Catalytic pyrolysis of date palm seeds on HZSM-5 and dolomite in a pyroprobe reactor in line with GC/MS

Vol.:(0123456789) 1 3 Biomass Conversion and Biorefinery (2024) 14:2799–2818 https://doi.org/10.1007/s13399-022-02493-2 ORIGINAL ARTICLE Catalytic pyrolysis ofdate palm seeds onHZSM‑5 anddolomite inapyroprobe reactor inline withGC/MS MiriamArabiourrutia1· GmarBensidhom2· MaiderBolaños1· AïdaBenHassenTrabelsi2· MartinOlazar1 Received: 6 December 2021 / Revised: 9 February 2022 / Accepted: 19 February 2022 / Published online: 11 March 2022 © The Author(s) 2022 Abstract Catalytic pyrolysis of date palm seeds (DPS) has been carried out in a pyroprobe connected online with a GC/MS. The effect of a HZSM-5 zeolite on the product distribution has been studied at 450 and 500 °C by using different catalyst/biomass mass ratios (1, 2, 5) and that of a dolomite catalyst at 450 °C using a catalyst/biomass mass ratio of one. Product distributions have been monitored and their trends explained based on the properties of the catalysts used. The HZSM-5 promotes the formation of incondensable gases and aromatic hydrocarbons due to its high acidity and shape selectivity. The concentrations of incondensable gases and hydrocarbons increase markedly with the catalyst/biomass mass ratio, with their peak area percentages ranging from 23.6 to 54.1% and from 7.1 to 24.5%, respectively. At the same time, a significative reduction in the amount of acids, ketones, phenols, furans, and anhydrosugars has been determined. The dolomite catalyst enhances ketonization reactions, which leads to a significant increase in the content of ketones, accounting for a value of around 27%. Keywords DPS biomass· Py-GC/MS· Catalytic pyrolysis· Zeolite HZSM-5· Dolomite 1 Introduction Biomass is a renewable energy source, which may be used to replace fossil fuels, and so meet the increasing energy demand. Pyrolysis of biomass is an interesting option to manage forestry and agricultural wastes and, at the same time, obtain products with a high potential application for energy production or source of value-added chemicals contained in the gaseous and/or liquid bio-oil fraction [1, 2]. The bio-oil or pyrolytic oil generated from the fast pyrolysis of biomass and wastes may have several potential applications, such as those related to the production of high value-added chemicals and substitutes of petroleum-based sources for a wide range of fuels [3]. Crude bio-oil derived from the conventional fast pyrolysis is a low-grade liquid fuel due to the high oxygen content, poor stability, high acidity, and low calorific value. Furthermore, recovery of valuable chemicals is a very difficult task due to their low contents in the bio-oil. Accordingly, the liquid product must be upgraded prior to use in relevant applications by means of suitable processes, such as catalytic cracking, which in turn must involve reasonable costs. Catalytic fast pyrolysis is considered a promising approach to convert oxygenate compounds into a variety of hydrocarbons and therefore improve the bio-oil quality. The use of a catalyst generally enhances the targeted reactions; reduces the reaction time and temperature; improves the liquid oil quality by removing oxygen via certain reactions, such as dehydration (removing oxygen as H2O), decarboxylation (removing oxygen as CO2), and decarbonylation (removing oxygen as CO) [4, 5]; and increases the overall process efficiency [6]. The surface area, acidity, and pore size and volume are the key features of any catalyst affecting the pyrolysis process [7]. There are many studies in the literature dealing with the catalytic pyrolysis of biomass and wastes as a way to obtain upgraded pyrolytic products [8, 9]. Thus, acid catalysts such as HZSM-5 zeolite-based ones have been reported to perform well in deoxygenation to obtain hydrocarbons. * Miriam Arabiourrutia miriam.arabiourr[email protected] 1 Department ofChemical Engineering, University oftheBasque Country UPV/EHU, P.O. Box644, E48080Bilbao, Spain 2 Centre de Recherches et des Technologies de l’Energie Technopole De Borj-C´edria, BP: 95, Hamam Lif, BenArous, Tunisia 2800 Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 This behavior has been attributed to their acidity and shape selectivity [5, 10], with the latter being a consequence of its small/medium-pore size coupled with its two-dimensional channel-like pore system [11]. In the pyrolysis of biomass, deoxygenation of holocellulose and lignin fragments occurs via dehydration and decarbonylation/decarboxylation reactions [12, 13]. Subsequently, protolytic cracking or β-scission, alkylation, isomerization, cyclization, oligomerization, and aromatization reactions take place. Among the zeolites, the ZSM-5 has been widely used as a catalyst for biomass pyrolysis, as it dramatically changes the composition of the volatiles generated. One of the main purposes of using zeolitic catalysts lies in its capacity for deoxygenating phenolic and oxygenated compounds [14]. Other catalysts, such as alkali salts [15] and metal oxides [16], have been used, but a much lower deoxygenating activity has been reported. Low-cost catalysts, either natural (olivine, alumina) or synthetic (spent FCC catalyst), have also been used in line with the pyrolysis reactor, and they led to a significant decrease in acid and phenolic compounds in the volatile stream, making it suitable for further catalytic valorization for the production of H2, fuels, and chemicals [17]. Other studies in which natural materials have been used as catalysts are those by Aljbour [18] and Aljeradat etal. [19]. Dolomite is a natural, inexpensive, and non-metallic catalyst, which has been widely used for tar conversion in biomass gasification [20, 21]. However, this natural catalyst has also been used successfully in the catalytic pyrolysis of biomass to improve the bio-oil quality by cracking heavy organic molecules to lighter ones or removing oxygen from the oxygenates [22]. Furthermore, this catalyst has also been used to upgrade the liquid bio-oil prior to feeding into the reforming reactor. Thus, Valle etal. [23] concluded that dolomite was effective for the deoxygenation of the bio-oil, as it reduces the O content, and so the O/C ratio, in the upgraded bio-oil. Ly etal. [22] used dolomite as a catalyst in a fluidized bed and proved that it leads to the formation of aromatic compounds (C5-C11), such as the derivatives of furfural, ketones, and phenolic compounds. Another positive benefit of dolomite lies in its capacity for CO2 capture, which allows obtaining a gaseous product with a low yield of CO2 [24]. Dolomite removes oxygen from the pyrolysis stream mostly through dehydration, instead of decarboxylation or decarbonylation [22]. In this work, date palm seeds have been used as the raw material. The date palm tree is a typical cultivated tree in the arid and semi-arid regions of the world. There are more than 100–120 million date palm trees worldwide, with most of them (70–90%) being located in the Middle East and North Africa (MENA) countries [25]. It is especially abundant in several regions in the South of Tunisia [26]. Date seeds are low-cost agricultural by-products, which are traditionally used for animal feed. Their derived powder is used as a coffee substitute [27, 28]. They are also used as a source of oil in cosmetics due to their antioxidant properties, raw material for activated carbon, adsorbent for dye-containing waters, and CO2 capture material [29–31]. The annual world production of dates is of around 9 million tons [29]. Depending on the variety, date seeds account for 6.10–11.4% of the whole fruit weight [32]. This study analyzes the performance of a HZSM-5 zeolite catalyst by varying temperatures (450 and 500 °C) at the catalyst/biomass mass ratio of C/B=1 and catalyst/biomass mass ratio (C/B=1, 2, and 5) at the temperature of 450 °C. A detailed quantification and identification of the compounds formed have been carried out, with emphasis placing on the different trends observed in the product distribution and relating these trends to the properties of the catalysts used. Furthermore, a low-cost natural catalyst with very different properties, as is dolomite, has been used to analyze its effect on the product distribution and compare its performance with that of the HZSM-5. The aim of this study is to show that upgrading of the condensable fraction (bio-oil) allows improving the quality of the liquid and therefore increases its potential for use as fuel. In fact, the presence of aliphatic and aromatic hydrocarbons in the liquid is crucial for a highquality fuel. Furthermore, it is well-known that catalytic pyrolysis enhances the production of hydrocarbons. To our knowledge, there are no studies reported in the literature about the catalytic pyrolysis of date palm seeds. Therefore, this study contributes to promoting pyrolysis processes as an option to valorize these wastes. 2 Experimental 2.1 Preparation andcharacterization ofdate palm seed samples Date palm seeds (DPS) were supplied by the National Institute of Arid Zone (IRA-Kebili, Tunisia). The sort of date used was Deglet Noor seeds (Phoenix Dactylifera L.). The DPS were harvested from the date fruit by hand and then cleaned with distilled water to eliminate all dust. They were then sundried for 3 days. Moreover, the sundried biomass was crushed into particle sizes ranging between 0.125 and 0.25 mm and stored in airtight plastic bags to prevent moisture absorption. This particle size range is the suitable one to carry out fast pyrolysis in a Py-GCMS, where very small quantities of sample are used, of around 1 mg. A thermogravimetric analyzer (TGA Q5000 IR) was used in this study to determine the proximate analysis of the DPS samples. The procedure was described elsewhere [33]. DPS ultimate analysis was performed using an elemental analyzer (LECO CHNS TRuSpec). The O content was determined by difference, according to the following expression: 2801Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 The higher heating value (HHV) of the raw material DPS was measured by means of a CAL-2 K Oxygen Bomb Calorimeter according to the ASTM D5865-13 standard method. The lignocellulosic components (cellulose, hemicellulose, and lignin) of the DPS sample were determined according to the method described elsewhere [34]. 2.2 Py‑GC/MS equipment The pyrolysis of DPS has been carried out in a Pyroprobe 5150 of CDS. One milligram of the sample was inserted in the pyrolysis tube, with quartz wool being placed above and below the sample. Pyrolysis runs were carried out at 450 and 500 °C for 40 s. This time is sufficiently long to ensure all the volatile matter is pyrolized. The experiments were conducted in triplicate and the mean values and the standard deviations were determined. In the catalytic pyrolysis, the biomass sample was mixed with the catalyst at the catalyst/ biomass (C/B) mass ratios of 1, 2, and 5 for the HZSM-5 zeolite and 1 for the dolomite catalyst. The heating rate was 20 °C/ms. The volatiles generated were transferred through a hot line into a GC/MS (QP2010 Shimadzu), where they were analyzed. The chromatographic separation was performed using a BPX-5 capillary column (30 m × 0.22 mm ID, 0.25 μm film thickness). The oven temperature was programmed from 45 °C (maintained for 3 min) to 295 °C (5 min) with a heating rate of 4 °C/min. The MS detector was a quadrupole type. The identification of the compounds was carried out using the NIST library. 2.3 Catalysts The catalysts used are a HZSM-5 zeolite and a dolomite. The HZSM-5 zeolite has been chosen because of its good deoxygenation capacity given by its specific properties (acidity and shape selectivity). The dolomite catalyst has been chosen because of, on the one hand, low cost and, on the other hand, different properties to those of the zeolite, e.g., poor porous structure and basic nature. The ZSM-5 zeolite has been supplied by Zeolyst International (USA) and the dolomite by Minerals Sibelco (Spain). The ZSM-5 zeolite was supplied in ammoniac form and calcined at 575 °C for 2 h in order to obtain the acid form and so a suitable surface acidity. The dolomite has been calcined at 900 °C for 4 h in order to attain full decarboxylation of calcium and magnesium carbonates and so obtain the active phases of CaO and MgO. XRD analysis has been carried out to determine the crystalline phases in the dolomite. The crystalline structure of the dolomite was analyzed using X-ray powder diffraction (XRD) patterns. A Bruker O (wt.%)=100– [ C(wt.%)+H(wt.%)+N(wt.% ) D8 Advance diffractometer with Cu Kα1 radiation was used to conduct the analysis. XRF analysis has been carried out to measure the chemical composition of the catalyst. This analysis was carried out using a sequential wavelength dispersion X-ray fluorescence (WDXRF) spectrometer (Axios 2005, PANalytical) under a vacuum atmosphere. The textural properties of both catalysts have been determined from the N2 adsorption-desorption curves obtained in a Micromeritics ASAP-2100 equipment. The total acidity of the HZSM-5 zeolite has been determined in a calorimeter (Setaram TG-DSC 111) coupled to a mass spectrometer (Thermostar of Balzers Instruments). 3 Results 3.1 Biomass characterization Table1 shows the proximate and ultimate analyses of the studied DPS sample, as well as the percentages of their main constituents (cellulose, hemicellulose, and lignin). Date seeds are characterized by their high content of volatile matter and low one of ash components. High volatility makes these biomasses attractive for the pyrolysis process in order to obtain bio-oil and syngas [35]. 3.2 Catalyst characterization Table2 sets out the physicochemical properties of the HZSM-5 zeolite and dolomite catalysts. As observed, the zeolite has much higher surface area and pore volume than the dolomite, whereas the average pore size of the dolomite is much higher than that of the zeolite. The latter is evidence of the microporous structure of the zeolite. Concerning acidity, the zeolite is an acid catalyst, whereas Table 1 Ultimate and proximate analyses and lignocellulosic components of the studied DPS *Calculated by difference Proximate analysis  Moisture content (wt.%) 1.73  Volatile matter content (wt.%) 78.61  Ash content (wt.%) 4.97  Fixed carbon* (wt.%) 14.69 Ultimate analysis  Carbon 48.05  Hydrogen 7.67  Nitrogen 0.70  Oxygen* 43.57  H/C atomic ratio 2.23  O/C atomic ratio 0.13  HHV (MJ/kg) 20.46 2802 Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 the dolomite is a basic one. The HZSM-5 has a silica/ alumina ratio of 30, which confers high total acidity upon this catalyst. The main mineral constituents of the calcined dolomite used have been determined by X-ray fluorescence (XRF) analysis. The chemical composition is as follows: MgO (wt. %) 43.61, SiO2 (wt. %) 0.12, Fe2O3 (wt. %) 0.02, CaO (wt. %) 56.07, Al2O3 (wt. %) 0.15, Na2O (wt. %) 0.01, and TiO2 (wt. %) 0.02. Fig.1 shows the XRD diagram of the calcined dolomite. As observed, all the peaks correspond to MgO and CaO phases. Both analyses show that the main components of the dolomite catalyst are CaO and MgO, which are oxides containing basic sites. Besides, its specific surface area (BET area) is very low and therefore has a small number of strong acid sites available. In addition, it has a slightly developed surface structure leading to low activity. Nevertheless, the HZSM-5 zeolite has a high specific surface area and strong acidity, leading to a great number of surface acid sites on its surface. Accordingly, the better properties of the HZSM-5 zeolite are responsible for its higher cracking capacity, as well as higher deoxygenation capacity. 3.3 Py‑GC/MS results In this section, the results obtained in the catalytic pyrolysis on the HZSM-5 zeolite and dolomite catalysts are shown and they are compared with those obtained in a previous study carried out without any catalyst [33]. 3.3.1 Thermal pyrolysis In order to determine the effect of the catalysts on the volatile product distribution, the results obtained without catalyst are firstly shown in this subsection. The volatiles generated in the pyrolysis of biomass cover a wide range of compounds of different nature, which may be classified as acids, ketones, aldehydes, phenols, alcohols, furans, ethers, and anhydrosugars, as well as hydrocarbons, N compounds, and S compounds in a much lower amount. Those preferred for biofuel are aromatic hydrocarbons, aliphatic hydrocarbons, and alcohols, whereas phenols and furans are regarded as high added-value chemicals. Acids are responsible for the corrosiveness of the bio-oil, and they are therefore undesired compounds. The same stands for ketones and aldehydes, which are related to the instability of the bio-oil during transport and storage. Ethers, esters, and oxygenates in general are also undesired compounds, as they reduce the heating value of the bio-oil. Polyaromatic hydrocarbons and nitrogen and sulfur compounds are detrimental for the environment [12]. Figure2 shows the total ion chromatogram corresponding to the fast pyrolysis of DPS performed at 450 °C Table3 shows the retention times, compound names, and peak area percentages of the main compounds obtained in the thermal pyrolysis at 450 °C. As observed, ketones (acetone and 1-hydroxy-2-propanone), acids (acetic, undecanoic, dodecanoic, and octadecanoic), and anhydrosugars (levoglucosan) are the prevailing compound families. In addition, the content of 5-(hydroxymethyl)-2-furancarboxaldehyde is also considerable. Table4 shows the peak area percentages of the different compound families obtained by the chromatographic analysis of the outlet stream of the pyrolysis of DPS samples at 450 and 500 °C. As observed, anhydrosugars, acids, ketones, and furans are the more abundant compound families in the condensable fraction obtained. The content of acids and furans increases moderately with temperature, whereas that of anhydrosugars decreases. The sugar content decreases (from 23.1% at 450 °C to 19.2% at 500 °C). Levoglucosan is the most abundant compound in the sugar family. In the acid product-fraction, acetic acid, long-chain acids (fatty acids), and alkyl ester acids are the prevailing ones. The main individual compounds identified are Table 2 Physicochemical properties of the HZSM-5 zeolite and dolomite catalysts Catalyst BET surface area (m2/g) Micropore volume (cm3/g) dp (Å) Acidity (mmol NH3/g cat.) HZSM-5 zeolite 377 0.098 5.2–5.5 0.765 Dolomite 23 0.0026 173 ----- Fig. 1 The XRD diagram of the calcined dolomite 2803Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 acetic acid, decanoic acid, undecanoic acid, dodecanoic acid, and octadecanoic acid, with the concentration of each of them being of around 2% at 450 °C. Among the ketones, acetone prevails, with its concentration being in the 2.2–2.4% range. The remaining compounds in this ketones family (others) are mainly linear and cyclic C3-C8 ketones. Among the furan family, 5-hydroxymethyl-2-furancarboxaldehyde was the main compound identified with high concentration, followed by furfural and furan derivatives. Its total concentration increased moderately from 9.6% at 450 °C to around 14% at 500 °C. 3.3.2 Catalytic pyrolysis ontheHZSM‑5 zeolite As observed in the previous section, the oxygenated compounds are the predominant ones in the volatile stream obtained. This high oxygenated compound content confers undesirable properties, such as high acidity, instability, and low heating value, upon the bio-oil for liquid fuel applications, as well as great difficulty for valuable chemical extraction [36]. Therefore, upgrading of crude bio-oil is necessary to improve fuel properties or increase the concentration of valuable chemicals. The addition of catalysts in the pyrolysis process is a good option to overcome this problem. Thus, Fig. 2 Chromatogram obtained in the pyrolysis of the DPS sample, T=450 °C 1 2 3 4 56 78910 11 12 13 14 15 16 17 ytisnetnI Retentiontime (min) ytisnetnI Table 3 Retention times, compound names, and peak area percentages of the main compounds obtained in the thermal pyrolysis at 450 °C Peak number Retention time (min) Compound Peak area (%) 1 3.36 Acetone 2.51 2 4.31 Acetic acid 2.13 3 5.21 1-Hydroxy-2-propanone 3.27 4 8.64 Acetic anhydride 0.84 5 10.30 Furfural 1.51 6 11.05 2-Furanmethanol 1.30 7 14.14 Cyclohexanone 1.35 8 18.30 3-Methyl-1,2-cyclopentanedione 0.98 9 21.49 Cyclopropyl carbinol 0.86 10 25.41 1,4:3,2-Dianhydro-d-glucopyranose 2.07 11 26.63 5-(Hydroxymethyl)-2-furancarboxaldehyde 4.18 12 27.22 3,4-Anhydro-d-galactosan 1.28 13 35.87 Levoglucosan 20.89 14 37.20 Undecanoic acid 2.54 15 42.77 Dodecanoic acid 2.45 16 47.91 Octadecanoic acid 2.13 17 54.28 9-Octadecenal 0.70 2804 Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 catalysts with suitable properties favor deoxygenation reactions, and they therefore allow (i) obtaining bio-oils with low oxygen content for liquid fuel applications [37]; (ii) decreasing the content of the oxygenated compounds, and so reducing the acid content in the bio-oil; (iii) removing the unstable components, such as aldehydes and ketones; and (iv) increasing the content of phenols and hydrocarbons, especially those of monocyclic aromatic hydrocarbons (promising products for both liquid fuels and chemical raw materials). The last one not only improves the energy density of the bio-oil, but also makes it easier to blend it with crude oil [38]. Thus, Huynh etal. [39] used HZSM5, Zn/HZSM-5, and Fe/HZSM-5 catalysts for upgrading the pyrolysis oil. They observed that the quality of the oil was improved, as fuels with higher heating value and lower acidity and viscosity were obtained. They determined that the total combustion characteristic index of pyrolysis oils increased and that they were more flammable than fuel oil. These results prove that the upgraded oil might be used as fuel oil in industrial applications. Concerning high-quality fuels, a high content of aliphatic hydrocarbons is essential, as well as the presence of aromatic hydrocarbons to improve the octane number of the fuel [40]. Besides, aliphatic and aromatic hydrocarbons increase the higher heating value of the bio-oil [41]. Product distribution at 450 °C Figure3 shows the total ion chromatogram corresponding to the catalytic pyrolysis of DPS on the HZSM-5 zeolite (C/B=1, 2, 5) performed at 450 °C. Table5 shows the retention times, compound names, and peak area percentages of main compounds obtained in the catalytic pyrolysis on the HZSM-5 zeolite at 450 °C. When a C/B=1 is used, the formation of aromatic compounds is remarkable, i.e., toluene, p-xylene, 1,2,3-trimethyl-benzene, and 2,3-dimethyl-naphthalene. The most abundant compounds correspond to ketones, acids, and anhydrosugars. For C/B=2, the increase in the relative content of aromatic compounds is worth mentioning, which is not the case when a C/B ratio of 5 is used. Furthermore, the relative content of acetaldehyde increases and those of acids and anhydrosugars decrease when the C/B ratio is raised. Table6 shows the peak area percentages of the different compound families obtained by the chromatographic analysis of the outlet stream in the catalytic pyrolysis of DPS samples at 450 °C on the HZSM-5 zeolite. As observed in Table6, the most abundant compound family is the one of incondensable gases. Its content increases significantly (from 23.6 to 54.1%) as catalyst/ biomass (C/B) ratio is increased from 1 to 5. Only certain compounds have been identified in this lump, with propene being the most significant one, especially when the highest Table 4 Mean peak area percentages (95% confidence interval) of the different compound families obtained in the thermal pyrolysis of DPS at 450 and 500 °C The bold entries significance is to remake the different families categories 450 °C 500 °C Incondensable gases 16.4±0.3 12.2±0.4 Acids 16.9±2.6 20.2±2.0  Acetic anhydride 0.7±0.2 0.6±0.2  Acetic acid 2.2±0.1 2.0±0.2  Formic acid 0.3±0.1 0.2±0.01  Fatty acids 11.5±2.5 12.1±4.0  Esters (alkyl ester acids) 2.3±0.3 5.3±2.4 Ketones 15.7±0.5 16.4±2.3  Acetone 2.4±0.1 2.2±1.0  1-Hydroxy-propanone 3.3±0.1 1.4±1.6  2,3-Butanedione 1.2±0.1 1.6±0.3  Cyclohexanone 1.3±0.1 0.7±1.0  Pyran derivatives 0.45±0.1 0.4±0.1  Others 7.0±0.3 10.1±0.1 Aldehydes 2.7±0.1 2.7±0.1 Phenols 2.8±0.1 3.8±1.4  1,2-Benzenediol - 1.0±0.3  3-Methyl-1,2-benzenediol 0.8±0.4 0.6±0.3  Phenol 0.4±0.1 0.6±0.02  Phenol derivatives 1.4±0.2 1.4±0.7  Others 0.1±0.02 0.2±0.04 Ethers 0.7±0.2 0.5±0.01 Alcohols 1.9±0.03 2.0±1.3  Lineal 1.7±0.05 1.3±0.7  Cyclic 0.2±0.02 0.8±0.5 Furans 9.6±0.9 14.4±0.5  Furan derivatives 3.5±0.2 3.6±0.7  Furan derivatives (ketones) 0.7±0.1 0.7±0.04  Furan derivatives (aldehydes) 3.9±0.9 8.0±1.4  Furfural 1.5±0.04 2.0±0.3 Anhydrosugars 23.1±4.7 19.2±1.0  Levoglucosan 18.3±3.7 13.1±1.0  d-Allose 0.9±1.2 1.6±0.7  2,3-Anhydro-d-mannosan 0.4±0.1 0.5±0.1  3,4-Anhydro-d-galactosan 1.3±0.1 2.3±0.02  Dianhydro glucopyranose 2.2±0.2 1.8±0.6 HC 0.3±0.1 0.3±0.1  Aliphatics 0.01±0.01 0.1±0.1  Aromatics 0.3±0.1 0.1±0.2 N compounds 0.3±0.02 0.3±0.1  Pyrrole 0.2±0.03 0.3±0.1 S compounds 0.6±0.1 0.4±0.01  Methanethiol 0.6±0.1 0.2±0.3 Pyrans 0.004±0.01 0.03±0.04 Non-identified compounds 9.1±3.7 7.3±5.5 2805Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 Fig. 3 Chromatogram obtained in the catalytic pyrolysis of DPS on the HZSM-5 zeolite at (a) C/B=1, (b) C/B=2, and (c) C/ B=5, at T=450 °C (a) (b) 1 2 3 4 7 5 6 9 810 11 13 14 12 17 15 16 18 19 20 21 22 Iytisnetn Retention time (min) d 3 5 8 10 12 1314 c 15 fg 22 23 20 21 19 1 2 a 24 h ytisnetnI Retention time (min) (c) d 13 4 25 3 a 12 20 6 19 15 14 11 10 8 c h 23 21 24 b 18 g e 17 ytisnetnI Retentiontime (min) 2806 Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 C/B ratio of 5 is used. This is a consequence of cracking, decarbonylation, and decarboxylation reactions promoted by the HZSM-5 zeolite due to its acidity (Si/Al=30). The second most abundant compound family is the one of hydrocarbons. This lump accounts for aromatic and non-aromatic compounds. The content of non-aromatic compounds decreases slightly from 1.2 to 0.7% when the B/C ratio is increased, whereas that of aromatic compounds (prevailing fraction in this lump) increases markedly from 5.9% when the C/B ratio is 1 to 23.8% when the C/B is 5. Toluene, xylenes, naphthalene derivatives, and benzene derivatives are the most abundant compounds identified. Other compounds identified are indane, indene, fluorene, anthracene and their derivatives, and biphenyl. Figure4 shows the peak area evolution of the whole aromatic family, and of benzene, toluene, xylenes, and polyaromatic hydrocarbons (PAH), when different catalyst/biomass (C/B) mass ratios are used. As observed, the area increases when the C/B ratio is increased, and especially when C/B=5 is used. This is the consequence of the reactions favoring the formation of aromatic compounds, which are enhanced when a higher amount of zeolite is used. Regarding the PAH fraction, the compounds identified are naphthalene, fluorene, anthracene, and their derivatives, with naphthalene and its derivatives being the most abundant ones. This high concentration of hydrocarbon compounds is a consequence of the deoxygenation caused by the HZSM-5 Table 5 Retention times, compound names, and peak area percentages of the main compounds obtained in the catalytic pyrolysis on the HZSM-5 zeolite (C/B=1, 2, 5) at 450 °C Peak area (%) Peak number Retention time (min) Compound C/B=1 C/B=2 C/B=5 1 3.39 Acetaldehyde 0.76 1.17 3.14 2 4.0 Acetone 1.99 2.64 1.94 3 5.28 2,3-Butanedione 0.84 0.81 0.32 4 5.65 Acetic acid 0.83 0.6 0.04 5 6.74 1-Hydroxy-2-propanone 4.10 1.87 1.04 6 10.15 Acetic acid, propyl ester 0.65 - 0.12 7 10.72 Propanoic acid, 2-oxo, methyl ester 0.46 0.18 0.08 8 11.18 Toluene 0.70 3.18 3.73 9 11.25 Carbonocyanidic acid, ethyl ester 0.73 0.52 - 10 13.02 Furfural 1.59 0.84 0.46 11 14.25 1-Acetyloxy-2-propanone 1.73 0.23 0.12 a 15.21 Ethylbenzene 0.19 0.67 0.72 12 15.66 p-Xylene 0.73 1.84 2.72 b 16.6 m-Xylene 0.09 0.24 0.40 13 16.93 2-Methylcyclopentanone 1.09 0.54 0.30 14 18.73 5-Methyl-2-furancarboxaldehyde 0.96 0.61 0.31 c 19.76 1,2,3-Trimethyl-benzene 0.66 1.01 0.91 d 21.1 1,2,4-Trimethyl-benzene 0.10 0.61 0.67 15 21.53 3-Methyl-1,2-cyclopentanedione 1.30 0.60 0.32 16 28.46 1,2-Benzenediol 1.91 0.43 0.25 e 28.72 Naphthalene 0.07 0.46 0.79 f 28.83 1-Methyl-4-(1-methyl-2-propenyl)-benzene - 1.93 - 17 28.92 5-(Hydroxymethyl)-2-furancarboxaldehyde 3.31 - 0.84 18 29.61 2,3-Anhydro-d-mannosan 1.11 0.33 0.12 g 32.93 1-Methyl-naphthalene 0.24 1.49 1.28 19 37.49 Levoglucosan 13.51 8.73 2.55 h 36.85 2,3-Dimethyl-naphthalene 0.61 0.79 0.70 20 38.59 d-Allose 1.86 0.88 0.15 21 41.51 Dodecanoic acid 6.05 7.91 1.53 22 47.28 Tetradecanoic acid 2.88 0.78 0.08 23 48.39 Anthracene - 0.53 0.43 24 51.6 9-Methyl-anthracene 0.29 0.57 0.77 2807Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 zeolite. Many authors have determined that HZSM-5 zeolites change the composition of the bio-oils by both reducing the amount of oxygenate compounds via deoxygenation reactions and increasing the aromatic species, which leads to an organic fraction (bio-oil) that can be upgraded to gasoline and diesel fuels [10, 42, 43]. Carlson etal. [44] determined that the first stage in cellulose degradation involves dehydration reactions to form anhydrosugars, and they subsequently undergo acid-catalyzed dehydration on the active sites of the catalyst, leading to the formation of dehydrated products. These products undergo further oligomerization, decarboxylation, and decarbonylation, or cracking reactions, to form C2-C6 olefins, which then combine to yield aromatics. The deoxygenation leads to the production of CO, CO2, and H2O. Figure5 shows the evolution of the content of C3-C7 olefins in the catalytic pyrolysis carried out at 450 °C when the C/B ratios of 1, 2, and 5 are used. As observed, the content of the lighter C3-C4 olefins (propene, 2-methyl-propene, 2-butene) increases markedly as the C/B ratio is increased, whereas that of C5-C7 ones (2-pentene, 2-methyl-1-butene, 3-hexene, 3-methyl-1,3,5-hexatriene) goes through a slight Table 6 Mean peak area percentages (95% confidence interval) of the different compound families obtained in the catalytic pyrolysis of DPS at 450 °C when the C/B mass ratios of 1, 2, and 5 are used The bold entries significance is to remake the different families categories Biomass/catalyst (B/C) mass ratio 1/1 1/2 1/5 Incondensable gases 23.6±5.5 32.5±2.3 54.1±4.1  Propene 1.7±0.3 5.3±0.5 11.4±1.1  2-Methyl-1-propene 2.0±2.3 2.8±1.2 3.6±0.9  1-Butene - 1.6±0.6 1.3±0.3 Acids 11.7±2.3 11.4±3.3 2.4±0.2  Acetic acid 1.1±0.2 1.0±0.5 0.2±0.2  Fatty acids 7.6±2.3 9.5±2.3 1.8±0.2  Esters (alkyl ester acids) 2.6±0.02 1.0±0.1 0.4±0.2 Ketones 14.8±3.2 8.6±1.1 5.4±0.8  Acetone 2.0±0.01 2.7±0.4 1.7±0.4  1-Hydroxy-propanone 3.6±0.7 1.9±0.3 0.8±0.3  2,3-Butanodione 0.9±0.1 0.7±0.01 0.3±0.04  2-Butanone 0.8±0.1 0.8±0.4 0.4±0.1  Others 7.5±2.6 2.9±0.5 2.3±0.02 Aldehydes 1.5±0.5 1.7±0.2 3.2±0.4 Acetaldehyde 0.6±0.2 1.1±0.1 2.9±0.3 Phenols 3.3±1.2 1.2±0.5 0.7±0.04  1,2-Benzenediol 1.5±0.6 0.5±0.2 0.2±0.07  1,2-Benzenediol derivatives 1.0±0.4 - 0.04±0.005  1,4-Benzenediol (hydroquinone) - 0.2±0.01 0.06±0.08  1,4-Benzenediol derivatives 0.2±0.03 0.1±0.1 0.02±0.03  Phenol 0.1±0.02 - 0.01±0.01  Phenol derivatives 0.5±0.2 0.3±0.1 0.4±0.2 Ethers 0.4±0.0 - 0.3±0.2 Alcohols 2.2±0.2 0.5±0.3 0.5±0.04  Lineals 1.9±0.2 0.5±0.3 0.4±0.07  Cyclics 0.2±0.1 - 0.02±0.02 Furans 7.4±1.4 3.6±0.8 1.9±1.3  Furane 0.4±0.1 0.7±0.1 0.3±0.1  Furane derivatives 1.2±0.1 0.8±0.1 0.4±0.2  Furane derivatives (ketones) 0.7±0.2 0.4±0.05 0.2±0.2  Furane derivatives (aldehydes) 3.7±0.8 0.7±0.2 0.7±0.6  Furfural 1.4±0.3 1.0±0.3 0.3±0.2 Anhydrosugars 18.0±1.9 8.7±7.1 2.5±0.6  Levoglucosane 15.1±2.3 7.8±6.7 2.2±0.5  d-Allose 1.9±0.004 0.5±0.4 0.2±0.03  2,3-Anhydro-d-mannosan 0.9±0.3 0.4±0.1 0.1±0.04  2,3-Anhydro-d-galactosan - - 0.03±0.04  Dianhydro glucopyranose 0.2±0.1 0.1±0.03 0.06±0.002 Hydrocarbons 7.1±1.1 19.9±0.3 24.5±6.1  Aliphatics 1.2±0.5 1.5±0.4 0.7±0.3  Aromatics 5.9±0.6 18.3±0.7 23.8±6.4 N compounds 1.9±0.7 1.3±0.01 0.6±0.5  Acetonitrile 0.3±0.2 0.8±0.002 0.3±0.3 S compounds 0.1±0.2 2.1±0.01 2.0±0.1  Methanethiol 0.1±0.2 2.1±0.01 2.0±0.1 Non-identified compounds 8.1±0.2 8.2±1.0 1.7±1.6 0E+00 2E+07 4E+07 6E+07 total aromacbenzene toluenexylenes PAH Peak area C/B=1C/B=2C/B=5 Fig. 4 Evolution of the total aromatic content and those of benzene, toluene, and xylenes for different catalyst/biomass ratios 0E+00 2E+07 4E+07 6E+07 C/B=1C/B=2 C/B=5 Peak area C3-C4 C5-C7 total (C3-C7) Fig. 5 Distribution of C3-C7 olefins in the catalytic pyrolysis at 450 °C for different catalyst/biomass ratios 2814 Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 by CaO as reactant; that is, the reaction of CaO with acids or other carboxyl groups yields calcium carboxylates, which are subsequently decomposed into CaCO3 and ketones [65, 66]. Consequently, the relative content of acids decreases. This can also explain the high acetone, 2,3-butanedione, and 2-butanone peak areas obtained. Other compounds identified in high percentages are 2-cyclopenten-1-one and derivatives, cyclopentanone and derivatives, 1-(acetyloxy)-2-propanone, and 2,3-pentanedione. Zhou etal. [67] reported that the significant formation of cyclic ketones can be explained by the transformation of anhydrosugars (mainly levoglucosan) via rearrangement reactions of furfuryl type compounds, such as furfural. Other authors explained this phenomenon as ketonization of carbolic acids to form acetone, which can couple with furans or acetone itself via aldol condensation to elongate the carbon chain length by numerous base catalysts [68, 69]. The results obtained in this study show that ketones have a markedly higher relative content and furans a significant decrease with respect to the values obtained in the thermal pyrolysis. Besides, the content of acids is lower, especially of short carbon chained ones, such as formic and acetic acids. Valle etal. [23] upgraded the bio-oil on dolomite and obtained a high amount of acetone. They state that this result is evidence of the dolomite activity for acetic acid ketonization and, furthermore, other ketonization reactions involving carboxylic acids may also occur, which lead to the formation of linear ketones. Anhydrosugar compounds are the next most abundant ones, with their content being 16.6%. Levoglucosan is the prevailing compound in this family with a content of 14.8%. Incondensable gases account for a relative content of 13.2% and acids for 16.5%. In the acid family, the long-chain acids are the main compounds identified, e.g., undecanoic, hexadecanoic, and octadecanoic acids, with their contents being 3.9, 3.5, and 2.0%, respectively. The families made up of ethers and hydrocarbon compounds are also produced in a significant amount (contents of 5.4% and 4.8%, respectively). Within ethers, 1-methoxy9-octadecene and 1,1′-dimethoxy-9-octadecene have been identified and account for 3.9 and 1.4%, respectively. The hydrocarbon compounds are C9-C18 aliphatic hydrocarbons (paraffins and olefins). The aromatic hydrocarbons identified have been toluene, ethylbenzene, and 1,2,3-trimethylbenzene, with the first one being the prevailing one with a content of 0.2%. Concerning the deoxygenating activity of the dolomite, this catalyst lowers the content of oxygenated compounds from 98% (corresponding to thermal pyrolysis) to 93%, under the conditions tested (450 °C and a C/B ratio of 1). Therefore, it has a much lower deoxygenating capacity than the HZSM-5 zeolite (83% of oxygenate compounds), which is explained by the better features of the latter (acidity and porous structure) for this process. Table 10 Peak area percentages of the different compound families obtained in the catalytic pyrolysis of DPS on dolomite at 450 °C with a C/B mass ratio of 1 The bold entries significance is to remake the different families categories Peak area % Incondensable gases 13.2±3.7 Acids 16.5±3.9  Acetic acid 0.2±0.06  Fatty acids 12.9±3.7  Esters (alkyl ester acids) 3.4±0.4 Ketones 26.9±2.3  Acetone 2.7±0.8  1-Hydroxy-propanone 2.3±0.25  2,3-Butanedione 1.5±0.1  2-Butanone 1.3±0.6  Others 19.0±1.5 Aldehydes 2.7±0.5  Acetaldehyde 1.3±0.4 Phenols 2.4±0.5  1,2-Benzenediol 0.6±0.3  1,2-Benzenediol derivatives 0.1±0.08  Phenol 0.3±0.03  Phenol derivatives 1.4±0.25 Ethers 5.4±1.0 Esters 0.8±0.1 Alcohols 1.7±0.1  Lineal 1.7±0.1  Cyclic 0.08±0.01 Furan 3.2±1.2  Furan derivatives 0.3±0.03  Furan derivatives (ketones) 0.4±0.1  Furan derivatives (aldehydes) 2.3±1.1  Furfural 0.09±0.04 Anhydrosugars 16.6±5.8  Levoglucosan 14.8±5.4  d-allose 0.25±0.2  2,3-Anhydro-d-mannosan 0.2±0.05  3,4-Anhydro-d-galactosan 0.6±0.15  Glucopyranose 0.1±0.02  Others 0.6±0.5 HC 4.8±0.4  Aliphatics 4.5±0.4  Aromatics 0.25±0.03 N compounds 0.8±0.2 S compounds 0.7±0.2  Methanethiol 0.7±0.2 Pyrans 0.08±0.01 Non-identifiedcompounds 4.5±2.2 2815Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 Comparison of thermal and catalytic pyrolysis on HZSM‑5 and dolomite Given that the product distribution obtained is very different depending on whether a catalyst is used or not and on the type of catalyst used, Fig.11 compares the product distributions obtained in the three situations (without catalyst and on HZSM-5 and dolomite catalyst) at a C/B ratio of 1 and 450 °C. As observed, there are significant differences in the peak area percentages of the product families. Thus, a comparison of the results obtained in the thermal pyrolysis and those obtained on the dolomite shows that there is a large increase in the contents of ketones (from 15.7 to 26.9%), ethers (from 0.7 to 5.4%), and hydrocarbons (from 0.4 to 4.8%) when this catalyst is used, but a significant decrease in those of sugars (from 23.1 to 16.6%), with levoglucosan being the main compound, and specially furans (from 9.6 to 3.2%). The lower content of levoglucosan on dolomite or CaO has also been detected by other authors [22, 70]. A comparison of the results obtained in the catalytic pyrolysis on the dolomite and HZSM-5 zeolite shows that the major differences are the higher peak area percentages of incondensable gases, furans, and hydrocarbons obtained on the HZSM-5 zeolite. Aromatic hydrocarbons are the most abundant ones on the HZSM-5 zeolite, whereas nonaromatic hydrocarbons are the most abundant ones on the dolomite. It is noteworthy that the dolomite enhances the formation of ethers and especially of ketones. 4 Conclusions The HZSM-5 zeolite is a suitable zeolite for the deoxygenation of the volatiles (bio-oil) generated in the pyrolysis of DPS biomass. This effect has been observed especially at 450 °C with a high C/B mass ratio (C/B =5) and leads to a significant increase in the content of incondensable gases (especially C3-C4 olefins) and a large increase in that of aromatic hydrocarbons. The most abundant compounds identified are benzene, toluene, xylenes, and polyaromatic hydrocarbons, such as naphthalene, fluorene, anthracene, and their derivatives. Simultaneously, a significant reduction in the content of acids, ketones, furans, and sugars has been determined, which is higher as the C/B ratio is higher. The acids and ketones are related to the acidity and instability of the bio-oil, and therefore, the decrease in their content improves the quality of the bio-oil. This deoxygenating activity of the HZSM-5 zeolite is due to its properties, such as acidity and porous structure (shape selectivity), which promote cracking and deoxygenation reactions, and so the formation of aromatic compounds. In the case of the dolomite catalyst, a low deoxygenating activity has been determined due to its basic nature and low specific surface area. The most remarkable effect of this catalyst is the high content of ketones it allows obtaining. This is the consequence of ketonization reactions involving carboxylic acids, which are promoted by the dolomite catalyst to give linear ketones. Acknowledgements The authors gratefully acknowledge the Tunisian Ministry of Higher Education and Scientific Research (MESRST), the Spanish Ministry of Science and Innovation (PID2019-107357RB-I00) (AEI/FEDER, UE), and the Basque Government (KK-2020/00107) for their financial support. Author contribution MA, MO, and ABH designed the study. GB and MB conducted the experiments and collected the data. MA wrote the draft of the manuscript, while all other co-authors provided substantial feedback. All authors gave final approval for publication. Funding Open Access funding provided thanks to the CRUE-CSIC agreement with Springer Nature. This project has received funding from the European Union’s Horizon 2020 research and innovation Fig. 11 Mean peak area percentages obtained in thermal and catalytic pyrolysis (on HZSM-5 and dolomite, C/B=1) at 450 °C 0 5 10 15 20 25 30 Peak area % thermal zeolite dolomite 2816 Biomass Conversion and Biorefinery (2024) 14:2799–2818 1 3 programme under the Marie Sklodowska-Curie grant agreement no. 823745. Data availability Data and materials supporting the conclusions of the manuscript are available from the corresponding author on reasonable request. Code availability Not applicable Declarations Competing interests The authors declare no competing interests. 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