Bimetallic Lanthanum-Cerium-Loaded HZSM-5 Composite for Catalytic Deoxygenation of Microalgae-Hydrolyzed Oil into Green Hydrocarbon Fuels

Due to their high lipid content, microalgae are one of the most significant sources of green hydrocarbons, which might help lessen the world’s need for fossil fuels. Many zeolite-based catalysts are quickly deactivated by coke production and have a short lifetime. In this study, a bimetallic Lanthanum-Cerium (La-Ce)-modified HZSM-5 zeolite catalyst was synthesized through an impregnation method and was tested for the conversion of hydrolyzed oil into oxygen-free hydrocarbon fuels of high energy content. Initially, hydrolyzed oil (HO), the byproduct of the transesterification process, was obtained by the reaction of crude oil derived from Chlorella vulgaris microalgae and a methanol. Various catalysts were produced, screened, and evaluated for their ability to convert algal HO into hydrocarbons and other valuable compounds in a batch reactor. The performance of HZSM-5 was systematically tested in view of La-Ce loaded on conversion, yield, and selectivity. NH3-TPD analysis showed that the total acidity of the La-Ce-modified zeolites was lower than that of the pure HZSM-5 catalyst. TGA testing revealed that including the rare earth elements La and Ce in the HZSM-5 catalyst lowered the catalyst propensity for producing coke deposits. The acid sites necessary for algal HO conversion were improved by putting La and Ce into HZSM-5 zeolite at various loading percentages. The maximum hydrocarbon yield (42.963%), the highest HHV (34.362 MJ/Kg), and the highest DOD% (62.191%) were all achieved by the (7.5%La-2.5%Ce)/HZSM-5 catalyst, which was synthesized in this work. For comparison, the hydrocarbon yield for the parent HZSM-5 was 21.838%, the HHV was (33.230 MJ/Kg), and the DOD% was 44.235%. In conclusion, La and Ce-loading on the parent HZSM-5 may be responsible for the observed alterations in textural properties; nevertheless, there is no clear correlation between the physical features and the hydrocarbon yield (%). The principal effect of La and Ce modifying the parent HZSM-5 zeolite was to modify the acidic sites needed to enhance the conversion (%) of the algal HO during the catalytic deoxygenation process, which in turn raised the hydrocarbon yield (%) and increased the HHV and DOD%.


Introduction
The global research on alternative and sustainable energy sources has been sparked by the fact that fossil fuels are running out and that too much carbon dioxide is being released into the atmosphere [1][2][3][4][5][6]. Using petroleum derivatives made from fossil crude oil pollutes the environment by releasing greenhouse gases, which cause serious environmental problems related to global warming [7][8][9][10][11][12].

Extraction of the Crude Oil from Chlorella vulgaris Microalgae
A Soxhlet extractor system was used to create the crude oil from Chlorella vulgaris microalgae. The original purpose of a Soxhlet extractor was to obtain a lipid out of a solid material. Most of the time, a soxhlet extraction is used when the target compound does not dissolve well in a solvent and the impurity does not dissolve in that solvent. Figure 1 shows how the Soxhlet extractor system works. It recirculates hexane by boiling and condensing it over and over again. Microalgae powder made from Chlorella vulgaris was put in the algae reservoir and 200 mL of liquid hexane was added to the hexane-oil reservoir. The hexane completely covers the powdered microalgae and breaks up a small amount of it. When a certain amount of hexane is in the algae reservoir, a siphon is made and the hexane and any oil it has dissolved drain into the hexane-oil reservoir. Here, a hot plate was used to heat the mixture of hexane and oil to (110 • C). The hexane is heated until it turns into a vapor, which rises through the tubes, shown by the dashed path in Figure 1. Oil, which has a higher boiling point, does not turn into vapor. When the vapor of hexane reaches the condenser tube, the hexane loses heat to the water that surrounds the tube. This causes the hexane to condense. The condensed hexane flows into the algae reservoir, where it soaks the microalgae powder and dissolves more oil. At 110 • C, the recirculation continues for eight hours. At the end of this extraction process, the hexane-oil reservoir is left with a mixture of hexane and oil, and the hexane-soaked filtration papers with leftover microalgae powder are left in the algae reservoir. At the end of the 8 h extraction time, the hexane-oil mixture was taken from the hexane-oil reservoir and kept well in the flask. It was then sent to the rotary evaporator to separate the hexane from the crude oil of Chlorella vulgaris microalgae. In the rotary evaporator machine, the mixture of hexane and oil is put into the hexane and oil reservoir and heated to 74 • C to remove the hexane an add it to another reservoir (the hexane reservoir), where the vaporized hexane passes through a condenser so that it can be recovered in the hexane reservoir [51]. In this study, the steps of the extraction process are shown in Figure 2.

Hydrolysis of the Crude Oil of Chlorella vulgaris Microalgae
A transesterification reaction was used to turn the crude oil of Chlorella vulgaris microalgae into fatty acid methyl esters (FAMEs), also known as algal hydrolyzed oil of Chlorella vulgaris microalgae (HO). The transesterification reaction was conducted with a hydrolysis setup that included a distillation column with a 250 mL round bottom flask with a stirrer. This flask was heated in a water bath, as shown in Figure 3. We weighed 5 g of the crude oil and heated it to 48 • C while stirring at 300 rpm for 10 min. At the same time, the methoxide (methanol-sodium hydroxide) solution was made by mixing 110 mL of methanol with 4.5 g of solid NaOH and shaking the mixture until all of the sodium hydroxide particles were dissolved. Due to the low lipid weight of the crude oil for Chlorella vulgaris microalgae, the amount of this solution (methoxide) was increased to be around 20 times greater than the crude oil weight. A total of 100 g of the methoxide solution was added to the heated crude oil, and this mixture was heated to 48 • C for 1 h while being stirred at 400 rpm [52]. After the flask cooled to room temperature, the mixture was neutralized with diluted sulfuric acid H 2 SO 4 (1 M) to a pH of 7 and then it was put in the separating funnel for 10 h. In the separating funnel, there are two layers. The top layer is made up of FAMEs and the bottom layer is made up of glycerol. Figure 3 shows in detail how 5 g of the crude oil from the microalgae Chlorella vulgaris was turned into FAMEs.
lution was added to the heated crude oil, and this mixture was heated to 48 °C for 1 h while being stirred at 400 rpm [52]. After the flask cooled to room temperature, the mixture was neutralized with diluted sulfuric acid H2SO4 (1 M) to a pH of 7 and then it was put in the separating funnel for 10 h. In the separating funnel, there are two layers. The top layer is made up of FAMEs and the bottom layer is made up of glycerol. Figure 3 shows in detail how 5 g of the crude oil from the microalgae Chlorella vulgaris was turned into FAMEs.
The resulting slurry was heated to 90 • C while being stirred at a constant temperature until all the water evaporated and it became a paste. Next, the paste was dried in an oven at 110 • C for one night and then calcined at 750 • C for three hours to get rid of any impurities [54]. It was then put in a desiccator to cool to room temperature. The synthesized catalysts were then crushed with a mortar and pestle and packed well so they could be used later in this study. The remaining catalysts ((2.5%La-7.5%Ce)/HZSM-5 and (7.5%La-2.5%Ce)/HZSM-5) were created in the same manner.

Catalyst Characterization
Characterizations of synthesized catalysts were performed to learn more about their physical and chemical properties. All of the techniques for characterization were used in the standard way. X-ray diffraction was used to figure out how crystallized the catalysts were (XRD). Using a Philips (USA) PW1730 diffractometer at 40 kV and 30 mA with Cu as the anode material (k = 1.54 Å), we obtained powder XRD patterns. In the 2θ range of 5-100 • , the scanning step size was 0.04 • /min and each step took 1 s. At −196 • C, a BELSORP-mini II (BEL Japan Inc., Toyonaka, Japan) was used to measure the isotherms for the adsorption of nitrogen. Before the samples were analyzed, they were degassed for 6 h at 200 • C under a vacuum to get rid of any compounds that had stuck to them. The Brunauer-Emmett-Teller (BET) and t-plot models were used to figure out the specific surface area and porosity. At p/p 0 = 0.95, the total pore volume was worked out. The Barrett-Joyner-Halenda (BJH) method was used to figure out the surface area and size distribution of micropores and mesopores.
Scanning electron microscopy (MIRA III, TESCAN, Brno, Czech Republic) with an energy-dispersive X-ray spectroscopy (EDS) detector (SAMX, Trappes, France) was used to figure out the shape of the zeolite surface and the size of the crystals.
Using a NanoSORD-NS91 (Sensiran Co., Pardis, Iran) analyzer, the temperatureprogrammed desorption of ammonia (NH 3 -TPD) method was used to figure out how acidic the samples were. Thermogravimetric analysis (TGA) with a Q600 (TA, New Castle, DE, USA) in an atmosphere at a heating rate of 20 • C/min between 40 • C and 800 • C was used to measure the likelihood that coke would form on all newly made catalysts. This instrument was used in an air atmosphere to perform a thermal gravimetric analysis (TGA) of the parent zeolite HZSM-5 and Lanthanum-Cerium-modified HZSM-5 zeolite catalysts with different loading weight percentages. About 20 mg of the sample was put onto the instrument and kept there for 1 min at 40 • C. The sample was then heated to 720 • C at a rate of 20 • C per minute in dry air flowing at 100 mL/min. The experiments showed that the rate of change in the sample's mass depends on the temperature (dm/dT, %/ • C).

Catalytic
Deoxygenation of the Algal HO Using the Parent HZSM-5, and Lanthanum-Cerium Modified Zeolites Figure 4 shows that the algae (HO) was deoxygenated by a catalyst in a 100 mL stirring batch reactor (Zhengzhou Keda Machinery and Instrument Co., Zhengzhou, China) (ZZKD). A total of 23.6 g of algal HO and 3.54 g of the catalyst were mixed together and then poured into the reactor. To get rid of the air, the reactor was closed and compressed three times with five bars of nitrogen (N 2 ). The initial pressure of N 2 was then compressed to 7 bar and kept in the reactor. The reactor was then heated to 300 • C and maintained at that temperature for 6 h while the impeller rotated at 1000 rpm. When the reaction was completed, the mixtures were left to cool to room temperature. The gaseous state was produced (not studied). To separate the catalyst from the liquid phase, filtration was used. Figure 5 shows that a sample of the liquid product was taken and analyzed. 2022, 27, x FOR PEER REVIEW 9 of 43 duced (not studied). To separate the catalyst from the liquid phase, filtration was used. Figure 5 shows that a sample of the liquid product was taken and analyzed.

Product Analysis
Gas chromatography-mass spectrometry (GC-MS) was used to figure out what was in the algal HO and the liquid product. The gas chromatography system used was an Agilent Technologies 7820A GC System with a mass selective detector GC-5977E MSD in electron ionization (EI) mode at 70 eV. A 100% dimethylpolysiloxane Ultra Alloy Capillary Column UA-5MS column (P/N UA1-30M-1.OF, Frontier Laboratories Ltd., Koriyama, Japan) with an inner diameter of 250 µm, a film thickness of 0.25 µm, and a length of 30 m was used. The oven was kept at 45 • C for one minute before the temperature was raised by 6 • C per minute for 40 min until it reached 300 • C. The standard mass spectrum library from the National Institute of Standards and Testing (NIST) was used to figure out what the product chemicals were. The peak area percentage of the GC-MS chromatogram, which can also be called the yield percentage, can be used to figure out the relative fraction of product chemicals [55], which was shown to be Equation (1). Equation (2) [56] and the same method described by Katikaneni et al. were used to figure out the percentage of algal HO that was converted [57]. Equation (3) was used to figure out the average content (wt%) of X, where X = C, H, and O [58]. Equation (4) was used to figure out what the product's higher heating value (HHV) was [58,59]. Equation (5) Figure 6 and Table 1 show that X-ray diffraction (XRD) was used to check the purity and crystallinity of the parent HZSM-5, (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5 catalysts. The characteristic XRD peaks of HZSM-5 at 2θ = 7. 96, 8.52, 14.8, 22.88, 24.24, 29.92, and 45.48 • match the ZSM-5 peaks of the reference standard for a highly pure calcined ZSM-5. This means that the parent HZSM-5 zeolite samples have a typical MFI-type structure (mordenite framework inverted) [61][62][63][64][65]. The different X-ray sources used were thought to be the cause of the small shift in the characteristic angles from the reference standard peaks [66].  (5%La-5%Ce)/HZSM- 5 79 The XRD patterns of (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5 are very similar to those of the parent HZSM-5 in peak positions and shapes. This also shows that the Lanthanum-Cerium-modified HZSM-5 zeolites have a typical MFI (Mobil fifth) structure [67]. As a result, no impurity peaks were found in the XRD data and crystalline phases of Lanthanum and Cerium oxides were not found in the XRD patterns. This could mean that Lanthanum and Cerium oxides are either highly dispersed and amorphous on the outside of HZSM-5 or they are much smaller and have reached the channels of HZSM-5 [39,68]. As a result, using the incipient wetness impregnation method, the mentioned weight percentages of Lanthanum-Cerium did not change the parent HZSM-5 framework. This shows that all four of the synthesized zeolites have an MFI topology and are very pure.
The XRD patterns for (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and  The XRD patterns of (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5 are very similar to those of the parent HZSM-5 in peak positions and shapes. This also shows that the Lanthanum-Cerium-modified HZSM-5 zeolites have a typical MFI (Mobil fifth) structure [67]. As a result, no impurity peaks were found in the XRD data and crystalline phases of Lanthanum and Cerium oxides were not found in the XRD patterns. This could mean that Lanthanum and Cerium oxides are either highly dispersed and amorphous on the outside of HZSM-5 or they are much smaller and have reached the channels of HZSM-5 [39,68]. As a result, using the incipient wetness impregnation method, the mentioned weight percentages of Lanthanum-Cerium did not change the parent HZSM-5 framework. This shows that all four of the synthesized zeolites have an MFI topology and are very pure.

No.
Catalyst S BET (m 2 /g) S micro (m 2 /g) S extern (m 2 /g) V total (cm 3 /g) V micro (cm 3  S BET : BET surface area was calculated by Brumauer-Emmett-Teller (BET) mode. S micro : Micropore area was determined from the t-plot micropore area. S extern : External surface area was determined from the t-plot area. V total : The total pore volumes were obtained from the adsorbed amount at P/P 0 = 0.95. V micro : The micropore volume was measured by the t-plot method. Figure 7 shows that, based on the IUPAC classification, the N 2 adsorption-desorption isotherms of the Lanthanum-Cerium-modified zeolite catalysts are type I isotherms with an H 3 hysteresis loop at a high P/P 0 region. This is typical of micropore and mesoporous samples [63,76], which are very similar to those of the HZSM-5. However, when Lanthanum and Cerium were added to the original HZSM-5 catalyst, the N 2 adsorption decreased as the relative pressure (P/P 0 ) increased. The sharp rise in the amount of N 2 that was absorbed by the samples in the low and medium pressure regions P/P 0 (0-0.35) proved that a microporous zeolite material had formed [77]. ever, when Lanthanum and Cerium were added to the original HZSM-5 catalyst, the N2 adsorption decreased as the relative pressure (P/P0) increased. The sharp rise in the amount of N2 that was absorbed by the samples in the low and medium pressure regions P/P0 (0-0.35) proved that a microporous zeolite material had formed [77]. The hysteresis loops come from the change in the uptake of nitrogen (N2) at a relative pressure (P/P0) in the range of 0.35-0.9, which shows the presence of slit-shaped pores [78,79]. The hysteresis loops come from the capillary condensation within the mesopores through nitrogen multilayers adsorbing on the inner surface [80]. As a result, both HZSM-5 and Lanthanum-Cerium-modified catalysts show a small step of N2 uptake at a relative pressure (P/P0) between 0.9 and 1.0. This is a sign of interparticle macroporosity [81]. Because of this, both the parent HZSM-5 and Lantha- The hysteresis loops come from the change in the uptake of nitrogen (N 2 ) at a relative pressure (P/P 0 ) in the range of 0.35-0.9, which shows the presence of slit-shaped pores [78,79]. The hysteresis loops come from the capillary condensation within the mesopores through nitrogen multilayers adsorbing on the inner surface [80]. As a result, both HZSM-5 and Lanthanum-Cerium-modified catalysts show a small step of N 2 uptake at a rel-ative pressure (P/P 0 ) between 0.9 and 1.0. This is a sign of interparticle macroporosity [81]. Because of this, both the parent HZSM-5 and Lanthanum-Cerium-modified catalysts have both micropores and mesopores.
3.1.3. Ammonia TPD Analysis NH 3 -TPD has been used to describe the strong acid sites and the weak acid sites on the parent HZSM-5 and Lanthanum-Cerium-modified HZSM-5 zeolite catalysts ((2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5) [82,83]. Figure 8 shows the NH 3 -TPD profiles for the parent HZSM-5 and the Lanthanum-Cerium-modified HZSM-5 zeolite catalysts. The typical NH 3 -TPD profile for the parent HZSM-5 catalyst has two maximum peaks at low and high temperatures. The low-temperature desorption peak at 216 • C has been linked to the release of NH 3 from Lewis sites (weak acid sites), such as extra-framework aluminum [84,85], while the high-temperature desorption peak at 439 • C has been linked to the release of NH 3 from the Bronsted acid sites (strong acid sites) coming from framework aluminum [86][87][88]. As shown in Figure 8, the peak areas indicate the number of acid sites and the peak temperature show the acid strength [81]. Figure 8 also shows that, for all the Lanthanum-Cerium-modified HZSM-5 zeolite catalysts compared to the parent HZSM-5, when Lanthanum and Cerium are loaded (wt.%) on the parent HZSM-5, the number and strength of all of the weak and strong acid sites decrease to a different degree, which lowers the total acidity. The alteration of zeolites with metals alters the overall acidity of the parent zeolite, which is consistent with the findings of earlier studies [63,89,90]. num-Cerium-modified HZSM-5 zeolite catalysts compared to the parent HZSM-5, when Lanthanum and Cerium are loaded (wt.%) on the parent HZSM-5, the number and strength of all of the weak and strong acid sites decrease to a different degree, which lowers the total acidity. The alteration of zeolites with metals alters the overall acidity of the parent zeolite, which is consistent with the findings of earlier studies [63,89,90].  In fact, the Lanthanum and Cerium species could enter the parent HZSM-5 zeolite tunnel by dispersing or exchanging with H + . This would change some of the strong Bronsted acid (B) centers into Lewis acid (L) centers, changing the surface acidity of the catalysts [91][92][93][94]. Moreover, Lewis-type acid sites in zeolite catalysts are mostly linked to aluminum species that are not part of the framework (extra-framework) [95], while aluminum in the zeolitic framework can cause strong acid sites [96]. Therefore, the fact that the number of Lewis acid sites is more than the number of Bronsted acid sites in doped catalysts suggests that there are more aluminum species that are not part of the framework. The XRD results suggest that the increase in aluminum species that are not part of the framework could have come from dealumination in the framework of HZSM-5. Therefore, the removal of the aluminum species from the framework can lead to a drop in the number of strong acid sites. Ouyang et al. showed that it would be helpful to stop In fact, the Lanthanum and Cerium species could enter the parent HZSM-5 zeolite tunnel by dispersing or exchanging with H + . This would change some of the strong Bronsted acid (B) centers into Lewis acid (L) centers, changing the surface acidity of the catalysts [91][92][93][94]. Moreover, Lewis-type acid sites in zeolite catalysts are mostly linked to aluminum species that are not part of the framework (extra-framework) [95], while aluminum in the zeolitic framework can cause strong acid sites [96]. Therefore, the fact that the number of Lewis acid sites is more than the number of Bronsted acid sites in doped catalysts suggests that there are more aluminum species that are not part of the framework. The XRD results suggest that the increase in aluminum species that are not part of the framework could have come from dealumination in the framework of HZSM-5. Therefore, the removal of the aluminum species from the framework can lead to a drop in the number of strong acid sites. Ouyang et al. showed that it would be helpful to stop coke deposits from forming if the number of strong acid sites were to decrease. It was also shown that reducing the number of strong acid sites made the active sites of the catalyst more stable [97].
As shown in Figure 8, for all of the Lanthanum-Cerium-modified zeolite catalysts, the low-temperature peak slightly moved to lower temperatures, with a peak profile that was similar to the parent HZSM-5 peak temperatures (at 216 • C), while the high-temperature desorption peak at (439 • C) clearly decreased, and in the case of (7.5%La-2.5%Ce)/HZSM-5, this peak disappeared. This is in line with the results of previous researchers who explained that the modification of zeolites with metals could lead to the disappearance of the hightemperature desorption peak and stated that the reason for the disappearance of this peak is due to the presence of metal ions and metal oxides. Consequently, the number and strength of sites are expected to depend on the content and location (e.g., specific cation exchange sites and extra framework) of the doped metal species [90,98].
The calibration curves of the TCD values were used to obtain the values of the desorbed NH 3 in mmol/g, which are provided in Table 3. These values were acquired from the TCD values in volts (V). However, after Lanthanum and Cerium loaded on the parent HZSM-5, the total acidities of the Lanthanum-Cerium-modified zeolite catalysts were reduced from 0.740 mmol/g for the parent HZSM-5 to 0.524 mmol/g for (2.5%La-7.5%Ce)/HZSM-5, indicating that the loading of Lanthanum-Cerium affects the acidic characteristics of the parent HZSM-5 catalysts, which led to the decrease in both strong and weak acid site amounts.
In conclusion, adding Lanthanum-Cerium to the parent HZSM-5 zeolite has a great effect on the total acid sites, especially the acidic Bronsted sites. However, this area of strong acid sites (the Bronsted sites) is thought to be the main catalytic center and include the dominant acid sites during catalytic deoxygenation reactions [32], whereas the number of weak acid sites (the Lewis sites) was deemed to be not catalytically important but it is assumed to effectively influence the proton mobility in zeolites [40]. Table 3. NH 3 -TPD properties of HZSM-5, (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5.

Thermogravimetric Analysis
Thermogravimetric analysis (TGA) was utilized to estimate the quantity of carbon that would fill the pores of freshly synthesized catalysts employed in the catalytic deoxygenation process in this study [99]. Figure 9 shows the results of the thermogravimetric analysis (TGA) for all of the freshly synthesized catalysts. It can be seen that the total mass loss for HZSM-5 is 5.4%, while it is 0.82%, 3.0%, and 3.8% for (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5, respectively, which is apparently due to the release of water from narrow channels [100,101], especially in the range of 30-170 • C, which was accompanied by water removal from the fresh samples [102]. As a result, adding Lanthanum and Cerium to the HZSM-5 catalyst makes it less likely that coke deposits form compared to the original HZSM-5. The (2.5%La-7.5%Ce)/HZSM-5 had the least mass loss.  Figure 10 shows the surface structure of the parent HZSM-5 and Lanthanum-Cerium-modified HZSM-5 zeolite catalysts with different amounts of Lanthanum and Cerium. These are (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5. Figure 10 shows that all of the samples have nanometer-sized particles that are distinctly crystalline and grouped together. Images also show that some of the particles are broken up into smaller pieces during desilication [103,104]. These pieces can also be seen in pictures of Lanthanum-Cerium-modified zeolites, and adding rare earth metals does not seem to change the structure of the zeolites very much [63]. Both the pure HZSM-5 zeolite catalysts and the Lanthanum-Cerium-modified HZSM-5 zeolite catalysts have the same shape and structure of the crystallites. In addition, the surface of Lanthanum-Cerium-modified zeolite catalysts clumped together, which may have been caused by the connection of small particles during the calcination process. After the Lanthanum-Cerium metals were added, some small particles covered the surface, and these doped samples looked a little rougher than the pure HZSM-5 [39,63]. However, at this level of magnification, it was not possible to see how the Lanthanum-Cerium particles were spread out, which is in line with the XRD patterns. The average size of the crystallites in HZSM-5 and HZSM-5 modified with Lanthanum and Cerium is 100-400 nm.  Figure 10 shows the surface structure of the parent HZSM-5 and Lanthanum-Ceriummodified HZSM-5 zeolite catalysts with different amounts of Lanthanum and Cerium. These are (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5. Figure 10 shows that all of the samples have nanometer-sized particles that are distinctly crystalline and grouped together. Images also show that some of the particles are broken up into smaller pieces during desilication [103,104]. These pieces can also be seen in pictures of Lanthanum-Cerium-modified zeolites, and adding rare earth metals does not seem to change the structure of the zeolites very much [63]. Both the pure HZSM-5 zeolite catalysts and the Lanthanum-Cerium-modified HZSM-5 zeolite catalysts have the same shape and structure of the crystallites. In addition, the surface of Lanthanum-Cerium-modified zeolite catalysts clumped together, which may have been caused by the connection of small particles during the calcination process. After the Lanthanum-Cerium metals were added, some small particles covered the surface, and these doped samples looked a little rougher than the pure HZSM-5 [39,63]. However, at this level of magnification, it was not possible to see how the Lanthanum-Cerium particles were spread out, which is in line with the XRD patterns. The average size of the crystallites in HZSM-5 and HZSM-5 modified with Lanthanum and Cerium is 100-400 nm.  In this study, all of the experiments were performed in the batch reactor under the same operating conditions (temperature, time, initial nitrogen pressure, catalyst-to-HO ratio (wt.), and stirring), which were 300 °C, 6 h, 7 bar of N2 inert gas (initial pressure), 15%, and 1000 rpm, respectively. This made it possible to compare the effects of the catalysts on conversion and product composition. The background for this study on catalytic deoxygenation, the operating conditions, were chosen based on studies completed with different types of reactants [13,43,[105][106][107]. Figure 11 and Table 4 show that the parent HZSM-5 catalyst had the lowest conversion of algal HO, 94.589%, of all the liquid products of the reactions conducted in this study. This could be because the HZSM-5 catalyst was not as effective under these reaction conditions. The percentage of algal HO conversion was higher in liquid products produced with Lanthanum-Cerium-modified zeolite than in liquid products produced with the parent HZSM-5. For the liquid product of catalytic deoxygenation for (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5, the algal HO conversion rates were 100%, 100%, and 98.035%, respectively. As a result, adding different amounts of Lanthanum-Cerium to HZSM-5 zeolite improved the acid sites that were needed to enhance the algal HO conversion.

Catalytic
Deoxygenation of the HO for the Parent HZSM-5, (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5 Catalysts In this study, all of the experiments were performed in the batch reactor under the same operating conditions (temperature, time, initial nitrogen pressure, catalyst-to-HO ratio (wt.), and stirring), which were 300 • C, 6 h, 7 bar of N 2 inert gas (initial pressure), 15%, and 1000 rpm, respectively. This made it possible to compare the effects of the catalysts on conversion and product composition. The background for this study on catalytic deoxygenation, the operating conditions, were chosen based on studies completed with different types of reactants [13,43,[105][106][107]. Figure 11 and Table 4 show that the parent HZSM-5 catalyst had the lowest conversion of algal HO, 94.589%, of all the liquid products of the reactions conducted in this study. This could be because the HZSM-5 catalyst was not as effective under these reaction conditions. The percentage of algal HO conversion was higher in liquid products produced with Lanthanum-Cerium-modified zeolite than in liquid products produced with the parent HZSM-5. For the liquid product of catalytic deoxygenation for (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5, the algal HO conversion rates were 100%, 100%, and 98.035%, respectively. As a result, adding different amounts of Lanthanum-Cerium to HZSM-5 zeolite improved the acid sites that were needed to enhance the algal HO conversion.

Compounds of the Algal HO
Tonya et al. looked at the conversion of soybean oil into hydrocarbons by catalytic deoxygenation for Pt/C, Pd/C, and Ni/C under an inert gas of nitrogen. They found that the conversion of soybean oil into hydrocarbons under the same operating conditions depends on the type of catalyst. The conversion percentages were 23%, 30%, and 93% for Pt/C, Pd/C, and Ni/C, respectively [105].
Mathias et al. studied the conversion of stearic acid for twenty different catalysts during catalytic deoxygenation at 300 • C and 6 bar of helium. They found that the percentage of stearic acid conversion depends on the type of catalyst, with 100% conversion for Pd/C and 4.6% conversion for Ir/SiO 2 being the highest and lowest, respectively [106].
Botas et al. also showed that the conversion of rapeseed oil in the catalytic cracking of HZSM-5, Ni/HZSM-5, and Mo/HZSM-5 under the same operating conditions produces different conversion percentages for rapeseed oil with different amounts of compounds [43].
In conclusion, when Lanthanum-Cerium is added to nanocrystalline HZSM-5 zeolite, it changes its acid sites and textural properties. The Lanthanum-Cerium oxides are spread out across the zeolite support, with most of them staying in the micropores. Changes in the properties of the catalyst caused by adding metals also have a great effect on how well the catalyst works.

Chemical Composition Group
In this study, the components and amounts of algal HO and the products of the catalytic deoxygenation of algal HO for the synthesized catalysts were determined using gas chromatography-mass spectrometry (GC-MS) and measured using the area normalization method. These results are shown in Figure 12a and Table 5. Algal HO contains 11.538% alkane, 61.12% esters, and 21.62% alcohol (phytol) by weight (%). Compared to the GC-MS results of algal HO and the liquid products of catalytic deoxygenation (see Table 5), the yield of phytol increased in all of the experiments performed in this study, while the yields of alkanes and esters decreased and were changed into other compounds (oxygenated compounds and non-oxygenated compounds). In conclusion, the phytol was not a reactant compound but it can be thought of as a product compound in this study. The alkanes with the fatty acid methyl esters can be thought of as reactant compounds.
The reason for this might be backed up by what other studies have found. As of now, as far as we know, there is no other study in the literature that is similar to the catalytic deoxygenation of algal HO performed in this study using the catalysts that were used. Therefore, this study's operating conditions (such as the type of reactor, temperature, time, fatty acids or FAMEs as reactants, and the initial pressure of the pumped gas) were compared with those of close catalytic studies.
Tonya et al. looked at the conversion of soybean oil into hydrocarbons by catalytic deoxygenation for Pt/C, Pd/C, and Ni/C under an inert gas of nitrogen. They found that the conversion of soybean oil into hydrocarbons under the same operating conditions depends on the type of catalyst. The conversion percentages were 23%, 30%, and 93% for Pt/C, Pd/C, and Ni/C, respectively [105].
Mathias et al. studied the conversion of stearic acid for twenty different catalysts during catalytic deoxygenation at 300 °C and 6 bar of helium. They found that the percentage of stearic acid conversion depends on the type of catalyst, with 100% conversion for Pd/C and 4.6% conversion for Ir/SiO2 being the highest and lowest, respectively [106].
Botas et al. also showed that the conversion of rapeseed oil in the catalytic cracking of HZSM-5, Ni/HZSM-5, and Mo/HZSM-5 under the same operating conditions produces different conversion percentages for rapeseed oil with different amounts of compounds [43].
In conclusion, when Lanthanum-Cerium is added to nanocrystalline HZSM-5 zeolite, it changes its acid sites and textural properties. The Lanthanum-Cerium oxides are spread out across the zeolite support, with most of them staying in the micropores. Changes in the properties of the catalyst caused by adding metals also have a great effect on how well the catalyst works.

Chemical Composition Group
In this study, the components and amounts of algal HO and the products of the catalytic deoxygenation of algal HO for the synthesized catalysts were determined using gas chromatography-mass spectrometry (GC-MS) and measured using the area normalization method. These results are shown in Figure 12a and Table 5. Algal HO contains 11.538% alkane, 61.12% esters, and 21.62% alcohol (phytol) by weight (%). Compared to the GC-MS results of algal HO and the liquid products of catalytic deoxygenation (see Table 5), the yield of phytol increased in all of the experiments performed in this study, while the yields of alkanes and esters decreased and were changed into other compounds (oxygenated compounds and non-oxygenated compounds). In conclusion, the phytol was not a reactant compound but it can be thought of as a product compound in this study. The alkanes with the fatty acid methyl esters can be thought of as reactant compounds. 11      In this study, the parts of the products were broken down into seven groups of biobased chemicals. Two groups of non-oxygenated compounds (alkanes and alkenes) and five groups of oxygenated compounds (esters, ethers, aldehydes, ketones, and alcohols) made up the seven groups. Figure 12a and Table 5 show the composition groups of the algal HO and the liquid products of the catalytic deoxygenation of the algal HO in a batch reactor at 300 • C, for 6 h, at a 15% catalyst-to-HO weight ratio, with an initial pressure of 7 bar N 2 , and at 1000 rpm.
In this study, the highest amounts of alcohol and ketones were found in the liquid products of the catalytic deoxygenation of algal HO for the (2.5%La-7.5%Ce)/HZSM-5 zeolite catalyst. The percentages of alcohol and ketones in the liquid products were 50.5% and 5.861%, respectively. The produced proportions of the oxygenated compounds ester, ether, and aldehyde were 8.152%, 4.613%, and 1.52%, respectively. Most of this catalyst's products were from the alcohol group. The produced amount of non-oxygenated compounds was 24.5% and those compounds were split between alkane (6.198%) and alkene (18.302%).
The third Lanthanum-Cerium-modified zeolite catalyst ((7.5%La-2.5%Ce)/HZSM-5) produced the most ether and hydrocarbons out of all of the catalysts made for this study (HZSM-5, (2.5%La-7.5%Ce)/HZSM-5, and (5%La-5%Ce)/HZSM-5). The percentages were 5.831% and 42.963%, respectively. The hydrocarbons (alkane and alkene) were distributed so that each contained 5.33% alkane and 37.63% alkene. On the other hand, we found that this catalyst produced the least amount of ester and ketone out of all of the catalysts that were synthesized; the percentages were 3.03% and 1.623%, respectively. The amount of aldehyde formed was 4.546% and the amount of alcohol made was 35.259%.
Furthermore, the parent HZSM-5 catalyst formed the highest amounts of the oxygenated compounds (esters and aldehydes) and the lowest amounts of the hydrocarbons (alkanes and alkenes). In this work, (7.5%La-2.5%Ce)/HZSM-5 produced the highest amounts hydrocarbons. The results also reveal that the catalyst (7.5%La-2.5%Ce)/HZSM-5 produced the least amount of ester and ketone. In this study, the highest amounts of alcohol were produced for (2.5%La-7.5%Ce)/HZSM-5.
Based on Figure 12b, there is no clear link between the physical and chemical properties of the yield of the hydrocarbon percentages. The micropore areas and surface areas of the parent HZSM-5 catalyst were the highest of all of the Lanthanum-Cerium-modified zeolites in this study. However, the yield percentages of the hydrocarbons from this catalyst (HZSM-5) were the lowest (21.833%). Meanwhile, the catalyst with the fewest micropores, (2.5%La-7.5%Ce)/HZSM-5, did not produce the highest hydrocarbon yield percentage (24.50%). As mentioned before, the micropore areas and surface areas of all of the Lanthanum-Cerium-modified zeolites were smaller than those of the HZSM-5 zeolite (see Table 2). For (7.5%La-2.5%Ce)/HZSM-5, a yield of 42.963% of hydrocarbons was found to be the highest.
It can be determined that the physical properties of the Lanthanum-Cerium loading percentages on the parent HZSM-5 are not the primary cause for the generation of hydrocarbons. This conclusion is consistent with the explanation by Zaki et al. that these physical properties, such as the surface area and micropore area, have no effect on the effectiveness of the parent catalyst (HZSM-5) for the production of olefins after it has been modified with metals, such as Cu/HZSM-5 and Ni/HZSM-5 [40]. Figure 12c shows that the acidity of all of the synthesized catalysts in this study is related to the percentage of hydrocarbon yield. It can be seen that the parent HZSM-5, which had the most acid sites (0.740 mmol/g), had the lowest hydrocarbon yield, while the (2.5%La-7.5%Ce)/HZSM-5 catalyst, which had the fewest acid sites (0.524 mmol/g) in this study, did not have the highest hydrocarbon yield. As mentioned previously, the total acid cites for all the Lanthanum-Cerium-modified zeolite catalysts were fewer than for the original HZSM-5 (refer to Figure 8 and Table 3). The total acid increased as the Lanthanum loading percentage on the parent HZSM-5 increased and the Cerium loading percentage decreased for all of the composite catalysts in this study ((2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5), which were 0.524, 0.584, and 0.602 (mmol/g), respectively.
However, the performance of catalytic deoxygenation in producing hydrocarbons changed depending on how much Lanthanum and Cerium were added to the parent HZSM-5.
In general, all of the composite Lanthanum-Cerium-modified zeolite catalysts produced higher amounts of hydrocarbons compared to the parent HZSM-5 (see Figure 12c). On the other hand, for all of the composite catalysts in this study, increasing the Lanthanum loading percentage and decreasing the Cerium loading percentage on the parent HZSM-5 increases the total acidity and the yield percentages of hydrocarbons, as shown in Figure 12c. As a result, as compared to the HZSM-5 parent catalyst, the production of hydrocarbons increased as the total acidity decreased. Figure 13 shows the proposed overall reaction pathways for the catalytic deoxygenation of algal HO for all of the synthesized catalysts in this study (HZSM-5, (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5). As mentioned before, all of these experiments were completed in the batch reactor at the same operating conditions: 300 • C, 6 h, 7 bar of N 2 , 1000 rpm, and 15% (wt.%).

Overall Reaction Pathways Proposed
Several different studies [17,24,[108][109][110][111] were used to come up with the suggested reaction pathways. In addition to the results of this study for several catalysts (see Table 5), the catalytic deoxygenation of algal HO made products, such as non-oxygenated compounds (alkane and alkene) and oxygenated compounds (aldehyde, ketone, ester, ether, and alcohol).
In this study, theories were made about how these products were made, and Figure 13 shows those theories. The type of catalyst used had a great effect on how the reaction went. As a result, it was important to figure out how each product was made during the catalytic deoxygenation of the algal HO so that the effects of the catalysts on the yield of these products could be evaluated in a realistic way. Several different studies [17,24,[108][109][110][111] were used to come up with the suggested reaction pathways. In addition to the results of this study for several catalysts (see Table  5), the catalytic deoxygenation of algal HO made products, such as non-oxygenated compounds (alkane and alkene) and oxygenated compounds (aldehyde, ketone, ester, ether, and alcohol).
In this study, theories were made about how these products were made, and Figure  13 shows those theories. The type of catalyst used had a great effect on how the reaction went. As a result, it was important to figure out how each product was made during the catalytic deoxygenation of the algal HO so that the effects of the catalysts on the yield of these products could be evaluated in a realistic way.
In this study, theories were made about how these products were made, and Figu  13 shows those theories. The type of catalyst used had a great effect on how the reactio went. As a result, it was important to figure out how each product was made during th catalytic deoxygenation of the algal HO so that the effects of the catalysts on the yield these products could be evaluated in a realistic way.

Demethylation (2a, 2b) and decarboxylation or deketonization (2c, 2d) upo the ester bond cracking
At first, FAMEs go through a thermal deoxygenation transformation mechanism described by Seames et al. [109], where FAMEs are changed into intermediates of an aldoketone (R1), acrolein (R2), and fatty acid (R3) [24], however, these intermediates are so unstable that they were not found in our results in this study (see Table 5).
The aldoketone is unstable and quickly changes into hydrocarbon radicals (R • or R \• ) or aldehyde through decarbonylation (R4 and R5) or hydrogenation (R6). By hydrogenation, the aldehyde made by this reaction (R6) could also be turned into alcohol (R7).
The fatty acids formed by R3 are deoxygenated by either decarboxylation (R10) to produce an alkane or decarbonylation (R11) to form alcohol. The alcohol formed by R11 and R7 could then be turned into an alkene by dehydration (R12, R13).
The products of ethers that were shown in this study (see Table 5), such as Disparlure and tridecyl-Oxirane, can be mostly attributed to the bimolecular dehydration of alcohols caused by R7 and R11 to produce ethers R14 and R15, as shown in Table 5. Table 5 shows the ketonic compounds, which are a type of ketone that can be produced by the ketonization process. As shown in R16, two fatty acids were combined in a dehydration process to make the anhydride. Then, the anhydride was turned into a ketone in a ketonization process while CO 2 was removed (R17). This study did not detect any symmetric ketones. This means that symmetric ketones could be broken down into olefins (R18) and non-identical ketones through γ-hydrogen transfer (R19).
The paraffins and olefins that were produced were then broken up into smaller pieces (R20-R21).
In addition to ketones, we observed the formation of aldehydes, such as Tetradecanal and Octadecanal. However, there have not been many reports of aldehyde being produced in thermal or catalytic cracking reactions. Aldehyde has only been found to form in thermal cracking at temperatures above 600 • C [112,113], which is much higher than the reaction temperature in this study (300 • C). These differences show that the aldehyde formation seen in this study is unique to the reactions on zeolite catalysts with enhanced hydrogen transfer activity and is different from thermal cracking. Even in a hydrogen-free atmosphere, algal HO deoxygenation on zeolite catalysts with increased hydrogen transfer activity still produces aldehydes as intermediates and involves hydrodeoxygenation. These signs show that there were reduction, hydrogenation, and dehydration reactions.
Reductions, such as R14, and hydrogenation, such as R6, can be explained by a mechanism called "hydrogen transfer" in which active hydrogen species are released when intermediate hydrocarbons are broken down and transferred to fatty acids and aldehydes. The reaction paths to produce alkanes through hydrogenation are the same as those proposed for the hydrocracking reactions of triglycerides on metal oxide catalysts [114]. This shows that hydrogen transfer reactions during catalytic deoxygenation have strong hydrogenation activity and that algal HO can be turned into hydrocarbons in an efficient way without using a hydrogen atmosphere.
When the hydrocarbon yield was looked at, it was found that C 11 , C 12 , C 14 , and C 19 hydrocarbons were more selective in almost all processes. This could be because of the fatty acids in the oil esters. They have a lot of oleic (C18:1) and palmitic (16:0) acids, which can cause this behavior. C 11 -C 14 hydrocarbons can be produced from oleic acid by β-scission to the double bond, followed by fatty acid deoxygenation [111] and radical reactions (disproportionation, condensation, and β-scission to the radical carbon). In addition, C6, C 8 -C 13 can be made by deoxygenating oxygenating fragments made by β-scission to a double bond. This can be achieved through similar radical reactions. Moreover, cyclic and aromatic hydrocarbons can be made from olefinic fragments, which are also formed by acid oleic β-scission [111].

The Distribution of Carbon Numbers
Based on the results shown in Figure 12a and Table 5, when looking at the algal HO conversion into product chemical composition groups, it can be seen that the catalytic deoxygenation for the synthesized catalysts conditions of an initial 7 bar N 2 pressure, 300 • C, 6 h, 15% catalyst-to-HO weight ratio, and 1000 rpm showed the high conversion of HO and the interesting chemical groups. In this study, the results are expressed in terms of carbon number and product content so that the carbon number distributions of the liquid products from these operating conditions could be compared to those of all of the synthesized catalysts.
As previously stated, there were seven groups of liquid products: two for compounds without oxygen (alkanes and alkenes) and five for compounds with oxygen (esters, ethers, aldehydes, ketones, and alcohols). The main results that were found were non-oxygenated compounds (alkenes) and oxygenated compounds (alcohols). Small amounts of alkanes, esters, ethers, aldehydes, and ketones were also found. Figure 12a and Table 5 show the compounds and contents of the algal HO. The main components of the algal HO are made up of three chemical groups: alkane (11.538%), esters (61.123%), and alcohol (phytol) (21.62%). Based on the GC-MS results (Figure 12a and Table 5), the yield of phytol increased in all of the experiments performed in this study, while the yield of alkanes and esters decreased and were turned into other compounds (oxygenated compounds and non-oxygenated compounds). In conclusion, the phytol was not a reactant compound but it can be thought of as a product compound in this study. The alkanes and the fatty acid methyl esters can be thought of as reactant compounds.
As shown in Figure 14a, the esters made up most of the algal HO (61.123%). Most of them had C 19 carbon atoms (42.776%), where those distributed 15.084% in 9,12,15-Octadecatrienoic acid, methyl ester, (Z,Z,Z)-(C 19 H 32 O 2 ) and 27.692% in 9,12-Octadecadienoic acid, methyl ester, (Z,Z,Z)-(C 19 H 34 O 2 ). The other esters were made up of 15.325% Hexadecanoic acid, methyl ester (C 17 ), 1.728% 6-Octen-1-ol, 3,7-dimethyl-, formate (C 11 ), and 1.294% Di-n-octyl phthalate (C 24 ). In Hexacosane (C 26 H 54 ), the alkane group was shown in C 26 carbon atom (26) at a yield of 11.538%. In phytol (C 20 H 40 O), the alcohol chemical group was made up of C 20 carbon atoms at a yield of 21.620%. ated compounds and non-oxygenated compounds). In conclusion, the phytol was not a reactant compound but it can be thought of as a product compound in this study. The alkanes and the fatty acid methyl esters can be thought of as reactant compounds.
For the liquid product of the catalytic deoxygenation of algal HO for the (7.5%La-2.5%Ce)/HZSM-5 zeolite (Figure 14e

Outstanding Bio-Based Chemical Products
In Equation (1), the percentage yield of the selected outstanding compounds of hydrocarbons (alkanes and alkenes) and alcohol groups from the catalytic deoxygenation of algal HO for the parent HZSM-5 catalyst and Lanthanum-Cerium-modified zeolite catalysts was calculated and is shown in Table 6. Table 6 shows that non-oxygenated compounds (hydrocarbons) and oxygenated compounds (alcohols) had higher yield percentages (<20%) during catalytic deoxygenation reactions of algal HO using the parent HZSM-5 and Lanthanum-Cerium-modified zeolites as catalysts. Consequently, these catalysts are interesting for catalyzing the deoxygenation of FAMEs even at a low Nitrogen pressure (7 bar), which means they are cheaper. Table 6. Product yield percentages of outstanding hydrocarbon (alkanes and alkenes) and alcohol compounds from catalytic deoxygenation of the algal HO for the parent and Lanthanum-Ceriummodified zeolites at 300 • C for 6 h under initial N 2 pressure of 7 bar, at 1000 rpm and with 23.6 g of algal HO/3.54 g of the catalyst in the batch reactor.  Table 6 and Figure 15 show that the yields of hydrocarbons from the catalytic deoxygenation of algal HO from Lanthanum-Cerium catalysts were higher than the yields of hydrocarbons from the parent HZSM-5 catalyst. In more detail, the total yield of hydrocarbons from the catalytic deoxygenation of algal HO for the parent HZSM-5, (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5 were 21.833%, 24.50%, 35.149%, and 42.963%, respectively. The highest yield of hydrocarbons was 42.963% and the highest conversion of algal HO was 100% (see Table 6 and Figure 16). This was completed in a batch reactor at 300 • C for 6 h with 7 bar of initial inert N 2 gas and a catalyst-to-HO ratio of 15% (by weight).  16). This was completed in a batch reactor at 300 °C for 6 h with 7 bar of initial inert N2 gas and a catalyst-to-HO ratio of 15% (by weight).    16). This was completed in a batch reactor at 300 °C for 6 h with 7 bar of initial gas and a catalyst-to-HO ratio of 15% (by weight).  In this study, the products from the parent HZSM-5 had the lowest yield of hydrocarbons (21.833%) and the lowest conversion (94.589%) of the algal HO. This could be because of the number of other compounds with oxygen. For example, the fact that the catalytic deoxygenation of algal HO makes fewer hydrocarbons than the parent HZSM-5 catalyst might be because it makes more alcohols, esters, aldehydes, ketones, and ethers (refer to Table 5).

Hydrocarbon
In this research, the yield percentages of alkanes are much lower than those of alkenes. This may be because the catalytic deoxygenation of algal HO only produced a small amount of hydrogen, which was not enough to fill the double bonds during these reactions. However, this study was completed under an initial pressure of 7 bar, which was the pressure of the inert gas nitrogen.
In conclusion, as was explained in the Ammonia TPD discussion, adding Lanthanum-Cerium to the parent HZSM-5 zeolite has a great effect on the total acid sites, especially the acidic Bronsted sites. However, this area of strong acid sites (the Bronsted sites) is thought to be the main catalytic center and include the dominant acid sites during catalytic deoxygenation reactions [32], whereas the number of weak acid sites (the Lewis sites) was deemed to be not catalytically important but it is assumed to effectively influence the proton mobility in zeolites as shown in the investigation of Zaki et al. [40]. Table 7 shows the results of different studies on the catalytic deoxygenation process using different types of catalysts to make hydrocarbons from different feeds (fatty acids or FAMEs). The operating conditions of those studies (reactor type, time, temperature, and the initial value of the charged gas pressure) are very close to the operating conditions used in this study. However, our results show that Lanthanum-Cerium-modified zeolite showed deoxygenating activity under a low pressure of an inert gas (Nitrogen). This could mean that the cost of making hydrocarbons without using hydrogen gas would be much lower.
Many researchers have discussed catalytic cracking deoxygenation using different catalysts and reactants under an initial H 2 pressure or N 2 inert gas pressure. Studies on catalytic deoxygenation with the initial pressure of an inert gas are a lot fewer than those on the same process with the initial pressure of hydrogen gas. In the meantime, there is no other research that is similar to this study's catalytic deoxygenation of algal HO using these catalysts. As a result, this study's operating conditions (such as the type of reactor, temperature, time, fatty acids or FAMEs reactants, and the initial pressure of the pumped gas) were compared to similar catalytic studies (refer to Table 7).
Paying the most attention to catalytic deoxygenation under the pressure of H 2 gas, Sousa et al. (see Table 7) talked about the catalytic deoxygenation of palm kernel oil and the hydrolysis of palm kernel oil for HBeta zeolite under 10 bar of H 2 as the initial pressure. The yields of hydrocarbons were 82 ± 3% and 24 ± 9%, respectively. However, they explained that the yields of hydrocarbons for the catalytic deoxygenation of olein oil and hydrolyzed olein oil were 43 ± 3% and 98 ± 4%, respectively, using the same catalyst and the same operating conditions as shown in Table 7. They demonstrated that the type of reactants (the size of the reactant molecule and the length of the carbon chain of the reactants) has a significant impact on the number of hydrocarbons produced using the same catalyst and operating conditions [13].
Meller et al. looked at how the type of solvent and the temperature affected the catalytic deoxygenation of hydrolyzed castor oil to make hydrocarbons using a Pd/C catalyst and 25 bar of H 2 at the start (refer to Table 7). According to Table 7, the type of solvent used and the temperature of the reaction have a significant impact on the number of hydrocarbons produced [14].
Peng et al. looked at the catalytic deoxygenation of stearic acid for 10%Ni/HZSM-5 in the presence of a solvent (dodecane) under an initial pressure of 40 bar of H 2 . At 260 • C for 8 h, the total yield of hydrocarbons was about 56% (refer to Table 7). Peng et al. also conducted a study on the catalytic conversion of microalgae oil for 10%Ni/ZrO 2 at 270 • C with 40 bar of initial H 2 pressure, and no solvent. They searched for the effect of reaction time on the total yield of hydrocarbons under the same operating conditions. The total yield of hydrocarbons after 6 h was 72% and after 4 h it was 61% [16] (as presented in Table 7).    [17] (refer to Table 7).
Considering catalytic deoxygenation under pressure from an inert gas, Snare et al. [18] discussed the catalytic deoxygenation of methyl oleate in an initial reaction atmosphere of H 2 and Ar. They showed that the type of initial gas pressure has a great effect on the conversion percentage and the number of hydrocarbons made under the same catalyst, temperature, feed-to-catalyst ratio, reaction time, the highest conversion percentage, and the selectivity of the hydrocarbons [18].
Morgan et al. studied the catalytic deoxygenation of soybean oil with 20% Ni/Al 2 O 3 under 7 bar of inert gas (N 2 ) at 350 • C. The highest hydrocarbon yield percentage was 79.5% and the conversion was 74% [26] (refer to Table 7).
Hollak et al. showed that the total selectivity of hydrocarbons was 35% in the catalytic deoxygenation of stearic acid for Pd/Al 2 O 3 under 7 bar of nitrogen inert gas pressure at 350 • C for 6 h with a 43% conversion percentage [27] (refer to Table 7).
In general, the Lanthanum-Cerium-modified zeolites produced more non-oxygenated compounds than the algal HO for the parent HZSM-5 when it came to catalytic deoxygenation. This finding agrees with what Li, J., et al. found when they used HZSM-5 and 5%Fe/HZSM-5 to catalyze the liquefaction of cellulose in the presence of the solvent (nheptane) at 350 • C in a batch reactor. They found that the parent HZSM-5 produced higher yields of oxygenated compounds and lower yields of non-oxygenated compounds [28].
In conclusion, the above studies show that the percentage of hydrocarbons produced by catalytic deoxygenation depends on several factors, such as temperature, use of solvent, type of solvent, type of reactant, feed-to-catalyst ratio, reaction time, and the type of initial pressure that is pumped into the reactor before the reaction happens.
Paying the most attention to the alcohol compounds made in this study, Figure 15 shows that the alcohol yields from the catalytic deoxygenation of algal HO for all of the Lanthanum-Cerium-modified zeolite catalysts were less than the alcohol yields from the parent HZSM-5 catalyst, except for (2.5%La-7.5%Ce)/HZSM-5. In more detail, the total yield of alcohol from the catalytic deoxygenation of algal HO for the parent HZSM-5, (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5 was 49.549%, 50.5%, 42.748%, and 35.259%, respectively. The most alcohols were made when (2.5%La-7.5%Ce)/HZSM-5 was used. The highest yield value was 50.5%. In this study, the catalytic deoxygenation of algal HO in the batch reactor at 300 • C for 6 h with 7 bar of initial inert N 2 gas and a catalyst-to-algal HO ratio of 15% (wt.%) led to the lowest conversion rate of 94.589% for the parent HZSM-5 (see Table 6 and Figure 15).
In conclusion, the parent HZSM-5 catalyst had the lowest hydrocarbon yield percentage. Additionally, (7.5%La-2.5%Ce)/HZSM-5 had the lowest percentage of alcohol yield and the highest percentage of hydrocarbon yield. This could be because HZSM-5 (0.214 mmol/g) has more strong acid sites than (7.5%La-2.5%Ce)/HZSM-5 (0.154 mmol/g). Moreover, strong acid sites play a key role in the catalytic deoxygenation of oxygenated compounds [32]. Therefore, a small number of strong acid sites could make it easier for oxygenates to be turned into hydrocarbons.
Placing the most effort into studies about the catalytic deoxygenation process, which is about making oxygenated compounds, such as alcohol, most studies on catalytic deoxygenation have discussed the yields of non-oxygenated compounds (hydrocarbons). There are not as many studies on the production of oxygenated compounds during catalytic deoxygenation as there are on the production of non-oxygenated compounds (hydrocarbons). In the meantime, as mentioned previously, there is no other study in the literature that is similar to the catalytic deoxygenation of algal HO conducted in this study using these catalysts. Therefore, studies of close catalytic cracking were compared in terms of the reactants and the percentages of alcohol that were made during these reactions. Duongobia et al. wrote about how the reaction time affects the yield percentage of alcohol when palmitic acid is treated with a Limonite catalyst. At 5 h and 3 h, the yield percentages of alcohol were 51.84% and 38.35%, respectively [17].
J. Li et al. looked at the catalyzed liquefaction of cellulose with the help of glycerol for HZSM-5 and 5% Fe/HZSM-5 under the same operating conditions. They found that the modification of the parent HZSM-5 with Fe metal gave a lower yield percentage of alcohol (20%) than the parent HZSM-5 (26%) [28].
Rozmyslowics et al. looked at the catalytic deoxygenation of Lauric acid for 5% Pd/C under the same operating conditions (except for the initial pressure gas). They found that the type of initial pressure had a great effect on the amount of alcohol that was made. The total amount of alcohol made under 20 bar of H 2 was 9% but none was made under 20 bar of Ar [19,20]. Furthermore, Rozmyslowics et al. showed the effect of the reaction time in the catalytic deoxygenation of stearic acid for 4% Ru/TiO 2 under the same operating conditions (except for the reaction time). The yield percentage of alcohol was 20% at 1 h but none was made at 6 h [29]. On the other hand, they showed that the type of catalyst has a great effect on the amount of alcohol that is made during the catalytic deoxygenation of stearic acid. Two experiments were performed with the same operating conditions (except for the type of catalyst. The total amount of alcohol made from 4% Re/TiO 2 was 81% but there was no alcohol made from 4% Ru/TiO 2 [29].
In the catalytic cracking of soybean oil for a composite catalyst (35%

Circular, Green and A
The Circular City is particular, with Circular inition of the CE is prob ing [3] and interdisciplin city is based on closing, the potential for conser and virtualization has b ergy being covered as fa resources". Circular citie  [115] found that the highest yield of alcohol was 12.3%.
Balasundram et al. claimed that the yield percentage of alcohol in the catalytic pyrolysis of sugarcane bagasse for the parent HZSM-5 and 1% Ce/HZSM-5 was about 14% and 5%, respectively [39].
In conclusion, the above studies show that the percentage of alcohols produced by different reactions, such as catalytic deoxygenation, depends on several factors, such as temperature, type of catalyst, reaction time, and the type of initial pressure that is pumped into the reactor before the reaction happens.

Liquid Product Characterization
The liquid products were obtained from the catalytic deoxygenation of the algal HO for the parent HZSM-5 and the Lanthanum-Cerium-modified zeolite catalysts at the same operating conditions: a 300 • C reaction temperature for 6 h with a 15% catalyst-to-HO weight ratio at 1000 rpm and with 7 bar N 2 in the batch reactor. Table 8 shows the elemental compositions of liquid products, which were calculated using Equation (3).
Compared to the algal HO, the carbon and hydrogen weight percentages of the products of the catalytic deoxygenation for (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5 increased, while the oxygen weight percentages decreased. The results of the parent HZSM-5 show that the weight percentage of carbon increased, while the weight percentages of hydrogen and oxygen decreased. The Jafarian study [116] found that the higher heating value (HHV) increased when the amount of carbon and hydrogen increased and the amount of oxygen decreased. As shown in Table 8, compared to the HHV (MJ/kg) of HO (32.377), the HHV of the catalytic deoxygenation liquid products for the parent HZSM-5, (2.5%La-7.5%Ce)/HZSM-5, (5%La-5%Ce)/HZSM-5, and (7.5%La-2.5%Ce)/HZSM-5 were higher by 33.230, 33.738, 34.036 MJ/kg, respectively. As calculated from the O/C molar ratios using Equation (5), the degree of deoxygenation percentage (DOD%) of the liquid products from the modified Lanthanum-Cerium zeolite (7.5%La-2.5%Ce)/HZSM-5 was higher than the DODs of the liquid products from other synthetic catalysts in this work. If oxygen is taken out of the fuel, the viscosity and acidity of the fuel may be improved [117]. However, compared to fossil crude oil, the HHVs of all of the products of the catalysts were low [118]. The atomic ratios of H/C and O/C are shown in Table 8, which is a van Krevelen diagram ( Figure 16). Compared to algal HO, the ratio of H/C in the liquid products of all Lanthanum-Cerium-modified zeolite catalysts increased, while the ratio of O/C decreased. The H/C and O/C atomic ratios of the parent HZSM-5 zeolite were lower than those of the raw algal HO. The (7.5%La-2.5%Ce)/HZSM-5 had the highest H/C ratio of 1.994 and the lowest O/C ratio of 0.031 among the Lanthanum-Cerium-modified zeolites. Even though the H/C ratios of the liquid products were high, the O/C ratios stayed high when compared to the O/C ratio of fossil crude oil (~0). It should be noted that the highest value of DOD% was 62.109% for (7.5%La-2.5%Ce)/HZSM-5.
Comparing the results of this study with those of a previous one [17], which looked at the hydrotreatment of palmitic acid for a Ni/LY catalyst under 30 bar H 2 at 300 • C in a batch reactor, the highest DOD% was 65.15%, which is low compared to the amount of hydrogen used. The highest H/C and HHV were also 2.03 and 32.4 MJ/Kg, respectively, while the highest H/C and HHV in this study were 1.994 and 34.362 MJ/Kg, respectively.

Conclusions
Using a batch reactor, the performance of composite Lanthanum-Cerium -impregnated HZSM-5 for the catalytic conversion of algal HO to non-oxygenated and oxygenated compounds was evaluated. The physical alterations observable in the textural qualities were caused by the loading percentages of lanthanum and cerium. From the physical qualities, no direct link can be inferred toward increasing the hydrocarbon yield. The addition of Lanthanum-Cerium into HZSM-5 zeolite at varying percentages improved the acid sites required for algal HO conversion. The conversion percentages of algal HO using all Lanthanum-Cerium-modified HZSM-5 (in the range of 98.035% to 100%) were greater than the conversion percentage utilizing the original HZSM-5 percentage (94.589%). The incorporation of Lanthanum-Cerium into HZSM-5 has the added impact of producing a greater hydrocarbon yield (24.5-42.963%). In general, the rising performance of catalysts in converting algal HO to hydrocarbons is as follows: (7.5%La-2.5%Ce)/HZSM-5 > (5%La-5%Ce)/HZSM-5 > (2.5%La-7.5%Ce)/HZSM-5 > HZSM-5. The alcohol products from the Lanthanum-Cerium-modified zeolite ranged from 35.259% to 50.5%, while the alcohol products from the HZSM-5 parent were 49.549%. The DOD percentages for liquid products from Lanthanum-Cerium-modified HZSM-5 catalysts ranged from 46.755 to 62.109%, while the DOD% for liquid products from the pure HZSM-5 catalyst was 44.235%. The HHV of the liquid products from all of the Lanthanum-Cerium-modified HZSM-5 catalysts (ranging from 33.738 to 34.362 MJ/Kg) was greater than the HHV of the liquid product from the parent HZSM-5 (33.230 MJ/Kg). The catalyst (7.5%La-2.5%Ce)/HZSM-5 provided the greatest yield of hydrocarbons, highest HHV, and highest DOD%, which were 42.963%, 34.362 MJ/Kg, and 62.109%, respectively, among all the synthesized catalysts in this investigation.