Kinetic Parameters of Nut Shells Pyrolysis

Abstract

The European Union created a European Green Deal Program (EGDP). This program aims at a sustainable economy through the transformation of the challenges related to climate and the environment. The main goal of EGDP is climate neutrality by 2050. The increase of alternative biomass residues utilization from various food processing industries and cooperation in the energy and waste management sector is required to meet these expectations. Nut shells are one of the lesser-known, yet promising, materials that can be used as an alternative fuel or a pre-treated product to further applications. However, from a thermal conversion point of view, it is important to know the energy properties and kinetic parameters of the considered biowaste. In this study, the energy and kinetic parameters of walnut, hazelnut, peanut, and pistachio shells were investigated. The results showed that raw nut shells are characterized by useful properties such as higher heating value (HHV) at 17.8–19.7 MJ∙kg⁻¹ and moisture content of 4.32–9.56%. After the thermal treatment of nut shells (torrefaction, pyrolysis), the HHV significantly increased up to ca. 30 MJ∙kg⁻¹. The thermogravimetric analysis (TGA) applying three different heating rates (β; 5, 10, and 20 °C∙min⁻¹) was performed. The kinetic parameters were determined using the isothermal model-fitting method developed by Coats–Redfern. The activation energy (E_a) estimated for β = 5 °C∙min⁻¹, was, e.g., 60.3 kJ∙mol⁻¹∙K⁻¹ for walnut, 59.3 kJ∙mol⁻¹∙K⁻¹ for hazelnut, 53.4 kJ∙mol⁻¹∙K⁻¹ for peanut, and 103.8 kJ∙mol⁻¹∙K⁻¹ for pistachio, respectively. Moreover, the increase in the E_a of nut shells was observed with increasing the β. In addition, significant differences in the kinetic parameters of the biomass residues from the same waste group were observed. Thus, characterization of specific nut shell residues is recommended for improved modeling of thermal processes and designing of bioreactors for thermal waste treatment.

1. Introduction

The European Union (EU) and all the associated countries, including Poland, belong to the European Green Deal Program. The Green Deal assumes a common plan for the sustainable economy through the transformation of the challenges related to climate and the environment [1]. The EU aims to achieve climate neutrality by 2050. The goal is achievable via transitioning to cleaner and renewable energy sources. Renewable energy creates possibilities to be implemented in several sectors: manufacturing, cement, consumer goods production processes, transport, food, or agriculture [1]. Climate neutrality can be promoted via shorter-term EU 2030 goals such as reducing greenhouse gases (GHG) by 40%, increasing the share of the renewable energy sources to 32%, and increasing energy efficiency by 32.5% [2,3].

Biomass can play an important role in an attempt to achieve climate neutrality by 2050. The biomass is responsible for energy biodiversity, carbon capture and storage (CCS), air quality, and GHG emissions [4]. It is still possible to increase the biomass role and share in climate neutrality achievement plans, especially in energy generation, agriculture, and food processing. We have been promoting biomass conversion and utilization opportunities, especially focused on less popular, variable, random, and often scattered materials such as organic waste from food processing. Furthermore, processing the waste from this sector is in line with current trends covering sustainable waste management and effective reuse of biomass residues. Such an approach allows for the reduction of the waste storage amounts and, thus, negative environmental footprint.

Biomass has a significant potential, which can be an alternative source for reuse in other processes. The data analysis performed by the European Commission (EC) within the EU showed that ~88 million tons of food waste are generated annually with associated costs estimated at 143 billion euros [5]. Waste generated during the food processing amounted to 20% (16.9 million tons) [6]. Similarly, a significant amount of food waste (mostly fruits and vegetables) was also observed in Asia and the U.S. [7]. The whole logistic chain of the fruit and vegetable sector, including processing, packing, distribution, and consumption, generates approximately 1.81, 32.0, and 15.0 million tons of waste in India, China, and the U.S., respectively [7].

According to the data presented by The Food and Agriculture Organization of the United Nations [8], nuts crops cover close to 1,200,000 ha in Europe (

Table 1. Harvested area, fruit production, and nut waste generation in Europe and Poland [8].

Crops	Europe			Poland
	Area, ha	Production, Mg	Waste, Mg	Area, ha	Production, Mg	Waste, Mg
Fruit (total)	7,481,716	87,574,401	-	379,056	5,140,130	-
Nuts (total)	1,191,510	1,254,799	501,920	6322	15,119	6048
Hazelnut	117,057	173,946	69,578	3716	6642	2657
Pistachio	37,754	20,699	8280	-	-	-
Walnut	139,037	392,446	156,978	2606	8477	3391

), producing ca. 1.2 Gt of nuts per year. Assuming that an average amount of wastes from nuts is 40% [9], over 500 kt of nut shells are generated. In Poland, taking into account the domestic production of hazelnut and walnut, over 15 kt of nuts are produced, which corresponds to approximately 6 kt of waste. It should be marked that in practice, the total amount of wastes from nuts is higher due to the nuts import and their processing in Poland. However, this biomass residue requires proper management to use its energy potential.

Thermal processing via torrefaction and pyrolysis significantly increases and expands its application potential (energy generation, fertilizers, and bio-polymers production), which makes the circular economy goals more attractive (Figure 1).

The impact of thermal processing on the physicochemical properties of many popular types of biomass is known. The studies about biomass torrefaction and pyrolysis [10,11,12,13,14,15] showed that the higher temperature of the biomass processing improves its thermal properties. The biochar is characterized by higher heating value, lower moisture content, lower volatile matter content, and improved hydrophobicity. The torrefied biomass is initially sterile and much more resistant to decay, and therefore it can be stored for a longer time [11]. As it is known, the first stage in thermal processes is dehydration. The raw nut shells have much less moisture content (MC) in comparison to the other organic waste biomass. The MC in nuts depends on their type and amounts to 20% for walnut [16], 6% for peanuts [17], 7% for pistachio [18], and 28% for hazelnut [19]. Thanks to the lower MC, nut shells require less heat for dehydration and are interesting materials for thermal processing.

Kinetics helps in understanding how to control and optimize the process of biomass thermal treatment. Description of the kinetic process includes such kinetic parameters as activation energy (E_a), pre-exponential factor (A), the reaction rate constant (k), and reaction order (n). Improved knowledge of these parameters enables modeling the thermal process, designing and optimizing the bioreactor for biomass torrefaction and pyrolysis. The kinetic process presents the biomass material response to the temperature change during the treatment process. It identifies the range of temperatures in which specific reactions take place in the material.

There are many kinetic models in use. Some of the better-known kinetics modeling methods include Freidman, Kissinger–Ozawa, Kissinger–Akahira–Sunose (KAS), Flynn–Wall–Ozawa (FWO), and the Coats–Redfern Method [20]. Due to the different content of the lignin, cellulose, and hemicellulose in biomass, there are differences between the thermal decomposition of these materials. The easiest fiber to depolymerize is hemicellulose due to its low molecular weight. Next is cellulose, and the hardest fiber to decompose is lignin [21,22,23].

The thermogravimetric (TGA)-based studies have shown that hemicellulose decomposes at the lowest temperature (200 °C to 350 °C), then the cellulose (300 °C to 400 °C), and the lignin decompose at the wider range of temperatures (150 °C to as high as 900 °C) [24,25,26]. Similar thermal decomposition characterization of the lignin, cellulose, and hemicellulose was observed by Zhou [27]. These studies were carried out based on the agricultural biomass samples like sugar cane bagasse, rice straw, rice husk, cotton stalk, and corncob; wooden biomass like pine sawdust; and the pure chemical hemicellulose, cellulose, and lignin. The biomass multi-reaction decomposition was confirmed by Lu et al. [28]. The TGA showed that biomass conversion was characterized by a two-stage reaction and different E_a. For the first stage decomposition, E_a was from 75 to 85 kJ∙mol⁻¹, and for the second stage was 3–4 kJ∙mol⁻¹ [28]. Types of biomass influence the E_a that can range from 66 kJ∙mol⁻¹ (corn stalk) to 227 kJ∙mol⁻¹ (filter paper). The wooden chips and the wheat straw have E_a of 85 kJ∙mol⁻¹ and 70 kJ∙mol⁻¹, respectively [29]. The relations between the type of biomass and decomposition kinetics were also observed in other studies; the E_a was from 150 to 550 kJ∙mol⁻¹ depending on the type of biomass [30,31]. It should be noted that the heating rate (β) also has an important impact on the kinetics. As a result, the different E_a was noted, according to the various heating rates. An increasing β resulted in higher E_a for the polyethylene materials [32].

To date, the nut shells are used as an alternative fuel, mainly in the untreated form. The common use is, pelletizing the nut shells, e.g., from walnut, pistachio, or hazelnut [33,34]. There are a few studies describing the basic energy properties of the nut shells. Investigating the Brazil nut shells the authors have shown that the HHV amounted to 20.4 MJ∙kg⁻¹, ash content varied from 1.7 to 3.2%, and volatiles were 71.6% [35,36]. In other studies, the walnuts, hazelnuts, and pistachio shells were investigated and characterized by HHV = 20.2; 21.6; 17.4 MJ∙kg⁻¹, ash content (AC) = 1.4; 2.8; 0.41%, and volatile matter content (VMC) = 59.3, 70.3, 77.5%, respectively [37,38]. Nut shells were also investigated during the pyrolysis and torrefaction process. The effect of thermal processing on the basic properties of the nut shells such as walnut, hazelnut, or pistachio was confirmed. Torrefied nut shells were characterized by higher HHV, lower VMC, and higher fixed carbon content with the increasing temperature of the process [37,39,40]. Torrefied hazelnut shells were characterized by HHV of 26.7 MJ∙kg⁻¹ (at 300 °C) [40]. Walnut, hazelnut, almond, and sunflower shells pyrolyzed at 500 °C were characterized by HHV of 30 MJ∙kg⁻¹ [37]. Such values of HHV are very competitive in comparison to bituminous coal, which is still a very common fossil fuel used for energy purposes.

In addition to the energetic use (heat and power production through combustion or co-combustion), the nut shells are also valuable for the acquisition of bio-components. Due to their lignocellulosic structure, they are used for pure lignin and cellulose production. Especially the pistachio shells are processed for the cellulose nanocrystals acquisition [41]. The cellulose nanocrystals are also produced from other nut shells such as walnut [42]. There are also studies investigating the kinetics of walnut, hazelnut, peanut, and pistachio shells thermal decomposition. However, many of these studies use different kinetic models and reactions mechanism.

Therefore, the aim of this work was to characterize the thermal decomposition and to determine the kinetic parameters of the pyrolysis process of the wastes from nuts processing applying the Coats–Redfern method. Shells from different types of nuts (walnut, hazelnut, peanut, and pistachio) were selected. The objectives of this research were: (i) carrying out detailed thermogravimetric analysis (TGA) of the nut shells, (ii) determination of the characteristic points in the nut shells thermal decomposition process, (iii) finding the temperature range of the hemicellulose, cellulose, and lignin decomposition in the investigated nut shells, (iv) estimation of the basic kinetic parameters of the nut shells thermal decomposition, (v) characterization of the nut shells conversion rates as a function of the process temperature.

2. Materials and Methods

2.1. Characteristic of the Materials Used in the Research

Four types of nuts biomass wastes were investigated (Figure 2): (a) walnut shells (WS), (b) hazelnut shells (HS), (c) peanut shells (PES), and (d) pistachio shells (PIS).

The research materials were initially dried in the drying chamber KBC–65 W (WAMED, Warszawa, Poland) (Figure 3a) for 24 h at 105 °C. For the TGA, the waste biomass from nuts (shells) was ground in the mill (LMN 400, TESTCHEM, Pszów, Poland) (Figure 3b) with a sieve size of 1 mm.

In order to characterize the fruit waste biomass—nut shells, the proximate and elemental analyses were carried out. The proximate analysis included determination of ash MC, AC, VMC, higher and lower heating value (HHV and LHV), and calculation of fixed carbon content (FFC) based on the basic energy properties. The proximate analysis was carried out in accordance with the standards listed in

Table 2. Analysis standards and methods of proximate analysis.

Analysis	Standard
Moisture content (MC)	PN EN ISO 18134-2:2017-03E
Ash content (AC)	PN EN ISO 18122:2015
Volatile matter content (VMC)	PN EN ISO 18123:2016-01
Higher heating value (HHV)	PN EN ISO 18125:2017-07
Lower heating value (LHV)	Calculation based on the HHV and MC [10]
Fixed carbon content (FCC)	ASTM D-3172-73

. Three repetitions were performed.

The elemental analysis of the used waste biomass was carried out in the organic elemental analyzer FLASH 2000 CHNO/S (THERMO SCIENTIFIC, Waltham, MA, USA).

2.2. Thermogravimetric Analysis

The prepared material (3 g per sample) was inserted into the thermogravimetric analyzer Pyrolytic Biomass Gasifier No. 11/14/3 (ROTAMETR, Gliwice, Poland) (Figure 3c). The crucible with the research material introduced into the reactor is integrated with the laboratory scale (AS 220.R2, RADWAG, Radom, Poland) to control the change of its mass as a function of time and process temperature. Inert gas (CO₂ from the compressed gas cylinder at 6 dm³∙h⁻¹) was introduced to the chamber to maintain pyrolysis conditions. The TGA was carried out from 30 °C to 900 °C. Three heating rates (β; 5, 10, 20 °C∙min⁻¹) were applied at n = 3 repetitions.

2.3. Kinetic Modelling

The kinetics of the biomass samples were studied considering a constant β. The pyrolysis of the biomass can be generally described as [20,43]:

Raw biomass	→	Biochar	+	Pyrolysis gases
(solid fraction)		(solid fraction)		(volatile fraction)

The recommendations of kinetic modeling of the biomass thermal decomposition were well described and published by ICTAC Kinetics Committee and other researchers [43,44,45]. Decomposition of the solid biomass under the isothermal conditions can be expressed as:

$$\frac{d\alpha }{dt}=kf\left(\alpha \right)$$

(1)

where: k is a process rate constant (-), α is a conversion rate of the process (-).

The α of the solid material during the pyrolysis is described as:

$$\alpha =\frac{M_i-M_t}{M_i-M_f}$$

(2)

where: M_i is an initial mass of the sample (mg), M_t is a mass of the sample in the given time (mg), and M_f is a final mass of the sample (mg). The reaction rate constant and relative mass loss can be described by the Arrhenius law:

$$k=A·e^{\frac{-E_a}{RT}}$$

(3)

where: k is a reaction constant (-), A is the pre-exponential factor (s⁻¹), E_a is activation energy (kJ∙kmol⁻¹), R is a universal gas constant (R = 8.3145 kJ∙kmol⁻¹∙K⁻¹), and T is the temperature (K). Merging Equation (3) with Equation (1) yields:

$$\frac{d\alpha }{dt}=A·e^{\frac{-E_a}{RT}}·f\left(\alpha \right)$$

(4)

The function of the conversion level f(α) can be described by many reaction models (

Table 3. Kinetic reactions models f(α) and g(α) [43,46,47].

Reaction Model	Code	f(α)	g(α)
Avrami–Erofeev	A2	2(1 − α)[−ln(1 − α)]1/2	[−ln(1 − α)]1/2
Avrami–Erofeev	A3	3(1 − α)[−ln(1 − α)]2/3	[−ln(1 − α)]1/3
Avrami–Erofeev	A4	4(1 − α)[−ln(1 − α)]3/4	[−ln(1 − α)]1/4
1-D diffusion	D1	1/2α−1	α2
2-D diffusion	D2	[−ln(1 − α)]−1	(1 − α)ln(1 − α) + α
3-D diffusion	D3	3/2(1 − α)2/3[1 − (1 − α)1/3]−1	[1 − (1 − α)1/3]2
Mampel (first-order)	F1	1 − α	−ln(1 − α)
Power law	P2	4α3/4	α1/2
Power law	P3	3α2/3	α1/3
Power law	P4	2α1/2	α1/4
Power law	P2/3	2/3α−1/2	α3/2
Contracting cylinder	R2	2(1 − α)1/2	1 − (1 − α)1/2
Contracting sphere	R3	3(1 − α)2/3	1 − (1 − α)1/3
n-order reaction	-	(1 − α)n	1 − (1 − α)1−n/1 − n

).

In this study, three different βs were applied, which are also a function of time. For the non-isothermal conditions, the linear β can be described as:

$$\beta =\frac{dT}{dt}$$

(5)

where: dT is a temperature change (K), dt is a time change (h).

The final formula for the thermal decomposition of the biomass is determined by inserting Equation (5) to Equation (4):

$$\frac{d\alpha }{dt}=\beta \frac{d\alpha }{dT}=A·e^{\frac{-E_a}{RT}}·f\left(\alpha \right)\mathrm{or}$$

(6)

$$\frac{d\alpha }{dT}=\frac{A}{\beta }·e^{\frac{-E_a}{RT}}·f\left(\alpha \right)$$

(7)

Equation (8) below is the general formula of the thermal decomposition of the solid biomass material. It is integrated and recombined with Equation (7), where g(α) is a known integrated kinetic reaction model (Table 3):

$$g\left(\alpha \right)={\int }_0^{\alpha }\frac{d\alpha }{f\left(\alpha \right)}=\frac{A}{\beta }{\int }_0^{T}exp\left(\frac{-Ea}{RT}\right)dT$$

(8)

2.4. Model-Fitting Method: Coats–Redfern Method

The biomass decompositions kinetic model was based on the Coats–Redfern method [29,43,48,49,50]. The Coats–Redfern method uses the Taylor series applied to the experimental data and limits the numbers of terms in the series. The Taylor series approach can be described as:

$$\begin{array}{c}g\left(x\right)=\frac{AE}{\beta R}p\left(x\right)=\frac{AE}{\beta R}\left[\frac{e^{-x}}{x^2}\left(1-\frac{2!}{x}+\frac{3!}{x^2}+\frac{4!}{x^3}+\dots \right)\right]=\frac{AE}{\beta R}\left[\frac{e^{-x}}{x^2}\left(1-\frac{2}{x}\right)\right]=\\ =\frac{AE}{\beta R}\left[\frac{e^{-E/RT}}{{\left(\frac{E}{RT}\right)}^2}\left(1-\frac{2}{\left(\frac{E}{RT}\right)}\right)\right]=\frac{{ART}^2}{\beta E}\left(1-\frac{2RT}{RTE}\right)e^{\left(\frac{-E}{RT}\right)}\end{array}$$

(9)

Applying the n-order reaction function from Table 3 to Equation (8) results in:

$$g\left(\alpha \right)={\int }_0^{\alpha }\frac{d\alpha }{{\left(1-\alpha \right)}^n}=\frac{A}{\beta }{\int }_0^{T}exp\left(\frac{-E}{RT}\right)dT$$

(10)

According to the order of reaction, the expression of Equation (10) is:

$$\mathrm{for}n=1g\left(x\right)=-ln\left(1-\alpha \right)$$

(11)

$$\mathrm{for}n\ne 1g\left(x\right)=\frac{1}{1-n}[{\left(1-\alpha \right)}^{1-n}-1]$$

(12)

Applying Equations (11) and (12) into Equation (9), the final formulas are:

$$\mathrm{For}n=1ln\left(-\frac{ln\left(1-\alpha \right)}{T^2}\right)=ln\left[\frac{AR}{{\beta E}_a}\right]-\frac{E_a}{RT}$$

(13)

$$\mathrm{For}n\ne 1ln\left(\frac{1-{\left(1-\alpha \right)}^{1-n}}{T^2\left(1-n\right)}\right)=ln\left[\frac{AR}{{\beta E}_a}\right]-\frac{E_a}{RT}$$

(14)

The $\frac{2RT}{RTE}$ was dropped from Equations (13) and (14) because its value is <1. Then, by plotting the left side of Equations (13) and (14) versus 1/T, the straight line was fitted using linear regression. The E_a was estimated as a slope of the straight line based on the best fitted linear regression and the coefficient of determination (R²). The A was calculated based on the intercept of the straight line.

$$intercept=ln\frac{AR}{\beta ·E_a}$$

where: A is the pre-exponential factor (s⁻¹), R is a universal gas constant (R = 8.3145 kJ∙kmol⁻¹∙K⁻¹), β is the heating rate (°C∙min⁻¹), E_a is activation energy (kJ∙kmol⁻¹).

3. Results and Discussion

3.1. Proximate and Ultimate Analysis

The obtained results (

Table 4. Proximate and ultimate analysis of nut shells.

Parameter			WS	HS	PES	PIS
Proximate analysis	MC	%	4.32 ± 0.11	9.56 ± 0.00	6.32 ± 0.01	7.05 ± 0.01
	HHV	MJ∙kg−1	19,604 ± 330	18,887 ± 80	19,692 ± 57	17,780 ± 57
	LHV		18,731 ± 316	17,078 ± 72	18,446 ± 53	16,528 ± 53
	AC	%	1.10 ± 0.20	1.00 ± 0.20	2.20 ± 0.40	3.10 ± 0.60
	VMC		81.44 ± 1.26	78.04 ± 0.05	78.84 ± 0.40	81.24 ± 0.26
	FC		13.14 ± 0.57	11.39 ± 0.09	12.57 ± 0.33	8.26 ± 0.25
Ultimate analysis	C	%	48 ± 10	49 ± 10	49 ± 10	44 ± 9
	H		8.0 ± 1.6	7.8 ± 1.6	7.9 ± 1.6	7.9 ± 1.6
	N		0.31 ± 0.06	0.43 ± 0.09	1.2 ± 0.2	0.2 ± 0.04
	O		42.6 ± 8.5	41.8 ± 8.4	39.6 ± 7.9	44.8 ± 9.0
	S		0.014 ± 0.003	0.019 ± 0.004	0.083 ± 0.017	0.014 ± 0.003

) indicate that the raw nut shells have potentially useful energy potential. Their average HHV was approximately 19.4 MJ∙kg⁻¹ (excluding the PIS, for which HHV = 17.8 MJ∙kg⁻¹. The MC was between 4.3% (for WS) and 9.6% (for HS). Whereas the AC ranged from 1.0% for HS to 3.1% for PIS. The highest content of the FC was observed for the WS (13.14%), the lowest for PIS (8.26%).

The ultimate analysis showed that the elemental characteristics of nut shells are similar. Their carbon content was between 44% (PIS) and 49% (HS, PES). Hydrogen, N, and O content was from 7.8 to 8.0%, 0.2–1.2%, and 39.6–44.8%, respectively. The S content was below 0.1%.

It can be concluded that nut shells have a remarkable energy potential. The investigated WS, HS, PES, and PIS meet fuel properties limitations of the non-woody biomass pellets (A standard). In accordance with the ISO 17225-6: 2014 (E), the non-woody pellets (A standard) can have HHV ≥ 14.5 MJ∙kg⁻¹, AC ≤ 6%, and MC ≤12%. All tested materials meet this HHV, AC, and MC limitations. However, the energy parameters for WS and HS are superior to PES and PIS. Their properties, especially HHV, AC, and MC, meet the limitations for the woody biomass—ISO 17225-2: 2014 (E). WS and HS meet industrial use standard I1, which limits HHV ≥ 16.5 MJ∙kg⁻¹, AC ≤ 1%, and MC ≤10%. Additionally, WS and HS meet standard A2 for the small scale use (HHV ≥ 16.5 MJ∙kg⁻¹, AC ≤ 1.2%, and MC ≤10%).

3.2. Thermogravimetric Analysis (TGA) and Derivative Thermogravimetric Analysis (DTG)

Analyzing the data obtained for nut shells (WS, HS, PES, and PIS), it can be seen that the β in the process of thermal treatment of waste biomass affects the values of kinetic parameters of the process (E_a, pre-exponential factor, and k). The three stages were observed for the tested materials (Figure 4) as in other studies [51]. Analyzing the TGA curves for nut shells (Figure 4), the shift in the initiation of the decomposition process for all materials was observed. This thermal decomposition shift between the heating rates was approximately 50–70 °C. It is associated with the thermal capacity of the material, which influences its internal heat transfer. The faster heating rate causes that the biomass is exposed to a given temperature effect for a shorter period of time. Thus, the material requires a higher temperature to start decomposing.

The first characteristic stage of the process for β = 5 °C∙min⁻¹ starts at approximately 140 °C and ends at approximately 264 °C for all the investigated nut shells. At 360 °C, materials intensively released volatiles, which was the second stage of the thermal decomposition. The temperature of the start and end of the first and second stage was different for the three βs.

The main process of the pyrolysis started between the 500 °C and 600 °C. Interestingly, at approximately 600 °C WS, HS, and PIS reached the same weight loss (60–70%) of the initial mass. The obtained TGA curve was characteristic for lignocellulosic biomass decomposition. Similar results and TGA waveform were also noted for other waste and biomass [23,52].

The TGA is also based on the derivative thermogravimetric analysis (DTG), where the amount of mass loss was determined for each material. The main characteristic feature is an increased amount of weight loss. It can be observed that nut shells were characterized by a higher rate of weight loss at β = 20 °C∙min⁻¹ than at β = 5 °C∙min⁻¹. For the WS and HS, the maximum weight loss was approximately 0.76 and 0.56%∙°C⁻¹ for β = 20 °C∙min⁻¹, 0.51 and 0.49%∙°C⁻¹ for β = 10 °C∙min⁻¹, and 0.54 and 0.45%∙°C⁻¹ for β = 5 °C∙min⁻¹, respectively. For the PES, the maximal derivative mass loss was 0.5–0.6%∙°C⁻¹ and was increasing with the β. Interestingly, for the PIS, the maximal derivative mass loss was decreasing with increasing β (0.85%∙°C⁻¹ for β = 5 and 10 °C∙min⁻¹; 0.60%∙°C⁻¹ for β = 20 °C∙min⁻¹).

3.3. Peak Analysis during TGA

Analyzing the peaks observed on the DTG curves of the nut shells it is possible to characterize the main thermal decomposition stages and determine their kinetic parameters. The fit peaks analyzer tool was used to find the peaks and their temperatures. The fitted peaks reflect the processes of the fibers’ decompositions such as cellulose, lignin, and hemicellulose (Figure 5 and Figure 6). For all tested materials, three main peaks (characterized by a different range of temperatures and kinetic parameters) were fitted.

The first peak was characteristic of the decomposition of the hemicellulose. This process took place at the range of temperature from 140 to 264 °C (β = 5 °C∙min⁻¹) for all nut shells. Depending on the β, it shifted from 196 to 322 °C and from 252 to 449 °C for β = 10 °C∙min⁻¹ and β = 20 °C∙min⁻¹, respectively.

The second reaction was typical for cellulose decomposition. This stage is significant due to its highest weight loss (DTG), by which the process was very dynamic, and the material released considerable amounts of volatile matter. The degradation of cellulose for WS and HS (at β = 5 °C∙min⁻¹) and for PIS (at both 5 and 10 °C∙min⁻¹) was represented by two reactions (confirmed by two peaks). Decomposition of the cellulose for β = 5 °C∙min⁻¹ took place approximately from 353 °C to 546 °C. The second stage was detected for β = 10 °C∙min⁻¹ and β = 20 °C∙min⁻¹, namely, from 400 °C and 472 °C, respectively.

The third stage (lignin fibers decomposition) took place at a wide range of temperature from 200 °C to 800 °C, in the case of PIS even from 50 °C to 900 °C. This process was characterized by the slowest weight loss, often during the whole thermal treatment process. Similar results of biomass decomposition and its three main fibers were also observed in other studies [24,53,54,55,56]. Cellulose, hemicellulose, and lignin were degraded in similar ranges of temperature. Yeo [57] and Senneca [58] confirmed the order of the distribution of biomass fibers. These studies showed that hemicellulose starts to decompose at approximately 100 °C, cellulose at approximately 300 °C, and lignin at approximately 70–100 °C up to even 900 °C. Decomposition of lignin caused by different drying temperatures affects other biomass conversion processes, i.e., grinding [59] and agglomeration [60].

The comprehensive analysis of the TGA peaks includes the determination of the activation energy (E_a) and pre-exponential factor (A).

Table 5. The activation energy (E_a) [kJ∙(mol∙K)⁻¹] and pre-exponential factor (A) [s⁻¹] for the WS fitted peaks.

		Kinetic Parameters	Heating Rate, β
			5 °C∙min−1		10 °C∙min−1		20 °C∙min−1
Walnut shell	Peak 1	Ea, kJ∙mol−1∙K−1	From 148.0 °C ± 9.1 to 265.0 °C ± 17.7	34.5 ± 9.6	From 196.0 °C ± 5.0 to 322.7 °C ± 4.0	45.3 ± 2.8	From 232.7 °C ± 12.4 to 517.3 °C ± 51.7	44.8 ± 4.2
		A, s−1		2.00 ± 2.65 × 10−4		2.96 ± 1.97 × 10−4		9.47 ± 5.97 × 10−5
		R2		0.9562		0.9678		0.9402
	Peak 2	Ea, kJ∙mol−1∙K−1	From 350.7 °C ± 6.6 to 446.7 °C ± 4.1	56.5 ± 4.4	From 397.7 °C ± 1.7 to 485.0 °C ± 2.2	74.3 ± 0.6	From 478.7 °C ± 9.1 to 609.0 °C ± 12.0	140.0 ± 22.1
		A, s−1		1.05 ± 0.96 × 10−3		1.85 ± 0.26 × 10−2		4.48 ± 5.34 × 103
		R2		0.9914		0.9894		0.9847
	Peak 3	Ea, kJ∙mol−1∙K−1	From 425.0 °C ± 1.6 to 497.7 °C ± 5.7	60.3 ± 2.5	From 461.7 °C ± 1.7 to 538.3 °C ± 3.3	74.2 ± 1.5	From 375.7 °C ± 90.4 to 889.7 °C ± 1.9	65.0 ± 7.4
		A, s−1		1.48 ± 0.58 × 10−3		1.84 ± 0.49 × 10−2		4.17 ± 2.81 × 10−3
		R2		0.9887		0.9887		0.9430
	Peak 4	Ea, kJ∙mol−1∙K−1	From 155.3 °C ± 53.7 to 852.0 °C ± 55.9	27.9 ± 1.2	From 176.3 °C ± 5.6 to 890.7 °C ± 1.9	36.8 ± 0.7	-	-
		A, s−1		2.73 ± 1.05 × 10−6		2.15 ± 0.25 × 10−5		-
		R2		0.9431		0.9568		-

,

Table 6. The activation energy (Ea) [kJ∙(mol∙K)⁻¹] and pre-exponential factor (A) [s⁻¹] for the HS fitted peaks.

		Kinetic Parameters	Heating Rate, β
			5 °C∙min−1		10 °C∙min−1		20 °C∙min−1
Hazelnut shell	Peak 1	Ea, kJ∙mol−1∙K−1	From 145.7 °C ± 8.8 to 274.3 °C ± 15.8	36.2 ± 9.8	From 198.7 °C ± 3.7 to 330.7 °C ± 4.9	48.7 ± 7.2	From 272.3 °C ± 6.2 to 448.0 °C ± 8.6	51.5 ± 8.1
		A, s−1		2.70 ± 3.43 × 10−4		1.56 ± 1.97 × 10−3		9.81 ± 12.6 × 10−3
		R2		0.9332 ± 0.0329		0.9329 ± 0.0251		0.8986 ± 0.0042
	Peak 2	Ea, kJ∙mol−1∙K−1	From 358.8 °C ± 3.6 to 449.7 °C ± 5.2	53.8 ± 3.9	From 403.3 °C ± 0.9 to 487.3 °C ± 3.4	75.8 ± 8.6	From 477.7 °C ± 5.7 to 621.7 °C ± 2.5	113.9 ± 2.4
		A, s−1		5.24 ± 4.22 × 10−4		5.07 ± 5.76 × 10−2		5.57 ± 1.72 × 100
		R2		0.9935 ± 0.0003		0.9904 ± 0.0000		0.9859 ± 0.0007
	Peak 3	Ea, kJ∙mol−1∙K−1	From 426.7 °C ± 7.8 to 502.7 °C ± 4.6	59.3 ± 0.4	From 462.0 °C ± 2.9 to 541.3 °C ± 3.1	75.5 ± 2.5	From 426.7 °C ± 9.0 to 882.7 °C ± 11.1	65.4 ± 0.9
		A, s−1		1.02 ± 0.16 × 10−3		2.17 ± 0.76 × 10−2		2.36 ± 0.28 × 10−3
		R2		0.9892 ± 0.0012		0.9897 ± 0.0007		0.9503 ± 0.0019
	Peak 4	Ea, kJ∙mol−1∙K−1	From 173.0 °C ± 61 to 846.7 °C ± 64.1	28.2 ± 1.4	From 201.°C ± 30.1 to 880.7 °C ± 16.0	36.8 ± 0.9	-	-
		A, s−1		2.87 ± 1.14 × 10−6		2.07 ± 0.25 × 10−5		-
		R2		0.9422 ± 0.036		0.9593 ± 0.0111		-

,

Table 7. Activation energy (E_a) [kJ∙(mol∙K)⁻¹] and pre-exponential factor (A) [s⁻¹] for the PES fitted peaks.

		Kinetic Parameters	Heating Rate, β
			5 °C∙min−1		10 °C∙min−1		20 °C∙min−1
Peanut shell	Peak 1	Ea, kJ∙mol−1∙K−1	From 131.3 °C ± 11.1 to 251.0 °C ± 2.4	34.3 ± 13.0	From 183.3 °C ± 9.7 to 306.7 °C ± 3.9	36.7 ± 9.7	From 245.7 °C ± 2.9 to 397.7 °C ± 3.9	47.2 ± 14.1
		A, s−1		2.00 ± 2.33 × 10−4		1.92 ± 2.62 × 10−4		2.41 ± 3.39 × 10−3
		R2		0.9316		0.9617		0.9488
	Peak 2	Ea, kJ∙mol−1∙K−1	From 350.0 °C ± 7.9 to 505.7 °C ± 3.3	53.4 ± 4.5	From 399.3 °C ± 4.6 to 546.7 °C ± 5.8	75.5 ± 2.9	From 475.3 °C ± 17.6 to 593.0 °C ± 14.4	116.0 ± 9.9
		A, s−1		4.62 ± 3.42 × 10−4		2.22 ± 0.87 × 10−2		2.84 ± 3.46 × 101
		R2		0.9868		0.9892		0.9920
	Peak 3	Ea, kJ∙mol−1∙K−1	From 426.7 °C ± 39.7 to 688.3 °C ± 14.3	19.2 ± 7.0	From 142.7 °C ± 33.2 to 892.7 °C ± 0.5	36.3 ± 2.5	From 217.3 °C ± 21.3 to 863.7 °C ± 28.1	53.1 ± 4.4
		A, s−1		9.34 ± 9.65 × 10−3		1.99 ± 0.69 × 10−5		5.53 ± 3.82 × 10−4
		R2		0.9009		0.9666		0.9718
	Peak 4	Ea, kJ∙mol−1∙K−1	-	-	-	-	-	-
		A, s−1		-		-		-
		R2		-		-		-

and

Table 8. Activation energy (E_a) [kJ∙(mol∙K)⁻¹] and pre-exponential factor (A) [s⁻¹] for the PIS fitted peaks.

		Kinetic Parameters	Heating Rate, β
			5 °C∙min−1		10 °C∙min−1		20 °C∙min−1
Pistachio shell	Peak 1	Ea, kJ∙mol−1∙K−1	From 137.0 °C ± 27.9 to 266.0 °C ± 7.9	30.0 ± 6.6	From 204.3 °C ± 22.8 to 328.0 °C ± 5.4	43.7 ± 9.1	From 255.0 °C ± 11.2 to 434.3 °C ± 9.9	51.5 ± 9.3
		A, s−1		2.45 ± 3.31 × 10−5		5.72 ± 7.62 × 10−4		1.01 ± 1.34 × 10−3
		R2		0.9549		0.9289		0.9226
	Peak 2	Ea, kJ∙mol−1∙K−1	From 350.7 °C ± 8.7 to 414.0 °C ± 8.3	103.8 ± 22.8	From 400.0 °C ± 9.9 to 461.3 °C ± 11.6	152.5 ± 19.8	From 456.7 °C ± 2.6 to 540.7 °C ± 2.6	150.3 ± 5.8
		A, s−1		9.11 ± 12.9 × 102		5.05 ± 7.01 × 105		4.29 ± 3.68 × 103
		R2		0.9667		0.9636		0.9594
	Peak 3	Ea, kJ∙mol−1∙K−1	From 417.3 °C ± 6.6 to 494.3 °C ± 4.5	63.0 ± 6.5	From 454.7 °C ± 6.6 to 535.3 °C ± 10.8	80.2 ± 5.5	From 508.7 °C ± 2.1 to 607.3 °C ± 1.2	96.1 ± 3.3
		A, s−1		5.24 ± 5.96 × 10−3		7.77 ± 4.80 × 10−2		6.21 ± 3.31 × 10−1
		R2		0.9768		0.9785		0.9805
	Peak 4	Ea, kJ∙mol−1∙K−1	From 155.3 °C ± 49.4 to 865.7 °C ± 29.2	31.5 ± 5.8	From 239.7 °C ± 1.7 to 888.0 °C ± 2.9	45.1 ± 5.2	From 405.7 °C ± 6.6 to 860.3 °C ± 4.1	67.4 ± 1.3
		A, s−1		8.69 ± 9.01 × 10−6		1.31 ± 1.20 × 10−4		3.96 ± 0.61 × 10−3
		R2		0.9376		0.9394		0.9331

summarize the E_a and A for the four nut shells. These values refer only to the best-fitted order of the reaction (The R² for the fitting method was ≥0.90). It can be concluded that the highest energy demand (activation energy) is needed for the cellulose decomposition. For the WS, HS, PES, and PIS at β = 5 °C∙min⁻¹, the E_a values amounted to 60.3 ± 2.5 kJ∙(mol∙K)⁻¹, 59.3 ± 0.4 kJ∙(mol∙K)⁻¹, 53.4 ± 4.5 kJ∙(mol∙K)⁻¹, and 103.8 ± 22.8 kJ∙(mol∙K)⁻¹, respectively. The E_a for hemicellulose for nut shells was approximately 30.0–36.2 kJ∙(mol∙K)⁻¹, and for the lignin was approximately 19.2–31.5 kJ∙(mol∙K)⁻¹. The highest E_a demand for cellulose decomposition was also observed in Burhenne studies of spruce biomass [22]. In these studies, E_a for cellulose was 236 kJ∙(mol∙K)⁻¹, and for hemicellulose and lignin, it was 100 and 40 kJ∙(mol∙K)^−1, respectively.

The increase in the E_a during the cellulose decomposition was observed with the increase of β. For the WS, E_a was 74.3 and 140.0 kJ∙(mol∙K)⁻¹ for the β of 10 and 20 °C∙min⁻¹, respectively. In the case of the HS, E_a was 75.8 kJ∙(mol∙K)⁻¹ (β = 10 °C∙min⁻¹) and 113.9 kJ∙(mol∙K)⁻¹ (β = 20 °C∙min⁻¹). Whereas, for PES, the E_a was 75.5 kJ∙(mol∙K)⁻¹ (β = 10 °C∙min⁻¹) and 116.0 kJ∙(mol∙K)⁻¹ (β = 20 °C∙min⁻¹). Finally, for the PIS, the E_a amounted to 152.5 kJ∙(mol∙K)⁻¹ (β = 10 °C∙min⁻¹) and 150.3 kJ∙(mol∙K)⁻¹ (β = 20 °C∙min⁻¹). A similar dependence was also noted for the lignin decomposition stage.

3.4. Conversion Rate and the Kinetic Parameters of the Pyrolysis Process

No significant differences were observed for the conversion rate (α) vs. T and the type of nuts shell (Figure 7). It can be assumed that WS, HS, PES, and PIS have very similar thermal decomposition characteristics. Their hemicellulose, cellulose, and lignin degradation started at a similar range of temperatures. The materials reached comparable α at the related T. Thus, based only on the analysis of α, it may be concluded that WS, HS, PES, and PIS belonging to nut shells biomass type were characterized by similar thermal degradation kinetics.

However, using the more detailed analysis of kinetic, some differences may be observed. Tables S1–S4 (Supplementary Materials), the values of E_a and A for α with the interval of 0.05 are shown. The TGA from 30 to 900 °C was fitted into the n = 1.5 reaction order (R² ≥ 0.97). Again, the most energy-demanding reaction in the thermal degradation of nut shells was the decomposition of cellulose. This stage had the highest energy demand, so the E_a of each nut shells was determined for the second peak obtained from DTG analysis. The E_a for nut shells was then estimated using the values from Table 5 and Table 6. The resulting E_a (β = 5 °C∙min⁻¹) was 60.3 ± 2.5 kJ∙(mol∙K)⁻¹ (WS), 59.3 ± 0.4 kJ∙(mol∙K)⁻¹ (HS), 53.4 ± 4.5 kJ∙(mol∙K)⁻¹ (PES), and 103.8 ± 22.8 kJ∙(mol∙K)⁻¹ (PIS). Likewise, the E_a increased with the increase of β (Table 5 and Table 6).

Other studies describe an application of TGA to nut shells. For the HS, the E_a amounted to 215 kJ∙(mol∙K)⁻¹ [61]. The differences in results may arise from different sets of β and other kinetic models used. In this study [61], the FWO model was applied. Analyzing the E_a of HS determined by the Coats–Redfern method, the similarity of the resulting values can be confirmed. In the Haikiri-Acma study [62], the E_a for HS was between 33 and 58 kJ∙(mol∙K)⁻¹, depending on the particle size. Some differences can be observed when comparing these data with ours. In the Demirbas study [63], the HS activation energy was from 89 to 129 kJ∙(mol∙K)⁻¹. For the other materials (e.g., WS) a similarity in kinetic parameters was also observed. The values of E_a ranged from 45.6 to 78.4 kJ∙(mol∙K)⁻¹ [64] and were very close to the data presented in this work. Acikalin [65] studied the kinetics of the PIS. The E_a for PIS was from 121 to 187 kJ∙(mol∙K)⁻¹ (model-fitting method), and 153 kJ∙(mol∙K)⁻¹ (FWO method). The A for the tested materials in this study (β = 5 °C∙min⁻¹) for different conversion rates was 5.2 ± 2.9 × 10⁻⁹ to 4.4 ± 5.4 × 10⁴, 6.1 ± 6.7 × 10⁻⁹ to 1.0 ± 1.2 × 10⁴, 9.7 ± 2.2 × 10⁻⁸ to 4.9 ± 6.8 × 10⁵, and 8.3 ± 12 × 10⁻⁸ to 2.2 ± 3.1 × 10⁸ for WS, HS, PES, and PIS, respectively. The A for the other β is presented in Tables S1–S4. The significant difference between the E_a for PIS and other nut shells may be from the different content of the hemicellulose and cellulose. The PIS consists of 40% cellulose and 34% hemicellulose [66] in comparison to the WS, HS, and PES, where the cellulose content ranges from 25–35%, and hemicellulose content ranges from 8–30% [37,41].

Kinetic parameters play an important role in designing the experimental processes and bio-reactors. Based on the kinetic parameters of thermal degradation of biomass materials, it is possible to estimate the temperature range of the lignocellulose degradation and heat demand to start the decomposition of the material. This is crucial from the practical point of view to determine the production costs. Moreover, the knowledge of the kinetic parameters can be useful to optimize the process conditions to obtain the final products with specific properties.

4. Conclusions

Raw nut shells from walnuts (WS), hazelnuts (HS), peanuts (PES), and pistachios (PIS) have a remarkable energy potential (their average HHV was approximately 19.4 MJ∙kg⁻¹, excluding the PIS, for which HHV = 17.8 MJ∙kg⁻¹. After the thermal treatment of nut shells (torrefaction, pyrolysis), the HHV significantly increased up to ca. 30 MJ∙kg⁻¹. However, their thermal treatment requires basic knowledge of kinetic parameters to facilitate the design of bioreactors and to optimize the conditions for obtaining specific properties of the processed waste.

The ultimate analysis showed that the elemental characteristics of nut shells were similar. Their carbon content was between 44% (PIS) and 49% (HS, PES), and the oxygen content was 39.6–44.8%. The heating rate (β) in the process of thermal treatment of waste biomass affected the values of kinetic parameters of the process (especially E_a). Faster β resulted in higher E_a. No significant differences were observed for the conversion rate (α) vs. temperature and the type of nuts shells.

The cellulose content had a significant impact on the E_a. The highest E_a was needed at the second stage of reaction, which was related to the cellulose decomposition. At this range of temperatures, the highest mass (volatile matter) loss and the fastest α were observed.

The nut shells had a characteristic pattern with three reaction stages characteristic for hemicellulose, cellulose, and lignin decomposition. The hemicellulose decomposition took place at 140 to 264 °C (β = 5 °C∙min⁻¹) for all nut shells. However, depending on the β, it shifted from 196 to 322 °C and from 252 to 449 °C for β = 10 °C∙min⁻¹ and β = 20 °C∙min⁻¹, respectively. The degradation of cellulose for WS and HS (at β = 5 °C∙min⁻¹) and for PIS (at both 5 and 10 °C∙min⁻¹) was represented by two reactions (confirmed by two peaks). Decomposition of the cellulose for β = 5 °C∙min⁻¹ took place approximately from 353 °C to 546 °C. The second stage was detected for β = 10 °C∙min⁻¹ and β = 20 °C∙min⁻¹, namely, from 400 °C and 472 °C, respectively. The third stage (lignin fibers decomposition) took place at a wide range of temperature from 200 °C to 800 °C, in the case of PIS even from 50 °C to 900 °C. This process was characterized by the slowest weight loss, often during the whole thermal treatment process.

Based on the estimated kinetic parameters, it can be concluded that the Coats–Redfern method may be used as an alternative to other models. The results were comparable with other kinetic description methods. Characterization of specific nut shell residues is recommended for improved modeling of thermal processes and designing of bioreactors for thermal waste treatment. Further research can be continued to optimize the thermal treatment process to achieve expected properties not only for energy purposes but also for other applications, such as biofilters media, sorbents, and other value-added products.