The material selection of the main furnace of the pyrolysis plant is related to the service life, operation stability, operation safety, etc. of the entire project. If the material is too poor, the service life of the pyrolysis equipment may be shortened and there may be production risks. How to choose the main furnace of pyrolysis plant depends on several factors, including operating conditions, the type of raw materials, the durability and cost required of the main furnace, etc. The following are the two main materials of pyrolysis reactors commonly seen on the market:
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1. Carbon steel
Carbon steel is commonly used in various industrial applications, including the reactors of pyrolysis equipment. The main difference lies in mechanical properties and chemical composition. Carbon steel has cost-effectiveness and durable strength, suitable for low-temperature pyrolysis, but has low corrosion resistance. For common pyrolysis raw materials such as waste tires and plastics, the cracking temperature is low and the corrosion is less, and carbon steel materials can fully cope with it, with high-cost performance. Carbon steel also has different models, such as Q245R and Q345R. For a pyrolysis plant, if the application requires high strength with high pressure and temperature requirements, Q345 will be a better choice. If the application does not require such high strength and the cost is limited, Q245 may be a suitable substitute.
2. Stainless steel
The commonly used stainless steel materials for the pyrolysis reactor are 304 stainless steel and 316 stainless steel, which have good corrosion resistance and mechanical properties at high temperatures. If there are PVC plastics in your waste plastics, or you want to recycle oil sludge(such as coal tar residue, oil sludge pollutants, hazardous waste, etc.), then ordinary carbon steel materials are not enough to withstand the corrosiveness and excessive pyrolysis temperature. It is better to use stainless steel as the main furnace material of the pyrolysis plant, which not only extends the service life of the main furnace but also alleviates the coking phenomenon of some raw materials. Compared with carbon steel, the cost of stainless steel materials is higher, which will also make the overall cost of the equipment more expensive.
Through thermogravimetric analysis (TG) experiments, the mass change curves (TG) and weight loss rate curves (DTG) of oil shale at different temperatures were obtained, as shown in Fig. 2. The experimental results showed that:
From Fig. 2 TG curve (a), it can be concluded that as the temperature increases, the TG curve shows a gradual decrease in the mass of the oil shale sample, indicating thermal decomposition and the release of volatile substances. As the heating rate increases, the TG curve shifts to the right (higher temperature region), suggesting that a higher heating rate requires a higher temperature for thermal decomposition to occur. This is due to the thermal lag effect.
Low-temperature region (0–200 °C): The curve shows minimal changes, mainly due to the evaporation of moisture and a small amount of volatile matter. Medium-temperature region (200–650 °C): Significant mass loss occurs, which is the primary temperature range for the pyrolysis of organic matter in oil shale. High-temperature region (650–950 °C): The curve levels off, indicating that pyrolysis is nearly complete, leaving ash and inorganic residues.
From the DTG curve (b), it can be observed that the DTG curve exhibits multiple peaks, representing different stages of mass loss. A prominent peak appears in the range of approximately 400–650 °C, corresponding to the rapid pyrolysis of organic matter in oil shale, during which a large amount of volatile components is released. Smaller peaks at lower and higher temperatures correspond to moisture evaporation and the decomposition of certain inorganic carbonates, respectively. As the heating rate increases, the position of the DTG peaks shifts toward higher temperatures, and the peak intensity (rate) also increases. This indicates that the pyrolysis reaction rate accelerates with an increasing heating rate. The phenomenon of DTG peak temperature shifting with increasing heating rate can be attributed to three mechanisms: firstly, the thermal hysteresis effect leads to a temperature gradient inside the sample during rapid heating, causing the actual decomposition temperature to be higher than the detection value; Secondly, according to the Arrhenius kinetic relationship, higher rates require higher temperatures to achieve the same reaction rate; Finally, the heating rate affects the competitive relationship between primary cracking and secondary reactions (such as coke deposition) by regulating the retention time of volatiles. These factors work together to cause the DTG peak temperature to shift towards higher temperatures.
To further analyze the pyrolysis behavior of oil shale, key combustion characteristic parameters were extracted from the thermogravimetric (TGA) and derivative thermogravimetric (DTG) curves. These parameters include the ignition temperature (Ti), peak temperature (Tp), burnout temperature (Tf), and the mass loss ratio. These parameters reflect the thermochemical characteristics of the combustion process, including the initiation, main reaction, and final completion stages. Specifically, the ignition temperature (Ti) marks the starting point of significant weight loss in the sample, which is reflected on the TG curve as the first obvious mass loss starting position, and corresponds to the temperature at which the DTG curve begins to deviate significantly from the baseline. The peak temperature (Tp) reflects the peak of the sample weight loss rate, which is the temperature point at which the DTG curve reaches the maximum weight loss rate. The burnout temperature (Tf) represents the endpoint at which the sample weight loss process is essentially completed, usually corresponding to the temperature point on the TG curve when the mass loss tends to stabilize. The combustion characteristic parameters extracted from the experimental data at different heating rates are listed in Table 2.
As shown in Table 2, the heating rate has a significant impact: as the heating rate increases, the ignition temperature, peak temperatures, and burnout temperature all shift to higher temperature regions. An increase in the heating rate causes the total mass loss to decrease slightly, indicating that the sample decomposes incompletely at higher heating rates. As the heating rate increased from 5 to 25 °C/min, the total mass loss of the sample decreased from 13.3 to 11.1%, indicating incomplete decomposition of oil shale at higher heating rates. This phenomenon is mainly attributed to the internal heat transfer delay and temperature gradient caused by thermal hysteresis effect5,8, which leads to insufficient thermal decomposition of internal particles, and rapid heating shortens the residence time of organic matter in the critical temperature range, hindering the secondary cracking of heavy components and mineral decomposition6. In addition, primary cracking reactions dominate at high heating rates, while secondary reactions that require higher activation energies (such as mineral decomposition and coke formation) are partially suppressed due to insufficient reaction time13. These factors work together to lead to a decrease in decomposition efficiency at high heating rates. Temperature is the main driving factor for the pyrolysis of organic matter in oil shale, and a higher final temperature promotes the complete decomposition of organic matter.
During the pyrolysis of oil shale, temperature has a significant influence on the release patterns of gaseous products. Figure 3 shows the variations in gas release at different final pyrolysis temperatures.
From Fig. 3a, it can be observed that as the temperature increases, the total gas yield increases. High temperatures promote the deep cracking of heavy components and enhance the generation of combustible gases such as H2 and CH4. This indicates that temperature control can significantly influence the production rate and compositional ratio of gaseous products.
In the retort pyrolysis experiment, the gas components (H2, CO2, CH4, etc.) generated at different temperatures were analyzed using gas chromatography. The results showed the following trends:
H2 content gradually increased from a low proportion at 400 °C to a maximum at 650 °C, reaching nearly 70%. This indicates that as the temperature increases, the pyrolysis reaction of organic matter intensifies, and the release of H2 significantly increases, becoming the main product of high-temperature pyrolysis. This phenomenon is mainly attributed to the condensation dehydrogenation reaction of aromatic hydrocarbons and the free radical recombination generated during the β—chain cleavage process of fatty chains. These processes not only promote the generation of hydrogen, but also reflect the complex chemical change mechanisms during pyrolysis. In addition, pyrite (FeS2) acts as a catalyst to promote the dehydrogenation reaction of organic matter, helping to remove hydrogen atoms from hydrocarbons, promote the formation of aromatic hydrocarbons, and increase H2 production, playing a key regulatory role in the type and distribution of pyrolysis products.
CO2 is predominantly released at lower temperatures (450 °C) and then gradually decreases. The generation of CO2 during oil shale pyrolysis originates from multiple reaction pathways involving both inorganic and organic components. The inherent carbonate minerals in the inorganic matrix (particularly calcite and dolomite) undergo thermal decomposition reactions in the medium–high temperature range (400–650°C) to produce CO214. Simultaneously, carboxyl functional groups in the organic kerogen undergo decarboxylation reactions during the initial pyrolysis stage (300–400 °C), while hydroxyl and carbonyl groups generate CO or CO2 through thermal cracking or rearrangement reactions at higher temperatures4. Furthermore, primary pyrolysis products (such as CO and CH4) can further promote CO2 generation through gas-phase reactions or secondary reactions with mineral oxides, particularly under sustained thermal conditions.
CO content increases with temperature, reaching a significant proportion at high temperatures (650 °C). This suggests that carbon oxidation and cracking reactions intensify at higher temperatures, leading to increased CO production.
CH4 content is relatively low at 400 °C but increases significantly as the temperature rises to 550–650 °C, indicating a trend of methane release during the pyrolysis of organic matter. The generation of CH4 is closely related to the release of methyl radicals, mainly from the cleavage of fatty side chains and the demethylation of methyl aromatic hydrocarbons, which together promote the formation of methane. In addition, dolomite (MgCa(CO3)2) decomposes into MgO, CaO, and CO2 during pyrolysis, where CO2 interacts with free radicals or intermediates generated by pyrolysis through reduction reactions to promote the formation of CH4, while calcium oxide and magnesium oxide act as alkaline catalysts to neutralize acidic substances and optimize the environment for methane formation.
C2 and higher hydrocarbons (C2H4, C2H6, C3H8, etc.) are primarily released during the mid-temperature stage, but their content gradually decreases at higher temperatures. This reflects the decomposition trend of long-chain organic compounds.
By studying the effect of pyrolysis conditions on shale oil yield and composition, process parameters can be optimized to improve the yield and quality of shale oil. To determine the optimal pyrolysis temperature range for maximizing shale oil yield, experiments were conducted to analyze the yield and compositional variations of shale oil at different final pyrolysis temperatures, as shown in Fig. 4.
From Fig. 4a, it can be observed that as the pyrolysis temperature increases, the oil yield increases significantly but tends to level off at higher temperatures. At low temperatures, the organic matter in oil shale is not completely decomposed, resulting in a lower shale oil yield. In the medium to high-temperature range (450–650 °C), the organic matter undergoes progressive pyrolysis, releasing a large amount of oil, thereby significantly increasing the shale oil yield. However, at excessively high temperatures, although the oil yield continues to rise, secondary cracking may occur, leading to an increase in light fractions and a gradual increase in coke formation.
From Fig. 4b, it can be seen that with increasing temperature, the content of alkanes and aromatics increases, while the proportion of resins and asphaltenes decreases. At 400 °C, the content of heavy components (colloids and asphaltenes) is relatively high, indicating a lower degree of organic matter cracking. At 650 °C, the content of alkanes reaches a high level, suggesting that high temperatures promote the cracking of heavy components, making the oil lighter in composition.
From Fig. 4c, at low temperatures (400 °C), the content of C21 + (heavy components) is relatively high, while the content of light components (< C10 and C10–C14) is relatively low. As the temperature increases to 650 °C, the content of < C10 and C10–C14 increases, showing that light hydrocarbons gradually dominate. The C21 + heavy components decrease, indicating that high temperatures facilitate the thermal cracking of heavy oil.
By controlling the pyrolysis temperature, the yield and quality of shale oil can be effectively regulated. Selecting an appropriate temperature helps increase the yield of light oil and optimize the pyrolysis process.
As illustrated in Fig. 5: Effect of different final pyrolysis temperatures on semi-coke yield, the semi-coke yield decreased progressively from 88 to 78% as the pyrolysis temperature increased from 400 to 650 °C. At lower temperatures (400–450 °C), the pyrolysis reaction of organic matter was relatively weak, resulting in only partial release of volatile components and a higher semi-coke yield. As the temperature increased (450–550 °C), the pyrolysis of organic matter in oil shale intensified, releasing significant amounts of volatile substances and reducing the semi-coke. When the temperature reached 650 °C, further cracking of the carbonaceous material in the semi-coke occurred, leading to a further decrease in the semi-coke yield.
To investigate the changes in mineral composition and crystal structure during the pyrolysis process, X-ray diffraction (XRD) analysis was conducted on both the oil shale samples and the semi-coke samples obtained at 650 °C. The findings are presented in Fig. 6.
The XRD spectrum of the oil shale sample (Fig. 6) shows: A pronounced quartz (Q) characteristic peak, indicating that quartz is one of the primary mineral components. Clear dolomite (M) characteristic peaks, suggesting that dolomite is present in significant proportions in the oil shale sample. High-intensity calcite (C) peaks, showing that calcite is an important carbonate mineral in the oil shale sample. The presence of pyrite (P) characteristic peaks, indicating a certain amount of sulfides in the oil shale. Multiple distinct diffraction peaks, demonstrating that the minerals in the oil shale sample exhibit good crystallinity. No significant features for organic matter in the XRD spectrum, as organic matter is primarily amorphous.
The XRD spectrum of the semi-coke sample (Figure b) shows:
The quartz (Q) characteristic peaks remain prominent, and their intensity significantly increases, indicating that quartz becomes relatively enriched during the pyrolysis process. The calcite (C) characteristic peaks weaken considerably, indicating that under high temperature conditions, calcite may undergo decomposition to produce CO2, which is consistent with its known thermal decomposition characteristics. The pyrite (P) characteristic peaks also weaken, indicating that some sulfides may have decomposed or transformed. New potassium feldspar (K) characteristic peaks appear in the semi-coke sample, which may result from the recrystallization of minerals during high-temperature reactions. It is important to note that the changes in XRD peak intensity reflect relative crystallinity rather than absolute content.
High-temperature pyrolysis not only leads to the cracking of organic matter but also causes the decomposition, enrichment, and recrystallization of mineral components. These results highlight the profound impact of pyrolysis on the solid-phase composition of oil shale.
From the comparison analysis of Fig. 7 between the SEM images of oil shale and semi-coke samples, it is evident that under high-temperature conditions, the porosity of the residue surface increases, and the microstructure exhibits a porous characteristic. Temperature has a significant impact on the properties of the semi-coke. High temperatures not only promote the decomposition of minerals but also enhance the porous structure of the residue, making it more suitable for resource utilization in the field of construction materials.
Figure 8 shows the infrared spectra of pyrolysis products (shale oil and semi-coke) from oil shale.
C–H stretching vibration (, cm⁻1): Significant C–H absorption peaks appear in shale oil, indicating the presence of a large amount of methyl and methylene structures in alkanes and aromatic hydrocarbons. These peaks are weaker in semi-coke, suggesting that C–H bonds in the organic matter are partially broken during pyrolysis, resulting in the generation of gaseous and liquid hydrocarbons.
C=C double bond stretching vibration peaks (, cm−1): Shale oil exhibits noticeable C=C absorption peaks, indicating the presence of aromatic hydrocarbons or unsaturated compounds in shale oil. In semi-coke, the C=C peaks almost disappear, showing that most unsaturated bonds have been transformed or polymerized during high-temperature pyrolysis.
C=O stretching vibration peak ( cm−1): Shale oil contains C=O functional groups, which may represent characteristic peaks of organic acids, esters, or ketones. This peak weakens in semi-coke, indicating that oxygen-containing groups are gradually removed under high-temperature conditions.
Si–O–Si vibration peaks (, cm−1): Strong Si–O–Si absorption peaks are observed in semi-coke, primarily related to the mineral components (e.g., quartz) in oil shale. These peaks are weaker in shale oil, indicating that shale oil is mainly derived from organic matter, while the mineral residues remain in the semi-coke.
C–H bending vibration peaks (, cm−1 and 910, 500 cm−1): These absorption peaks are prominent in shale oil, reflecting the presence of methyl, methylene, and hydrocarbon skeletons. In semi-coke, these peaks weaken significantly, indicating that most hydrocarbons are converted into oil or gas during pyrolysis.
The infrared spectrum of shale oil exhibits strong C–H stretching and bending vibration peaks, indicating that its main components are alkanes and aromatic hydrocarbons. The presence of functional groups such as O–H, C=C, and C=O suggests that shale oil contains a certain amount of oxygenated and unsaturated compounds. In contrast, the infrared spectrum of semi-coke shows a significant reduction in the intensity of peaks corresponding to organic groups like C–H and C=O, indicating that the organic matter undergoes cracking during pyrolysis.
Infrared spectral analysis reveals that shale oil primarily consists of hydrocarbons, with a high content of alkanes and a small amount of oxygenated compounds. In semi-coke, organic groups are significantly reduced, and mineral components dominate. This indicates that the pyrolysis process decomposes the organic matter in oil shale into liquid oil and gas, leaving semi-coke enriched with minerals.
The pyrolysis process of oil shale is heavily influenced by temperature, which determines the reaction pathways and the formation of products. Based on experimental results and reaction kinetics analysis, the pyrolysis mechanism of oil shale is discussed from three aspects: decomposition stages, reaction pathways, and the regulatory role of temperature.
According to the characteristic temperatures and product distribution during the pyrolysis process, the pyrolysis of oil shale can be divided into the following three stages13,14,15,16:
Low-Temperature Dehydration Stage (< 200 °C):
In this stage, physical dehydration occurs as adsorbed and bound water in the sample evaporates. There is minimal mass loss, and no significant chemical reactions take place.
Medium-Temperature Organic Matter Cracking Stage (400–650 °C):
The organic matter in oil shale (e.g., kerogen) begins to undergo thermal cracking, generating volatile components. This stage is the main reaction phase, where significant amounts of liquid products (shale oil) and combustible gases (e.g., CO2, CH4) are released. The reactions primarily involve the breaking of carbon chains and the removal of functional groups, such as decarboxylation reactions (producing CO2) and methyl cracking (producing CH4).
High-Temperature Recombination and Residue Decomposition Stage (> 650 °C):
At high temperatures, the heavier components formed during cracking undergo further decomposition, generating additional gaseous products (e.g., H2, CO). Meanwhile, the mineral matter in the semi-coke (e.g., carbonates) thermally decomposes to form oxides, and the fixed carbon is converted into coke.
Based on the analysis of liquid and gaseous products, the primary reaction pathways of oil shale pyrolysis are proposed as follows17:
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Primary Cracking Reactions:
$${\text{Organic}}\;{\text{ matter }}\left( {{\text{kerogen}}} \right) \, \to {\text{ Shale}}\;{\text{ oil }} + {\text{ Gas }} + {\text{ Semi - coke}}$$During the medium-temperature stage, kerogen decomposes into tar and volatile components, while releasing gases such as CH4 and CO2. This reaction is primarily driven by the cleavage of chemical bonds with lower activation energy, such as weak C–C and C–H bonds.
Under high-temperature conditions, the heavier components in shale oil undergo further cracking, increasing the proportion of lighter components (e.g., ketones, ethers), while simultaneously producing gases.
At high temperatures, the carbonate minerals in the semi-coke decompose, forming porous oxide structures.
Temperature significantly affects the reaction rate, pathway selection, and product distribution in oil shale pyrolysis:
Regulation of Gas Product Pathways:
High-temperature conditions (> 600 °C) enhance secondary cracking reactions, promoting the production of light gases (H2, CH4). As the temperature increases, gas yield rises, and the proportion of CO and H2 increases, indicating that high temperatures favor the generation of gaseous products and improve the calorific value of the gas.
Regulation of Liquid Product Pathways:
Medium-temperature conditions (400–600 °C) represent the optimal range for tar generation. During this phase, primary cracking reactions dominate, resulting in the highest shale oil yield. At higher temperatures, shale oil undergoes secondary cracking into gases, leading to a reduction in liquid products.
Regulation of Semi-coke Pathways:
Increasing temperatures promote mineral decomposition and carbonization reactions, reducing the fixed carbon content in the residue and increasing its porosity.
The kinetic analysis of oil shale pyrolysis was conducted using the FWO (Flynn–Wall–Ozawa) and KAS (Kissinger–Akahira–Sunose) methods. These approaches comprehensively characterize the variation of activation energy during the pyrolysis process, providing a theoretical basis for optimizing the pyrolysis process and improving oil yield18,19,20.
In experiments conducted at different heating rates, the relationship between Log(dx/dt) and /T at the same conversion rate is shown in Fig. 9.
From Fig. 9, the following can be observed:
Initial Stage (low conversion rate α = 0.1–0.3): The slope is steep, and the activation energy is high. This stage likely corresponds to the initial decomposition of volatile substances.
Intermediate Stage (moderate conversion rate α = 0.4–0.6): The slope gradually decreases, and the activation energy lowers, indicating the main reaction phase of organic matter decomposition.
Final Stage (high conversion rate α = 0.7–0.9): The slope becomes nearly flat, and the activation energy reaches its lowest point. This stage likely corresponds to deep cracking and the formation of semi-coke.
The FWO method analyzes the pyrolysis reaction through non-isothermal processes, providing insights into the variation of activation energy with conversion rates. It is particularly suitable for analyzing activation energy during the initial and intermediate stages of the reaction.
The KAS method calculates the reaction activation energy more directly and is applicable to the entire pyrolysis process. It is especially useful for estimating energy requirements during high conversion rates (deep cracking stage).
In kinetic analysis, the non-isothermal reaction rate equation is derived by combining the Arrhenius equation with the law of mass action. Accordingly, the kinetic analysis of oil shale samples was performed. Table 3 presents the kinetic data calculated using the FWO and KAS model-free methods.
From Table 3, the following conclusions can be drawn:
Low Conversion Rate Stage (α = 0.1–0.3): The activation energy is relatively low, indicating that the initial stage of pyrolysis primarily involves the release of volatiles such as moisture and light organic compounds. This phase is characterized by reactions that are relatively facile and require minimal energy, consistent with the attributes of primary pyrolysis reactions.
Moderate Conversion Rate Stage (α = 0.5–0.7): There is a notable increase in the activation energy, signifying that the pyrolysis process has entered the main cracking phase of organic matter. During this stage, complex chemical bonds, such as C–C and C–H bonds within aromatic compounds, begin to break, necessitating higher energy input to sustain the reactions. This process predominantly entails the cracking of heavy organic compounds, leading to the formation of liquid products like shale oil and gaseous products such as CH4 and H2.
High Conversion Rate Stage (α = 0.9): The activation energy increases further, indicating that the latter stages of pyrolysis involve the decomposition of refractory materials, including aromatic compounds and coke precursors. These substances require significantly higher energies for their breakdown, resulting in a marked elevation in activation energy. This phase is characterized by the formation of semi-coke and a continued generation of gaseous products.
For the mechanism function, a G(α)−1/β linear fit was performed. Based on the analysis, the fit result should be a straight line passing through the origin, with the best linear correlation coefficient. When the intercept approaches 0, the corresponding G(α) is identified as the most probable mechanism function. Table 4 present the kinetic data results for four multi-step models.
This study employs multi-step kinetic models (such as Fn-Fn-Fn, An-D3-R3, etc.) to analyze the pyrolysis of oil shale. Oil shale pyrolysis encompasses multiple stages, including dehydration, organic matter cracking, and mineral decomposition, each characterized by distinct reaction mechanisms. A single model is inadequate for fully describing this complexity, whereas a multi-step model can more accurately reflect the characteristics of each stage. Although the Distributed Activation Energy Model (DAEM) is effective in describing activation energy distributions, it lacks the flexibility required for handling multi-stage reactions and is better suited for single reaction pathways. Given the multiplicity of reaction paths inherent in oil shale pyrolysis, multi-step kinetic models are more applicable and provide a more precise representation of the process dynamics.
From the kinetic analyses of the aforementioned four different models, the following conclusions can be drawn:
Fn-Fn-Fn Model.
The pyrolysis process is divided into three stages (Step 1, Step 2, Step 3), with the activation energy progressively increasing: 5.728 kJ/mol → 83.054 kJ/mol → 143.505 kJ/mol.
Step 1 contributes the most (46.4%), indicating that the initial reaction dominates. Low-temperature stage (Step 1), Activation energy is low, and the reaction proceeds easily, likely involving the initial release of volatile components in the organic matter. Medium-temperature stage (Step 2), Activation energy increases, indicating more complex reactions, such as the formation of intermediate products. High-temperature stage (Step 3), Activation energy reaches 143.505 kJ/mol, suggesting that deep cracking reactions require higher energy.
An-D3-R3 Model.
This model combines nucleation and growth (An), diffusion (D3), and reaction control (R3) mechanisms. The contributions of each stage are as follows: 48.7% (An) → 22.3% (D3) → 28.9% (R3).
Nucleation and growth (An), The activation energy is the lowest (13.171 kJ/mol), suitable for the initial cracking of organic matter.
Diffusion control (D3), The activation energy is moderate (19.792 kJ/mol), indicating that the reaction is influenced by the diffusion of volatile components.
Reaction control (R3), The activation energy is higher (207.312 kJ/mol), indicating that deep cracking processes require overcoming significant energy barriers.
D3-An-R3 Model.
The pyrolysis process involves three stages: diffusion control (D3), nucleation and growth (An), and reaction control (R3). The activation energy increases progressively: 25.168 kJ/mol (D3) → 228.926 kJ/mol (R3), reaching a maximum of 269.833 kJ/mol (An) in the high-temperature stage.
Diffusion control (D3), At the low-temperature stage, the reaction rate is primarily influenced by diffusion.
Nucleation and growth (An), At high temperatures, complex gas decomposition occurs, requiring high activation energy.
Reaction control (R3), Complex cracking reactions dominate, requiring the highest activation energy.
R3-D3-An Model.
This model follows the sequence of reaction control (R3) → diffusion control (D3) → nucleation and growth (An). The activation energy progressively increases: 7.554 kJ/mol (D3) → 269.833 kJ/mol (R3) → 269.833 kJ/mol (An).
Key control factors in the kinetic process: Low-temperature stage: Dominated by diffusion control and nucleation. High-temperature stage: Dominated by complex chemical reactions.
Application of Multi-Step Kinetic Models: The multi-step kinetic model helps optimize the operational parameters of oil shale pyrolysis, control the pyrolysis reaction pathways, and improve shale oil yield and quality.
Insights into the Pyrolysis Process of Oil Shale: The pyrolysis of oil shale is a complex multi-stage, multi-path reaction system. Temperature regulation is a critical factor influencing cracking pathways and product distribution:
Medium-temperature stage: Dominated by primary cracking, making it ideal for shale oil production. High-temperature stage: Enhances secondary cracking and mineral decomposition, favoring the generation of gaseous products and highly porous residues.
This study’s mechanistic analysis provides theoretical support for optimizing the pyrolysis process, especially in temperature regulation. It offers guidance for achieving targeted product conversion and efficient resource utilization.
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