Thermochemical Transformation of Municipal Household Solid Waste Fractions into Bio-Oils and Bio-Adsorbents

1. Introduction

The growth in population density, economic development and the increasing availability of products and services have brought with them the constant challenge of dealing with the management and disposal of urban solid waste [1,2]. About 40% of the Municipal Solid Waste (MSW) produced globally is directed to landfills, while approximately 30% is disposed of in open dumps [3]. According to Sustainable Development Goal 11 (SDG 11) [4], proper municipal waste management is critically significant for advancing sustainability and ensuring the preservation of natural resources for future generations [5].

As a result, the proper management of Municipal Solid Waste (MSW) represents a substantial challenge for medium and large cities, as it requires complex considerations related to logistics, safety, environment, and energy aspects to ensure efficient management [6]. The projection is that, by the year 2030, global waste production will reach the mark of 2.59 billion tons [3].

In 2021, the Northern Region of Brazil was responsible for generating approximately 35.8% (about 1.773.927 tons per year) of Municipal Solid Waste (MSW) properly disposed of, while 64.4% (approximately 3.209.013 tons per year) had an inadequate destination [7]. The constant increase on the amount of solid waste entails several problems regarding the transportation, storage, and disposal of these materials, making the efficient management of solid waste challenging [8]. Despite the pressing needs for more sustainable approaches to waste management in order to address the environmental and public health challenges associated with this growing problem [9]. In addition, solid waste (SR) covers several categories, including domestic, industrial, commercial, institutional, hospital, urban, agricultural, process, construction and demolition waste, and sweeping services [10].

Notably, the Sars-covid pandemic has intensified the accumulation of waste, altering the pattern of generation with a significant increase in the production of plastics and household waste [11]. This increase was driven by the growth in demand for food deliveries, resulting in an increase in the use of common plastic waste in packaging, such as polypropylene, low-density polyethylene, high-density polyethylene, polyethylene terephthalate and polystyrene [12].

It is a fact that plastics are present everywhere and have become essential components of contemporary society, due to their characteristics of lightness, ease of molding and affordable cost. This scenario has contributed to a remarkable 20-fold increase in annual plastic production over the past five decades [13]. By the year 2050, it is estimated that this production will consume more than 500 million metric tons of crude oil. Due to the overuse of plastic products and inadequate waste management, about 60% (wt.) of plastic solid waste is disposed of in the environment or destined for landfills [14,15]. In addition, Municipal Solid Waste (MSW) has considerable economic potential, and the efficiency of waste management systems plays a crucial role in determining this potential economic value [16,17]. The heterogeneous nature of solid waste, which often contains elements that are difficult to degrade and treat, presents challenges to assimilation by the environment, resulting in risks to environmental protection and consequences for public health [18]. However, in order for MSW to be properly disposed of and treated, several steps are indispensable, following applicable guidelines through the development of solid waste management and management systems. These phases are essential to ensure that the handling, transportation, treatment, and final disposal of waste occur effectively [19].

Effective implementation of an integrated system for Municipal Solid Waste (MSW) requires an in-depth understanding of the per capita generation and gravimetric composition of this waste. This aspect has been the subject of investigation in recent years by researchers such as [20,21,22]. These studies focus on the sectorization of waste collection routes, gravimetric characterization, and energy valuation of the technological routes of MSW treatment [8].

Carneiro [23], one of the pioneers in exploring the economic potential of MSW generated in the municipalities of Belém, host of COP Conference 30 in 2025, and the municipality of Ananindeua in the state of Pará [22]. Their research allowed the identification of an average change of 13% in the amount of recycled material between 2000 and 2006, influenced by the social profile of the population [20]. These significant contributions provide valuable insights for the development of comprehensive strategies in the integrated management of MSW, considering economic, environmental, and social aspects [24].

In this scenario, it becomes imperative to adopt advanced waste management practices to preserve the environment, protect public health, preserve ecosystems, and promote global quality of life in the future [6,17]. Over the past decades, significant advances have been made in sustainable waste management, especially in response to the challenges presented by a circular economy [17,24]. This paradigm involves the application of thermochemical technologies, such as pyrolysis, gasification, or combustion, aimed at reducing, reusing, recycling, and recovering waste [25,26]. Among them, the pyrolysis of biomass and waste plastics has recently become a hot topic and has gained much more attention as the fundamental and main stage of thermochemical conversion Kumar et al. [14].

Pyrolysis is a process of thermal conversion of biomass into energy, where in an inert environment, high temperatures are used to produce gaseous products, liquids named bio-oil and solids named biochar [27,28], occurs at temperatures above 400 °C in the absence of oxygen. There are distinct forms of pyrolysis, covering 1) slow pyrolysis, 2) fast pyrolysis, and 3) ultrafast pyrolysis, also referred to as flash pyrolysis. These categories encapsulate variations in terms of temperature, heating rate, residence time, and the resulting products of each technique [29,30].

In the case of biomass raw materials, flash pyrolysis results in a higher proportion of oil compared to rapid pyrolysis. However, this dynamic shifts to plastic waste, where rapid pyrolysis generates a higher amount of gas compared to other products [31]. The products of waste plastic pyrolysis include solid waste, liquid waste, and gaseous waste Suresh et al., [32].

Catalytic pyrolysis is widely used to process mixtures of hydrocarbons, in controlled composition, to obtain fuels or chemical products. Thus, conventional catalytic cracking uses silica-alumina, zeolites, basic catalysts such as Na₂CO₃ and CaO [33], or FCC catalysts (fluid catalytic cracking).

It is important to highlight that catalytic pyrolysis (catalytic cracking) is one of the most important processes in the refining industry, especially when it comes to the process of obtaining a gasoline of better quality and higher octane (through the optimization of aromatic and olefin contents) [34,35]. To date, no research has investigated the effect of temperature and percentage of FCC zeolite-type catalyst on the MSW fraction (organic matter + paper + plastic) and its implications on biochar morphology and crystal structure, as well as on the yield of reaction products, chemical composition and acidity of bio-oils obtained by pyrolysis and catalytic pyrolysis.

In this context, this work proposes to investigate the process of production of biofuels, via thermal pyrolysis and catalytic pyrolysis using the zeolite FCC in the mass percentages of 5%, 10% and 15% for the fractions of MSW (organic matter + paper + plastic) on a laboratory scale, evaluating the quality and yield of the products obtained at temperatures of 400 °C, 450 °C and 475 °C at 1 atm. In addition to analyzing the organic liquid products (Bio-oil) obtained in relation to their chemical composition and production yields. As well as to evaluate the crystallographic and morphological characteristics of the biochars produced.

3.1.1. Pyrolysis Process Experimental Apparatus

The laboratory-scale Pyrolysis unit consists of a cylindrical-shaped borosilicate reactor with a volumetric capacity of approximately 200 ml. The reactor was inserted into a cylindrical furnace with a collar-type ceramic resistance, with a power of 800 W, which was connected to the digital temperature and heating rate controller (THERMA, Model TH90DP202-000), which had a K-type temperature sensor (Ecil, Model: QK. 2), as described in detail else-where Assunção et al. [37]; De Castro et al. [44]. Figure 3 and Figure 4 exemplify the description of the Pyrolysis laboratory unit.

3.1.2. Experimental Procedures

In the bench-scale (laboratory) investigation, thermal and catalytic pyrolysis experiments were carried out to verify the influence of catalyst percentage variations on the yields and characteristics of the products obtained, at temperatures of 400°C, 450°C and 475°C. , aiming to evaluate the influence of process parameters, yield and characteristics of the products obtained, all carried out at a heating rate of 10° C/min.

Table 2 shows the experimental conditions used in the pyrolysis processes of urban solid waste (organic fraction + paper + plastic), in the absence and presence of an FCC catalyst.

The experiments were carried out, in semi-continuous mode, at a temperature of 475 °C at 1.0 atm, and the percentages of 5, 10 and 15% of the FCC catalyst in order to evaluate the influence of this difference in final process temperature on the yield of the products obtained and the physical-chemical characteristics of the liquid product obtained (bio-oil). The masses of the MSW fractions (organic + paper + plastic) for each experiment were initially weighed on a semi-analytical balance (QUIMIS, Q – 500L210C), with this quantity being around 40 g.

They were then deposited in the 200 mL borosilicate glass reactor. With this, the reactor was inserted into the jacketed cylindrical furnace, and with the help of the control system (temperature controller) the reaction time, heating rate and final process temperature (set-point) were programmed, starting from of Equation 3, that is, for each pre-defined temperature, different process times were obtained. Given the established parameters, a time of 10 minutes was programmed to maintain constant each final operating temperature. The experimental apparatus was assembled by connecting the cooling condenser to the reactor, where the refrigerant fluid was at 20 °C. Thus, at room temperature (25 °C), the slow Pyrolysis process began at a heating rate of 10ºC/min to monitor and collect operational process parameters such as: temperature rise (heating ramp); time and temperature of product formation.

3.2. Physicochemical and Chemical Composition of Bio-Oil

3.2.1. Physicochemical Characterization of Bio-Oil and Aqueous Phase

The bio-oil and the aqueous phase were characterized in terms of acidity according to the AOCS Cd 3d-63 method. As described elsewhere Almeida et al.[45], Castro et al.[44].

3.2.2. Chemical Composition of Bio-Oil and Aqueous Phase

The chemical composition of bio-oil and aqueous phase were determined by GC-MS and the equipment and procedure described in details by Almeida et al. [45], Castro et al. [44]. The concentrations were expressed in area, as no internal standard was injected for comparison the peak areas. In addition, a qualitative analysis of the bio-oil was performed by FT-IR. Almeida et al. [45], Castro et al. [44].

3.3. Characterization of Biochar

3.3.1. SEM and EDS Analysis

The morphological characterization of biochars obtained by thermal and catalytic pyrolysis (5.0, 10.0 and 15.0% (by mass) FCC) of organic matter + paper + plastic was carried out by scanning electron microscopy using a microscope (Tescan GmbH , Czech). Republic, Model: Vega 3). The samples were covered with a thin layer of gold using a Sputter Coater (Leica Biosystems, Germany, Model: Balzers SCD 050). Elemental analysis and mapping were performed by energy dispersive X-ray spectroscopy (Oxford instruments, UK, model: X-MAX-80).

3.3.2. Análise de Difratometria de Raios-X (DRX)

The crystallographic characterization of biochars obtained by thermal and catalytic pyrolysis with 5.0, 10.0 and 15.0% (by mass) of FCC) of organic matter + paper + plastic was carried out by X-ray diffraction with a PANalytical Empyrean diffractometer with a ceramic ray tube X and cobalt anode (Kα1 = 1.78901 Å), long fine focus, Fe Kβ filter and PIXCEL3D-Medpix3 1 × 1 detector operating in scan mode. The following analysis conditions were used: voltage of 40 kV, current of 35 mA, step size of 0.0263° in 2θ, 2θ scan range of 3.0072° to 94.9979°, scan speed of 30 .6 s/step, 1/4° slit angle, 1/2° anti-scattering slit and 10 mm beam mask. The phases were identified using the PANalytical X'Pert High Score software version 3.0., SANTOS et al. [46].

3.4. Yields of Bench-Scale Thermal and Catalytic Pyrolysis Experiments

The yield of condensable liquid products, oily, aqueous and other phases, as well as the carbonaceous materials formed, cokes, from each experiment carried out on a bench scale, were calculated in terms of the percentage of their mass in relation to the mass initial sample inserted into the reactor (RSU, RSU +catalyst). The yield of non-condensable gas phases was determined by difference, considering a total yield of 100%. The yields of the products obtained were determined by Equations 1,2 and 3.

Process performance was evaluated by calculating the bio-oil, solid (biochar) and gas yields defined by equations (1) and (2), and the gas yield by difference, using equation (3).

$$Y_{bio-oil}\left[\%\right]=\frac{M_{bio-oil}}{M_{Feed}}x100$$

(1)

$$Y_{solids}\left[\%\right]=\frac{M_{solids}}{M_{Feed}}x100$$

(2)

$$Y_{gas}\left[\%\right]=100-(Y_{bio-oil}+Y_{solids})$$

(3)

4. Results

4.1. Characterization of Biochar

4.1.1. SEM Analysis

To carry out the scanning electron microscopy analysis, it was necessary to coat the samples with gold. Figure 5 presents the magnifications in magnitude of [3.0 kx] x and [6.0kx] x [10 kx] of the biochars from the experiments carried out by thermal pyrolysis at 400°C (a), 450°C (b) and 475° C (w).

Biochar is mainly composed of CO, while the inorganic portion mainly contains minerals such as Ca, Mg, K, P and inorganic carbonates depending on the feedstock Trazzi et al. [50]. The surface morphology of biochar after the MSW pyrolysis process is reported in Figure 5, in which the scanning electron microscopy (SEM) image obtained using a backscattered electron detector is shown. Both illustrated images show a charred surface (black color) and granules (white color) of different sizes spread across the surface as reported by Assunção et al. [37], being similar to the SEM images of CaCO₃ (calcite) reported by Cabrera-Penna et. al. [51], Hassani et. al. [55], and SEM images of biochar obtained by MSW pyrolysis reported by Gopu et. al. [52]. The MSW biochar particles showed irregular shape and size.

Microscopies of biochars covered with gold show magnifications in magnitude of [3.0 kx] x and [6.0kx] x [10 kx] of biochars from experiments carried out by catalytic pyrolysis of the fraction (organic matter + paper + plastic) of MSW at 450° C at 5%, 10% and 15% (by mass) of FCC, respectively, 1.0 atmosphere, on a laboratory scale, are illustrated in Figure 6, Figure 7 and Figure 8.

The size of the catalyst pores has a great influence on the reaction activity, as it affects the mass exchange of reactants and the yield. The larger the zeolite pore size, the greater the mass exchange and the easier the diffusion of larger molecules Rezaei et al. [49]. In both micrographs in images 6, 7 and 8, an opening of the pores can be seen as the catalyst content increases; in general, its surface appears smooth, although some areas are bumpy (Figure 8). After the addition of FCC zeolite, the pore structure of the biochar was more complex: the pore structure was dominated by megalopores with evidence of pore collapse for some pores, and its arrangement was very irregular. It showed many small particles on the inner and outer surfaces of the pore structure, making the surface of the sample rough.

4.1.2. EDS Analysis

The results of the elemental analysis performed by energy dispersive X-ray spectroscopy at one point for biochars obtained by pyrolysis of the fraction (organic matter + paper+plastic) of MSW at 450 °C, 1.0 atmosphere and by catalytic pyrolysis (organic matter + paper + plastic) of MSW at 450 °C, 1.0 atmosphere, with 10.0% (by mass) FCC as catalyst, on a laboratory scale, are illustrated in Table 3.

Generally, biochars from municipal solid waste are mainly composed of CO, while the inorganic portion mainly contains minerals such as Ca, K, P and inorganic carbonates depending on the raw material Trazzi et al., [2018]. It is worth noting that the biochars in this study predominantly contain C, Ca, Cl, K and O. The biochars in this study presented a high content of C (70.6% by mass) for the experiment with FCC and O (22.3% by mass) for thermal pyrolysis. The high level of carbonization in MSW-derived biochars makes them rich in carbon, which makes them resistant to degradation in the environment Li and Chen, [57]. This recalcitrance of MSW-derived biochars can help combat the increase in carbon emissions from soils when these materials are used for carbon sequestration Lefebvre et al., [56].

While there was a decrease for Ca (2.1% by mass) and Na (1.7% by mass), and a small increase in the percentage for Cl (3.5% by mass) and K (2.8% by mass), mass) with the addition of the FCC catalyst. Therefore, the pyrolysis of MSW led to the phase separation of the salts from the carbonaceous part. This separation may be a result of the evaporation of water from MSW during pyrolysis, which led to the crystallization of cubic NaCl crystals on the surface of the biochar. Similar results were also observed in the case of thermal pyrolysis of MSW and MSW using zeolite as catalyst in the studies by Raček et al [58].

4.1.3. XRD Analysis

The XRD analysis of biochar obtained by pyrolysis of the fraction (organic matter + paper+plastic) of MSW at 400 °C and MSW at 450ºC, 1.0 atmosphere are illustrated in Figure 9, Figure 10 and Figure 11. The XRD showed the presence of two peaks associated with the CaCO3 crystalline phase (Calcite), one of high intensity at position 2θ: 29.5 (100%), another of medium intensity at position 2θ: 20.8 (50%), and a third of low intensity at 2θ position: 36.6 (16.2%). Which is consonant according to the 2θ position: 29.4 (100%), characteristic of calcite CaCO₃ [54]. According to Ghavanati et. al. [54], the organic fraction of urban household solid waste contains 4.6 ± 0.6% (by mass) of calcium (Ca) in its proximate composition. The presence of quartz (SiO₂) is probably due to the presence of small sand particles inside the MSW.

The XRD analysis of biochar obtained by catalytic pyrolysis of the fraction (organic matter + paper + plastic) of MSW at 450 °C, 1.0 atmosphere, with 5% (by mass) of FCC, illustrated in Figure 12, identified the presence of two crystalline phases, KCl (Potassium Chloride) and Zeolite (FCC).

Three peaks are associated with the zeolite crystalline phase (FCC), two of high intensity at the 2θ position: 31.0 (100%) and 2θ: 42.61 (98.95%), and one of low intensity at the 2θ position: 34.25 (37.07%). A peak of medium intensity is associated with the crystalline phase Furthermore, analyzing the XRD, the high intensity of the zeolite peaks (FCC) was observed, the chemical cracking capacity was attributed to the Lewis and Brønsted acidity, which helps to catalyze the cracking of biomass potassium chloride (KCl) at position 2θ: 47.38 (18.54%). Furthermore, analyzing the XRD, the high intensity of the zeolite peaks (FCC) was observed, the chemical cracking capacity was attributed to the Lewis and Brønsted acidity, which helps to catalyze the cracking of biomass.

This causes a decrease on the carbonization degree, that is, the carbon content in biochar, being according to the findings reported by Kumagai et. al. [53].

XRD analysis of biochar obtained by catalytic pyrolysis of the fraction (organic matter + paper + plastic) of MSW at 450 °C, 1.0 atmosphere, with 10% (by mass) of FCC, illustrated in Figure 13, identified the presence of three crystalline phases, CaCO3 (calcite), SiO3 (quartz) and KCl (Potassium Chloride). One peak is associated with the crystalline phase of high-intensity quartz at position 2θ: 30.90 (76.55%), another referring to calcite 2θ: 34.23 (69.28%), and finally the peak referring to the phase crystalline potassium chloride at position e 2θ: 58.94 (100.0%).

The XRD analysis of biochar obtained by catalytic pyrolysis of the fraction (organic matter + paper + plastic) of MSW at 450 °C, 1.0 atmosphere, with 15% (by mass) of FCC, illustrated in Figure 14, identified the presence of two crystalline phases, CaCO3 (Calcite) and Zeolite (FCC). Three high intensity peaks are associated with the zeolite crystalline phase at position 2θ: 58.94 (100%), 2θ: 33.01 (25.72%) and 2θ: 27.42 (12%), and finally the peak referring to the crystalline phase of calcite at position 2θ: 34.23 (69.28%), 2θ: 36.62 (12.28%) and 2θ: 46.05 (14.70%).

4.2. Pyrolysis of MHSW Fraction (Organic Matter + Paper+Plastic) in Fixed Bed Reactor

4.2.1. Process Conditions, Mass Balances, and Yields of Reaction Products

4.2.1.1. Influence of Pyrolysis Temperature

Thermal pyrolysis (thermal cracking) (performed without a catalyst) was used as a reference in this study. Figure 15 and Table 4 illustrate the mass yields in products obtained (liq-uids, solids, H2O, and gas) with the MSW fractions (organic matter+paper+plastic) with final temperatures of 400, 450, and 475 ° C, 1.0 atmosphere, on laboratory scale, with heating rates at 10 °C/min. The thermal pyrolysis of MSW aimed to obtain mixtures of hydrocarbons and other compounds with potential for use as fuel, with an emphasis on obtaining products similar to gasoline and diesel oil.

The bio-oil yield was the highest at the temperature of 450 °C, going from 9.34% (wt.) to 9.44% (wt.) with the increase in final temperature from 400°C to 450°C. It can be observed that the variation in final temperatures did not show significant influence in the experiments to obtain bio-oil. According to Mothé and Azevedo [59], it is necessary to vary the heating rate, as it directly influences the temperature at which degradation begins. This can be understood by analyzing that for degradation to occur, the vapor pressure of the sample must overcome the ambient pressure and the released gases must diffuse freely throughout the environment. In other words, at lower rates there is greater uniformity of the temperature in the material and the heat transfer between the molecules also ends up being more balanced, causing more regular volatilization and greater liquid formation. For thermal pyrolysis, slow pyrolysis is beneficial for oil formation and hinders gas formation. This phenomenon is different from the observed trend of biomass with respect to the warming rate Aboelela et al. [61].

The biochar yields varied inversely to the condensed product yields, with the highest yield being 65.97% (wt.) at a temperature of 400°C. The aqueous fraction varied between 18.78% (wt.) and 22.15% (wt.) at 400°C and 475°C, respectively. While the gaseous fraction obtained had its highest percentage at 475°C with 28.97% (wt.). The results for byproducts obtained through pyrolysis are in line with studies reported in the literature for MSW pyrolysis [47,48,62,63,64].

In all studies reviewed, an increase in bio-oil yield was observed within the temperature range between 450°C and 600°C. However, this yield tends to decrease after exceeding 600°C. On the other hand, the bio-char yield shows an inverse pattern, decreasing in the range of 400°C to 600°C after reaching a peak, while the gas yield shows a continuous increase over the entire mentioned temperature range.

In a specific study conducted by Buah et al. 2007 [48], focused on the pyrolysis of municipal solid waste (MSW), it was reported that the yield of bio-char reaches its maximum at 400°C, and then declines after exceeding this point. On the other hand, bio-oil yield increases at higher temperatures, reaching its maximum at 700°C. Once again, the gas yield continues to increase consistently, remaining in line with the general yield standards of reaction products in relation to temperature, as evidenced in Figure 15 of the study, also reported by Assunção et al. 2021 [37].

4.2.1.2. Influence of the FCC Catalyst on the Pyrolysis Process

Catalytic pyrolysis (thermal-catalytic cracking) was used as a reference in this study. Figure 16 and Table 5 illustrate the mass yields in products obtained (liquids, solids, H₂O, and gas) with the MSW fractions (organic matter + paper + plastic) with final temperatures at 450°C, 1.0 atmosphere, with the percentages of 5%, 10% and 15% of commercial catalyst (in mass) from FCC, on a laboratory scale, with heating rates at 10 °C/min. Remembering that the FCC catalyst has an acidic character (Bronsted acidity predominantly).

The bio-oil yield was the highest at 10% FCC (by mass), it went from 3.83% (wt.) to 4.83% (wt.) with the percentage increasing from 5% to 10% (in large scale). In general, there was no significant increase in bio-oil production, according to Wang et al [47] in their studies of MSW pyrolysis using the FCC catalyst in the process, for catalytic pyrolysis, oil yields are decreased markedly, and the gas yield is increased significantly. In their results for catalytic pyrolysis using PET and LDPE, bio-oil yields were reduced by 12.7 mass % and 13.3 mass % for slow and fast pyrolysis, respectively, compared to no pyrolysis catalytic.

It can also be seen that there was a decrease in the production of the aqueous phase and biochar, going from 22.49% [wt.] to 13.47% [wt.] and 48.08% [wt.] to 36.70 % [wt.], at a percentage of 10% and 15% [wt.] and 5% and 15% [wt.], respectively of FCC. The increase in the amount of catalyst led to a significant increase in the amount of gas generated, reaching a value of 54% [wt.] gas with 15% FCC catalyst. This fact can be explained by the greater activity of this catalyst in both primary and secondary cracking reactions [64].

4.2.2. Physicochemical and Compositional Characterization of Bio-Oil

4.2.2.1. Acidity of Bio-Oil

Table 6 shows the effect of temperature on the acidity of bio-oil by pyrolysis of the MSW fraction (organic matter + paper + plastic) at 400, 450 and 475 °C, 1.0 atm, on a laboratory scale. The acidity of the bio-oil increased with increasing process temperature, while that of the aqueous phase decreased. The acidity of the bio-oil obtained at 475 °C, 1.0 atm, on a laboratory scale is close to that of the bio-oil (126.80 ± 1.0 mg KOH/g) obtained by pyrolysis of waste cooking oil at 550 °C, 1.0 atm, on laboratory scale Trabelsi et al. [60]. This strong indicated acidity of bio-oil is explained by its high levels of carboxylic acids and constitutes a disadvantage that limits its direct use as fuel in the transport sector. It can cause corrosion problems in the mechanical components of engines. To avoid these problems caused by the high acidity of bio-oils, the use of catalytic cracking is recommended Trabelsi et al. [60].

Table 7 shows the effect of FCC content on the acidity of bio-oil by catalytic pyrolysis (thermal-catalytic cracking) of the RSU fraction (organic matter + paper + plastic) at 450 °C, 1.0 atm, with 5 0, 10.0 and 15.0% (in mass), on a laboratory scale.

According to [66] solid acid catalysts play a significant role in catalytic pyrolysis by affecting the distribution of functional groups in bio-oil. Factors such as channel structure, pore size and acidity play a crucial role in regulating catalytic reactions in zeolite catalysts. Functional groups, such as sugars, acids, aldehydes, ketones, furans, and alcohols, resulting from the decomposition of biomass, have a high diffusion capacity in the zeolite channels. They are involved in several reactions that lead to the release of oxygen, culminating in the formation of aromatic hydrocarbons and deposition of coke.

The acidity of the catalytic pyrolysis bio-oil increased and remained constant in all percentages used with the FCC catalyst, in addition, the pH value of the catalytic pyrolysis bio-oil is much higher than that of bio -oil from a thermal process because of the elimination of acid groups by decarboxylation over solid acid catalysts [66,67].

4.2.3. FT-IR of Bio-Oil

The qualitative analysis by FT-IR of the chemical functions presents in bio-oils obtained by thermal pyrolysis of the MSW fraction (organic matter + paper + plastic) at 400, 450 and 475 °C, 1.0 atm, on a laboratory scale, are illustrated in Figures 17,18 and 19. It is worth noting that all analyzed samples present vibrations in their spectra typical of unsaturated hydrocarbons. Bands related to the CH2 group were observed at 1376 cm^-1. The bands at 2924-2855 cm-1 refer to asymmetric and symmetric stretching of this same group, and 1602-1603 cm^-1 indicates an angular deformation. The band at 1455 cm^-1 can be attributed to sections of the CH₂ bond, in this region the peaks at 1710 cm^-1 indicate the presence of ketones, all spectra present bands of angular deformation outside the plane of the C-H bond close to 908 cm^-1. The stretching of the C-O bond of phenol was assigned to be 1277 cm-1. At 1680 - 1820 cm -1, which corresponds to the axial deformation vibration of carbonyl (C=O).

Figure 17. FT-IR of bio-oil obtained by pyrolysis of MHSW fraction (organic matter + paper+plastic) at 400°C, 1.0 atmosphere, in laboratory scale.

Figure 17. FT-IR of bio-oil obtained by pyrolysis of MHSW fraction (organic matter + paper+plastic) at 400°C, 1.0 atmosphere, in laboratory scale.

Figure 18. FT-IR of bio-oil obtained by pyrolysis of MHSW fraction (organic matter + paper+plastic) at 450 °C, 1.0 atmosphere, in laboratory scale.

Figure 18. FT-IR of bio-oil obtained by pyrolysis of MHSW fraction (organic matter + paper+plastic) at 450 °C, 1.0 atmosphere, in laboratory scale.

Figure 19. FT-IR of bio-oil obtained by pyrolysis of MHSW fraction (organic matter + paper+plastic) at 475 °C, 1.0 atmosphere, in laboratory scale.

Figure 19. FT-IR of bio-oil obtained by pyrolysis of MHSW fraction (organic matter + paper+plastic) at 475 °C, 1.0 atmosphere, in laboratory scale.

Qualitative analysis by FT-IR of the chemical functions present in bio-oils obtained by catalytic pyrolysis of the MSW fraction (organic matter + paper + plastic) at 450 °C, 1.0 atm, 5.0, 10.0 and 15, 0% (by mass) FCC, on a laboratory scale, is illustrated in Figure 20, Figure 21 and Figure 22.

As bandas 1680 a 1688 cm^-1 receberam espectros na banda de estiramento C = O. As bandas próximas a 2853 a 2916 cm^-1 referem-se às deformações ax-iais alifáticas das ligações C-H dos grupos metileno (CH₂) e metila (CH₃ ). Pode-se observar uma vibração axial C=C em 1642 cm^-1, Os picos em 1682 cm⁻¹ e 1285 cm⁻¹ são atribuídos a ligação dupla O e C– O, em 730-731 cm^-1 apresentou uma deformação media, em 1275 cm ^-1 sugere conter grupos NO₂ e, provavelmente, alguma parte alifática, estando de acordo com análise sem-elhante de bio-óleos por FT-IR relatado por [47,68,69].

4.2.3.1. Chemical Composition of Bio-Oil

Table 13 and Figure 23 illustrate the effect of temperature on the content of hydrocarbons and oxygenates in bio-oil obtained by pyrolysis of the MSW fraction (organic matter + paper + plastic) at 400, 450 and 475 °C, 1.0 atmosphere , on a laboratory scale. The chemical functions (alcohols, carboxylic, oxygenated and nitrogenous acids), sum of peak areas, CAS numbers and retention times of all molecules identified in the bio-oil by GC-MS, are illustrated in Supplementary Tables S1-S3 . The concentration of oxygenates in bio-oil has a maximum value at 400 °C and for nitrogenates it has a maximum value of 475 °C. This agrees with the acidity of bio-oils illustrated in Table 6, where the bio-oil obtained by thermal pyrolysis of the MSW fraction (organic matter + paper+plastic) at 400 °C, 1.0 atm, presents its lower acidity value. The results are in line with [70], who in their thermal co-pyrolysis studies using a mixture of biomass and low-density polyethylene obtained significant amounts of the different families of oxygenated compounds present, while almost no hydrocarbons were detected in the bio-oil thermal.

Table 13. Effect of temperature on the chemical composition, expressed in oxygenates/nitrogens, of bio-oils obtained by pyrolysis of the MSW fraction (organic matter + paper+plastic) at 400, 450 and 475 °C, 1.0 atm, on a laboratory scale.

Temperature [°C]	Concentration [%area.]
	Oxygenates	Nitrogenates
400	75.89	24.11
450	62.67	37.33
475	36.12	63.88

Table 13. Effect of temperature on the chemical composition, expressed in oxygenates/nitrogens, of bio-oils obtained by pyrolysis of the MSW fraction (organic matter + paper+plastic) at 400, 450 and 475 °C, 1.0 atm, on a laboratory scale.

Temperature [°C]	Concentration [%area.]
	Oxygenates	Nitrogenates
400	75.89	24.11
450	62.67	37.33
475	36.12	63.88

Figure 24 and Tables S4-S6 show the effect of the FCC-to-MSW fraction ratio on the hydrocarbon and oxygenated content in the bio-oil obtained by catalytic pyrolysis of the MSW fraction (organic matter + paper + plastic) at 475 °C, 1 .0 atm, 5.0, 10.0 and 15.0% (by mass) FCC, on laboratory scale. Chemical functions (alkanes, alkenes, alkynes, aromatics, esters, carboxylic acids, phenols, aldehydes, alcohols, amines, amides, nitrogenates and ketones), sum of peak areas, CAS numbers and retention times of all molecules identified in bio-oil by GC-MS are illustrated in Supplementary Tables S4-S6. The concentration of hydrocarbons in bio-oil decreases with an increase in the proportion of the FCC-to-RSU fraction, while that of oxygenates increases. The bio-oil compositions described in Tables S1-S6 are in accordance with those described in the literature for bio-oils obtained by pyrolysis of MSW [21,31,32,37,44,47].

The occurrence of nitrogen-containing compounds is probably due to the presence of nitrogen in MSW determined by elemental analysis as reported by AlDayyat et. Al. [20], and by Ghavanati et. Al. [67]. Regarding the influence of the catalyst content on the chemical composition, Figure 24 illustrates that increasing the catalyst content causes a decrease in the concentration of hydrocarbons and an increase in the concentration of oxygenates.

5. Conclusions

The SEM images of the biochars produced by pyrolysis show the formation of porous structures, proving that pyrolysis drastically altered the morphological structure of the fraction (organic matter + paper + plastic) of MSW.

XRD analysis of biochars obtained by catalytic pyrolysis identified the presence of crystalline phases, CaCO₃ (Calcite), SiO₃ (quartz), FCC (zeolite) and KCl (potassium chloride).

Thermal pyrolysis produces a bio-oil with yields between 9.24 and 9.44% (m). The bio-oil yield increases with the pyrolysis temperature. For catalytic pyrolysis, biochar gas yields increase slightly with FCC content, while bio-oil yields decrease, and the H₂O phase remains constant.

The acidity of the bio-oil increases with increasing process temperature and with the addition of FCC as a catalyst to the process. The concentration of hydrocarbons in the bio-oil increases with the increase in the proportion of the FCC-MHSW fraction due to the catalytic de-oxygenation of fatty acid molecules, through decarboxylation/decarbonylation, producing aliphatic and aromatic hydrocarbons.