperature synthesis (SHS) method shows itself to be a suitable procedure for the preparation of refractory materials with high purity and significantly lower energy and time consumption (González-Cortés and Imbert, 2013;Chang et al., 2014). This method, unlike other catalyst preparation methods, does not require the annealing of final powder at high temperatures (sometimes over 1,000 • C) for extended periods of time (Varma et al., 2016;Nayebzadeh et al., 2019). A primary heat is required to initiate the oxidation/reduction reactions, where microwave irradiation has shown to have efficient external heating due to its uniform heating, fast heating rates, and hot spots, as well as selective absorption of radiation by polar substances. This is why it is called microwave combustion synthesis (MCS) (Specchia et al., 2017;Deganello and Tyagi, 2018).
Although the effect of fuel type and other variables on the structure and properties of calcium aluminate fabricated by the MCS method has been studied with our previous work (Nayebzadeh et al., , 2017a, further studies can be performed to obtain a sample with the highest activity and stability. Other parameters such as fuel-to-oxidizer, or fuel ratio (FR), microwave irradiation output power, water content in precursor, and pH of the solution have influence on the properties of the final product synthesized by the MCS method (Rosa et al., 2013;Hashemzehi et al., 2020a). Hashemzehi et al. reported that, for preparation of a nanocatalyst with good crystallinity and high activity for biodiesel production, high microwave power must be used (Hashemzehi et al., 2016). Furthermore, it was reported that FR has the greatest influence on the properties and performance of the final powder due to its effect on the temperature of the exothermic combustion reaction during catalyst preparation (Nasiri et al., 2012;Khoshbin et al., 2016) that has not been studied previously. Therefore, in this study, the effect of FR was assessed on the properties of calcium aluminate as support prepared by the MCS method. After impregnation of the potassium component on the surface of supports, their activity was examined in the microwaveenhanced transesterification of canola oil. The samples were characterized using X-ray Diffraction (XRD), Fourier-transform infrared spectroscopy (FTIR), Brunauer-Emmett-Teller (BET), Thermogravimetric (TG), Energy-dispersive X-ray spectroscopy (EDX), Field Emission Scanning Electron Microscopy (FESEM) analyses, and basicity using Hammett indicator. The level of reusability as an optimum aim for industrial use using a catalyst was evaluated for KOH/Ca 12 Al 14 O 33 nanocatalyst fabricated at optimum FR in the biodiesel production process.

Materials
Chemical grades of aluminum nitrate (Al(NO 3 ) 3 .9H 2 O), calcium nitrate (Ca(NO 3 ) 2 .4H 2 O), potassium hydroxide (KOH), urea (CH 4 N 2 O), and methanol (CH 3 OH) were purchased from Merck. All the materials were used as received without any further purification. The canola oil was supplied from a local store.

Nanocatalyst Synthesis Procedure
In the MCS method, metal salts such as nitrates are mixed with water and soluble carbohydrates as fuel. In our study, Al(NO 3 ) 3 .9H 2 O (20 mmole) and Ca(NO 3 ) 2 .6H 2 O (10 mmole) were mixed with 30 mL of deionized water in a beaker and then a desirable amount of urea with 1, 1.5, 2, or 2.5 times of stoichiometric compositions was added. According to propellant chemistry, stoichiometric compositions of the fuel-to-oxidizer ratio were calculated using the total oxidizing and reducing valences of the components . The corresponding chemical reaction for preparation of calcium aluminate with different FRs is shown as follows: After gelling the mixture by heating at 80 • C, the beaker was transformed in the domestic microwave oven (Daewoo, Model No. KOC9N2TB, 900 watts, 2.45 GHz) and irradiated for 10 min. After exhausting the huge amount of gases, the combustion reaction started and the foamy catalyst was produced. The samples were labeled as CA(FR = 1), CA(FR = 1.5), CA(FR = 2), and CA(FR = 2.5). Potassium components as active phases were impregnated by mixing the supports with the KOH aqueous solution (35 wt.%) and refluxing at 80 • C for 2 h. After aging the mixture for 12 h, it was placed in an oven at 110 • C overnight to dry. Finally, the powders were calcined at 700 • C for 4 h to obtain KCA(FR = 1), KCA(FR = 1.5), KCA(FR = 2), and KCA(FR = 2.5) (Nayebzadeh et al., 2017a). The nanocatalysts synthesis method is shown in Figure 1.

Nanocatalysts Characterization Techniques
XRD analysis was performed to determine the crystalline phase of the samples, where a UNISANTIS/XMD 300 apparatus operating at 45 kV and 80 mA with scanning range of 10-60 • by means of Cu Kα radiation was utilized. The textural properties of the sample containing a specific surface area, mean pore size, and pore volume were determined using a PHS-1020 (PHSCHINA, China) apparatus by N 2 adsorption/desorption method. TG analysis was utilized for assessing the decomposition of raw materials during catalyst preparation. The phenomenon of microwave combustion reaction was evaluated by TG analysis under air flow in the range of 50-800 • C at a heating rate of 20 • C/min performed by on an Evolution STA (SETARAm, France) instrument. Using FESEM analysis performed by MIRA3 FEG-SEM (TESCAN, Czech Republic), the morphology and surface structure of the nanocatalysts were assessed. The surface elemental distribution of the samples was depicted by the EDX technique using VEGA II Detector (Czech Republic, TESCAN). The surface functional groups of the nanocatalysts were assayed by FTIR spectra in the range of 400-4,000 cm −1 using a SHIMADZU 4300 (Japan) spectrometer. The Hammett indicators method was used to determine the basic strength (H_) of the samples where bromothymol blue (H_ = 7.2), phenolphthalein (H_ = 9.8), and 2,4-dinitroaniline (H_ = 15.0) were utilized as indicators. By titration of each color changed mixture containing 0.2 g catalyst, 10 mL methanol, and 1 mL Hammett indicator solution via 0.02 mole benzene carboxylic acid/L anhydrous ethanol solution, the basicity of the nanocatalysts was measured (Ye et al., 2014).

Experimental Setup for Catalytic Performance Test
The microwave-enhanced transesterification reaction of canola oil was carried out in a 100 mL glass reactor equipped with a water-cooled condenser for assessment of the catalytic activity of the samples. A modified domestic microwave with a hole of 20 mm at its top was utilized to carry out the reaction at microwave output power of 450 W for 1 h. For each reaction, the glass reactor was loaded by 20 g canola oil, 12 mL methanol (12 methanol/oil molar ratios), and 0.8 g catalyst (4 wt.%). Although the reaction was not performed at the optimum conditions, it can provide a suitable conversion for comparing the catalysts. At the end of the reaction, the biodiesel layer mixture was separated from glycerol and used as a catalyst by centrifuging the mixture at 2,500 rpm for 25 min. Its layer was heated to remove excess methanol and obtain pure biodiesel. The conversion of the reaction was determined based on the FAME content of the produced biodiesel. The FAME content of biodiesel was calculated by the following equation: [(area of all FAME ×weight of reference)/(area of reference ×weight of biodiesel sample)]×100 ( 2) where reference is assigned to methyl non-adecanoate as an internal standard. Area of FAME and reference were mentioned to the area of gas chromatographic (GC; Teif Gostar Faraz co., Iran) peaks of produced biodiesel equipped with FID detector and SUPRAWAX-280 capillary column (30 m × 0.25 mm × 0.25 µm).

XRD Analysis
The effect of FR on the crystalline structure of calcium aluminate is illustrated in Figure 2.  temperatures up to 1,050 • C and higher temperatures are required to have a full crystallinity (Janáková et al., 2007). The theoretical combustion temperature can be obtained using enthalpy of the reaction and a specific heat capacity of the product when the combustion process assumes adiabatic (Hashemzehi et al., 2020b). If it is assumed that only CaAl 2 O 4 was formed, the adiabatic combustion temperature obtains 923, 1,263, 1,444, and 1,557 • C for a fuel ratio of 1-2.5 (see Supplementary Material). It shows that the combustion temperature increased sharply by loading higher amounts of fuel while the rate of temperature increasing reduced at a higher fuel ratio. Moreover, less crystallinity of the sample fabricated at a fuel ratio of 1 can be proven by the calculated temperature which was under the minimum temperature needed to obtain well crystalline structure of CaAl 2 O 4 (1,050 • C). Thus, it is proven that the temperature of combustion reaction medium is extremely high (Rodríguez et al., 2012). Therefore, the nanocatalysts at the FR above 1.5 contain CaO, C 12 A 7 , CA, and Al 2 O 3 , with CA being the dominant phase (Rivas Mercury et al., 2005;Ruszak et al., 2011). The diffraction peaks of Al 2 O 3 (JCPDS No. 76-0144) and C 12 A 7 (JCPDS No. 78-0910) can be, respectively, observed at 2θ = 25.4 • and 18.1 • , especially at CA(FR = 2) nanocatalyst.
When the amount of urea increased in the mixture, the burning flame continued from seconds to minutes. An increase of combustion duration caused the formation of the welldefined crystalline structure of CA. The relative crystallinity of the as-prepared CA nanocatalyst, calculated based on the peak at 2θ = 30.1 • , clearly proves the effect of fuel increase on the formation of CA (shown in Table 1). However, the relative crystallinity decreased at a FR of 2.5. Rapid oxygen transport from air to reaction medium is significantly necessary for complete combustion, as in fuel-rich conditions. However, oxygen diffusion limitations result in incomplete combustion for the CA(FR = 2.5) nanocatalyst (Ghosh et al., 2010). The effect of reaction temperature can be significantly observed in the crystalline size of CA, as the CA(FR = 2) shows the lowest crystalline size ( Table 1).
The XRD patterns of the KOH/Ca 12 Al 14 O 33 nanocatalyst are shown in Figure 3. It can be clearly observed that the samples were transformed from CA structure to C 12 A 7 phases due to the additional heat treatment and dopant concentration (Avci et al., 2012). The phase transformation is related to the diffusion of Ca 2+ ions through the CA layer to react with Al 2 O 3 in order to form Ca 3 Al 2 O 6 (C 3 A) and C 12 A 7 , as the stable phase is finally formed at the expense of CA and C 3 A (Tao et al., 2012). In addition, the K 2 O (JCPDS No. 22-0493) and K 2 CO 3 (JCPDS No. 73-0470) phases can be recognized in the XRD patterns of the samples, especially at the KCA(FR = 2) and KCA(FR = 2.5) nanocatalysts. Less amorphous structures in the samples with high crystallinity may allow the potassium component to make individual phases. This phase has a significant effect on the activity of the catalyst in the transesterification reaction .
The relative crystallinity and crystalline size of the samples are also listed in Table 1. The KCA(FR = 2) and KCA(FR = 2.5) nanocatalysts show the highest relative crystallinity and the largest crystalline size, respectively, which might be due to the greater formation of large crystals of C 12 A 7 .

FTIR Analysis
The FTIR spectra of the KOH/Ca 12 Al 14 O 33 nanocatalysts are illustrated in Figure 4. The spectra of all the samples exhibit a bond between 3,200 and 3,400 cm −1 , which is related to O-H stretching vibration of absorbed water molecules on the surface of the nanocatalysts. Moreover, a peak at 1670 cm −1 is also assigned to the bending vibration of water molecules (Khoshbin and Haghighi, 2014;Kazemifard et al., 2019). The characteristic bond in the range of 3,400-3,600 cm −1 can be assigned to Ca/Al-OH groups (Chang et al., 2014). In addition, stretching vibration of Al-O-K groups, due to the attachment of K + ions to alumina, is also observed around 3,600 and 1,100 cm −1 . The bonds at 1,470, 1,395, 1,020, and 935 cm −1 may be associated with the characteristic vibrations of the Al-OH or Al-O-K bonding (Hashemzehi et al., 2016). The characteristic absorption regions of Al-O stretching vibrations for tetrahedral (AlO 4 ) and octahedral (AlO 6 ) are, respectively, observed in the 700-850 cm −1 and 500-700 cm −1 (Kazemifard et al., 2018). The tetrahedral bonds of Al-O confirm the formation of C 12 A 7 structure (Lu et al., 2012). The Ca-O bond is observed around 470 cm −1 (Alba- Rubio et al., 2010;Hojjat et al., 2016).

BET and Basicity Analysis
The BET properties of the samples are listed in Table 1. The specific surface area of the samples sequentially increased from 58.14 to 95.40 m 2 /g by increasing the FR. This could be due to an increase of the amounts of exhausted gas and combustion time during catalyst preparation. A similar phenomenon was also detected for pore volume and mean pore size of the samples, whereas these decreased by increasing the FR from 2 to 2.5.  27.8, 29.8, 33.4, 36.7, 41.2, 46.7, 55.2, 57.5). In the biodiesel production process, porosity of the catalyst can even play a larger role than the surface area. The diffusion of triglycerides molecules into catalyst pores contains seven stages, including: (1) passing through the external film of the catalyst, (2) diffusing into the pores, (3) adsorbing on the active surface, (4) reacting the reactants, (5) disposing the products (biodiesel and glycerol) from the catalyst surface, (6) diffusing toward the outside through the pores, and (7) passing through the external film (Ebadinezhad and Haghighi, 2020). Therefore, the pore size must be insufficient in order to perform the stages 3-7. It was mentioned that the pores must be at least 6 nm in diameter for easy permeation of triglycerides macromolecules (Jacobson et al., 2008). A number of studies have emphasized that restricted diffusion transpires when reactant molecules and pores have comparable dimensions (Lukić et al., 2010). Therefore, triglycerides molecules can easily diffuse through the pores of the major part of the KCA(FR = 2) nanocatalyst, leading to an efficient contact to be established between the reactant and active site. In addition, the KCA(FR = 2) nanocatalyst also shows the largest pores volume. As shown in Table 1, the basicity of the as-prepared catalysts was not meaningfully changed by an increased FR. The basicity is defined as a basic site for a catalyst where KOH plays the most important role in increasing the basic strength. Here, the support (CA) showed insignificant basicity strength in the studied region. Since the amount of impregnated potassium compounds on the catalysts is constant, the samples showed a similar basicity strength.

TG Analysis
The TG plots of the monocalcium aluminate prepared by different FRs, which explain the level of completing the combustion reaction, are illustrated in Figure 5. The weight loss below 150 • C is assigned to the elimination of water from the surface of supports and/or in raw material structure where the CA(FR = 1) showed the highest weight loss (5.5%) . The second reduction in weight in the range of 150-500 • C is owed to pyrolysis of organic groups and/or nitrate precursors, which exhibit incomplete combustion reaction . CA(FR = 1) and CA(FR = 2.5) have high weight loss (around 15%), which is in good agreement with the results of relative crystallinity obtained from the XRD patterns. It confirms that the optimization of the FR in the combustion method is important for obtaining the highest combustion temperature to synthesize the catalyst with a good structure and high crystallinity (Rahmani Vahid and Haghighi, 2016). The last reduction in weight occurred in the range of 500-600 • C, which could correspond to the incorporation of calcium components in the alumina lattice to form CaAl 2 O 4 . Moreover, such a reduction could be attributed to the transition of alumina from the amorphous to crystalline phase, where the CA(FR = 1) illustrates the highest amount of amorphous phases followed by the CA(FR = 1.5) and CA(FR = 2.5) samples with 3.7 and 5.2% weight loss, respectively (Yousefi et al., 2019). The CA(FR = 2) nanocatalyst with 2.5% weight loss confirms that the fuel-to-oxidizer ratio of 2 is an appropriate amount for the preparation of monocalcium aluminate (CaAl 2 O 4 ) as support.

EDX Analysis
The EDX analysis results of the KOH/Ca 12 Al 14 O 33 nanocatalysts (KCAs) are depicted in Figure 6. It can be seen that all the samples contain Al, Ca, K, and O elements and no impurity was observed. The KCAs nanocatalysts show similar element distribution percentages of Al, Ca, and K to the parent solution (35.1, 31.8, and 33.1% for Al, Ca, and K, respectively). Due to the increased combustion reaction and increased alumina in the structure with an increasing fuel ratio, the amount of Al element subsequently increased from 29.4% for the KCA(FR = 1) to 40.3% for the KCA(FR = 2.5). Moreover, the potassium component increased with an increase of the FR from 1 to 2 and then was decreased by more fuel loading. This can be related to the extreme increase of the KCA(FR = 2.5) specific surface area that caused the potassium components' distribution to decrease (as seen in Figure 6D). The dot-mapping of the samples clearly exhibited that the potassium components were homogeneously dispersed on the surface of support, especially in the KCA(FR = 2) nanocatalyst ( Figure 6C), which can result in an appropriate activity of the sample.

FESEM Analysis
The FESEM images of the CA(FR = 2) and KCA(FR = 2) nanocatalysts are illustrated in Figure 7. The combustion cavities as external gates provided during the CA(FR = 2) preparation show large diameters in the range of 300-600 nm, and cause the penetration resistance to be reduced for permeation of the reactant (especially large molecules of triglycerides) (Rahmani Vahid and Haghighi, 2016). Moreover, the morphology of the sample shows that the temperature of the combustion reaction was appropriate, such that the particle size with good distribution sizes can be observed. According to a surface particle size distribution histogram, the CA(FR = 2) nanocatalyst shows the size of the particles to be in the range of 5-17 nm with an average size of 11 nm, where the particles with 10-12 nm have the highest frequency.
The KCA(FR = 2) nanocatalyst is shown in the right side of Figure 7, in which the morphology of the CA(FR = 2) was not clearly changed by potassium loading. However, the surface particles size distribution was changed; accordingly, the average particle size increased from 11 nm to 12 nm by potassium loading. The results can be proved by the XRD analysis, where the crystalline size increased due to phase transformation from CA to C 12 A 7 . The phase transformation effect on the particle size is due to the increased bond length between Ca, Al, and O in the mayenite structure as compared to monocalcium aluminate. Minimum and maximum particle sizes of the KCA(FR = 2) nanocatalyst are, respectively, 7.4 and 18.9 nm.

Catalytic Performance Study Toward Biodiesel Production
The activity of the KOH/Ca 12 Al 14 O 33 nanocatalysts is illustrated in Figure 8. As expected, the KCA(FR = 2) and KCA(FR = 2.5) nanocatalysts showed higher activity in the conversion of canola oil to biodiesel. The samples showed a high specific surface area and mean pore size, which led to unimpeded permeation of reactants through the porosity of the catalysts, making more contact with their active phases. Moreover, the crystallinity and basicity of these samples were much more than those of the other samples, proving their higher activity. Therefore, the KCA(FR = 2) nanocatalyst was selected as the optimum catalyst and the FR of 2 seemed to be the best ratio for the preparation of calcium aluminate supported by the potassium components.
Dall 'Oglio et al. (2014) have conducted a study on the aluminum, calcium, manganese, titanium, and magnesium oxides as support for biodiesel production under microwave irradiation. The results exhibited that alumina was the best support where K 2 CO 3 /Al 2 O 3 showed the highest activity (98%) at the reaction conditions of methanol/oil molar ratio of 16 and 10 wt.% of the catalyst and reaction time of 30 min. The other potassium precursor showed an intermediate biodiesel conversion. The yield of 60 and 40% was, respectively, obtained using the KOH/Al 2 O 3 and KI/Al 2 O 3 catalyst in the microwave-assisted biodiesel production. At these conditions, the CaO/Al 2 O 3 , CaO/TiO 2 , and CaO/MnO 2 catalysts converted 46.2, 36.6, and 49.2% of soybean oil to biodiesel, respectively. This means that the Ca 12 Al 14 O 33 might be one of the best supports for the loading of active phases for biodiesel production.

Reusability of KCA(FR = 2) Nanocatalyst in the Biodiesel Production
The reusability of catalysts is an important element in the industrial application of catalysts (Nayebzadeh et al., 2014). To assess the stability of KCA(FR = 2) as an optimum nanocatalyst, it was separated from the reaction mixture after each run by centrifuging the mixture at 6,000 rpm for 20 min and washed with methanol twice time to eliminate the reactants and products from porosities. Then it was dried and calcined at 700 • C for 1 h and reused. The results are presented in Figure 9. It can be seen that the catalytic activity of KCA(FR = 2) nanocatalyst decreased from 94.5 to 80.7%, which can be related to leaching and/or poisoning of active phases (potassium components), that can be proven by the brown color of glycerol. However, in the third use, the activity of the catalyst did not meaningfully change and a yield of 76.4% was obtained. The yield slightly decreased with further uses, as a yield of 70.6% was obtained in the fifth run. The results signify that some potassium components have weak bonds with the surface of calcium aluminate as support. The results confirm that the calcium aluminate as support protects its stability during the reaction and could be an appropriate support among those reported so far for loading species for industrial application in the biodiesel production process.

Comparing the Results With Other Studies
The activity of the samples was compared with other studies as illustrated in Table 2. KOH/calcium aluminate presents good activity in the transesterification reaction as high as CaO [used in conventional (Ye et al., 2016) or microwave (Hsiao et al., 2011) heating systems]. However, CaO can react to methanol to form calcium methoxide in reaction mediums, reduce the  reaction conversion, and cause high leaching due to the solubility of methanol in a biodiesel layer (de Sousa et al., 2016). Although eggshell as a catalyst, which contains CaO as major material, shows high activity, it was obtained at a high microwave power and duration, or at a high methanol and catalyst concentration (Khemthong et al., 2012;Peng et al., 2018).
The prepared nanocatalyst also presented good activity when the reaction conditions were milder than in other studies. Doping the calcium into an alumina structure can enhance the basicity of the support along with improving the leaching problem of Ca ions reported in previous studies. In addition, the calcium aluminate has different structures that can be studied  to obtain the most active and stable structure for the biodiesel production process.
Moreover, the production procedure is so simple to set up on an industrial scale to reduce the catalyst preparation cost. However, bonding the potassium ions with the surface of the calcium aluminate can be a challenge for enhancing its reusability. It seems that utilizing other types of potassium precursors and the optimization of impregnation conditions may facilitate bonding of K ions with Ca and Al ions, which will be studied in our future work. Therefore, it seems that KOH/calcium aluminate can be further studied to assess its ability to be used for industrial application.

CONCLUSIONS
CaAl 2 O 4 as alkali calcium aluminate was successfully synthesized by the MCS method, and the effect of fuel amount during the catalyst preparation was assessed. Furthermore, the samples were impregnated by the potassium components to improve their catalytic activity for the transesterification of canola oil to biodiesel through microwave irradiation. The characterization results revealed that the monocalcium aluminate prepared by urea as fuel with twice the stoichiometric amount has a high crystallinity and good precursor decomposition during combustion. This structure was transformed to Ca 12 Al 14 O 33 structure during potassium loading and calcination due to the diffusion of Ca 2+ ions in a monocalcium aluminate lattice and/or reaction of the potassium component with alumina to form potassium aluminate. KOH/Ca 12 Al 14 O 33 showed nanoscale particles where the potassium components were uniformly dispersed on the surface of support. The nanocatalyst, due to its high specific surface area, mean pore size, crystallinity, and basicity, converted high amounts of canola oil to biodiesel through microwave irradiation. The microwaveenhanced biodiesel production was performed under conditions of 450 watts, 12 molar ratio of methanol/oil, 4 wt.% of catalyst, and 1 h reaction time, where a yield of 94.5% was obtained. The nanocatalyst presented a suitable reusability although it required optimizing amounts of the potassium components.